Instrumentation for Process Measurement and Control, Third Editon

RAONaR,

THIRD EDITION

for

NORMAN

CHILTON COMPANY

A. ANDERSON

PENNSYLVANIA

CONTENTS

Preface

SECTION

I FEEDBACK

1 Introduction

PROCESS

to Process

Control

CONTROL

Types of Processes 5 Processes with More Than One Capacity and Resistance 6 Dead Time 6 Measurement 7 Symbols 1.0 The Feedback Loop 1.0 Feedback Control 1.4 ControIling the Process 1.4 Selecting ControIler Action 1.6 Up sets 1.7 Process Characteristics and ControIlability 1.7 Controller Responses 1.8 On/Off Control 1.9 Proportional Action 20 Integral Action (Reset) 23 Derivative Action 25 Selecting the ControIler 27 Conclusion 29 Questions 30 2 Process/Pressure

Measuring

Instruments

What Is Pressure? 33 Units of Measurement 35 Pressure Measurement 35 The Pascal 36 Bar Versus Pascal 37 Gauge, Absolute, and Differential Pressure 37 Understanding the Effects of Gravity 38 GravityDependent Units 38 Gravity-Independent Units 39 Pressure Standards 39 Plant Instruments That Measure Pressure Directly 44 Bell

CONTENTS

Instrument 44 Slack .or Limp-Diaphragm 44 Pressure Gauges 46 Liquid or Steam Pressure Measurement 48 Seals and Purges 48 Pulsation Dampener 48 Metallic Bellows 49 Pressure Transmitters 52 Signal Transmissions 52 Pneumatic Recorders and Indicators 53 Mechanical Pressure Seals 55 Calibration Techniques 59 Field Standard 59 Portable Pneumatic Calibrator 59 Force-Balance Pneumatic Pressure Transmitter 60 Pneumatic Relay 62 Principle of Operation 63 Absolute Pressure Transmitter 64 Questions 65 3 Level and Density Measurements 69 Level Measurement Methods 69 Float-and-Cable 70' Displacement (Buoyancy) 71 Head or Pressure 73 Capacitance 78 Conductance 79 Radiation 79 Weight 79 Ultrasonic 80 Thermal 81 Density Measurement Methods for Liquids and Liquid glumes 81 Hydrostatic Head 82 Radiation 84 Vibration 84 Temperature Eft'ects and Considerations 84 Dift'erential Pressure Transmitter 85 Questions 87 4 Flow Measurement 90 Constriction or Differential Head Type 91 Primary Devices 94 Secondai-y Devices 99 Relating Flow Rate to Differential 100 Effect of Temperature on Flow Rate 103 Variable Area Meters (Rotameter) 109 Open-Channel Flow Rate Measurements 109 Primary Devices 110 Installation and Selection Considerations 116 Velocity Flowmeters 117 Magnetic Flowmeter 117 Vortex Flowmeter 121 Turbine Flowmeter 122 Other Flowmeters 123 Conclusion 124 Questions 124 5 Temperature and Humidity Measurements

126

Temperature 126 Filled Thermal Systems 128 Electrical Systems 130 Thermocouples 130 Resistance Thermal Detectors 139 Thermistors 144 Humidity Measurements 144 Questions 148 6 Analytical Measurements 151 Electrical Conductivity 151 Types of Calibration 154 Calibration in Conductivity 154 Calibration in Terms of Concentration of Electrolyte 155 Polarization 156 Cell Construction 156 Electrodeless Conductivity Measurements 157 Hydrogen Ion Activity (pH) 159 Ionization or Dissociation 159 The pH Scale 161 Measurement of pH-The Glass Electrode 164 Reference Electrode 165 Temperature Compensation 168 Reading the Output of the pH Electrodes 169 pH Control 170 Summary 172 Oxidation-Reduction Potential 172 Ion-Selective Measurement 173 Chromatography 174 Capacitance 175 References 176 Questions 176

FEEDBACK PROCESSCONTROL

PROCESS

REACTIONCURVE EC

(a)

EDc TIME

(b)

TIME

PRESSURE IN TANK

(cI

SUPPLY TIME

TEMP.

(dI

TIME

Fig. 1-2. Four types or systems: (a) electric, (b) hydraulic, (c) pneumatic, and (d) thermal. Each has a single capacity and a single resistance and all bave identical response characteristics.

regulate a process and certain aspects of process behavior will be discussed in this text. Examples of some completely instrumented process systems will be given to demonstrate the practical application of the instrument components. The physical system to be controlled mar be electrical, thermal, hydraulic, pneumatic, gaseous,mechanical, or any other physical type. Figure 1-2 and Table 1-1 compare severa! common systems. All followthe same basic laws of physics and dynamics.

INTRoDucnON TO PROCESSCONTROL 5

The behavior of a process with respect to time defines its dynamic characteristics. Behavior Dot involving time defines its static characteristics. Both static (steady) and dynamic (changing with time) responses must be considered in the operation and understanding of a process control system. Types

ot Processes

The simplest process contains a single capacity and a single resistance. Figure 1-2 illustrates a single-capacity, single-resistance process in (a) electrical, (b) hydraulic, (c) pneumatic, and (d) thermal forms. To show how these behave with respect to time, we can impose a step upset (sudden change) in the input to the process and examine the output. The resulting change in process::variable with respect to time is plotted in Figure 1-3. The reaction curve of all four types of systems will be identical. This type of curve (exponential) is basic to automatic control. It can be obtained easily with an electrical capacitor and resistor arranged as in Figure l-2a.

Fig. 1-3. Universaltirne-constantchart, showingexponentialrise anddecay.

FEEDBACK PROCESSCONTROL

Figure l-2a shows a simple RC circuit-a resistor, capacitor, and battery source in series. The instant the circuit is closed, the capacitor starts to charge to the voltage of the battery. The rate at which the capacitor charges gradually decreases as the capacitor voltage approaches the battery voltage (voltage curve A in Figure 1-3). Although the rate varies, the time it takes the capacitor to charge to 63 percent of the battery voltage is a constant for any one value of Rand C. Thus, no matter what the voltage of the battery, the capacitor charges to 63 percent of the battery voltage in a time interval called the time constant, or characteristic time (T) ofthe circuit. The value orT in seconds is the product of the resistance (in ohms) and the capacitance (in farads). Note thai the charging time increases with an increase in either R orC. ~ This simple RC circuit is often used to produce the transient waveform shown, which is called an exponential-rise transient. On discharge, the circuit reacts similarly. For example, if the battery in Figure l-2a is replaced by a solid conductor, the charged capacitar discharges 63 percent of its charge in RC seconds. The simple RC circuit shown in Figure l-2a symbolizes many real physical situations. It is important to examine the circuit in detail. InRC seconds, the capacitar charges to 63.2 percent ofthe applied voltage. In the nextRC seconds, the capacitar charges to 63.2 percent ofthe remaining voltage, or to 87 percent ofthe applied voltage. In the third interval of RC seconds, the capacitar charges to 95 percent of the applied voltage. Although the capacitar never charges to exactly 100 percent of the applied voltage, it does charge to 99 percent in 4.6 RC seconds as shown in Figure 1-3, which is a curve of capacitar voltage (or current) versus time. Note that time is plotted inRC (time-constant) units. Processes with More Than One Capacity and Resistance In practice, a process will contain many capacitance and resistance elements. Figure 1-4 illustrates a process containing two resistance elements and two capacitance elements. Figure 1-5 shows the resulting process reaction curve. Note that the additional capacitance and resistance essentially affect the initial curve shape, adding a delay to the processo Dead Time Dead time is a delay between two related actions. For example, assume that the temperature sensor shown in Figure 1-1 was located 10 feet

I~RODUCTION TO PROCESSCONTROL 7

Fig. 1-4. Multicapacitysystem.

(3.048 m) away from the beat exchanger. lf the liquid travels at a velocity of 10 feet (3.048 m) per second, a dead time of one second will occur. ln some process control situations, dead tim e becomes the most difficult factor in the equation'. Dead time mar also be called pure delay, transport lag, or distance/velocity lag. Dead time is rarely found in its pure form, but occurs frequently in combination with resistancecapacitance and other types of lags. Dead time is a difficult factor to equate when applying control to the processo Measurement

To employ feedback control, we musi first measure the condition we wish to maintain at the desired standard. The condition (variable) mar be temperature, pressure, ftow, level, conductivity, pH, moisture content, or the like.

Fig. l-S. Characteristiccurve oCmulticapacitysystem.

FEEDBACK PROCESSCONTROL

The measuring element is connected to the control element. ln many installations, the measurement is located far from the controller. This problem is solved by using a measuring transmitter (Figure 1-6). The measuring transmitter usually develops an electrical signal for an electronic controller or a pneumatic signal for a pneumatic controller. Measuring transmitters bave attained great popularity in the process industries. They perform the measurementand develop a pneumatic or electric signal proportional to the variable in one unit. This signal can be transmitted long distances. Pneumatic transmitters generally produce an air pressure change of 3 to 15 psi or 20 to 100kPa (see p. 36 for definition of pascal unit) for measurement change of O to 100per-

Fig. 1.6. Measuringtransmittersconvertthe variableto be measuredinto a proportionalpneumaticor electricalsignal.

INTRODUCTIONTO PROCESSCONTROL 9

Table 1.2. StandardISA and SAMA FunctionalDiagramElements

, /

~ FLOW \:-..:I TRANSMITTER

~ L!-J

SQUARE ROOT EXTRACTOR

r:-ï ~

1:"';\ LEVEL \!:!I TRANSMITTER

r:ï ~

MUL TIPlIER

L.LJ

~ ~

PRESSURE TRANSMITTER

~ L.:::...J DIVIDER

r'd:"":':1DERIVATIVE ~ CONTROL ACTION

l1:r" ~

TEMPERATURE TRANSMITTER

r:¡:-, BIAS, ADDITION L..=..J OR SUBTRACTION

r::;-, ~

TIME FUNCTION CHARACTERIZER

1::\ ~

POSITION TRANSMITTER

rA""l ~

COMPARATOR DIFFERENCE'

~ ~

UNSPECIFIEDOR NONLINEAR FUNCTION CHARACTERIZER

~ L!.J

ADDER SUMMÉR

O /,LIGHT PANEL 1';"\ \.!oI

INDICA

t:'\ ~

RECORDER

t:;:'\

RELAY

COlL

TOR

rJ1 CONTROL INTEGRAL (RESEn ACTION

r:-::l ~ *

A VERAGER

~ ~

INTEGRATOR

-11-

rl.. \J

NORMALLYOPEN

PROPORTIONAL CONTROL ACTION

RELAYCONTACT

QUOTATION ITEM NUMBER MOUNTED FRONT

ON PANEL

REGULATED PROCESS

THE

AIR

NORMALLYCLOSED RELAYCONTACT

~ V

AUTO/MANUAL TRANSFERSWITCH

A\. 'W

MANUAL SIGNAL GENERATOR

/::'~

ANALOG SIGNAL GENERATOR

m L-:-J

TRANSFEROR TRIP RELAY

m ~

SOLENOID ACTUATOR

~ ~

ELECTRIC MOTOR

r;ï ~

HIGH SIGNAL SELECTOR

m ~

HIGH SIGNAL lIMITER

~ ~

HIGH SIGNAL MONITOR

m LOW SIGNAL L.::::..J SELECTOR

m ~

LOW SIGNAL lIMITER

r:-:--l L!:!-J

LOW SIGNAL MONITOR

~ ~

HIGH AND LOW lIMITER

~ ~

HIGH AND LOW SIGNAL MONITOR

VELOCITY OR RATE lIMITER

~ ANALOG TO ~DIGITALCONV.

r::-1 RESISTANCE TO ~CURRENTCONV.

I;ViVITHERMOCOUPLETO

~VOLTAGE

~VOLTAGECONV.

L.:::..JCURRENTCONV.

~VOLTAGECONV.

r-viV1 VOLTAGE TO ~VOLTAGECONV.

rp;j1 PNEUMATIC TO ~CURRENTCONV.

~ PNEUMATIC TO ~VOLTAGECONV.

r;;;::\ MOTORIZED ~OPERATOR

r:;:-, CURRENT TO ~PNEUMATICCONV.

~ ~

f";¡O\ HYDRAUlIC ~OPERATOR

r:::::\ UNSPECIFIED ~OPERATOR

..JA "'D'"

r::';::"1 RESISTANCE TO ~VOLTAGECONV. ~CURRENTTO

VOL TAGE TO PNEUMAnCCONV.

PNEUMATIC OPERATOR

h..L.. STEM ACTION ~ (GLOBE)VALVE

THREE-WAY SELECTOR VAL VE

ROTARYACnON (BALLI VALVE

FEEDBACK PROCESSCONTROL

cent; that is, O percent of measurement yields an output pressure of 3 psi or 20 kPa, 50 percent of measurementyields 9 psi or 60 kPa and 100 percent yields 15 psi or 100 kPa output. Electronic transmitters produce either voltage or current signat outputs. For instance, the output of analog transmitters is commonly 4 to 20 mA dc. Symbols A set of symbols has beenadopted to show instrumentation layouts and to make these layouts more uniformo Once rou become familiar with these symbols, it will become easy to visualize the system. At present, two sets of symbols are in use. One set is provided by the Scientific Apparatus Makers Association (SAMA) and the other by Instrument Society of America (ISA). In ibis book the ISA symbols will be used where applicable. Figure 1-7 and Tables 1-2 and 1-3 describe the symbols and identification letters often used. If rou are involved in the preparation or use of instrument loop diagrams, it is suggested thai rou obtain the publication thai defines the standards employed. A loop diagram musi contain the information needed for both engineering and construction. This includes identification, description, connections and location, as well as energy sources.

The Feedback

Loop

The objective of a control system is to maintain a balance between supply and demand over a period of time. As noted previously, supply and demand are defined in terms of energy or material into (the manipuINSTRUMENT

FOR SINGLE MEASURED

INSTRUMENT

INSTRUMENT MOUNTED ON BOARD

LOCALLY MOUNTED

VARIABLE

INSTRUMENT MOUNTED BEHIND BOARD

NSTRUMENT

FOR TWO

MEASURED

Fig. 1-7. Instrumentfor measuredvariables.

VARIABLES

INTRODUCTIONTO PROCESSCONTROL II

Table 1-3. Meanings of Identification Letters SUCCEEDINGLE1TERS

FIRST LE1TER Measured or Inilialing Variable A

Readoulo, Passive Funclion

Modijier

User'scooice

Voltage (EMF)

F G

F1ow rate

User', choice

User',cboic.

Control

Conductivity (electrical) Density (mass) or specitX:

Modi]ier

Alarrn

Analysis Burner flame

Output Function

Differential

gravity Primary element Ratio (fraction)

Glas.

Gaging (dimensiooal) Hand (manually initiated)

Current

(electrical) Power

Time or time

High

Indicat. Controlstation

scheduIe L

Level

Moisture or

humidity User's cboice

User's cboic.

Oritice (restriction)

Pressure or

Paint (test connection)

Middle or inter-

mediate User's cboice

vacuum Q

Quantity or event

Radioactivi¡y

Speed or

Low

Light (pilot)

Integrate

User'schoice

User's cboice

totalize Recordor pnn! Switch

SafelY

frequency Transmit

Temperature

MuItivariable

Viscosity

w x

Weight or force

Well

Unclassified

Multifunction

Valve, damper, or louver Unclassified

User's cboice

Relay or compute

Position

Drive, actuate or unclassified final control

element

Unclassified

FEEDBACK PROCESSCONTROL

Fig. }-8. Heatexchanger.

lated variable) and out of (the controlled variable) the processo The closed-loop control system achieves this balance by measuring the demand and regulating the supply to maintain the desired balance over time. The basic idea of a feedback controlloop is most easily understood by imagining what an operator would bave to do if automatic control did Dot exist. Figure 1-8 shows a common application of automatic control found in many industrial plants: a beat exchanger that uses steam to beat cold water. In manual operation, the amount of steam entering the beat exchanger depends on the air pressure to the valve, which is set on the manual regulator. To control the temperature manually, the operator would watch the indicated temperature, and by comparing it with thedesired temperature, would open or close the valve to admit more or less steam. When the temperature had reached the desired value, the operator would simply hold that output to the valve to keep the temperature constant. Under automatic control, the temperatufe controller performs the same function. The measurement signat to the controller from the temperature transmitter is continuously compared to the set-point signat entered into the controller. Based on a comparlson of the signats, the automatic controller can tell whether the measurement signat is above or below the set point and move the valve accordingly until the measurement (temperature) comes to its final value. The simple feedback controlloop shown in Figure 1-9 illustrates the four major elements of any feedback controlloop.

INTRODUCTION TO PROCESS CONTROL

+ ~;~OL~:¡'-=- --.or I MEASUREMENT

SUPPLV-* FINAL ACTUATOR

CONTROLLED VARIABLE

Fig. 1-9. Feedbackcontrolloop.

I. Measurementmust be made to indicate the current value of the variable controlled by the loop. Commonmeasurementsused in industry include ftow rate, pressure,level, temperature,analytical measurementssuchas pH, ORPand conductivity; and manyotherg particular to specificindustries. 2. For every processthere mustbe afina! actuator that regulatesthe supply of energyor materialto the processand changesthe measurementsignal. Most oftenthis is somekind of valve, but it might also be a belt or motor speed,louver position, and so on.3. The kinds of processesfound in industrial plants are as varied as the materials they produce. They range from the commonplace, suchas loops to control ftow rate, to the large and complex, such as distillation columns in the petrochemicalindustry. Whether simple or complex, they all consistof somecombinationof capacity resistanceand deadtime.4. The last elementof the loop is the automaticcontroller. Its job is to control the measurement.To "control" meansto keep the measurement at a constant, acceptablevalue. In this chapter, the mechanismsinsidethe automaticcontroller will Dotbe considered. Therefore, the principIesto be discussedmar be applied equally well to both pneumaticand electronic controllers and to the controllers from any manufacturer.All automaticcontrollers use the samegeneralresponses,althoughthe internalmechanismsand the definitions given for these responsesmar differ slightly from one another.

14 FEEDBACK PROCESSCONTROL

One basic concept is thai for automatic feedback control to exist, the automatic controlloop musi be closed. This means thai information musi be continuously passed around the loop. The controller musi be able to move the val ve, the valve musi be able to atrect the measurement, and the measurement signal musi be reported to the controller. If ibis path is broken at any point, the loop is said to be open. As soon as the loop is opened-for example, when the automatic controller is placed on manual-the automatic unit in the controller is no longer able to move the valve. Thus, signats from the controller in response to changing measurementconditions do noi atrect the valve and automatic control does noi exist. Feedback Control Several principIes associated with feedback control can be observed by considering a familiar control situation-adjusting the temperature of water in a bathtub. This is obviously a manually controlled system. One hand feels the water in the tub while the other manipulates the inftow to reach the desired temperature. If a thermometer were used to measure the temperature, greater accuracy would resulto Improved measurement generally results in improved control. The bathtub also illustrates the important effect of process capacity. Capacity (Figure 1-2)is a measure ofthe amount ofenergy it takes to change a system a unit amount; thermal capacity is Btu/°F, or the amount of beat required to increase the temperature 1°F. Since the bathtub has a large capacity, it can be controlled in any of several ways-by partially filling the tub with cold water, for example, and then adding enough bot water to reach the desired temperature; or by mixing the bot and cold to get the same resulto

Controlling

the Process

In performing the control function, the automatic controller uses the difference between the set-point and the measurement signats to develop the output signat to the valve. The accuracy and responsiveness of these signats is a basic limitation on the ability of the controller to control the measurement correctly. If the transmitter does Dot send an accurate signat, or ifthere is a lag in the measurementsignat, the ability of the controller to manipulate the process will be degraded. At the same time, the controller must receive an accurate set-point signat. In

INTRODUCTIONTO PROCESSCONTROL 15

controllers using pneumatic or electronic set-point signals generated within the controller, miscalibration of the set-point transmitter will develop the wrong value. The ability of the controller to position the valve accurately is ret another limitation. If there is friction in the valve, the controller mar Dot be able to move the valve to a specific stem position to produce a specific flow, and this will appear as a difference between measurement and set point. Repeated attempts to position the valve exactly mar lead to hunting in the valve and in the measurement. Or, if the controller is able only to move the valve very slowly, the ability of the controller to control the process will be degraded. One way to improve the response of control valves is to use a valve positioner, which acts as a feedback controller to position the valve at the exact position corresponding to the controller output signal. However, positioners should be avoided in favor of volume boosters on fast-responding loops such as flow and liquid pressure. For proper process control, the change in output Cromthe controller must be in such a direction as to oppose any change in the measurement value. Figure 1-10 shows a direct-connected valve to control

CONTROLLER SPAN OF MEASUREMENT

--rINLET FLOW

,-', ,,"

[[], =

". ,'~~~""'-1

...,...,-

~}f~

-"..,¿"~ 2--=~.;:

-~-=-~_.=~.

f OUTLET

_E/ I 100

I 50

I O

PERCENT OPENING OF VALVE

FLOW

Fig. 1-10. In proportionalcontrol, the controllingvalve's positionis proportionalto the controlled variable(level).

,:--=('i ~--=~ ~I

16 FEEDBACK PROCESSCONTROL

level in a tank at midscale. As the level in the tank rises, the fioat acts to reduce the fiow rate coming in. Thus, the higher the líquid level, the more the fiow will be reduced. In the same way, as the level falls, the fioat will open the valve to add more líquid to the tank. The response of this system is shown graphically. As the level moves from O to 100 percent, the valve moves from fully open to fully closed. The function of an automatic controller is to produce this kind of opposing response over varying ranges. In addition, other responses are available to control the process more efficiently. Selecting

Controller

Action

Depending on the action of the valve, increases in measurement mar require either increasing or decreasing outputs for control. All controllers can be switched between direct and reverse action. Direct action means that, when the controller sees an increasing signal from the transmitter, its output will increase. For reverse action, increasing measurement signals cause the controller output to decrease. To determine which of these responses is correct, an analysis of the loop is required. The first step is to determine the action of the valve. In Figure 1-1, for safety reasons the valve must shut if there is a failure in the plant air supply. Therefore, this valve must be air-toopen, or fail-closed. Second, consider the effect of a change in measurement. For increasing temperature, the steam ftow to the beat exchanger should be reduced; therefore, the valve must close. To close this valve, the signal from the automatic controller to the valve must

decrease. Therefore, this controller requires reverse, or increase/ decrease, action. Ifdirect action is selected, increasing signals from the transmitter will result in a larger steam ftow, causing the temperature to increase further. The result would be a runaway temperature. The same thing will occur on any decrease in temperature, causing a falling temperature. Incorrect selection of the action of the controller always results in an unstable controlloop as soon as the controller is put into automatic. Assuming that the proper action is selected on the controller, how does the controller know when the proper output has been reached? In Figure 1-10, for example, to keep the level constant, a controller must manipulate the ftow in to equal the ftow out. Any difference will cause the level to change. In other words, the ftow in, or supply, must balance the ftow out, or demandoThe controller performs its job by maintaining this balance at a steady rate, and acting to restore this balance between supply and demand whenever it is upset.

INTRODUCTION TO PROCESS CONTROL

U psets

There are three conditions that require different ftows to maintain the level in the tank. First, if the position of the output hand valve is opened slightly, more ftow leaves the tank, causing the level to fall. This is a change in demand, and to restore balance, the inlet ftow valve must be opened to supply a greater ftow rate. A second type of unbalanced condition is a change in the set point. Maintaining any other level besides midscale in the tank causes a different ftow out. This change in demand requires a different input valve position. The third type of up set is a change in the supply. If the pressure output of the pump increases, even though the inlet valve remains in the same position, the increased pressure causes a greater ftow, which at first causes the level to begin to rise. Sensingthe increased measurement, the level controller must close the val ve on the inlet to hold the level at a constant value. In the same way, any controller applied to the beat exchanger shown in Figure 1-1 must balance the supply ofheat added by the steam with the beat removed by the water. The temperature remains constant if the ftow of beat in equals the ftow of beat out.

Process

Characteristics

and Controllability

The automatic controller uses changes in the position of the final actuator to control the measurement signal, moving the actuator to oppose any change it sees in the measurement signal. The controllability of any process depends on the efficiency of the measurement signal response to these changes in the controller output. For proper control, the measurement should begin to respond quickly, but then Dot change too rapidly. Because of the tremendous number of applications of automatic control, characterizing a process by what it does, or by industry, is an almost hopeless task. However, all processes can be described by the relationship between their inputs and outputs. Figure 1-11 illustrates the temperature response of the beat exchanger when the control valve is opened by manually increasing the controller output signal. At first, there is no immediate response at the temperature indication. Then the temperature begins to change, steeply at first, then approaching a final, constant level. The process can be characterized by the two elements of its response. The first element is the dead time, or the time before the measurement begins to respond. In this example, a delay arises because the beat in the steam must be conducted to the

18 FEEDBACK PROCESSCONTROL

STEAM FLOW

(MANUAL) I

OUTLET

WATER

TEMPERATURE

L~,I"/"""' TIME

Fig. l-Il. Responseof beatexchangerto stepupset.

water before it can affect the temperature, and then to the transmitter before the change can be seen. Dead time is a function of the physical dimensions of a process and such things as belt speeds and mixing rates. Second, the capacity of a process is the material or energy that must enter or leave the process to change the measurements-for example, the gallons necessary to change level, the Btu's necessary to change temperature, or the standard cubic feet of gas necessary to change pressure. The measure of a capacity is its response to a step input. Specifically, the size of a capacity is measured by its time constant, which is defined as the time necessary to complete 63 percent of its total response. The time constant is a function of the size of the process and the rate of material or energy transfer. For this example, the larger the tank and the smaller the ftow rate of the steam, the longer the time constant. These numbers can be as short as a few seconds, or as long as several hours. Combined with dead time, they define the time it takes the measurement signal to respond to changes in the valve position. A process will begin to respond quickly, but then not change too rapidly, if its dead time is small and its capacity is large. In short, the larger the time constant of capacity compared to the dead time, the better the controllability of the processo

Controli er Responses

The first and most basic characteristicoí the controller responsehas beenshownto be either direct or reverseaction. Oncethis distinction

-..TIME

INTRODUCTION TO PROCESS CONTROL

has been made, severa! types oí responses are used to control a processoThese are (1) on/otI, two-position, control, (2) proportional action, (3) integral action (reset), and (4) derivative action. On/off Control

On/off control is illustrated in Figure 1-12for a reverse-acting controller and an air-to-close valve. An on/off controller has only two outputs, either full maximum or full minimum. For this system, it has been determined that, when the measurement falls below the set point, the valve must be closed to cause it to increase. Thus, whenever the signal to the automatic controller is below the set point, the controller output will be 100 percent. As the measurement crosses the set point, the controller output goes to O percent. This eventually causes the measurement to decrease, and as the measurement again crosses the set point, the output goes to maximum. This cycle will continue indefinitely because the controller cannot balance the supply against the load. This continuo us oscillation mar or mar Dot be acceptable, depending on the amplitude and length ofthe cycle. Rapid cycling causes freqüent upsets to the plant supply system and excessive valve wear. The time of each cycle depends on the dead time in the process because the dead time determines the time it takes for the measurement signal to reverse its direction once it crosses 'the set point and the output of the controller changes. The amplitude of the signal depends on how rapidly the measurement signal changes during each cycle. On large capacity processes, such as temperature vats, the large capacity causes

MEASUREMENT

100 % SIGNAL TO VALVE

Fig. 1-12. On-off control for reverse-actingcontrollerand air-to-closevalve.

20 FEEDBACK PROCESSCONTROL

Fig. 1-13.Automatic controller with artificial signal.

a long time constant. Therefore, the measurement can change only slowly. As a result, the cycle occurs within a very narrow band around the set point, and this control mar be quite acceptable, if the cycle is Dot too rapid. The on/off control is the one used most frequently in commercial and domestic installations. However, if the process measurement is more responsive to changes in the supply, the amplitude and frequency ofthe cycle begins to increase. At some point, this cycle will become unacceptable and some Corm of proportional control will be required. In order to study the remaining three modes of automatic control, open-loop responses will be used. Open-Ioop means that only the response ofthe controller will be considered. Figure 1-13shows an automatic controller with an artificial signal Croma manual regulator introduced as the measurement. The set point is introduced normally and the output is recorded. With this arrangement, the specific controller responses to any desired change in measurement can be observed. Proportional

Action

Proportional response is the basis for the three-mode controller. If the other two, integral and derivative are present, they are added to the proportional response. "Proportional" means that the percent change in the output of the controller is some multiple of the percent change in the measurement. This multiple is caUedthe "gain" ofthe controUer. For some controUers, proportional action is adjusted by such a gain adjustment, while for others a "proportional band" adjustment is used. Both bave the same purposes and effect. (See Appendix for table showing the controUer adjustments from one manufacturer to another.) Figure 1-14 iUustrates the response of a proportional controUer from an inputl output pointer pivoting on one ofthree positions. With the pivot in the center between the input and the output graph, 100 percent change in

INTRODucnON TO PROCESSCONTROL 21

% OUTPUT

Fig. 1-14.Responseof proportionalcontroller, input to output, for three proportional band values.

measurement is required to obtain 100percent change in output, or full va1vetrave1. A controller adjusted to respond in this way is said to bave a 100 percent proportiona1 band. When the pivot is moved to the righthand position, the measurement input wou1d need to change by 200 percent in order to obtain full output change from Oto 100percent. This is c'alled a 200 percent proportiona1 band. Finally, if the pivot were in the 1eft-hand position, and if the measurement moved over on1y 50 percent of the sca1e,the output wou1dchange over 100 percent of the scale. This is called a 50 percent proportiona1 band. Thus, the smaller the proportional band, the smaller amount the measurement must change to cause full valve travel. In other words, the smaller the proportional band, the greater the output change for the same size measurement change. This relationship is illustrated in Figure 1-15. This graph shows how the controller output will respond as a measurement

Fig. 1-15. ProportionaI diagram.

22 FEEDBACK PROCESSCONTROL

deviates from set paint. Each line on the graph represents a particular adjustment of the proportional band. Two basic properties of proportional control can be observed from this graph: 1. For every value of proportional band, whenever the measurement equals the set paint, the normal output is 50 percent. 2. Each value of the proportional band defines a unique relationship between measurement and output. For every measurement value there is a specific output value. For example, using the 100percent proportional band line, whenever the measurement is 25 percent above the set paint, the output from the controller must be 25 percent. The output from the controller can be 25 percent only if the measurement is 25 percent above the set paint. In the same way, whenever the output from the controller is 25 percent, the measurement will be 25 percent above the set paint. In short, there is one specific output value for every measurement value. For any process controlloop, only one value of the proportional band is the best. As the proportional band is reduced, the controller response to any change in measurementbecomes increasingly greater. At some paint, depending on the characteristic of each particular process, the response in the controller will be large enough to drive the measurement back so far in the opposite direction as to cause constant cycling of the measurement. This proportional band value, known as the ultimate proportional band, is a límit on the adjustment of the controller in that loop. On the other hand, if too wide a proportional band is used, the controller response to any change in measurement is too small and the measurement is Dot controlled as tightly as possible. The determination of the proper proportional band for any application is part of the tuning procedure for that loop. Proper adjustment of the proportional band can be observed by the response ofthe measurement to an upset. Figure 1-16shows several examples ofvarying the proportional band for the beat exchanger. Ideally, the proper proportional band will produce one-quarter amplitude damping, in which each halí cycle is one-half the amplitude of the previous halí cycle. The proportional band that will cause onequarter wave damping will be smaller, thereby yielding tighter control over the measured variable, as the dead time in the process decreases and the capacity increases. One consequence of the application of proportional control to the basic controlloop is offset. Offset means that the controller will maintain the measurement at avalue different from the set paint. This is most easily seen in Figure 1-10. Note that ifthe load valve is opened,

INTRODUCTIONTO PROCESSCONTROL 23

WATER FLOW (LOAO)

i I

1~ TEMPERATURE

-j/'\/,~"-",,, I

,-~

PROPORTI ONA L BAND

TOOWIOE

CHANGE IN UEMANO

B C

TOO NARROW CORRECT

TIME

Fig. 1-16. Examples of varying proportional band for beat exchanger.

ftow will increase through the valve and the val ve would bave to open. But note that, because of the proportional action of the linkage, the increased open position can be achieved only at a lowered level. Stated another way, in order to restore balance between the ftow in and the ftow out, the level must stabilize at avalue below the set point. This difference, which will be maintained by the control loop, is called offset, and is characteristic of the application of proportional-only control to feedback loops. The acceptability ofproportional-only control depends on whether this offset can be tolerated. Since the error necessary to produce any output decreases with the proportional band, the narrower the proportional band, the less the offset. For large capacity, small dead time applications accepting a very narrow proportional band, proportional-only control will probably be satisfactory, since the measurement will remain within a small percentage band around the set point. If it is essential that there be no steady state difference between measurement and set point under all load conditions, an additional function must be added to the controller. This function is called integral action (an older term is reset). Integral

Action

(Reset)

The open-loop response of the integral mode is shown in Figure 1-17, which indicates a step change in the artificial measurement away from the set point at some instant in time. As long as the measurement remains at the set point, there is no change in the output due to the integral mode in the controller. However, when any error exists between measurement and set point, the integral action will cause the output to begin to change and continue to change as long as the error

24 FEEDBACK PROCESSCONTROL

% MEASUREMENT

L_-

SET paiNT

I I I

...riME Fig. l-I?

Open-loop response oCintegral mode.

exists. This function, then, causes the output to change until the proper output is achieved in order to hold the measurement at the set paint at various loads. This response is added to the proportional response of the controller as shown in Figure 1-17. The step change in the measurement first causes a proportional response, and then an integral response, which is added to the proportional. The more integral action there is in the controller, the more quickly the output changes due to the integral response. The integral adjustment determines how rapidly the output changesas a function oftime. Among the various controllers manufactured, the amount of integral action is measured in one of two ways-either in minutes per repeat, or the number of repeats per minute. For controllers measuring integral action in minutes per repeat, the integral time is the amount of time necessary for the integral mode to repeat the open-loop response caused by proportional mode, for a step change in error. Thus, for these controllers, the smaller the integral number, the greater the action of the integral mode. On controllers that measure integral action in repeats per minute, the adjustment indicates how many repeats of the proportional action are generated by the integral mode in one minute. Table 12-1 (p. 300) relates the controller adjustments from one manufacturer to another. Thus, for these controllers, the higher the integral number, the greater the integral action. Integral time is shown in Figure l-IS. The proper amount of integral action depends on how fast the measurement can respond to the additional valve trave 1 it causes. The controller must nat drive the valve faster than the dead time in the process allows the measurement to respond, or the valve will reach its límits before the measurement can be brought back to the set paint. The valve will then remain in its extreme position until the measurement crosses the set paint, whereupon the controller will drive the valve to its opposite extreme, where it

INTRpDUCTION TO PROCESSCONTROL 25

% MEASUREMENT

~ ,

:+-RT

% OUTPUT

(I/D)

SET paiNT

-+1

RT. RESETTIME MIN./RPT.

::::::""J--r-

b~I~

I I

a. b

TIME

Fig. l-IS. Open-loopresponseoCproportional plus integralmodes.

will remain until the measurementcrosses the set point in the opposite direction. The result will be an integral cycle in which the valve travels from one extreme to another as the measurementoscillates around the set point. When integral action is applied in controllers on batch processes, where the measurement is away from the set point for long periods between batches, the integral may drive the output to its maximum, resulting in "integral wind-up." When the next batch is started, the output will Dot corne off its maximum until the measurement crosses the set point, causing large overshoots. This problem can be prevented by including a "batch function" in the controller, a function specifically designed to prevent "wind-up."

Derivative

Action

The third response found on controllers is the derivative mode. Whereasthe proportional mode respondsto the size of the error and the integral mode respondsto the size and time duration of the error, the derivative moderespondsto how quickly the error is changing.ln Figure 1-19,two derivative responsesare shown.The first is a response to a stepchangeof the measurementaway from the set point. For a step, the measurementis changinginfinitely fast, and the derivative mode in the controller causesa considerablechangeor spike in the output, which dies immediatelybecausethe measurement hasstopped changingarterthe step. The secondresponseshowsthe responseofthe derivative mode to a measurementthat is changingat a constantrate. The derivative output is proportionalto the rate of changeofthis error. The greaterthe rate of change,the greaterthe output dueto the deriva-

...TIME

26 FEEDBACK PROCESSCONTROL

% MEASUREMENT

-_J==~

--~

"~!

-t__J-

% OUTPUT

(IlO)

+TIME J...

~ Fig. 1-19. Two derivative responses.

tive response. The derivative holds this output as long as the measurement is changing. As soon as the measurementstops changing, regardless oíwhether it is at the set point, above or below it, the response due to derivative action will cease. Among all brands oí controllers, derivative response is commonly measured in minutes, as shown in Figure 1-20. The derivative time in minutes is the time that the open-loop, proportional-plus-derivative response, is ahead oí the response due to proportional action alone. Thus, the greater the derivative number, the greater the derivative response. Changes in the error are the result oí changes in either the set point or the measurement, or both. To avoid a large output spike caused by step changes in the set point, most modem controllers apply derivative action only to ehanges in the measurement. Derivative action in controllers helps to control processes with especially large time constants. Derivative action is unnecessary on

% MEASUREMENT

DT' DERIVATIVE TIME, MINUTES

DT"" I

:.:::~J % OUTPUT

::::::::::~' .f"

PROPORTIONAL ONLY

PROPORTIONAL + DERIVATIVE

Fig. 1-20. Open-loop response oCproportional plus derivative modes.

INTRODUCTIONTO PROCESSCONTROL 27

processes thai respond fairly quickly to valve motion, and cannot be used at all on processes with noise in the measurement signal, such as flow, since the derivative in the controller will respond to the rapid changes in measurement it sees in the noise. This will cause large and rapid variations in the controller output, which will keep the valve constantly moving up and down, wearing the valve and causing the measurement to cycle. As previously described, the response of an element is commonly expressed in terms of a time constant, defined as the time thai will elapse until an exponential curve reaches 63.2 percent ora step change in input. Although the transmitter does nat bave an exact exponential response, the time constant for the pneumatic temperature transmitter and its associated thermal system is approximately 2 seconds. The reaction curve shown in Figure 1-21 incorporates the response of the beat exchanger and measuring system, and it represents the signal thai will actually reach the controller. This curve indicates thai, given a sudden change inside the beat exchanger, more than 30 seconds will elapse before the controller receives a signal thai is a true representation of thai change. From the reaction curve, or characteristic, we can determine the type of controller required for satisfactory control under ibis difficult, but common, delayed response characteristic. Selecting

the Controller

The beat exchanger acts as a small-capacity process; thai is, a small change in steam can cause a large change in temperature. Accurate

Fig. 1-21.The processreactioncurve is obtainedby imposinga stepchangeat input.

28 FEEDBACK PROCESSCONTROL

regulation of processes such as this calls for proportional rather than on/otI control. Variations in water rate cause load changes that produce offset, as described previously. Thus, the integral mode should also be used. Whether or Dot to include the derivative mode requires additional investigation of the process characteristic. Referring to the reaction curve (Figure 1-19), notice that the straight line tangent to the curve at the point of inftection is continued back to the 150°For 66°C (starting) level. The time interval between the start of the upset and the intersection of the tangentialline is marked TA;the time interval from this point to the point of inftection is TB.IfTB exceeds TA,some derivative action will prove advantageous. If TBis less than TA,derivative action mar lead to instability because of the lags involved. The reaction curve of Figure 1-21 clearly indicates that some derivative will improve control action. Thus, a three-mode controller with proportional, integral, and derivative modes satisfies the needs of the beat exchanger processo Figure 1-22shows the combined proportional, integral, and deriva-

Fig. 1-22. Open-loopresponseofthree-modecontroller.

INTRODUCTIONTO PROCESSCONTROL 29

tive responsesto a simulated' beat exchanger temperature measurement thai deviates from the set point due to a load change. When the measurement begins to deviate from the set point, the tirst response from the controller is a derivative response proportional to the rate of change of measurement thai opposes the movement of the measurement away from the set point. This derivative response is combined with the proportional response. In addition, as the integral mode in the controller sees the error increase, it drives the valve further still. This action continues until the measurement stops changing, at which point the derivative response ceases. Since there is still an error, the measurement continues to change due to integral action, until the measurement begins to move back toward the set point. As soon as the measurement begins to move back toward the set point, there is a derivative response proportional to the rate of change in the measurement opposing the return of the measurement toward the set point. The integral response continues, because there is still error, although its contribution decreases with the error. AIso, the output due to proportional is changing. Thus, the measurement comes back toward the set point. As soon as the measurement reaches the set point and stops changing, derivative response again ceases and the proportional output returns to 50 percent. With the measurement back at the set point, there is no longer any changing response due to integral action. However, the output is at a new value. This new value is the reguli ofthe integral action during the time thai the measurement was away from the set point, and compengates for the load change thai caused the original upset.

Conclusion

This chapter has describedthe responsesof a three-modecontroller when it is used in the feedbackcontrol of industrial measurements. The readershouldbave a clear understandingof the following points: 1. In order to achieve automatic control, the control loop musi be closed. 2. In order to maintainastable feedbackcontrolloop, the most important adjustmentto the controller is the selectionof the proper action, either reverseor direct, on the controller. Properselection of tbis action will causethe controller output to changein sucha way thai the movementofthe valve will opposeany changein the measurementseenby the controller. 3. The proper value of the settingsof the proportionalband, the integral mode, and derivative time dependson the characteristicsof

30 FEEDBACK PROCESSCONTROL

the processoThe proportional band is the basic tuning adjustment on the controller. The more narrow the proportional band, the more the controller reacts to changes in the measurement. If too narrow a proportional band is used, the measurement cycles excessively. If too wide a proportional band is used, the measurement will wander and the offset will be too large.4. The function of the integral mode is to eliminate offset. If too much integral action is used, the res uIt will be an oscillation of the measurement as the controller drives the valve from one extreme to the other. If too little integral action is used, the measurement will retum to the set point too slowly.5. The derivative mode opposes any change in the measurement. Too little derivative action has no significant effect. Too much derivative action causes excessive response of the controller and cycling in the measurement.

Questions

l-I. All control systemsthat fit into the usual patternare: a. Open-Ioop c. Closed-loop b. Nonself-regulating d. On/off 1-2. If operatingproperly,automaticcontrol will always: a. Reducemanpower b. Reducecosts c. Make the processoperatemore uniformly d. Decreasemaintenance 1-3. Automatic controllersoperateon the differencebetweenset point and measurement,which is called: a. Offset c. Error b. Bias d. Feedback 1-4. A two-positioncontroller (on/oil) always: a. Controls with a fixed offset b. Controlsarounda point c. Automaticallyadjustsits integraltime d. Requiresprecisetuning 1-5. Gainand proportionalbandsare: a. Reciprocallyrelated b. Two differentcontrol modes c. Adjusted independentlyof one another d. Controllerfunctionscalibratedin time units

INTR9DUCTION TO PROCESSCONTROL 31

1-6. Whenwe adjustintegraltime in a controller: a. We determineanRC time constantin the controller's internalfeedback path b. We adjustthe time it will take for integralto equalderivative c. We setthe processtime constantso that it will alwaysequal1 d. What happensspecificallydependson the type of controller,pneumatic or electronic 1-7. Match the following: Controller, two-position-a. Derivative -b. Deviation-c. Final-controllingelement-d. Proportionalband adjustment-f. Regulatedby control valve -g. Reset-h. Set point-

Gain Rate Integral Controller, on/otI e. Valve Desiredvalue Manipulatedvariable Error

1-8. A proportionalcontroller will bave an otIsetditIerencebetweenset point and control point: a. At all times b. Equal to the proportionalbandsetting c. That dependsuponprocessload d. That will eventuallyvanish 1-9. If it were possiblefor a proportionalcontrollerto bavea true Opercent proportionalband, the controller gainwould bave to be: a. Unity c. 100 b. O d. Infinite 1-10. If the proportionalbandof the controlleris adjustedto minimum possiblevalue,the control actionis likely to be: a. On/otI c. Excellent b. With maximumotIset d. Inoperative I-Il. The following symbol @ representsa: 8. Flow rate controller b. Fixed control point

appearsin an instrumentdiagram.It c. Frequencyconverter d. Final control element

1-12. With a proportional-onlycontroller if measurement equalsset point, the output will be: 8. O

c. 50 percent

b. 100percent

d. Impossibleto define

1-13. If in a proportional-plus-integral controller measurement is away from the set point for a long period,the controller's output will be:

32 FEEDBACK PROCESSCONTROL

8. Oor 100percent,dependingon actionselected b. Unknown c. O

d. 100percent 1-14. In the modemcontroller,derivative actionis appliedonly to the: 8. Error c. Setpoint b. Measurement d. Integral circuit 1-15. The functionof the integral(reset)modeis to: 8. Opposechangein measurement b. Automaticallyadjustthe controller's gain c. Eliminate offset d. Stabilizethe controlloop

Process/Pressure Measuring

Instruments

Pressureis a universalprocessingcondition. It is alsoa conditionoflife on this planet: we live at the bottom of an atmosphericocean that extendsupward for manymiles. This massof air has weight, and this weight pressingdownwardcausesatmosphericpressure.Water, a fundamentalnecessityof life, is suppliedto most of us underpressure.In the typical processplant, pressureinfluencesboiling point temperatures, condensingpoint temperatures,processefficiency, costs, and other important factors. The measurementand control of pressure,or lack of it-vacuum-in the typical processplantis critical. Instruments are availableto measurea wide rangeof pressures.How theseinstruments function is the subjectof this chapter. What Is Pressure?

Pressure is force divideél by the area over which it is applied. Pressure is often defined in terms of "head." For example, assume that we bave a water column 1 foot square and 23 feet tall. We want to find the pressure in the boUom ofthe column. The weight ofthe column mar be calculated by first finding the volume of water. This is the area of the 33

FEEDBACK PROCESSCONTROL

base multiplied by height, or 1 times 23 equals 23 cubic feet. Water weighs 62.43 pounds per cubic foot. So the weight of 23 cubic feet will be 23 times 62.43, or 1,435.89pounds. The area ofthe base is 1 square foot, or 12 inches times 12 inches, or 144square inches. The pressure equals 1,434.89 divided by 144 equals 9.9715, or approximately 10 pounds per square inch. In practice, we find that only the height ofthe water confits. It mar be present in a small pipe or beneath the surface of a pond. In any case, at a depth of 23 feet, the pressure will amo unt to approximately 10 pounds per square inch. If in your home the water pressure is 50 pounds per square inch and the system uses a gravity feed, the water tank, or reservoir, holds the water at a height of 50 divided by 10, or 5 times 23 equals 115 feet above the point where the pressure measurement is made. Head and pressure, then, mar mean the same thing. We must be able to convert from one to the other. You mar encounter reference to inches of mercury for pressure measurement. Mercury is 13.596times as heavy as an equal volume of water. Therefore, ahead ofmercuryexerts apressure 13.596times greaterthan an equivalent head of water. Because it is hazardous, mercury no longer is used commonly in manometers. The head or pressure terms cited thus far are called, collectively, "gauge pressure." For example, if a tire gauge is used to check the pressure in your automobile tires, it measures gauge pressure. Gauge pressure makes no allowance for the fact that on earth we exist under a head of air, or an atmosphere. The height of this head of air varies with elevation, and also to some degree with weather conditions. If rou ride an elevator from the bottom to the top floor of a tall building, rou will likely feel your ears "pop." This is caused by the change in atmospheric pressure. A simple method of measuring atmospheric pressure would be to take a length of small diameter (0.25 inches) glass tubing about 35 inches long, sealed at one end. Fill the tube entirely with mercury and temporarily seal the end. Invert this end into a deep dish of mercury and remo ve the seal. The result will be a column of mercury as shown in Figure 2-1 with some space remaining at the top. Atmospheric pressure on the surface of the exposed mercury will balance the height of mercury in the tube and prevent it from running out of the tube. The height of the mercury above the level in the dish is, then, a measure of atmospheric pressure. At sea level, this would amount to approximately 29.9 inches, or 14.7pounds per square inch. When the etfect of the atmosphere is included in our measurement, we then must use absolute pressure (gauge pressure plus atmospheric pressure).

PROCESS/PRESSURE MEASURINGINSTRUMENTS 35

Fig. 2-1. Mercurybarometer.

Units ot Measurement

Every major country has adopted its own favorite units of measurement. The United States has traditionally employed the English system. However, international trade has made it necessaryto standardize units of measurement throughout the world. Fortunately, during this standardization, there has be en rationalization ofthe measurementsystem. This has led to the adoption of the System lnternatíonal d'Unítes (SI), a metric system of units. The force of common usage is so strong that the familiar English system will undoubtedly persist for many years, but the changeover is definitely underway. The time will soon corne when process industries will deal exclusively with SI units.

Pressure

Measurement

Perhaps the area that has caused the most concern in the change to SI units is pressure measurement. The new unit of pressure, the pascal, is unfamiliar even to those who have worked in the older CGS (centimetre, gram, second) metric system. Once it is accepted and understood, it willlead to a great simplification of pressure measurement Cromthe extremes of full vacuum to ultrahigh pressure. It will reduce the multiplicity ofunits now common in industry to one standard that is compatible with other measurements and calculations. To understand the pascal and its relationship to other units of pressure measurement, we must return to a basic understanding of pressure. As noted previously, pressure is force per unit area.

36 FEEDBACK PROCESSCONTROL

From Newton's laws, force is equal to magstimes acceleration. In the English system, the distinction between mags and force became blurred with common usage of terms such as weight and mags. We live in an environment in which every object is subject to gravity. Every object is accelerated toward the center of the earth, unless it is restrained. The force acting on each object is proportional to its mags. In everyd ay terms ibis force is called the weight of the objecto W= m' G

where: W = weight of the object m = its mass G = accelerationdue to gravity Because gravity on the earth's surface is roughly constant, it has been easy to talk abolli a weight of 1 pound and a mass of 1 pound interchangeably. However, in faci, force and mass, as quantities, are as different as apples and pears, as the astronauts bave observed. A numbec of schemes bave be en devised to overcome ibis problem. For example, a quantity called the pound-force was invented and made equal to the force on a mass of one pound under a specified acceleration due to gravity. The very similarity between these two units led to more confusiott. The pascal, by its definition, removes all these problems. The Pascal The SI unit of pressure is defined as the pressure or stress that arises when a force of one newton (N) is applied uniformly over an area of one square metre (m2). This pressure has been designated one pascal (Pa). Thus, Pa = N/m2. This is a small unit, but the kilopascal (KPa), 1,000 pascals, and the megapascal (MPa), one million pascals, permit easy expression of common pressures. The definition is simple, because gravity has been eliminated. The pascal is exactly the same at every point, even on the moon, despite changes in gravitational acceleration. In SI units, the unit offorce is derived from the basic unit for mass, the kilogram (kg), and the unit of acceleration (metres per second per second, mls2). The product of mass times acceleration is force and is

Gauge,

PROCESS/PRESSURE MEASURING INSTRUMENTS 37

designated in newtons. One newton would be the force of one kilogram accelerating at one metre per second per second (N = kg' mls2). Bar versus Pascal

After the introduction of SI units, the use of the "bar" (lOSPa) gained favor, especially in European industry, where it closely resembles the CGS unit of kg/cm2 (kilograms per square centimetre). At thai time, the SI unit was called the "newton per square metre." As well as being quite a mouthful, it was found to be inconveniently small (one N/m2 equals 0.000145psi). The use ofthe millibar in meteorology lent weight to the acceptance of the bar. However, the use of a multiple like (lOS)in such an important measurement and the resulting incompatibility of stress and pressure units led to the adoption ofthe N/m2, giving it a new name, the pascal (Pa), in October 1971. The kilopascal (kPa), 1,000 pascals, equals 0.145 psi and most common pressures are thus expressed in kPa. The megapascal(mPa) equals 145 psi and is convenient for expressing high pressures. Absolute,

and Differential

Pressure

The pascal can be used in exactly the same way as the English or CGS metric units. The pascal may be regarded as a "measuring gauge," the size ofwhich has been defined and is constant. This gauge can be used to measure pressure quantities relative to absolute vacuum. Used in this way, the results will be in pascal (absolute). The gauge may also be used to measure pressures relati ve to the prevailing atmospheric pressure, and the results will be pascal (gauge). Ifthe gauge is used to measure the difference between pressures, it becomes pascal (differen-

tial). The use of gauge pressure is extremely important in industry, since it is a measure ofthe stress within a vesseland the tendency offtuids to leak auto It is really a special case of differential pressure measurement, inside versus outside pressure. Where there is any doubt about whether a pressure is gauge, differential, or absolute, it should be specified in full. However, it is common practice to shaw gauge pressure without specifying, and to specify by saying "absolute" or "differential" only for absolute or differential pressures. The use of "g" as in psig is disappearing, and the use of "a" as in psia is frowned upon. Neither g flor a is recognized in SI unit symbols. However, M is recognized for differential pressure in all units.

38 FEEDBACK PROCESSCONTROL

Understanding

the Effects

of Gravity

Before discussing the effects of gravity on pressure measurement, it is well to keep in mind the size of error thai can arise if gravity is regarded as constant. The "standard" gravitational acceleration is 9.806650rn/S2.This is an arbitrary figure selected as a near average of the actual acceleration due to gravity found all over the earth. The following are typical values

at different places: Melbourne (Australia) Foxboro (USA) Soest (The Netherlands)

9.79966 rn/S2 9.80368 rn/S2 9.81276 rn/S2

Hence the difference around the world is approximately :t 0.1 percent from the average. This is oflittle practicat importance in industrial applications. However, with some transmitters being sold with a rated accuracy of :t0.25 percent, it is well to consider the effect of a gravityinduced difference of more than halí the tolerance thai can arise if the transmitter was calibrated in Europe and tested in Australia. Gravity-Dependent

Units

Units such as psi, kglcm2, inches of water, and inches of mercury (Hg) are all gravity dependent. The English unit pounds per square inch (psi) is the pressure generated when the force of gravity acts on a mass of one pound distributed aveT one square inch. Consider a dead weight tester and a standard mass of one pound which is transported around the earth's surface: the pressure at each paint on the earth will vary as the gravitational acceleration varies. The same applies to units such as inches of water and inches of mercury. The force at the bottom of each column is proportional to the height, density, and gravitational acceleration. Dead weight testers are primary pressure standards. They generate pressure by applying weight to a piston that is supported by a fluid, generally oil or air. By selecting the weights and the cross-sectional aTea of the piston, the pressure generated in any gravity field can be calculated. Therefore, dead weight testers are gravity dependent. For accurate laboratory work, the gravity under which the tester was calibrated and that at the place of use must be taken into account. Similarly, the pressure obtained by a certain height of fluid in a manometer depends on density and gravity. These factors must be corrected for the

PROCESS/PRE:SSURE MEASURINGINSTRUMENTS 39

existing conditions ifprecision regulis are to be obtained. Factors given in the conversion tables in the Appendix, it should be noted, deal with units of force, noi weight. Dead weight testers will be discussed in more detaillater in ibis chapter. Gravity-lndependent

Units

While gravity plays no part in the definition of the pascal, it has the same value wherever it is measured. Units such as pounds-force per square inch and kilogram-force per square centimetre are also independent of gravity because a specific value of gravitational acceleration was selected in defining these units. Under equal gravity conditions, the pound-mass and pound-force are numerically equal (which is the cause of considerable confusion). Under nonstandard gravity conditions (the usual case), correction factors are required to compensate for the departure from standard. It should be noted that the standard value of actual gravity acceleration is llot recognized as such in the SI unit system, where only the SI unit of acceleration of one metre per second per second is used. In the future, only the measured actual gravity at the location of measurement (G) will be used when gravity plays a part in the system under investigation. The pascal is a truly gravity-independent unit and will be used to avoid the presently confusing question of whether a stated quantity is gravity dependent.

Pressure

Standards

Now let us consider the calibration standards that are employed with pressure-measuringinstruments and the basic instruments that are used to measure pressure. It mar help to look at the ways in which the standards for pressure calibration are established. You will recalI that head is the same as pressure. A measure of head, then, can be a dependable measure of pressure. Perhaps the oldest, simplest, and, in many respects, one of the most accurate and reliable ways of measuring pressure is the liquid manometer. Figure 2-2 shows a differential manometer. When only a visual indication is needed and static pressures are in a range that does Dot constitute a safety hazard, a transparent tube is satisfactory. When conditions for the visual manometer are unsuitable, a variety of ftoat-type liquid manometers are often employed.

40 FEEDBACK PROCESSCONTROL

HIGH PRESSURE

Fig. 2-2. Simple U-tube manometer.

The simplest differential gauge is the liquid-filled manometer: it is basic in its calibration and free of frictional effects. It is often used to calibrate other instruments. The most elementary type is the U-gauge, which consists of a glass tube bent in the form of a U, or two straight glass tubes with a pressure connection at the bottom. When a differential pressure is applied, the difference between the heights of the two columns of líquid is read on a scale graduated in inches, millimetres, or other units. In the more advanced designs, vertical displacement of one side of the manometer is suppressed by using a chamber of large surface area on that side. Figure 2-3 shows such a manometer. If the area ratio is in the vicinity of 1,600 to 1, the displacement in the large chamber becomes quite small and the reading on the glass tube will become extremely close to true inches or true millimetres. The large side would have to be of infinite area for the reading in the glass tube to be exact. This problem is sometimes overcome with a special calibration of the scale. However, if the glass tube becomes broken and must be replaced, the scale must be recalibrated. A more common and quite reliable design features a zeroing gauge glass as shown in Figure 2-4. The scale mar be adjusted to zero for each differential pressure change, and the reading mar be taken from a scale graduated in actual units of measurement arter rezeroing. The filling LOW PRESSURE

Fi2. 2-3. Well or reservoirmanometer.

PROCESS/PR¡;:SSURE MEASURINGINSTRUMENTS 41

Fig. 2-4. Well manometerwith zeroingadjustment.

líquid is usually water or mercury, or some other stable fluid especially compounded by the manometer manufacturers for use with their product. Incline manometer tubes, such as those shown in Figure 2-5, will give magnified readings, but must be made and mounted carefully to avoid errors due to the irregularities ofthe tube. It is also essential that the manometers be precisely positioned to avoid errors due to level. Still other types of manometers for functions other than simple indication, including those used with high pressure and hazardous fluids, employ a float on one leg of the manometer. When reading a manometer, there are several potential sources of error. One is the effect of gravity, and another is the effect of temperature on the material contained within the manometer. Correction tables are available which provide the necessary correction for the conditions under which the manometer is to be read. Perhaps even more important is the meniscus correction (Figure 2-6). A meniscus surface should always be read at its center-the bottom, in the case of water, and the top, in the case of mercury. To be practical, gravity and temperature corrections are seldom made in everyday work, but the meniscus correction, or proper reading, must always be taken into account.

HIGH PRESSURE

Fig. 2-5. Inclined manometer.

Fig.

FEEDBACK PROCESSCONTROL

LIQUID GLASS

DOES NOT WEl (MERCURY)

2-6. Readinga manometer.

The dead weight tester is shown in Figure 2-7. The principIe of a dead weight is similar to thai of a balance. Gravity acts on a calibrated weight, which in tom exerts a force on a known area. A known pressure then exists throughout the fluid contained in the system. This fluid is generally a suitable oil. Good accuracy is possible, bot requires thai several factors be well established: (1) the piston area; (2) the weight precision; (3) gravity corrections for the weight if the measurement is to be made in an elevation quite different Crom the original calibration elevation; (4) buoyancy, since as each weight displaces its volume of air, the air weight displaced should also be taken into consideration; (5) the absence offriction; (6) head oftransmitting fluid and (7) operation technique (the weight should be spun to eliminate frictional effect); unless the instrument being calibrated and the tester are at precisely the same level, the head of material can contribute an appreciable error. Perhaps the most important part of the procedure is to keep the piston floating. This is accomplished generally by spinning the weight platform.

--- WEIGHT DEAD WEIGHT

TESTER

Fig. 2-7. Ranges30psiandup: increasepressurewith crank unti! pressuresupportsan accuratelyknownweight. An accuratetestgaugemar beusedwith hydraulic pumpin a similarsetup.

PROCESS/PRE¡SSURE MEASURINGINSTRUMENTS 43

A properly operated dead weight tester should bave a pressure output accurate to a fraction of a percent (actually, 0.1 percent of its calibration or calibrated reading). Still another type of dead weight tester is the pneumatic dead weight tester. This is a self-regulating primary pressure standard. An accurate calibrating pressure is produced by establishing equilibrium between the air pressure on the underside of the ball against weights of known mass on the top. A diagram of an Ametek pneumatic tester is shown in Figure 2-8. In this construction, a precision ceramic ball is ftoated within a tapered stainless steel nozzle. A ftow regulator introduces pressure under the ball, lifting it toward the annulus between the ball and the nozzle. Equilibrium is achieved as soon as the ball beginsto lift. The ball ftoats when the vented ftow equals the fixed ftow from the supply regulator. This pressure, which is also the output pressure, is proportional to the weight load. During operation, the ball is centered with a dynamic film of air, eliminating physical contact between the ball and the nozzle. When weights are added or removed fro~ the weightcarner, the ball rises or drops, affecting the air ftow. The regulator sensesthe change in ftow and adjusts the pressure beneath the ball to bring the system into equilibrium, changing the output pressure accordingly. Thus, regulation of output pressure is automatic with change of weight mass on the spherical piston or ball. The pneumatic dead weight

INSTRUMENT UNOER TEST

Fig. 2-8. Pneumatictester. Courtesyof AMETEK Mfg. CD.

44 FEEDBACK PROCESSCONTROL

tester has an accuracy oí :t 0.1 oí 1 percent oí indicated reading. It is commonly used up to a maximum pressure oí 30 psi or 200 kPa gauge.

Plant Instruments

That Measure

Pressure

Directly

Thus far in tbis chapter we bave been concemed with the detinition of pressure, and some of the standards used bave been described. In the plant, manometers and dead weight testers are used as standards for comparison and calibration. The working instruments in the plant usually include simple mechanical pressure gauges, precision pressure recorders and indicators, and pneumatic and electronic pressure transmitters. A pressure transmitter makes a pressure measurementand generates either a pneumatic or electrical signal output thai is proportional to the pressure being sensed. We will discuss transmitters in detaillater in ibis chapter. Now we will deal with the basic mechanical instruments used for pressure measurement, how they operate and how they are calibrated. When the amount of pressure to be measured is very small, the following instruments might be used. Bell Instrument

This instrument measures the pressure difIerence in the compartment on each gide ora bell-shaped chamber. Ifthe pressure to be measured is gauge pressure, the lower compartment is vented to atmosphere. Ifthe lower compartment is evacuated, the pressure measured will be in absolute units. If the difIerential pressure is to be measured, the higher pressure is applied to the top of the chamber and the lower pressure to the bottom. The bell chamber is shown in Figure 2-9. Pressure ranges as low as Oto 1 inch (Oto 250 Pa) of water can be measured with this instrument. Calibration adjustments are zero and span. The difficulty in reading a manometer accurately to fractions of an inch are obvious, ret the manometer is the usual standard to which the bell difIerential instrument is calibrated. The bell instrument finds applications where very low pressures must be measured and recorded with reasonable accuracy. Slack or Limp-Diaphragm

The slack or limp-diaphragminstrument is used when very small pressuresare to be sensed.The most commonapplicationofthis gauge

Fig.

PROCESS/PRE$SURE MEASURINGINSTRUMENTS 45

2.9. Bell instrument.

is measurement of fumace draft. The range of this type instrument is CromO to 0.5 inches (125 Pa) of water to O to 100 inches (25 kPa) of water above atmospheric pressure. To make this instrument responsive to very small pressures, a large aTea diaphragm is employed. This diaphragm is made of very thin, treated nonporous leather, plastic, or rubber, and requires an extremely small force to deftect it. A spring is always used in combination with the diaphragm to produce a deftection proportional to pressure. Let us assume the instrument shown in Figure 2-10 is being used to measure pressure. The low-pressure chamber on the top is vented tothe atmosphere. The pressure to be measuredis applied to the high-pressure chamber on the bottom. This causesthe diaphragm to move upward. It

Fig. 2-10. Slack or limp-diaphragm instrument.

46 FEEDBACK PROCESSCONTROL

will move until the force developed by pressure on the diaphragm is equal to that applied by the calibrated spring. ln the process of achieving balance, the lever attached to the diaphragm is tipped and this motion transmitted by the sealed link to the pointer. This instrument is calibrated by means of zero and span adjustments. The span adjustment allows the ridged connection to the spring to be varied, thus changing the spring constant. The shorter the spring the greater the spring constant; thus, a greater force is required to deftect it. As the spring is shortened, a higher pressure is required for full deftection of

the pointer. The zero adjustmentcontrols the spring's pivot point, thereby shifting the Creeend of the calibrated spring and its attached linkages. Thrning the zero adjustment changes the pointer position on the scale, and it is normally adjusted to read zero scale with both the high and low pressure chambers vented to the atmosphere. lf pressure , is applied to both the high- and low-pressure chambers, the resultant reading will be in differential pressure. This instrument is extremely sensitive to overrange, and care should be taken to avoid this problem. The other long-term difficulty that can develop is damage to the diaphragm. The diaphragm mar become stiff, develop leaks, or become defective, which results in error. These difficulties mar be observed by periodically inspecting the diaphragm. Pressure Gauges In the process plant, we frequently find simple pressure ganges scattered throughout the process and used to measure and indicate existing pressures. Therefore, it is appropriate to devote some attention to the operation of a simple pressure gauge. The most common of all the pressure ganges utilizes the Bourdon tube. The Bourdon tube was originally patented in 1840. In bis patent, Eugene Bourdon stated: "I bave discovered that if a thin metallic tube be ftattened out then bent or distorted Croma straight line, it has the property of changing its Cormconsiderably when exposed to variations of internal or external pressure. An increase of interna! pressure tends to bring the tube to a straight cylindrical Corm, and the degree of pressure is indicated by the amount of alteration in the Corm of the

tube." Figure 2-11A shows such a tube. As pressure is applied internally, the tube straightens out and returns to a cylindrical Corm. The excursion of the tube tip moves linearly with internal pressure and is converted to pointer position with the mechanism shown. Once the

PROCESS/PRE;SSURE MEASURINGINSTRUMENTS 47

Fig. 2-11. (A) Bourdontube. (B) Typical pressuregauge.

internal pressure is removed, the spring characteristic of the material returns the tube to its original shape. Ifthe Bourdon tube is overranged, that is, pressure is applied to the point where it can no longer return to its original shape, the gauge mar take a new set and its calibration becomes distorted. Whether the gauge can be recalibrated depends on the extent ofthe overrange. A severely overranged gauge will be ruined, whereas one that has been only slightly overranged mar be recalibrated and reused. Most gauges are designed to handle approximately 35 percent of the upper range value as overrange without damage. Typically, a gauge will exhibit some amo unt of hysteresis, that is, a difference due to pressure moving the tube in the upscale direction versus the spring characteristic of the tube moving it downscale. A typical gauge mar also exhibit some amount of drift, that is, a departure from the true reading due to changes over a long period in the physical properties of the materials involved. All of these sources of error are typically included in the manufacturer' s statement of accuracy for the gauge. A typical Bourdon tube gauge, carefully made with a Bourdon tube that has been temperature-cycled or stress-relieved, will bave an accuracy of :t 1 percent of its upper range value. A carefully made test gauge will bave an accuracy of :t0.25 to 0.50 percent ofits upper range value. The range of the gauge is normally selected so that it operates in the upper part of the middle third of the scale.

48 FEEDBACK PROCESSCONTROL

In addition to the gauges used for visual observations of pressure throughout the plant, the typical instrument shop wi11bave a number of test gauges which are used as calibration standards. The gauge must be vertical to read correctly. A typical pressure gauge is shown in Figure

2-11 B. Liquid

or Steam Pressure

Measurement

Whena liquid pressureis measured,the piping is arrangedto prevent entrappedvaporswhich mar causemeasurement error. If it is impossible to avoid entrappingvapors, vents should be provided at all high points in the line. When steampressureis measured,the steamshouldbe prevented from enteringthe Bourdontube. Otherwise,the hightemperaturemar damagethe instrument.Ifthe gaugeis belowthe paint of measurement, a "siphon" (a singleloop or pigtail in a vertical plane)is provided in the pressureline to the gauge.A co*ck is installed in the lme betweenthe loop and the gauge.In operation,the looptraps condensate,preventing the steamfrom enteringthe gauge. Seals and Purges If the instrument is measuring a viscous, volatile, corrosive, or extremely bot or cold fluid, the use of a pressure seal or a purge is essential to keep the fluid out of the instrument. Liquid seals are used with corrosive fluids. The sealing fluid should be nonmiscible with the measured fluids. Liquid purges are used on bot, viscous, volatile, or corrosive líquids, or líquids containing solids in suspension. The purging líquid must be of such a nature that the small quantities required (in the order of I gph) (4 litres per hour) will not injure the product or processoMechanical seals will be described in detaillater in this chap-

ter. Pulsation Dampener If the instrument is intended for use with a fluid under pressure and subject to excessive fluctuations or pulsations, a deadener or damper should be installed. This will provide a steady reading and prolong the life of the gauge. Two other elements that use the Bourdon principIe are the spiral (Figure 2-12) and helical (Figure 2-13). The spiral and helical are, in effect, multitube Bourdon tubes. Spirals are commonly used for

Fig.

PROCESS/PRESSURE MEASURINGINSTRUMENTS 49

2-12. Spiral.

Fig. 2-13. Helical.

pressure ranges up to o to 200 psi or 1.4 MPa, and helicals are made to measure pressures as high as Oto 80,000 psi or 550 MPa. The higher the pressure to be measured, the thicker the walls ofthe tubing Cromwhich the spiral or helical is constructed. The material used in the construction mar be bronze, beryllium copper, stainless steel, or a special NiSpan C alloy. Spirals and helicals are designed to provide a lever motion of approximately 45 degrees with full pressure applied. If this motion is to be translated into pen or pointer position, it is common practice to utilize a four-bar linkage, and this necessitates a special calibration technique. If, instead of measuring gauge pressure, it is necessary to read absolute pressure, the reading must make allowances for the pressure of the atmosphere. This mar be done by utilizing an absolute double spiral element. In tros element, two spirals are used. One is evacuated and sealed; the second has the measured pressure applied. The evacuated sealed element makes a correction for atmospheric pressure as read on the second element. Thus, the reading can be in terms of absolute pressure, which is gauge plus the pressure of the atmosphere, rather than gauge. An absolute double spiral element of this type mar be used to measure pressures up to 100 psi or 700 Kpa absolute. This element is shown in Figure 2-14. Metallic

Bellows

A bellows is an expandableelementmade up of a series of folds or corrugationscalled convolutions(Figure 2-15).Wheninternalpressure is appliedto the bellows, it expands.Becausea sizablearcais involved.

SO FEEDBACK PROCESS CONTROL

Fig. 2-14. Absolutedoublespiral.

the applied pressure develops a sizable force to actuate an indicating or recording mechanism. (In some instruments, the bellows is placed in a sealed can and the pressure is applied externally to the bellows. The bellows will then compress in a fashion similar to the expansion just described. Such an arrangement is shown in Figure 2-16). A variety of materials are used to fabricate bellows, including brass, beryllium copper, copper nickel alloys, phospher bronze, Monel, steel, and stainless steel. Brass and stainless steel are the most commonly used. Metallic bellows are used from pressure ranges of a few

Fig. 2-15. Bellows receiver unit.

PROCESS/PRESSURE MEASURINGINSTRUMENTS 51

Fig. 2-16. Bellows in sealedcan.

ounces to many pounds per square inch. A bellows will develop many times the power available from a helical, spiral, or Bourdon tube. A bellows is typically rated in terms of its equivalent square inch area. To create a linear relationship between the excursion of the bellows and the applied pressure, it is common practice to bave the bellows work in conjunction with a spring, rather than with the spring characteristic of the metal within the bellows itself. Each bellows and spring combination has what is called a spring rate. The springs used with the bellows are usually either helical or spiral. Typically, the spring rate of the helical spring is ien times or more thai of the bellows material itself. Using a spring with a bellows has several advantages over relying on the spring characteristics of the bellows alone. The calibration procedure is simplified, since adjustments are made only on the spring. Initial tension becomes zero adjustment and the number of active turos becomes span adjustment. A spring constructed of stable material will exhibit long-term stability thai is essential in any component. .When a measurement of absolute pressure is to be made, a special mechanism employing two separate bellows mar be used. It consists of a measuring bellows and a compensating bellows, a mounting support, and an output lever assembly (Figure 2-17). The measuring and compensating bellows are fastened to opposite ends of the fixed mounting support: the free ends of both bellows are attached to a movable plate mounted between them. The motion of ibis movable plate is a measure of the difference in pressure between the two bellows.

52 FEEDBACK PROCESSCONTROL

Fig. 2-17. Absolutepressurebellows.

Since the compensating bellows is completely evacuated and sealed, ibis motion is a measure of pressure above vacuum, or absolute pressure applied to the measuring bellows. This movable plate is attached to the output lever assembly which, in turo, is linked to the instrument pen, or pointer. In many applications, the bellows expands very little, and the force it exerts becomes its significant output. This technique is frequently employed in force-balance mechanisms which will be discussed in some detail in Chapter 8.

Pressure

Transmitters

Signal Transmissions

In the process plant, it is impractical to locate the control instruments out in the plant near the processoIt is also true thai mostmeasurements are Dot easily transmitted from some remote location. Pressure measiIrement is an exception, but if a high pressure measurement of some dangerous chemical is to be indicated or recorded several hundred feet from the point of measurement, a hazard will be created. The hazard mar be from the pressure and/or from the chemical carried in the line. To eliminate ibis problem, a signal transmission system was developed. In process instrumentation, ibis system is usually either pneumatic (air pressure) or electrical. Becauseibis chapter deals with pressure, the pneumatic, or air pressure system, will be discussed first. Later it will become evident thai the electrical transmitters perform a similar function.

PROCESS/PRESSURE MEASURINGINSTRUMENTS 53

U sing the transmission system, it will be possible to install most of the indicating, recording, and control instruments in one location. This makes it practical for a mínimum number of operators to rUll the plant efficiently. When a transmission system is employed, the measurementis converted to a pneumatic signal by the transmitter scaled from O to 100 percent ofthe measured value. This transmitter is mounted close to the point of measurement in the processo The transmitter output-air pressure for a pneumatic transmitter-is piped to the recording or control instrument. The standard output range for a pneumatic transmitter is 3 to 15 psi, 20 to 100kPa; or 0.2 to 1.0 bar or kg/cm2. These are the standard signals that are almost universally used. Let us take a closer look at what this signal means. Suppose we have a field-mounted pressure transmitter that has been calibrated to a pressure range of 100 psi to 500 psi (689.5 to 3447.5 kPa). When the pressure being sensedis 100psi (69 kPa), the transmitter is designed to produce an output of 3 psi air pressure (or the approximate SI equivalent 20 kPa). When the pressure sensedris es to 300 psi (2068.5 kPa), or midscale, the outputwill climb to 9psi, or 60kPa, and at top scale, 500 psi (3447.5 kPa), the signal output will be 15 psi, or 100kPa. This signal is carried by tubing, usually V4-inchcopper or plastic, to the control room, where it is either indicated, recorded, or fed into a controller. The receiving instrument typically employs a bellows element to convert this signal into pen or pointer position. Or, if the signal is fed to a controller, a bellows is also used to convert the signal for the use of the controller. The live zero makes it possible to distinguish between true zero and a dead instrument. The top scale signal is high enoughto be useful without the possibility of creating hazards. Pneumatic Recorders and Indicators Pressure recorders and indicators were described earlier in this chapter. Pneumatic recorders and indicators differ only in that they always operate from a standard 3 to 15 psi or 20 to 100 kPa signal. The indicator scale, or recorder chart, mar be 1abeledO to 1,000 psi. This would represent the pressure sensed by the measuring transmitter and converted into the standard signat that is transmitted to the receiver.

54 FEEDBACK PROCESSCONTROL

The receiver converts the signat into a suitable pen or pointer position. Because the scale is labeled in proper units, it is possible to read the

measuredpressure. A typical pneumatic indicator is shown in Figure 2-18 (top) and its operation mar be visualized by studying Figure 2-18 (bottom, right). The input signal passes through an adjustable needle valve to provide damping, then continues to the receiver bellows. This bellows,

Fig. 2-18. Pneumaticindicator.

PROCESS/PRESSURE MEASURING INSTRUMENTS

acting in expansion, moves a fQrce plate. A spring opposing the bellows provides zero and span adjustments. Regulating the amo unt of spring used (its effective length) provides a span adjustment. Setting the initial tension on the spring provides a zero adjustment. The force plate is connected to a link thai drives the pointer arbor assembly. Changing the length ofthe link by turning the Dut on the link provides an angularity adjustment. The arm connecting the pointer and the arbor is a rugged crushed tube designed to reduce torsional effects. A takeup spring is also provided to reduce mechanical hysteresis. Overrange protection is provided to prevent damage to the bellows or pointer movement assembly for pressures up to approximately 30 psi or about 200 kPa. A pneumatic recorder also uses a receiver bellows assembly as shown in Figure 2-19 (top). This receiver provides an unusually high torque due to an effective bellows area of 1.1 square inches. The input signal tirst passesthrough an adjustable damping restrictor. The output of this signat is the input to the receiver bellows assembly. The receiver consists of a heavy duty impact extruded aluminum can containing a large brass bellows working in compression. The large effective area of the bellows assures an extremely linear pressure-topen position relationship. The motion, created by the input signal, is picked up by a conventionallink and transferred to an arbor. Calibration is easily accomplished by tuming zero, span, and angularity adjustments on ibis simple linkage system. All calibration adjustments are accessible through a door (Figure 2-19) on the gide of the instrument and mar be made while instrument is in operation. The arm interconnecting the pen and the arbor incorporates a rugged tubular member to reduce torsional effects and takeup spring to reduce mechanical hysteresis. Overrange protection is provided to prevent damage to the bellows or pen movement assembly for pressures up to 30 psi or about 200 kPa. Mechanical

Pressure

Seals

Application A sealedpressuresystemis usedwith a pressuremeasuringinstrument to isolate corrosive or viscousproducts, or products that tend to solidify, from the measuringelementand its connectivetubing.

Definition

A sealedpressuresystemconsistsof a conventionalpressuremeasuring elementor a force-balancepressuretransmittercapsuleassembly

PROCESS/PRESSURE MEASURINGINSTRUMENTS 57

connected, either directly orby capillary tubing, to a pressure seal as seen in Figure 2-20. The system is solidly filled with a suitable líquid transmission medium. The seat itself mar take many forms, depending on process conditions, but consists of a pressure sensitive flexible member, the diaphragm, functioning as an isolating membrane, with a suitable method of attachment to a process vessel or line. Principie or Operation Process pressure applied to the flexible member of the seal assembly forces some of the filling fluid out of the seal cavity into the capillary tubing and pressure measuring element, causing the element to expand in proportion to the applied process pressure, thereby actuating a pen, pointer, or transmitter mechanism. A sealed pressure system offers high resolution and rapid response to pressure changes at the diaphragm. The spring rate ofthe flexible member musi be low when compared with the spring rate of the measuring element to ensure thai the fill volume displacement will full stroke the measuring element for the required pressure range. A low-diaphragm spring rate, coupled with maximum fill volume displacement, is characteristic of the ideal system.

Fig. 2-20. SeaIconnected to 6-inch pressure gauge.

58 FEEDBACK PROCESSCONTROL

A sealed pressure system is somewhat similar to a liquid-filled thermometer, the primary differences being a flexible rather than rígid member at the process, and no initial filling pressure. The flexible member ofthe seal should ideally accommodate any thermal expansion of the filling medium without perceptible motion of the measuring element. A very stiff seal member, such as a Bourdon tube, combined with a low-pressure (high-volume change) element, will produce marked temperature effects Crom both varying ambient or elevated process

temperatures. The Foxboro l3DMP Series pneumatic d/p Cell transmitters with pressure seals (Figure 2-21) measure differential pressures in ranges of O to 20 to O to 850 inches of water or O to 5 to O to 205 kPa at static pressures Cromfull vacuum up to flange ralingo They transmit a proportional 3 to 15 psi or 20 to 100kPa or 4 to 20 mA dc signat to receivers located up to several hundred yards or melers Cromthe point of measurement.

Fig. 2-21. Sealsconnectedto differentialpressuretransmitter.

PROCESS/PRESSURE MEASURING INSTRUMENTS

FiUing Fluids Ideally, the filling fluid used in a sealed pressure system should be noncompressible, bave a high-boiling point, a low-freezing point, a low coefficient of thermal expansion, and low viscosity. It should be noninjurious to the diaphragm and containing parts, and should Dot cause spoilage in the event ofleakage. Silicone-based liquid is the most popular filling fluid. The system is evacuated before the filling fluid is introduced. The system musi be completely filled with fluid and free from any air pockets thai would contract or expand during operation, resulting in erroneous indications at the pen or pointer or in an output signat. The degree of accuracy of any filled pressure system depends on the perfection of the filling operation. Calibration

Techniques

The procedure for calibration of a pressure instrument consists of comparing the reading of the instrument being calibrated with a standard. The instrument under calibration is then adjusted or manipulated to make it agree with the standard. Success in calibration depends Dot only on one' s ability to adjust the instrument, but on the quality of the standard as well. Field Standards Field standards must be reasonably convenient to use and must satisfy the accuracy requirements for the instrument under calibration. A 100inch water column, for example, is extremely accurate but Dot practical to set up out in the plant. For practical reasons, we find that most field standards are test ganges.The test gaugeis quite similar, in most cases, to the regular Bourdon ganges. However, more care has gone into its design, construction, and calibration, making it very accurate. A good quality test gauge will be accurate to within ::\:0.25percent of its span. This is adequate for most field use. Under some conditions, a manometer mar be used in the field. This usually occurs when a low-pressure range is to be calibrated and no other suitable standard is readily available. Portable Pneumatic Calibrator All of the ingredients required to perform a calibration bave been combined into a single unit called a portable pneumatic calibrator. This unit

FEEDBACK PROCESSCONTROL

Fig. 2-22. Portablepneumaticcalibration.Courtesyoí Wallace& Tieman.

contains an accurate pressure gauge or standard, along with a pressure regulator and suitable manifold connections. The portable pneumatic calibrator will accurately apply, hold, regulate, and measure gauge pressure, differential pressure, or vacuum. The gauge case mar be evacuated to make an absolute pressure gauge. The pointer in the operation of the gauge in this calibrator differs in that it makes almost two full revolutions in registering full scale, providing a scale length of 45 inches. This expanded scale makes the gauge very easy to read. The calibrator is available in seven pressure ranges (SI unit ranges). Of these, three are sized for checking 3 to 15 psi or 20 to 100 kPa pneumatic transmission instrumentation. The calibrator is shown in both picture and schematic form in Figures 2-22 and 2-23. The air switching arrangement makes it possible to use the calibrator as both a source or signal and a precise gauge for readout. This portable pneumatic calibrator is manufactured by Wallace and Tieman, Inc., Belleville, New Jersey. Force-Balance

Pneumatic

Pressure

Transmitter

A pneumaticpressuretransmitter sensesa pressureand converts that pressureinto a pneumaticsignatthat mar be transmittedover a reason-

0/1"

PROCESS/PRE~SURE MEASURINGINSTRUMENTS 61

o~ ~~ ;c ~" ~m ~C

~~z mO~ ,,~~ cm~

z ~2 ~~ ~'"

~~~;~:~ ;

[

l ,t'i'

" ",' ~, \Òc: \\'i",:"

Fig. 2-23. Connectionsfor differentpressurereadouts(courtesyof Wallace& Tieman): For GaugePressure:testpressureis appliedto the capsulethroughthe appropriateP connection;the caseis opento atmospherethroughS. For DifferentialPressure:high-testpressureis appliedto the capsulethroUghthe appropriateP connection.Low-testpressureis appliedto the casethroughS. For AbsolutePressure:testpressureis appliedto the capsulethroughthe appropriateP connectionand the caseis continuouslysubjectedto full vacuumthroughS. For Vacuum:the capsuleis opento atmospherethroughconnectionP; the caseis connectedto test vacuumat S. For Positiveand NegativePressures:testpressureis appliedto the capsulethroughthe appropriateP connectionandthe caseis opento atmospherethroughS.

able distance. A receiving instrument is then employed to convert the signat into a pen or pointer position or a measurement input signat to a controller. The Foxboro Model llGL force-balance pneumatic pressure transmitter is an example of a simple, straightforward device that performs this service (Figure 2-24). Before its operation is discussed, the operation of two vital components must be described: the ftapper and the nozzle, or detector; and the pneumatic amplifier, or relay. These two mechanisms are found in nearly every pneumatic instrument. The ftapper and nozzle unit converts a small motion (position) or

62 FEEDBACK PROCESSCONTROL

FLE'~"

Fig. 2-24. ModelllGM pressure transmitter is a force-balance instrument that measures pressure and transmits it as a proportional 3 to 15 psi or 20to 100kPa pneumatic signa!.

force into an equivalent (proportional) pneumatic signal. Flapper movement of only six ten-thousandths of an inch (0.0015 cm) will change the nozzle pressure by 0.75 psi or 5.2 kPa. This small pressure change applied to the pneumatic amplifier or relay becomes an amplified change of 3 to 15 psi or 20 to 100kPa in the amplifier output. Let us take a closer look at the operation of the aÒlplifier or relay. It is shown in a cross-sectional view in Figure 2-25. Pneumatic

Relay

A relay is a pneumatic amplifier. Like its electronic counterpart, the function of the relay is to convert a small change in the input signal (an air pressure signal) to a large change in the output signal. Typically, a 1 psi or 7 kPa change in input will produce approximately a 12 psi or 80 kPa change in output. The supply enters the relay through a port on the surface of the

PROCESS/PRE$SURE MEASURINGINSTRUMENTS 63

INPUT DIAPHRAGM SUPPLY

STEM

VALVE

BALL VALVE OUTPUT EXHAUST

SPRING

Fig. 2-25. Cross-sectionalviewoCamplifier.

instrument on which the Telar is mounted. The input signal (nozzle pressure) enters the Telar through another port and acts on the diaphragm. SÍnce the diaphragm is in contact with a stem valve, the two move in uníson. As the input signal increases, the stem pushes against a ball valve which in turo moves a flat spring, allowing the supply of air to enter the Telar body. Further motion of the stem valve causes it to close off the exhaust port. Thus, when the input pressure increases, the stem (exhaust) valve closes and the supply valve opens; when the input decreases, the stem valve opens and the supply valve closes. This varies the pressure to the output. Principie

ot Operation

The 11GM Pneumatic Transmitter (Figure 2-24) is a force-balance instrument that measures pressure and transmits it as a proportional 3 to 15 psi pneumatic signal (20 to 100kPa). The pressure is applied to a bellows, causing the end of the bellows to exert a force (through a connecting bracket) on the lower end of the force bar. The metal diaphragm is a fulcrum for the force bar. The force is transmitted through the ftexure connector to the range rod, which pivots on the range adjustment wheel. Any movement of the range rod causes a minute change in the clearance between the ftapper and nozzle. This produces a change in the optput pressure from the relay to the feedback bellows until the force of the feedback bellows balances the pressure on the measure-

64 FEEDBACK PROCESSCONTROL

ment bellows. The output pressure which is established by this balance is the transmitted signal and is proportional to the pressure IlPplied to the measurement bellows. Ifthe pressure be measured is high, such as 5,000 psi or 35.MPa, a different sensing to element is employed. The pressure being measured is applied to a Bourdon tube. This pressure tends to straighten the tube and causes a horizontal force to be applied to the lower end of the force bar. The diaphragm seat serves as both a fulcrum for the force bar and as a seal for the pressure chamber. The force is transmitted through a ftexure connector to the range rod, which pivots on the range adjustment wheel. Any movement of the rangerod causes a minute change in the clearance between the ftapper and nozzle. This produces a change in the output pressure from the reláy to the feedback bellows until the force in the bellows balances the force created by the Bourdon tube. The output pressure, which establishes the force-batancing, is the transmitted pneumatic signal that is proportionat to the pressure being measured. This signat is transmitted to a pneumatic receiver to record, indicate, or control. The calibration procedure for this transmitter is the same as for the low pressure transmitter, but the clllibration pressure is developed with a dead weight tester. For safety, oil or liquid, never air, should be used for high pressure calibrations. Pressure measurements found in some applications require that absolute, rather than gauge pressure, be determined. To handle these applications, the absolute pressure transmitter mar be used. Absolute

Pressure Transmitter

The pressure being measured is applied to one side of a diaphragm in a capsule. The space on the other side of the diaphragm is evacuated, thus providing a zero absolute pressure reference (Figure 2-26). The pressure exerts a force on the diaphragm thai is applied to the lower end of the force bar. The diaphragm seal serves both as a fulcrum for the force bar and as a seal for the pressure chamber. The force is transmitted through the ftexure connector to the range bar, which pivots on the range adjustment wheel. Any movement of the range bar causes a minute change in the clearance between the ftapper and nozzle. This produces a change in the output pressure from the relay (Figure 2-26) to the feedback bellows

PROCESS/PRES:sURE MEASURINGINSTRUMENTS 65

i'ig. 2-26. Pneumaticabsolutepressuretransmitter.

until the force in the bellows balances the force on the diaphragm

capsule. The output pressure, which establishes the force-balanée, is the transmitted pneumatic signal, which is proportional to the 'absolute pressure being measured. This signal is transmitted to a pneumatic receiver to record, indicate, or control.

Ouestions 2-1. An ordinary commercial Bourdon gauge has a scale of O psi to 250 psi, and an accuracy of:t 1.percent of span. If the gauge reads 1.75psi, within what maximum and minimum values will the correct pressure fall? 8. 1.74to 1.76psi c. 1.76.5to 1.78.5psi b. 1.72.5to 1.77.5psi d. 1.79to 1.80psi 2-2. 8. b. c.

A manometer, read carefully: Always has zero error Has an error caused by the liquid's impurity unless corrected May bave an error caused by temperature and gravity effects on the various components and so on. d. Has an error that varies only with altitude

66 FEEDBACK PROCESSCONTROL

2-3. a. b. c. d.

Absolutepressurèis: Gaugepressureplus atmosphericpressure Gaugepressurelessatmosphericpressure Gaugepressureplus atmosphericpressuredivided by two Always referencedto a point at the peakof Mt. Washington,NH

2-4. The pressureat the bottomof a pondwhere it is exactly46 feet deep will be: a. 100psi c. 20 psi b. 46 psi d. 20 psi absolute 2-5. The advantagesof makingabsolutepressuremeasurements rather than gaugeare: a. Greateraccuracy b. Eliminateserrors introducedby barometricvariations c. Is more indicativeof true processconditions d. Is more relatedto safetythangaugepressure 2-6. A bellows elementis usedas a receiverfor a 3 to 15psi pneumatic signaland by error a 30-psipressureis appliedto it. The result will be: a. A damagedbellows b. An instrumentin needof recalibration c. No damage d. A severezero shift 2-7. A pressureinstrumentis calibratedfrom 100to 600psi. The spanof this instrumentis: a.600 c. 500 b. 100 d.400 2-8. Instrumentsthat measurepressureare generallyclassifiedas: a. nonlinear c. free of hysteresis b. linear d. Doneof the above 2-9. Whenreadinga manometer,it is goodpracticeto: a. Readat the bottomof the meniscus b. Readat the top of the meniscus c. Read at the centerof the meniscus d. Carefullyestimatethe averageof the meniscus 2-10. If a pressure range of O to 1 inch of water is to be measured and recorded, an instrument capable of doing this would be: a. A bellows c. A Bourdon tube b. A bell with a líquid seal d. A mercury manometer

2-11. Whenmeasuringa pressurethat fluctuatesseverely: a. A large-capacitytank shouldbe installed b. A pulsationdampenershouldbe employed

PROCESSlPRESSURE MEASURINGINSTRUMENTS 67

c. No problemis created d. Readthe peakand minimumand divide by two to obtainthe true pressure 2-12. A measurement of absolutepressureis to be madeusinga mechanism employingtwo separatebellows. Measurementis appliedto one bellowsand the other: 8. Is sealedat an atmosphericpressureof 14.7psi b. Is completelyevacuatedand sealed c. Containsalcoholfor temperaturecompensation d. Has an activeareatwice that of the measuringbellowsand is sealedat a pressuretwice atmospheric 2-13. The dangerof havinga high-pressureline carryinga dangerous chemicalrupture in the control room is: 8. Eliminated by usingspecialduty piping b. Ignored c. Eliminated throughthe useof a transmissionsystem d. Minimized by placingthe line within a protectivebarrier 2-14. The standardpneumatictransmissionsignalmost generallyused in the United Statesis: 8. 3 to 27 psi c. 3 to 15psi b. 10to 50 psi d. 2 to 12psi 2-15. A sealedpressuresystem: 8. Is similar in someways to a liquid-filled thermometer b. Sealsthe processmaterialin the instrument c. Must be usedat a fixed temperature d. Is alwaysusedwith manualtemperaturecompensation 2-16. A pneumaticrelay: 8. Is a setof electricalcontactspneumaticallyactuated b. Is a signalbooster c. Is a pneumaticamplifier d. Containsa regulatoractuatedby a bellows 2-17. Whenthe clearancebetweenflapper and nozzlechangesby 0.0006 inchesthe output of the transmitterwill changeby: 8. 3 psi c. 12psi b. 15psi d. 6 psi 2-18. An instrumentis to be calibratedto measurea rangeof Oto 6,000psi. For sucha calibration: 8. oil or líquid shouldbe used b. Air mustbe used c. An inert gas suchas nitrogenis required d. Any sourceof highpressureis acceptable

68 FEEDBACK PROCESSCONTROL

2-19. The kilopascal(kPa),an SI Ilnit of pressure: a. Is always equivalentto psi x 6.895 b. Isgravity dependent c. Is a force of 1.000newtons (N) applied uniformly over an areaof one squaremetre d. Changessubstantiallyfrom placeto place 2-20. A pneumaticpressuretransmitteris calibratedto a pressurerangeof 100to 500psi. The signaloutput is 10.2psi. Whatis the measuredpressurein psi? 8. 272psi c. 267psi b. 340psi d. 333psi 2-21. A viscoseline is located 100feet from the control roomwherea record of line pressuremustbe made.The maximumpressureis approximately85 psi. Selectthe instrumentationthat canhandlethis job: 8. A sealedsystemwith 100feet of capillaryconnectedto a special elementin a recordinginstrument. b. A sealedsystemconnectedto a nearbypneumatictransmittersendinga signalto a pneumaticreceivingrecorder c. A direct connectedspiral elementrecorder d. A pneumatictransmitterdirectly connectedto the line 2-22. A pressurerecorderreads38 psi and the barometerreads30.12inches of mercury. The absolutepressureis 8. 23.21 psi absolute c. 52.79psi absolute b. 68.12psi absolute d. 38 psi absolute 2-23. The lowestrangesof pressuremar be measuredby 8. a watercolumn c. a bell meter b. a bellows d. a slackor limp-diaphragm 2-24. A slack diaphragmindicatoris to be calibratedOto 1 inch of water. The standardwould likely be: 8. a water column b. a columnof kerosene c. a mercury-filledinclined manometer d. a water-filledinclined manometer

Level

Measurement

Methods

The typical processplant containsmanytanks, vessels,andreservoirs. Their function is to store or processmaterials.Accurate measurement of the contentsof thesecontainersis vital. The materialin the tanks is usually liquid, but occasionallyit mar consistof solids. Initially, level measurementappearsto presenta simple problèm. However, a closerlook soonrevealsa variety of problemsthat mustbe resolved.The materialmar be very corrosive; it mar tendto solidify; it mar tend to vaporize; it mar contain solids; or it mar create other difficulties. The commonmethodsemployed for automatic continuousliquid level measurementsare as follows (seealso Table 3-1): 1. Float-and-cable 2. Displacement(buoyancy) 3. Head (pressure) 4. Capacitance 5. Conductance 6. Radiation(nucleonic) 7. Weight 8. Ultrasonic 9. Thermal 69

70 FEEDBACK PROCESSCONTROL

Table3-1. Liquid Level Measurement Closedor Method Bubbletube Diaphragm box Head Pressure Diff. Pressure Displacement (buoyancy) Float-andCable Weight Radiation (nucleonic) Capacitance Ultrasonic Conductance

Available Upper Range Values

Open

10 in to 250 ft 0.25 to 75 m 4 in to 250 ft 0.lt075m 2 in to many ft. 50 mm to many metres 5 in to many ft. 0.25 to many metres 6 in to 12 ft 0.15 to 3.6 m 3 in to 50 ft. 75 mm to 15 m lnches to Feet mm to m Depends on Tank Dim.

Open

Any type including

Open

corrosive or dirty Clean

Tank

Open Both Both

Condition of Liquid

Any type with proper selection Any type with proper selection Any type with proper selection

Open

Any type

Both

Any type

Wide

Both

Any type

Wide Wide One or more Points

80th

Nonconductive

80th 80th

Any type Conductive

Float-and-Cable A ftoat-and-cable or ftoat-and-tape instrument (Figure 3-1) measures liquid level by transmitting to a mechanism the rise and fall of a ftoat thai rides on the surface of the liquido Mechanisms are available to accommodate level variations ranging from a few inches to many feet. Float-and-cable devices are used primarily in open tanks, whereas ftoat level switches mar be designed to operate in a pressurized tank. Float devices bave the advantage of simplicity and are insensitive to density changes. Their major disadvantage is their limitation to reasonably clean liquids. Thrbulence mar also create measurement problems. The ftoat and cable technique does Dot lend itselfto the transmitter concept as well as do some of the following techniques.

LF;VEL AND DENSITY MEASUREMENTS 71

Fig. 3-1. Float-and-cablerecorder.

Displacement

(Buoyancy)

The displacement, or buoyancy, technique is a type of force-balance transmitter (Figure 3-2). It mar be used to measure liquid level, interface, or density by sensingthe buoyant force exerted on a displacer by the liquid in which it is immersed. The buoyant force is converted by a force-balance pneumatic or electronic mechanism to a proportional 3 to 15 psi, 20 to 100kPa, 4 to 20 mAldc or 10 to 50 mAldc signal.

Fig. 3-2. Buoyancy type level measuring transmitter.

FEEDBACK PROCESSCONTROL

Archimedes' principIe states that a body immersed in a liquid will be buoyed upward by a force equal to the weight of the liquid displaced. The displacer element is a cylinder of constant cross-sectional area and heavier than the liquid displaced. It must be slightly longer than the level change to be measured (Figure 3-3). Since the displacer must accurately sense the buoyant force throughout the full range of measurement, displacer lengths and diameters wiU vary according to the particular process requirements. The formula to determine the buoyant force span for liquid level applications is as foUows:

where: f V Lw L B

= = = = =

buoyant force span (lbf or N) total displacer volume (cubic inches or cubic centimeters) working length of displacer (inches or millimeters) total displacer length (inches or millimeters) a constant (weight of unit volume of water) (0.036 Ibf/in3 or 9.8 x 10-3N/cm3 SG = specific gravity of the líquid The minimum buoyant force span for the buoyancy level transmitters is 1.47 pounds-force or 6.7 newtons. The maximum mass of the displacer-plus-hanger cable must not exceed 12 pounds or 5.4 kilograms (or buoyant force span x 6, whichever is smaller). For a cylindrical displacer, the formula for the volume is:

Fig. 3-3. Buoyancytype level transmitterinstallation.

LEVE.L AND DENSITY MEASUREMENTS

In the above formula, as well as the sizing of displacers, the working volume considered is .1imitedto the cylindrical volume of the displacer and does not include the volume of the dished end pieces or hanger connection. U nless certain precautions are taken, buoyancy transmitters are not recommended for extremely turbulent process conditions. The turbulence mar cause the displacer to swing erratically, resulting in unpredictable measurement effects or physical damage to the displacer, transmitter, or vessel. In such cases, some form of displacer containment should be used. Buoyancy transmitters mar be applied readily to glass-lined vessels, vessels in which a lower connection is not permissible or possible, density applications with ftuctuating pressures or levels, and high-

temperature service. Interface level measurementmar be accomplished by permitting the interface level to vary over the length of the displacer. f = V (B) (SG difi) SG difI = SG lower liquid minus the SG upper liquid Head or Pressure

Measurementof head, or pressure,to determine level is the most common approach.The ways in which level mar be determinedby measuringpressureare many and varied. Some of the more common techniques are presented befe. Hubble Thbe Method In the air purge, or hubble tube system (Figure 3-4), liquid level is determined by measuring the pressure required to force a gas into the liquid at a point beneath the surface. In this way, the level mar be obtained without the liquid entering the piping or instrument. A source of clean air or gas is connected through a restriction to a hubble tube immersed a fixed depth in the tank. The restriction reduces the air flow to a minute amount, which builds up pressure in the hubble tube until it just balances the fluid pressure at the end of the hubble tube. Thereafter, pressure is kept at this value by air bubbles escaping through the liquido Changes in the measured level cause the air pressure in the hubble tube to build up or dropo A pressure instrument connected at this point can be made to register the level or volume of liquido A small V-notch is filed in the bottom of the tube so that air

74 FEEDBACK PROCESSCONTROL

Fig. 3-4. Usingbubblepipe.

emerges in a steady stream of small bubbles rather than in intermittent large bubbles (Figure 3-5). An advantage ofthe hubble tube method is that corrosive or solids bearing líquids can damage only an inexpensive, easily replaced pipe. Diaphragm Box The diaphragm box is shown in Figure 3-6. It is similar to the diaphragm seals used for pressure gauges (Figure 2-20, p. 57) except that the fill is air and the diaphragm is very slack, thin, and flexible. The

DETAlL

OF NOTCH

IN BUBBLE PIPE

Fig. 3-5. Detail or notch in bubblepipe.

LEYEL AND DENSITY MEASUREMENTS 75

Fig. 3-6. Diaphragrn boxo

diaphragmbox is usuallysuspendedfrom a chain. The instrumentthat sensesthe pressurechangesand relatesthemto level mar be mounted above or below the vessel.The diaphragmbox is used primarily for water level measurementin openvessels. Pressure and Differential Pressure Methods Using Differential Pressure Transmitters These are the most popular methods of measuring liquid level and are shown in Figure 3-7. With an open tank, the pressure at the high pressure side of the cell is a measure of the liquid level. With a closed tank, the etfect of tank pressure on the measurement is nullified by piping this pressure to the opposite side of the cell. When a sealing fluid is used, it musi possess a specific gravity higher than that of the liquid in the vessel. The sealing fluid must also be immiscible with the liquid in the vessel.

76 FEEDBACK PROCESSCONTROL

OPEN TANK

Fig. 3-7. Span = xGL Suppression= yGL+ zG,

Span = xGL Suppression= yGL+ zG,

Span = xGL Elevation =/dG. -yGL

Where GL = specific gravity oCliquid in tank G. = specific gravity oCliquid in outside filled line or tines IC transmitter is at level oClower tank tap, or iC air purge is used, z = O. (Note: The density oCthe gas in the tank has been disregarded in these calculations.)

EXAMPLE: Assume an open tank withX = 80 inches,y = 5 inches, and z = 10 inches. The specific gravity ofthe tank liquid is 0.8; the specific gravity of the liquid in the connecting leg is 0.9. Span = 80 (0.8) = 64 inches head of water Suppression = 5 (0.8) + 10 (0.9) = 4 + 9 = 13 inches head of water Range = 13 to 77 inches head of water EXAMPLE:Assume a closed tank with X = 70 inches, y = 20 inches, and d = 100 inches. The specific gravity of the tank liquid is 0.8; a sealing liquid with a specific gravity of 0.9 is Ilsed. Span = 70 (0.8) = 56 inches head of water Elevation = 100 (0.9) -20 = 90 -16

(0.8)

= 74 inches head of water

Range = -74 to -18 inches head of water

LEVEL AND DENSITY MEASUREMENTS 77

Fig. 3-8. The repeateris a flanged,force-balance,pneumaticinstrumentthat measures pressureand delivers an outputequalto the measuredpressure.

(minus sign indicates thai the higher pressure is applied to the low side of the cell.) At times the liquid to be measured possessescharacteristics thai create special problems. Assume, for example, thai the liquid being measured will solidify if it is applied to a wet leg and it is virtually impossible to keep the leg dry. This type of application could use a pressure repeater. The repeater (Figure 3-8) is mounted above the maximum level of the liquid, and the liquid level transmitter is mounted near the bottom ofthe tank. The pressure in the vapor section is duplicated by the repeater and transmitted to the instrument below, (Figure 3-9). Thus, the complications of a wet leg are avoided, and a varying pressure in the tank will Dot atrect the liquid level measurement. The pressure range thai mar be repeated is O to 100 psi or Oto 700 kPa. The supply pressure musi exceed the pressure to be repeated by

78 FEEDBACK PROCESSCONTROL

Fig. 3-9. Liquid-level transmitter(electronicor pneumatic)used with a repeater.

20 psi or 140kPa. A somewhatsimilar configurationmar be arranged by usinga sealedsystemas describedin Chapter2 and shownin Figure 2-21,p. 58. Capacitance If a probe is inserted into a tank and the capacitance measured between it and the tank, a sizable change in capacitance will occur with liquid level. This phenomenon is due primarily to the substantial difIerence between the dielectric constant oí air and that oí the liquid in the tank. This technique is best applied to nonconductive liquids, since it is best to avoid the problems generated by conducting materials like acids

(Figure 3-10).

Fig. 3-10. Capacitance.

LEVEL AND DENSITY MEASUREMENTS 79

Conductance Conductivity level sensors consist of two electrodes inserted into the vessel or tank to be measured. When the level rises high enough to provide a conductive path from one electrode to the other, a relay (solid state or coil) is energized. The relay mar be used for either alarm or control purposes. Conductivity then becomes either point control or an alarm point. The líquid involved must be a conductor and must Dot be hazardous if a spark is created. Level by conductivity finds occasional applications in process plant s (Figure 3-11). Radiation

A radiation level measurement generally consists of a radioactive source on one gide of the tank and a suitable detector on the other. As the radiation passes through the tank, its intensity varies with the amount of material in the tank and can be related to level. One advantage is that nothing comes in contact with the liquido Among the disadvantages are the high cost and the difficulties associated with radioactive materials. Radioactive techniques do bave the ability to solve difficult level-measuring problems (Figure 3-12). Weight

Occasionally the measurement or the contents or a tank is so difficult that Done or the usual schemes will work. When this occurs it may be advantageous to consider a weighing system. Weight cells, either hy-

LlNE

Fig. 3-11. Conductivity.

80 FEEDBACK PROCESSCONTROL

DETECTOR

~~~Jr;~-~~'-==-L__~ \~::::-

\~" \ ::;""""" \ \'

\\"

INDICATOR

~-g

i~CONVERTER

NUCLEONIC(RADIATION) Fig. 3-12. Radiationtechnique.

draulic or strain gauge, are used to weigh the vessel and its contents. The tare weight of the tank is zero adjusted out of the reading, which will result in a signal proportional to tank contents (Figure 3-13). One advantage of the weight system is that there is no direct contact with the contents of the tank and the sensor. However, the system is not economical, and varying densities mar confuse the relationship between signal and true level. Ultrasonic

The ultrasonic level sensor(Figure 3-14) consists of an ultrasonic generator or oscillator operating at a frequency of approximately

Fig. 3-13. Level measurement using weight method.

LEVEL AND DENSITY MEASUREMENTS 81

Fig. 3-14. Ultrasonictechnique.

20,000 Hz and a receiver. The time required for the sound waves to travel to the liquid and back to the receiver is carefully measured. The time is a measure of level. This technique has excellent reliability and good accuracy. Furthermore, nothing comes in contact with liquid in the tank, which minimizes corrosion and contamination. The only generallimitation is economic. Thermal

One approach employing a thermal sensorto determine level relies on a difference in temperature between the líquid and air above it. When the líquid contacts the sensor, a point determination oí level is made. Another approach depends on a difference in thermal conductivity between the líquid level sensedand the air or vapor above it. Thermal techniques are inexpensive, but bave achieved only modest popularity in process applications. Density

Measurement

Methods

for Liquids

and Liquid

Slurries

Density is defined as mags per unit volume. Specific gravity is the unitless ratio of the density of a substance to the density of water at some standard temperature. In Europe, this is known as relative den-

sity. The measurement and control of liquid density are critical to a great number of industrial processes. Although density can be of interest, it is usually more important as an inference of composition, of concentration of chemicals in solution, or of solids in suspension.

82 FEEDBACK PROCESSCONTROL

Many methods are available to determine concentration, including measurement of changes in electrolytic conductivity and of rise in boiling paint. This section deals with common industrial methods of measuring density continuously (Table 3-2). Agitation in a process tank where density is being measured musi be sufficient to ensure uniformity ofthe líquid. Velocity effects musi be avoided; agitation should be sufficient to maintain a uniform mixture without affecting head pressure at measurement points. Nearly aU industrialliquid density instruments utilize the effect of density changes on weight as a measurement. Such instrumentation falls into three major categories, defined by the principIes employed. These include two other categories, radiation and vibration methods. For density measurement, a cylindrical displacer is located so as to be fuUy submerged. The buoyant force on the displacer changes only as a function of changing líquid density, and is independent of changing líquid level in the vessel. Buoyancy transmitters based upon the Archimedes principIe may be readily adapted to the measurement of líquid density or specific gravity. Hydrostatic Head Proved suitable for many industrial processes is the method that continuously measures the pressure variations produced by a fixed height of liquid (Figure 3-15). Briefly, the principIe is as follows: The ditIerence in pressure between any two elevations below the surface (A and B) is equal to the ditIerence in liquid head pressure between these elevations. This is true regardless of variation in level above elevation

TABLE 3-2. Liquid Density Measurement Minimum Method

Span

Hydrometer

0.1 0.005 0.05 0.05 O.O~ 0.05

Displacer Hydrostatic head Radiation Weight oCfixed volume Vibrating U-Thbe

Condition oi Liquid

Accuracy

Clean Clean

:!:1%

Any Any

Clean Clean

as % Span

:!:1% ~ to 1% 1% 1% 1-3%

Fig.

LEVEL AND DENSITY MEASUREMENTS 83

lz=ZZarZz= 3-15. Fixed heightofliquid for densitymeasurement.

A. This difference in elevation is represented by dimensionH. Dimension (H) must be multiplied by the specific gravity (G) ofthe liquid to obtain the difference in head in inches or metres of water, which are the standard units for instrument calibration. To measure the change in head resulting from a change in specific gravity from GI to G2, it is necessary only to multiply H by the difference between G2 and GI. Expressed mathematically: P = H (G2 -GJ

(3-3)

The change in head (P) is differential pressure in inches or metres of water. GI is mínimum specific gravity and G2 is maximum specific gravity. It is common practice to measure only the span of actual density changes. Therefore, the measurement zero is suppressed; thai is, the instrument "zero," or lower range value, is elevated to the minimum head pressure to be encountered. This allows the entire instrument measurement span to be devoted to the differential caused by density changes. For example, ifG1 is 1.0 andH is 100inches, the span of the measuring device musi be elevated 100 inches of water (H x G¡). For a second example, if GI is 0.6 and H is 3 metres, the zero suppression should be 1.8 metres of water. The two principal relationships thai musi be considered in selecting a measuring device are:

Vibration

84 FEEDBACK PROCESSCONTROL

Span = H X (G2,- GJ Zero suppression = H x GI,

(3-4)

For a given instrument span, a low gravity span requires a greater H dimension (a deeper tank). Radiation

Density measurements by this method are based on the principIe that absorption of gamma radiation increases with the increasing specific gravity of the material measured. The principal instrumentation includes a constant gamma source (usually radium), a detector, and an indicating or recording instrument. Variations in radiation passing through a fixed volume of ftowing process liquids are converted iota a proportional electrical signal by the

detector.

Damping a vibrating object in contact with the process fluid increases as the density ofthe process fluid increases. This principIe is applied to industrial density measurement. The object that vibrates (from externally applied energy) is usually an immersed reed or plate. A tube or cylinder that conducts, or is filled with, the process fluid can also be used. Density can be inferred from one of two measurements: changes in the natural frequency of vibration when energy is applied constantly, or changes in the amplitude of vibration when the object is "rung" periodically, inthe "bell" mode. Temperature

Effects and Considerations

The density of a liquid varies with expansion due to rising temperature, but Dot allliquids expand at the same rate. Although a specific gravity measurement must be corrected for temperature effects to be completely accurate in terms of standard reference conditions for density and concentration, in most cases this is Dot a practical necessity. For applications in which specific gravity measurement is extremely critical, it m~y be necessary to control temperature at a constant value. The necessary correction to the desired base temperature can then be included in the density instrument calibration.

LEVEL AND DENSITY MEASUREMENTS 85

Differential

Pressure Transmitter

There are a variety of system arrangements for hydrostatic head density measurements with d/p Cell transmitters. Although ftange-mounted d/p Cell transmitters are often preferred, pipe-connected transmitters can be used on líquids where crystallization or precipitation in stagnant pockets will noi occur. These d/p Cell transmitter methods are usually superior to those using bubble tubes. They can be applied wherever the vessel is high enough to satisfy the mínimum transmitter span. They are also well suited for pressure and vacuum applications. Constant level overftow tanks permit the simplest instrumentation as shown in Figure 3-16. Only one d/p Cell transmitter is required. With H as the height of líquid above the transmitter, the equations are still: Span = H X (G2

G¡}. zero suppression = H X GI

Applications with level and/or static pressure variations require compensation. There are three basic arrangements for density measurement under these conditions. FiTSt, when a seal fluid can be chosen that is always heavier than the process fluid and will Dot mix with it, the method shown in Figure 3-17 is adequate. This method is used extensively on hydrocarbons with water in the wet leg.

Fig. 3-16. Constant level, open overftow tanks require only one d/p Cell transmitter for density measurement.

Fig.

86 FEEDBACK PROCESSCONTROL

y-:'--=(

\ H

DENSITY ~ SIGNA L

A I

=í UQUID

a':iJ-l

PURGE

(SP.GR.=GS) 3-17. In an open or closed tank with varying level and/or pressure. a wet leg can be filled with seal fluid heavier than the process liquido

For a wet leg fluid oí specific gravity Gs. an elevated zero transmitter musi be used. The equations become: Span = H x (G2 -GJ,

zero elevation = H x (GB -GJ

When no seal or purge líquid can be tolerated, there are ways to provide a "mechanical seal" for the low-pressure leg, or for both legs, if needed. Figure 3-18 shows the use of a pressure repeater for the upper connection. The repeater transmits the total pressure at elevation B to the low pressure side of the d/p Cell transmitter. In this way, the pressure at elevation B is subtracted from the pressure at elevation A. Therefore, the lower transmitter measures density (or H x G, where G is the specific gravity of the líquid). The equations for the lower transmitter

are: Span = H X (G2 -GJ Zero suppression = H x G1

The equationfor the upper repeateris: Output (maximum) = d 1 (max) x G2 + P (max),

Fig. whered1

LEVEL AND DENSITY MEASUREMENTS 87

3-18. In an open or closed tank with varying level and/or pressure where seal fluid or purge is Rot suitable, a pressure repeater can be used.

is the distance from elevation B to the líquid surface, andP is the static pressure on the tank, if any. When there is no pressure on the tank, the upper repeater output is a measurement of level. Transmitter locations should be as high as possible above the bottom ofthe tank. The process líquid then can be drained below this level for removal and maintenance of the transmitter.

Questions

3-1. An opentank containsa liquid of varying densityand the level within the tank mustbe accuratelymeasured.The bestchoiceof measuringsystem would be: a. Hubble tube b. Diaphragmbox c. Float and cable d. Head type with differentialpressuretransmitter 3-2. A chain-suspended diaphragmbox and pressureinstrumentare usedto measureliquid level in a tank which is 10feet in diameterand 15feetdeep. The tank containsa liquid that hasa specificgravity of 0.9 at ambient temperature.The spanof the pressureinstrumentrequiredis approximate1y: a. 10 psi c. 5 psi b. 25 psi d. 15psi

88 FEEDBACK PROCESSCONTROL

3-3. A pressurized tank contains a líquid, SG = 1.0, and the level measuring pressure taps are 100inches apart. A pneumatic differential pressure transmitter is used to measure level. The leg that connects the top of the tank to the transmitter is filled with tank líquid. The top tap should be connected

to: a. The low-pressuretap on the transmitter. b. The high-pressuretap on the transmitter. è, Either the high- or the low-pressuretap. d. The high-pressuretap but througha sealchamber. 3.4. In Qu~stion3-3the bottom connectionis madeto the low-pressuretap on the transmitterand the top is madeto the high-pressure tap. The signal output, if the transmitteris calibratedOto 100inches,whenthe tank is full will be: a. Topscalevalue c. O b. Bottom scalevalue d. A measureof density 3.5. A plant hasa water tower mountedon top of an 80-footplatform. The tank is 30 feet high. Whatis the heightof water in the tank if a pressuregauge on the secondfloor, height 15feet,reads 40 psi. a. Full c. 4.74feet b. 12.42feet d. 27.42feet 3-6. A displaceris 5 inchesin diameterand 30 incheslong. If it is submerged to a depthof 20 inchesin líquid sa = 0.8, whatforce will it exert on the top works? a. 11.3pounds c. 35.5pounds b. 426.3pounds d. 1.47pounds 3.7. A closed tank level (Sa = 0.83)is measuredwith a differentialpressure transmitter.The level mar vary from 10to 100inches.The high-pressuretap is 10inchesabovethe transmitterand a watersealfluid is used.A pressure repeateris usedfor the top tank pressure.The differentialpressure transmittershouldbe calibrated: a. 10to 100inches b. 10to 84.7inches c. 8.3 to 74.7inches d. 8.3 to 98.3inches 3.8. To resistthe corrosiveeffectsof a very unusual,highlyexplosive chemical,a storagetank is lead-lined.Level measurement is difficult because the materialalso solidifiesonce it entersa measuringtap. To measurethe level with accuracythe bestchoicewould be: a. Weighthe tank and its contentsand zero out the tare weightof the tank. b. Use a radioactivelevel measurement. c. Install a conductivitylevel measurement. d. Use a thermal conductivitylevel detector.

LEVEL AND DENSITY MEASUREMENTS 89

3-9. A displacer48 incheslong and 1%inchesin diameteris usedto measure densityon a 4 to 20 mA dc transmitter.Its total submergedweightchanges from 1.42poundsto 5.7pounds.If the densityis checkedand determinedto be 0.4 whenthe output is 4 mA dc, the densityat an outputof 12mA dc is: a. 0.6 c. 1.0 b. 0.8 d. 1.6 3-10. A densitymeasuringsystemis set up as shownin Figure3-18.The H distanceis 100inchesand the lower transmitteris calibratedto a 120-inch span.If the transmitteris pneumaticand deliveringa 12-psisignal,the specificgravity of the tank's contentsis:

a. 1.0

c. 0.9

b. 0.83

d. 1.2

Flow Measurement

The process industries by their very nature deal constantly with flowing fluids, and measurement of these flows is essential to the operation of the plant. These measurements are indicated, recorded, totalized, and used for control. Flow measurement is generally the most common measurement found in the process plant. Fluid flow measurement is accomplished by: Ao Displacement lo Positive displacement meters 20 Metering pumps Bo Constriction Type, Differential Head lo Closed conduit or pipe ao Orifice plate

bo Venturi tube Co Flow nozzle do Pitot tube eo Elbow fo Target (drag force) go Variable aTea (rotameter) 20 Open channel ao Weir

bo Flume 90

FLOWMEASUREMENT 91

C. Velocity Flowmeters 1. Magnetic 2. Turbine 3. Vortex or swirl 4. Ultrasonic 5. Thermal D. Mass Flowmeters 1. Weighttypes 2. Head and magnetictypes compensatedfor temperature,pressure, and density 3. Gyroscopeprecisiontypes 4. Centrifugalforce (torque)types Positive displacementmeters and meteringpumps measurediscrete quantities of flowing fluid. This flow is indicated in terms of an integrated or totalized flow volume (gallons,cubic feet, litres, cubico metres, and the like). A typical applicationof this type of flow measurementis custodytransfer, and familiar examplesaredomesticwater metres and gasolinepumps. The other types of meters listed above measureflow rate. lt is flow rate-quantity per time, suchas gallons per minute or liters per second-which is most generallyused for measurementand related control applications in the processplant. The most common rate meter is the constriction or headtype. Constriction

or Differential

Head Type

In this type of flow measurement a primary device or restriction in the flow line creates a change in fluid velocity that is sensedasa differential pressure (head). The instrument u~ed to sensethis differential pressu~e is called the secondary device, and this measurementis related to flow rate. The flow-measuring system, orlen called a flowmeter, consists of primary and secondary devices properly connected. The operation of the head-type flow-measuring system depends on a theorem first proposed by Daniel Bernoulli (1700-1782). According to this theorem the total energy at a point in a pipeline is equal to the total energy at a second point if friction between the points is neglected. The energy balance between Points 1 and 2 in a pipeline can be expressed as follows:

+ Z2 = ~p + ~ (VmJ2+ Zl

92 FEEDBACK PROCESSCONTROL

where: P Vm Z p G

= = = = =

Static pressure, absolute Fluid stream velocity Elevation of center line of the pipe Fluid density Acceleration due to gravity

If the energy is divided into two forms, static head and dynamic or velocity head, some of the inferential flow devices can be more easily studied. For example, with an orifice plate, the change in cross-sectional aTeabetween the pipe and the orifice produces a change in flow velocity (Figure 4-1). The flow increases to pass through the orifice. Since total energy at the inlet to, and at the throat or, the orifice remains the same (neglecting losses), the velocity head at the throat must in.crease,causing a corresponding decrease in static head. Therefore, there is a head difference between a point immedlately ahead of the restriction and a point within the restriction or downstream from it. The resulting differential head or pressure is a function of velocity that can then be related to flow. Mechanical flow-measuring instruments use some device or restriction in a flow line that results in such a differential head. The following should clarify these relationships. Assume a tank as shown in Figure 4-2. A flow line enters the tank and replaces the out-

Fig. 4-1. Orifice plate differential producer. The difference in head (pressure) atP, and P 2is a function of velocity which can be related to ftow.

FLOW MEASUREMENT 93

-+ a=A.J2;

-..Q =AV2-;;h

Fig. 4-2. Free and tank-to-tankflow. usedto simplify conceptofflow formula(4-1).

ftow through the orifice located near the bottom of the tank. If the level in the tank is H, the velocity of outftow will be: y2 = 2GB

This is the lawof falling bodies that is developed in most physics books. The volume of liquid discharged per time unit through the orifice c3;nbe calculated by geometry.

=AV Substituting the expression for velocity in this equation:

(4-1) This expression may also be used to calculate the rate offtow past a point in a pipe. The actual ftow rate will be less than this equation will

V=Y2GH Q Q=A\f2Gii

O) Fig.

FEEDBACK PROCESS CONTROL;

calculate. The reduct"ionis caused by several factors, including friction and contraction of the stream within the pipe. Fortunately all common primary devices bave been extensively tested and their coefficients determined. These data become part of the ftow calculations. Primary Devices

The orifice plate is the most popular primary device found in most process plants. Orifice plates are applicable to all clean fluids, but are Dot generally applicable to fluids containing solids in suspension(dirty fluids). A conventional orifice plate consists of a thin circular plate containing a concentric hole (Figure 4-3). Thè plate is usually made of stainless steel but other materials, such as monel, nickel, hastelloy, steel, glass, and plastics, are occasionally used. The most popular orifice plate is the sharp-edged type. The upstream face of the plate usually is polished and the downstream gide is often counterbored to prevent any interference with the flowing fluid. The bore in the plate is held to a tolerance of a few ten-thousandths of an inch in small sizes and to within a few thousandths in sizes above 5 inches in diameter. ln addition to the conventional, sharp-edged, concentric plate, there are others that bave been designed to handle special situations. These special types constitute only a small percentage of the total, but they do occasionally solve a difficult problem. There are two plates (Figure 4-3) designed to accommodate limited amounts of suspended solids. The eccentric plate has a bote that is bored off-center, usually tangent to the bottom of the flow line (inside periphery of the pipe). The segmentat orifice plate has a segment removed from the lower halí of the orifice plate. ln addition, there are

CONCENTRIC

4-3. Orificeplate types.

ECCENTRIC

SEGMENTAL

Reynolds

FLOW MEASUREMENT 95

quadrant-edged or special-purpose orifice plates with rounded edges. This design minimizes the effect of low Reynolds number (see below). Orifice plates along with other primary devices operate most satisfactorily at high ftow rates. The reason is the change in ftow coefficient that occurs when the ftow rate changes from high to very low. When this happens the ftow velocity distribution changes from uniform to parabolic. This mar be related to a ratio of inertia forces to viscous forces called Reynolds number. Number = Average Fluid Velocity x Orifice Diameter Absolute Viscosity In most process plants the Reynolds numbers encountered will be high-between 10,000 and 1,000,000. Under these conditions the ftow coefficients stay fixed and head-type ftow measurementsare reasonably accurate. To achieve the ultimate in accuracy, a Reynolds number correction is made and this is described in the text Principies and Practices o/ Flowmeter Engineering by L. K. Spink. At low Reynolds number, the ftow changes from turbulent to parabolic or laminar and the coefficients undergo a change. The changeover cannot be precisely defined, which makes the application of head-type ftow measurements difficult at low-ftow velocities. The quadrant-edged orifice has the ability to perform well at lower velocities than the square-edged plate. However, it does Dot perform as well at high Reynolds numbers (velocities). Orifice plates that are to handle líquids containing small amounts of dissolved air should contain a small vent hole bored at the top to permit the air to pass through the plate. Specifications bave been established for the size of this vent hole in relation to the size of the orifice. Plates for use with steam should bave a similar hole drilled at the bottom to drain any condensed steam. In certain ftow measurements, the orifice plate should also bave a bottom drain hole to permit the condensation

to drain. Table 4-1 summarizes application factors to help in deciding whether the orifice plate can do a particular job. Another primary device that is frequently found in the process plant is the Venturi tube shown in Figure 4-4. The Venturi tube produces a large differential with a mínimum permanent pressure loss. It has the added advantage of being able to measure ftows containing suspended solids. The most significant disadvantage is its cost which, when compared with other primary devices, is high.

~~ G VP Fig.

96 FEEDBACK PROCESSCONTROL

Table4-1. Primary Flow MeasurementDevices

" t :§

o: Accuracy (empirical data)

None

Pressure loss #

, P

Use on dirty service

Differenlial produced for given ftow and size

p E

E P P

E P F

G G E

~ .9"

¡¡¡

.s~

".." .~ ~~~~"to"~ ~5

"='" " E

E EG

None E E

F None

Non.

G G F

U E

F P

F F

VP E

P F

For liquido containing

vapors

For vapors containing condensate

For viscous ftows

First cost

EGG * F E

E U G

Ease of changing capacity

E G

Ease of instalIalion

Excellent

G F

Good FairP Poor

VP U /I

Very poor Unknown E indicates lowest loss, P highest, etc.

EG p E G

None E

u uVP

E F

G F

.For measuring velocity at oRe point in conduit the well-designed Pitot tube is reliable. For measuring total ftow, accuracy depends on velocity traverse. t Excellent in verticalline if ftow is upward. 4;Excellent in verticalline if ftow is downward. § Requires a velocity traverse.

Several other primary devices mar be classified as modifications of the Venturi tube. The Lo-Loss and Dall tubes are similar in many ways to the Venturi. The flow nozzle (Figure 4-5) has some similarity but does not bave a diffuser cone, and this límits its ability to minimize permanent pressure loss. The Venturi family ofprimary devices is often

4.4. The HerschelVenturitube,developedin 1888,to producea largedifferentialpressure with a smallheadloss.

Fig.

FLOW MEASUREMENT 97

4-5. Flownozzleassembly.

chosen to minimize permanent pressure loss or to cope with solids suspended in the flowing material. Table 4-1 provides aid in making a selection. The Pitot tube is another primary device. It has the advantage of practically no pressure dropo Its limitations are its inability to handle solids carried by the flowing material and somewhat limited accuracy. Solids tend to plug the openings in the tube, and the classical Pitot tube senses impact pressure at only one point, thus decreasing accuracy. A multi-impact opening type (annubar tube) is available which improves the potential accuracy. In the process plant Pitot tubes are used more for testing than for continuous use. It is possible to install a Pitot tube into a flow line under pressure if the required equipment is available. Occasionally a pipe elbow (Figure 4-6) mar be used as a primary device. Elbow taps bave an advantage in thai most piping configurations contain elbows thai can be used. If an existing elbow is used, no additional pressure drop is created and the expense involved is minimal. The disadvantages are thai accuracy will be Iacking and dirty flows mar tend to plug the taps. Repeatability should be reasonably good. Two taps locations are used at either 45 or 22Y2degrees from the

Fig.

98 FEEDBACK PROCESSCONTROL

4-6. Elbow(usedas prirnarydevice).

inlet face ofthe elbow. At low-ftow velocities, the differential produced is inadequate for good measurement, thus the elbow is a usable choice only for high top-scale velocities. The target or drag body ftow device (Figure 4-7) is in many ways a variation of the orifice plate. Instead of aplate containing a bore through which the ftow passes,this device contains a solid circular disc and the ftow passes around il. An essential part of the measurement is the force-balance transducer that converts this force into a signal. This signal is related to ftow squared, just as it wouid be with any other primary device connected to a differential pressure transmitter. The

4-7. Targetflowmeter.

FLOW MEASUREMENT 99

target meter mar be generally applied to the measurement of líquids, vapors, and gases. Condensates pass freely along the bottom of the pipe, white gases and vapors pass easily along at the top. The target flow device has demonstrated the ability to handle many difficult assignments Dot possible with other primary elements. Both pneumatic and electronic force-balance transducers can be used, making either type signal, pneumatic or electrlc, available. Secondary

Oevices

Secondaryinstrumentsmeasurethe differential produced at the primary devices and convert it into a signal for transmissionor into a motion for indication, recording, or totalization. Secondaryinstrumentsinclude the mercury manometer,the socalled mercurylessor diaphragm(beUows)meterand various types of force-balanceand motion-balancepneumaticand electronictransmitters. In the past the mercury manometer was an extremely popular secondary device, but the high price and danger of mercury bave all but eliminated it from everyday use. However, a few mercury manometers are still employed for ftow rate measurements in gas pipelines. The bellows or diaphragm secondary devices are popular when a direct indication or record is desired. The most popular secondary device is the force-balance transmitter. The reasons for this popularity are virtually unliínited adjustability, no harm from extensive overrange, and the a vailability of a standard signal that can be fed into a recorder, a controller, or other instruments that may be combined to form a sys-

tem. Still another detail is the mounting of the secondary device (locations are shown in Figure 4-8). With liquid ftow, the secondary device is

LIQUID FLOW

Fia. 4.8. Flow.

GAS FLOW

STEAM FLOW

100 FEEDBACK PROCESSCONTROL

below the pipeline being measured to ensure that the connecting lines attached to the sicle of the pipe remain liquid filled. With steam, the lines should always remain filled with condensate; but with gas, the secondary device is mounted above the ftow line to drain away any liquid that mar be present. When any primary device is installed in a pipeline, the accuracy will be improved if as much straight run as possible precedes il. Straight run beyond the primary device is of far less concem. Still another important consideration is the location of the pressure taps. With nozzles, Venturi, Dall and Pitot tubes, and elbows, the pressure tap locations are established. For orifice plates, however, a variety of tap locations are used. These are ftange, corner, vena contracta, or D and D/2, along with full ftow or pipe taps. Figure 4-9 describes these tap locations, and Figure 4-10 shows the importance of tap location. In general, ftange taps are preferred except when physical limitations make pipe taps advantageous. Corner taps require a special ftange and vena contracta tap locations relate to orifice openings. Corner taps are advantageous for pipe sizes under 2 inches. Figure 4-11 describes the permanent head loss caused by the primary device selected. Relating

Flow Rate to Differential

The two basic formulas bave already been introduced. In the English system, G = 32 feet per second squared, and in the metric system, G = 980 centimetres per second squared. The height (h) would be expressed in feet in the English system and centimetres in the metric

Fig. 4-9. Taplocationsfor orifices.

FLOW MEASUREMENT 101

Fig. 4-10. Differentialpressureprofile with orifice plate. t

system. In Equation 4-1, area (A) would be expressed in square feet and in the metric system in square centimetres yielding cubic feet per second or cubic centimetres per second. In the United States, the English system is the most common. This system is in the process of being changed to the SI metric, but it appears that the total conversion

Fig. 4-11. Pennanent head los s in a ditferential producer may be plotted as a percent of measured ditferential for the several types of primary devices. These values must be interpreted according to the acceptable head loss limit for any particular application.

102 FEEDBACK PROCESSCONTROL

will take a long time to complete. For tros reason the sample calculations that follow will use the English system. In Equation 4-1, V is in fe et per second; the acceleration due to gravity (G) is in feet per second squared; H is the height in feet of a column of the fluid caused by the differential pressure across a primary device. To express this equation in terms of an equivalent differential (h), in inches of water, H is replaced by (h/12)G¡) where G¡ is the specific gravity of the fluid at flowing temperature. Substituting V into Equation 4-1:

(4-2) where: Q = Volumetric flow (cubic feet per second) A = Cross-sectional aTea of the orifice or throat of the primary device (square feet) h = Differential across the primary device (inches of water) G, = Specific gravity of the fluid (dimensionless) G = Acceleration due to gravity (a constant: 32.17feet per second2) For líquids, it is more useful to express Q in gallons per minute. AIso, it is convenient to express the area of the orifice or throat interms of its diameter (d in inches). Substituting in Equation 4-2:

(4-3)

Equation 4-3 most be modified to take into account several factors, such as the contraction of the jet, frictionallosses, viscosity, and the velocity of approach. This modification is accomplished by applying a discharge coefficient (K) to the equation. K is defined as the actual ftow rate divided by the theoretical ftow rate through the primary device. Basic texts carry K factors for most primary devices. For instance, K is listed according to vario us pressure tap locations, and di D ratios. Where extremely accurate results are required, however, the K factor must be determined in the laboratory by actual ftow calibration of the primary device.

FLOW MEASUREMENT 103

Applying K to Equatiort 4-3 gives:

Since both K and d are unknown, another value is defined. The quantity (S) is set equal to K (d/D)2. Since Kd2 then equals SD2, substitution produces:

S values (sizingfactor) are tabulated againstbeta ratios (di D) for various differential devices in Table 4-2. j Effect of Temperature on Flow Rate The above equations give the flow through the primary device at conditions that exist at the time the measurement is made. In most industries, it is more desirable to know the equivalent volume flow at a stated reference temperature, usually 600P(15.6°C). Por líquids, this correction can be applied by multiplying the equation by the ratio ofthe líquid specific gravity at the flowing temperature (G,) divided by the líquid specific gravity at the reference temperature (G¡). Thus Q gallons per minute at the reference temperature: Q

= 5.667

SD2

fE:: V G;

§ Gi

(4-6)

which simplifiesto: Q = 5.667 SIJ2 YG;l GI

Similar equations can be developed for steam or vapor ftow in weight units (such as pounds per ho ur) or for gas ftow in volume units such as standard cubic feet per hour (scfh).

W (poundsper hour) = 359SD2v'h:y; Q (scfh) = 218.4SD2~ ~

Pb" T;G

104 FEEDBACK PROCESSCONTROL

Table4-2. Sizing Factors S'ta or d/D

Ratio 0.100 0.125 0.150 0.175 0.200 0.225 0.250 0.275 0.300 0.325 0.350 0.375 0.400 0.425 0.450 0.475 0.500 0.525 0.550 0.575

Square-Edged Orifice, Flange Corner or Radius Taps

Ful/-Flow Quadrant-

2\-2& 8D

Nozz/e and

Lo-Loss

Dall

Taps

Venturi

Tub.

Tube

(PipèJ

0.005990

0.006100

0.009364

0.009591

0.01349

0.01389

Edged Orifice

0.01839

0.01902

0.02402

0.02499

0.0305

0.03044

0.03183

0.0390

0.03760

0.03957

0.0484

0.04558

0.04826

0.0587

0.05432

0.05796

0.08858

0.06390

0.06874

0.1041

0.07429

0.08068

0.1210

0.1048

0.08559

0.09390

0.1392

0.1198

0.09776

0.1085

0.1588

0.1356

0.1170

0.1267

0.1109

0.1247

0.1800

0.1527

0.1335

0.1443

0.1251

0.1426

0.2026

0.1705

0.1500

0.1635

0.1404

0.1625

0.2270

0.1900

0.1665

0.1844

0.1568

0.1845

0.2530

0.2098

0.1830

0.207

0.1745

0.2090

0.2810

0.2312

0.2044

0.232

0.1937

0.2362

0.3110

0.2539

0.2258

0.260

0.0700 0.0824 0.0959 0.1106

0.2144

0.2664

0.3433

0.2783

0.2472

0.292

O.(X)()

0.2369

0.3002

0.3781

0.3041

0.2685

0.326

0.625 0.650 0.675 0.700 0.725 0.750 0.775 0.800 0.820

0.2614

0.3377

0.4159

0.3318

0.2956

0.364

0.2879

0.3796

0.4568

0.3617

0.3228

0.3171

0.4262

0.5016

0.3939

0.3499

0.3488

0.4782

0.5509

0.4289

0.3770

0.3838

0.6054

0.4846

0.4100

0.4222

0.6667

0.5111

0.4430

O.4646

0.5598

0.4840

0.5113

0.6153

0.5250

0.6666

0.5635

FLOW MEASUREMENT 105

In Equations 4-8 and 4-9: . 'Yf= Specific weight of the steam or vapor at operating conditions in pounds per cubic foot T b = Reference temperature (absolute); (i. e., 460 plus the reference temperature in °F.) Pb = Reference pressure (psi absolute) Tf = Operating temperature at the primary device (absolute); (i.e., 460 plus operating temperature in °F.) Pf = Operating pressure (psi absolute) G = Specific gravity ofthe gas (molecular weight ofthe gas divided by the molecular weight of air or the weight of a volume ofthe gas at a given temperature and pressure divided by the weight ofanequal volumeofairatthe sametemperature and pressure). The reference temperature is very often 600P and the reference pressure atmospheric 14.7 psi absolute. Ifthese are the standard conditions, Equation 4-9 can be simplified to:

(4-10) Equation 4,.10is applicable to gas ftow only when the pressure differential is small enough so that gas density does Dot change significantly. A simple rule ofthumb is that the maximum differential in inches of water should Dot exceed the absolute operating pressure in psi absolut.~. For example, if the gas operating pressure is 22 psi absolute, at a particular installation, and the maximum differential is 20 inches of water, Equation 4-10 can be used. Flow rate 'measurements for gas and steam are more difficult to make with accuracy than those for liquido The reason is changes in specific gravity, weight, temperature, pressure, and so on, that mar occur under operating conditions. These changes will bave an effect on measurement accuracy and under certain conditions mar be difficult to predict. An abbreviated set of tables for the formulas given are included in this book. If more accuracy is required, more exact equations, along with detailed tables, such as those found in Principies and Practice oi Flow Meter Engineering by Spink, should be used. Another method of performing these ftow calculations is to use a ftow slide rule. The ftow slide role has the table values incorporated

106 FEEDBACK PROCESSCONTROL

into its scales. If the tables given are used, the resulting accuracy should be as good as the flow slide rule. Now several sample problems are given to demonstrate the procedure followed for each type of calculation. Additional problems are given at the end of tros chapter. SAMPLEPROBLEMJ A 4-inch schedule 40 pipe carries water that is measured by a concentric, sharp-edged, orifice plate, d = 2.000 inches, with flange taps. The differential is measured with an electronic differential pressure transmitter. The transmitter is calibrated Oto 100inches of water pressure and has an output of 4 to 20 mA dc. If the signal Crom the transmitter is 18.4 mA dc, find the flow rate. S/ep 1. Convert the electrical signal to differential pressure. 18.4 -4

x 100 = 90 inches oí water

20 -4

Step2. DetermineID of 4-inchschedule40pipe (seeAppendix, table A-4) = 4.026inches. 2.000 = 0.4968 Step3. Calculatelid = 4:026

Step4. From Table 4-2determineS. This will require interpolation.

S =

0.475

0.1404

0.4968

0.5000

0.1568

(0.5000 0.4968 -0.475 -0.475 )

(0.1568 -0.1404) ~0.1404

S = 0.1547 Step5. Substitute in Equation 4-7:

= 5.667 x 0.1547x 16.21 x 9.487 = 134.83or 135gpm

FLOW MEASUREMENT 107

SAMPLEPROBLEM 2 An elbow is used as a primary device. The taps are made at 45 degrees. The line is a 6-inch schedule 40 pipe. What is the water flow rate if the effective radius of curvature is 9 inches and a differential pressure of 35 inches of water pressure is produced.

= 172.66 .yj"5 =

,021.47gpm

SAMPLEPROBLEM 3 Dry-saturated steam is measured with a ftow nozzle. The d/D is 0.45 and the line size is a S-inch schedule SOpipe. The static pressure is 335 psi. Calculate the ftow rate at a differential pressure of 200 inches of water in pounds per hour. W(pounds per hr.) = 359SD2Vïï:y;

(4-8)

from Table 4-2

s = 0.2026 D = 7.625 inches (Table A-4) Yf = 0.754 pounds per cubic feet W(pounds per hour) = 359 x 0.2026 x 7.6252\1200 x 0.754

= 4,228.77x 12.28 W = 51,929 pounds per hour SAMPLEPROBLEM 4 A 6-inch schedule 40 pipe (1D-6.065) carries fuel gas with a specific gravity of 0.88. The line pressure is 25 psi. Plowing temperature is 60oPand the ftow is measured with an orifice plate with ftange taps. The maximum ftow rate is 2,000,000standard cubic feet per day. Pind the diameter of the hole to be bored in the concentric orifice plate if 20 inches of water pressure is full-scale differential.

108 FEEDBACK PROCESSCONTROL

2,000,000 = 7' 727 x S x. 6 0652 V120(25 +-~ 24 (460 + 6Ó~

8,3333.33= 7,727 x S x 36.78 x 1.322 S = 7,727 x83,333.33 36.78 x 1.322= O.18 22 From Table 4-2 .575

.2144

.2218

.2369

.600 ~ = D

( .2218 .2369

-.2144

d = (.583)(6.065)

)

025 + .575 = .5832

= 3.536 inches

SAMPLEPROBLEM5 Gasoline is carried in a 2-inch schedule 40 pipe (ID = 2.067). A concentric sharp-edged orifice plate with corner taps is used to measure flow rate. The orifice bare is 1 inch in diameter, and at full flow, 50 inches of water differential is produced. The specific gravity of the gasoline is 0.75. What is the flow rate?

Q = 5.667 x 0.1474 x 2.067 x 2.067 x 'V{SO 0-:75

= 5.667 x 0.1474x 2.067 x 2.067 x 8.165 = 29.14 gpm

Fig.

FLOW MEASUREMENT 109

Variable Area Meters (Rotameter)

The variable aTea(Figure 4-12) meter is a form of head meter. In this flowmeter the aTea of the flow restriction varies so as to maintain a constant differential pressure. The variable aTeameter, which is often called a rotameter, consists of a vertical tapered tube through which the fluid flow being measured passes in an upward direction. A float or rotor is contained within the tapered tube. This rotor or float is made of some material-usually metal-more dense than the fluid being measured. As the flow moves up through the tapered tube, it elevates the float until balance between gravity acting on the float and the upward force created by the flow is achieved. In achieving this balance of forces, the area through which the fluid passeshas automatically been adjusted to accommodate that flow rate. The tapered tube is often made of transparent material so the float position can be observed and related to a scale calibrated in units of flow rate. The rotameter is often used to measure low-flow rate. When very large flow rates are to be measured, a bypass rotameter may be used. This consists of an orifice in the main flow line with the variable aTeameter connected in parallel. An industrial rotameter is useful overthe upper 90 percent of its scale. The accuracy of the rotameter, like any head type, depends on many factors. Typical errors may vary between I and 10 percent of full scale value. Open-Channel

Flow Rate Measurements

Flow rate measUíements in openchannelsare fundamentalto handling water and waste. Environmentalconsiderationsbave madethesemea-

4-12. Variablearea(rotarneter)flowmeter.

110 FEEDBACK PROCESSÇONTROL

surements common in' the typical process plant. Open-channel measurements utilize head meter techniques. Primary

Devices

The primary devices used in open-channel ftow rate measurements are weirs and ftumes. There are two basic weirs-the rectangular and the V-notch. The rectangular weir is made in three varieties (Figure 4-13). The first has contractions or extensions into the channel that produce a boxlike opening. The second modification completely suppressesthese contractions, extending the weir across the entire width of the channel. The third type, the so-called Cippoletti weir, has end contractions set at a 4: 1 angle, rather than being perpendicular to the edge of the weir. Rectangular weirs are primarily designed for larger ftow; their límit on range is dictated by the design of the associated channels. Figure 4-14 shows the ranges of weir capacity for the different types and sizes of

welrs. V-notch weirs are essentially plates (usually metal) that contain a V-shaped notch (Figure 4-13). The angle of the V can vary, but the formulas given are for the most common angles 30, 60, and 90 degrees. V-notch weirs are employed for lower ftow rates than those that would be measured by a rectangular weir. In weir measurement (Figure 4-15) the nappe, or profi1e of water over the weir, must be completely aerated if good accuracy is to be obtained. All weirs then produce some head loss as the líquid falls free. If head loss is a problem, a ftume might be a better choice. Flumes, a further development of the basic weir concept, are designed primarily to reduce the head loss that is experienced with the

CIPPOLETTI

WEIR~S>2H

ECTANGULAR

WEIR-j

MAX I

: 4~

_L)2H

MAX

PREFERABLY

ANO >4H

MAX

I 0>3H

MAX

C\PPOLETTI WEIR

Fig. 4-13. Rectangular.Cippoletti,and V-notchweirs.

GPM 70000 50000

100

40000

30000

60 50

20000

40 30

10000 8000 6000 5000

4000

3000

6 5

2000

3 1000 800 600 500

1.0

400

300

0.6 05 0.4

200

0.3 100 80 60 50

0.08

006

0.05 20

0.04

FLOW

0.03

0.02

8 FLOW

6 5

001

0008

0.006 0005 0004 0003

0.002

Fig. 4-14. Rangeof weir capacityfor differenttypesand sizesof weirs. 111

weir.

112 FEEDBACK PROCESSCONTROL

AERATION'UNDE.

NAPPE

Fig. 4-15. Aerationundernappeoi weir.

Flumes are also able to handle solids suspended in the flowing liquido A very popular flume is the Parshali flume. lt is somewhat similar to one-half of a rectangular Venturi tube. ln flume measurement, head losses are reduced because it is Dot necessaryto create the nappe. The Parshall flume is shown in Figure 4-16 and Table 4-3 gives the dimen-

Ó.k.

,..~~--~~~:::::: ~~:.:--::::¿~ i o t7::::::;:::~~~t=:=f:~:::::::--i l CO"".~.,.....c"O" .. TH.OAT...TION!l/.".'N.'.cr' ON c~1

f ~~~--~:

..PLAN

'. "

.1 M

:~+ .1-0

.1.

Ir:--

'-'0-.,,

'LOW

, l

oi;;;. "" ,o

.";;,,

'¡'-

SECTION

o-o

Fig. 4.16. Diagramanddimensionsof Parshallflume.

~ :..:.¡; c;... ., '" ~< '"",:, ~'""

~~~--c

~-c..,

":";oC~.i~~~~@a~

, \oi

~~~tï;

a~~=~~:è",-c-co",

~~~:,¡

ci ci ci ci ci ci ci":":"¡";";

;... ~

;. .., .., .., .., .., .., .., .., .., .., ..,

~ ~

-"""""""""""""""'"

.1~ ...

~ ri:

'" G)

Q: .¡:

:; oc:

~~ ~~

~ '"ò' ~ r;:

'" ~

lo.

cE '" ~

~ e = e

~ t¡, .t

to¡.t

~ = ~

~ .t

§ e '~

.!, ~ ...

~ 'Q

~ '" =

NN'¡'~"""":'ob~=~~

~~~~~~~:!:!:!:f:f

e =

.;!;:-::i -::i.;!-::.;! ~-'c-~-¡;'-;'¡;'~;'

~ .¡;

~"!I!J;)ION sn!~ ..un;) qloowS

--.N

-..,

'" ~ ...

Li:

.., .., .., .., .., .., .., .., .., ..,

~~~~~~~~~~~~ 99~9O9°99999 N N N ...,J, ...,J,

. :.:.~..~... -"'-0-, = ...g ::-

;:- ::,..,.0--¡¡;

O':":'N"'~""""'obd,=

~":-~9~9"'99999 g--NN""",,",.o""~o. ..~.-!!!"~.-!!! c ;:;:- c '" ~ ;,- ~ ;,- "C> '9 'i' ";' "f "f ";' '" -.,. ";' -NN

b.b

..,.

o. o. o. o. o. o. o. o. o.

~~!~~:¡,:¡,~~~~:¡,

5 ,5 o ~.

..¡ to.

~ ;;: :::

.:.!:¡:~;¡:~~~:¡':~J. .~

!~;;;~~~~~~:!~~ ~,\,O-9'\'99"'9999 OO¿'--N""""'-o"'~

113

'!~

GPM

MGO 3000

CFS 4000

2000

3000 2000

1000 800 1000 800

600 500 400 300 200

100

so 60 40 50

600 500

400 300 200

80 100

60 50

40 20

30 20

10 8 6 5

4 3 2

10 08 06 O~

10 08

04 03

06 05

0.2

100

-t++

MGO

60 50 40

004

FLOW

10 8

006 QO~

FLOW

CFS

008

008 006

OO~ 004

002

I I

I 2

HEAD-INCHES L-I 2 HEAD-FEET

I I .I. 6

I 8 10

,.,.,.

,..

I~ 20

0.03

80 100

002 FLOW

.456810

2/:3

8 IQ

001

FIVE INCHES IS HINIHUN FLA.L SCALE HEAD III'H FDXBORD FLOA' ANO CABLE HE'ER

THIRTY SIX 'NCHES IS ",XIHUM FULL SCAL' H'AD N'TH FDXBDRD FLDAT AND CABL' "'T'R

Fig. 4.17. Level and ftow relationship for ParshaIl ftume. 114

FLOW MEASUREMENT 115

sions. By referring to Figure 4-17 the dimensions of a flume capable of measuring a prescribed flow rate mar be selected. Small flumes mar be purchased and installed while large flumes are generally fabricated on site. Several compaDiesspecialize in the construction and calibration of flumes. Under ideal conditions, measurements by weirs are very accurate. In actual plant measurement, however, ibis mar Dot be true because it is Dot practical to minimize the velocity of approach factor. The correlation between level and flow typically has an error of 3 to 5 percent. When the error of making the level measurementand relating it to flow rate is added, the total overall error mar be as high as :t5 percent. Equations for the more common open-channel flow devices are given in Table 4-4. The equations for most open-channel primary devices are nonlinear. To convert head into flow rate it would be necessary to perform an extensive calculation. This step is generally eliminated by having the instrument perform the calculation. This is accomplished either with a

Table4.4. Equationsfor Common Open-Channel Flow Devices V-Notch Weir 3(1'Qcfs= .6650 H5/2 6(1' Qcfs= 1.432 H5/2 9(1' Qcfs= 2.481 H5/2 Rectangular Weir (with end contractions) Q = 3.33 (L-0.2H) H3/2 Rectangular Weir (without end contractions) Q = 3.33 LH3/2 Cippoletti Weir Q = 3.367 LH3/2

Parshallfiume Flume size (in.) 3. Q = 0.992 HI,547 6 Q = 2.06 HI,58 9 Q = 3.07 HI,53 12 Q = 4.00 HI,522 Q = crs; L = crest length (fi); H

Flume size (in,) 18 Q = 6.00 H',538 24 Q = 8.00 HI,55. 36 Q = 12.00 HI,566 48 Q = 16.00 Hl.578 = head (fi)

116 FEEDBACK PROCESSCONTROL

carn or by means of a special chart or scale. The head is measured with any one of several instruments. Several popular types are: float-andcable, ball float, bubble, and pressure-sensing. A typical installation is shown in Figure 4-18. Installation and Selection Considerations To determine the type of primary device to be used for open-channel flow measurement, the following factors musi be considered: Probable ftow range Acceptable head loss Required accuracy Condition of liquid Probably all of the devices will work, but usually one type will be the most suited to the installation. It must be remembered that a weir will Dot function properly ifthe weir nappe is Dotaerated, and the flume must be maintained at criticat depth; otherwise these devices do Dot function properly. Nappe aeration is largely a question of level in the receiving channel. If the líquid rises so that clearance is insufficient for aeration, accurate flow measurement is impossible. When the flow drops so that the nappe is Dot aerated but is drawn to the weir edge by capillary attraction, the device does Dot operate properly. Minimum weir flows are difficult to calculate because they depend to some degree on the nature of the weir. If the weir is properly sized, mínimum flow will produce a substantial, measurable amount of head over the weir. Figure 4-17 shows the relationship between level and flow for the ParshalI flume (Figure 4-16). Dimensions and maximum and mínimum flows for the flume are tabulated in Table 4-3.

Fig. 4-18. V-Notchweir with ftoat-and-cable.

FLOW MEASUREMENT 117

Velocity

Flowmeters

Magnetic Flowmeter The principIe of the magnetic ftowmeter was first stated by Faraday in 1832, but did Dot appear as a practical measurement for the process plant until the 1950s.Its advantages are no obstruction to ftow, hence no head loss; it can accommodate solids in suspension; and it has no pressure connections to plug up. It is very accurate and has a linear ftow rate to output relationship. Its disadvantages are that measured material must be líquid; the líquid must bave some electrical conductivity; and it is expensive. Operation Operation ofthe magnetic ftowmeter is based on Faraday's well-known law of electromagnetic induction: The voltage (E) induced in a conductor oflength (D) moving through a magnetic field (H) is proportional to the velocity (V) of the conductor. The voltage is generated in a plane that is mutually perpendicular to both the velocity ofthe conductor and the magnetic field. Stated in mathematical form:

E = CHDV

(4-11)

where C is a dimensional constant. Industrial power generators and tachometer generators used for speed measurement operate on the same principIe, electrically conductive process liquid acts in a similar manner to a rotor in a generator. That is, the liquid passes through a magnetic field (Figure 4-19) induced by coils (Figure 4-20) built around a section of pipe. The process liquid is electrically insulated from the pipe, or flow tube, by the use of a suitable lining when a metal tube is used, so that the generated voltage is Dot dissipated through the pipeline. Two metallic electrodes are mounted in the flow tube and insulated from it; a voltage is developed across these electrodes that is directly proportional to the average velocity of the liquid passing through the magnetic field. Because the coils are energized by altemating current power, the magnetic field and resultant induced voltage is altemating. This generated voltage is protected from interference, amplified, and transformed into a standard dc current signal by a transmitter or converter. Line voltage variations are canceled by the circuits employed. The magnetic flowmeter measures volume rate at the flowing temperature independent of the effects of viscosity, density, turbulence or

FLOW MEASUREMENT 119

suspended material. Most industrialliquids can be measured by magnetic flowmeters. Exceptions are someorganic chemicals and most refinery products. Water, acids, bases, slurries, liquids with suspended solids, and industrial wastes are commou applications. The limitation is the electrical conductivity ofthe liquido The magnetic flowmeter offers no more restriction to flow than an equivalent length of pipe, Figure

4-21. Structurally, a magnetic flowmeter consists of either a lined metal tube, usually stainless steel because of its magnetic properties, or an unlined nonmetallic tube. Linings for the metal tubes can be polytetrafluoroethylene (Teflon), polyurethane, or some other nonmagnetic, nonconducting material. The electrodes are suitably insulated from the metal tube. Nonmetallic fiberglass flow tubes do llot require any lining. The electrodes most be insulated so that the voltage generated can be measured across the electrodes. The insulation has no bearing on the actual voltage generation, bot without the insulator, voltage would bleed off through the metallic walls of the tube. The coils are similar in design to the deflection coils used on a television picture tube. Two coils are used and work together to create a uniform magnetic field. The coils are generally series-connected, but mar be parallel-connected if the measured flow velocity is low. The signal output from the flow tube's electrodes is an altemating

Fig. 4-21. Unobstructedftow.

120 FEEDBACK PROCESSCONTROL

voltage at supply frequency. This 10w-Ievel voltage is generally between 1 mV and 30 mV at full flow rate. This 10w-Ievel altemating voltage must be measured and converted either into a record or display or into a dc common denominator transmission signal. This signal, typically 4 mA at zero and 20 mA at full scale, can be fed into a recorder or controller. The device that can accomplish tros is a special type of transmitter. This transmitter is located either directly on the flow tube (Figure 4-22), near it, or within the control room. The preferred location is as near to the flow tube as possible; temperature and corrosive conditions are the constraints that dictate location. In some applications a digital or pulse rate signal output Cromthe transmitter mar be required, and this option is available.

Accuracy The accuracy of most magnetic ftowmeter systems is 1 percent of fullscale measurement. This includes the accuracy of both the meter itself and its secondary instrument. Because ibis type of meter is inherently linear, its accuracy at low-ftow rates exceeds the practical accuracy of such inferential devices as the Venturi tube. Accuracy of the Venturi is :tO.75 percent, according to ASME Fluid Meters Report, and thai of the secondary instrument is abolli :tO.5 percent. At the low end ofthe measurement scale, secondary instrument readability decreases owing to the square root relationship. The magnetic ftowmeter can be labora-

Fig. 4-22. Foxboromagneticftow tube andtransmitter.

FLOW MEASUREMENT 121

torr calibratedto an accuracyof 0.5 percentof full scaleand is linear throughout. Vortex Flowmeter The Foxboro Vortex ftowmeter, as shown in Figure 4-23, measures liquid, gas, or steam ftow rates using the principIe of vortex shedding. The transmitter produces either an electronic analog or polse rate signallinearly proportional to volumetric ftow rate. Principie or Operation The phenomenon of vortex shedding can occur whenever a nonstreamlined obstruction is placed in a flowing stream. As the liquid passes around the obstruction, the stream cannot follow the sharp contours and becomes separated from the body. High-velocity liquid particles flow past the lower-velocity (or still) particles in the vicinity ofthe body to form a shearlayer. There is a large velocity gradient within this shear layer, making it inherently unstable. The shear layer breaks down arter some length oftravel into well-defined vortices as shown in Figure 4-24. These vortices are rotational flow zones that form altemately on each gide ofthe element with a frequency proportional to the liquid flow

Fie. 4-23. Vortexflowmeter.

122 FEEDBACK PROCESSCONTROL

Fig. 4-24. Vortexsheddingphenomenon.

rate. Differential pressure changes occur as the vortices are formed and shed. This pressure variation is used to actuate the sealed sensor at a frequency proportional to vortex shedding. Thus, a train of vortices generates an altemating voltage output with a frequency identical to the frequency of vortex shedding. This frequency is proportional to the flow velocity. The voltage signal from the detector (Figure 4-25) is conditioned and amplified for transmission by electronics located in a housing mounted integral with the flowmeter body. The final output signal is available either in pulse fonn with each pulse representing a discrete quantity of fluid for totalizing or, optionally, as a 4 to 20 mA dc analog signat for flow rate recording or control. Turbine

Flowmeter

The turbine meler derives its name from its operating principie. A turbine wheel (rotor) is set in the path ofthe flowing fluid. As the fluid enters the open volume between the blades of the rotor, it is deflected by the angle of the blades and imparts a force causing the rotor to turo. The speed at which the rotor turos is related, over a specified range, linearly to flow rate. Several methods are employed to transmit this motion to a readout device outside ofthe conduit. In some applications a mechanical device convers the rotor motion directly to a register. In process applications,

Fig. 4-25. Geometryofvortex generator.

FLOW MEASUREMENT 123

however, the usual method is to use an electrical method. A coil containing a permanent magnet is mounted on the meter body. The turbine flowmeter (Figure 4-26) consists of a section of metal pipe, a multibladed rotor mounted in the center ofthe straight-through passage,and a magnetic pickup coil mounted outside the fluid passage. A shaft held in place by fixed radian vanes supports the rotor assembly. As each blade tip of the rotor passesthe coil it changesthe flux and produces a pulse. The total number of pulses indicates the volum e of fluid which has passed through the meter and the rate of the pulses generated becomes a measure of flow rate. Turbine flowmeters are frequently employed as sensors for inline blending systems. Turbine flowmeters bave excellent accuracy and good rangeability. They are limited to clean fluids. They are expensive, but do bave unique features. Other Flowmeters

Other ftowmetersthat mar be found in someprocessplantsincludethe ultrasonic,the thermal, a varietyofpositive displacementtypes, metering pumps,and others. The ftowmetersdescribedaccountfor the majority of the ftow rate measuringdevices in everydayuse.

Fig. 4-26. Thrbineflowmeter.

124 FEEDBACK PROCESSCONTROL

Conclusion

Unfortunately, there is no best flowmeter. Factors such as accuracy, pressure loss, material to be measured, ease of changing capacity, and ease of installation along with cost must be carefully considered. Once the details of the problem bave been gathered and the possible alternatives considered, the best selection will usually be clear. Some of the systems described read correctly to within a few percent. Some are considerably better. All should bave good repeatability-the all important criterion for control.

Questions 4-1. Match the head meter primary devices with the application (select asingle rest answer for each): Orifice plate ~ r.I. T-. Hígh-pressure~~~._~recovery Flow nozzle Venturi tube Pitot tube-

Elbow taps-e.

-c.

b. Air ducts Sedimentin líquid d. Economyand accuracyare important No straightrun available

4-2. A differentialpressuretransmitteris calibratedOto 80 inchesof water and transmitsa 4 to 20 mA dc signal.This transmitteris placedacrossan orifice plate which is sizedto create80 inchesof water differentialat 6 gallons per minute. Whatis the flow rate whenthe signalis 13 mA dc? 8. 4.5 gpm c. 3.4 gpm b. 3.9 gpm d. 4.9 gpm 4-3. For the equipmentdescribedin the precedingquestion,what will the signalbe if the flow rate is 4 gpm? 8. 13.3mA dc c. 8.9 mA dc b.11.2mAdc d.6.7mAdc 4-4. Assumethe line used in Questions2 and 3 is a Yz-inchschedule40pipe (IV = 0.622inches).Pind the orifice boTeusedto satisfythe conditionsgiven if the measuredfluid is water at 600P. a. 0.190inches c. 0.414inches b. 0.556inches d. 0.352inches 4.5. The bestchoiceof orifice taps in the precedingproblemwould be: a. flangetaps c. pipetaps b. venacontractataps d. cornertaps

FLOW MEASUREMENT 125

4-6. A 2-inch schedule 40 line {lD = 2.067) is used to carry gasoline (SP GR = 0.75). The ftow rate is measured with an orifice plate (d = 1.034)and pipe taps are used. At full ftow rate a ditIerential pressure of 50 inches of water is produced. What is the approximate full ftow rate in gpm? 8. 30 gpm c. 250 gpm b. 53 gpm d. 36 gpm 4-7. Assume an 8-inch schedule 160 pipe (ID = 6.813 inches) carries a full ftow of 40,000pounds per botir of dry saturated steam. The static pressure is 335 psi. Flange taps are used and the ditIerential pressure across the orifice plate at full-ftow rate is 1OOinches of water. What is the size of the bare in the orifice plate? 8. 4.357 inches c. 2.271 inches b. 3.645 inches d. 5.109 inches 4-8. Fuel gas is carried in a 6-inch schedule 40 pipe (ID= 6.065 inches). Flow rate is measured with an orifice plate using fiange taps and the bare in the orifice is 3.457 inches. The specific gravity is 0.88, the fiowing temperatur~ is 60°F, and the static pressure is 25 psi. Maximum fiow rate creates a ditIerential of 20 inches of water. What is the approximate fiow rate in cubic feet per day? 8. 1,500,000SCFD c. 2,500,000SCFD b. 2,000,000SCFD d. 3,000,000SCFD 4-9. 8. b. c.

The output of a target fiowmeter is: Proportional to volumetric fiow rate Proportional to the square of volumetric fiow rate Proportional to the square root of volumetric ftow rate

4-10. 8. b. c. d.

The output signal or reading of a magnetic fiowmeter is: Proportional to volumetric fiow rate Proportional to the square of volumetric fiow rate Proportional to the square root of volumetric fiow rate Inversely proportional to volumetric fiow rate

4.11. With suspended solids and/or entrapped gas in a fiowing liquid, the magnetic fiowmeter will: 8. Read high b. Read low c. Read the liquid fiow only d. Read the correct total volume of the mixture 4-12. A turbine fiowmeter produces an output in the form of pulses. The total number of pulses is: 8. Inversely proportional to fiow b. Directly proportional to total ftow c. Proportional to the square root of fiow d. Proportional to the square of fiow

Temperature and Humidity Measurements

Temperature and moisture measurementsare important in process con-trol, both as direct indications of system or product state and as indirect indications of such factors as reaction rates, energy flow, turbineefficiency, and lubricant quality.

Temperature

Presenttemperaturescalesbave been in use for about 200years. The earliest instruments-variations of the common stem thermometer-were basedon the thermal expansionof gasesand liquids. Suchfilled systemsare still employedfrequently for direct temperaturemeasurement, although many other types of instrumentsare available. Rep-resentative temperaturesensorsinclude: Filled thermal systems Liquid-in-glassthermometersThermocouplesResistance temperaturedetectors (RTDs) 126

TEMPERATUREAND HUMIDITY MEASUREMENTS 127

Thermistors Bimetallic devices Optical and radiation pyrometers Temperature-sensitive profitS Various types of measurement control systems are compared in Table

5-1. Instrument selection must anticipate overall control requirements. Low cost often justifies consideration of filled systems for measurements below 1,200oPor 650°C. Other advantages of mechanically or pneumatically transmitted temperature measurements include lowexplosion hazard, simple maintenance requirements, high reliability, and independence Crom external power. Advantages of electrical systems include higher accuracy and sensitivity, practicality of switching or scanning several measurement points, larger distances possible between measuring elements and controllers, replacement of components Table5.1. Comparisonof TemperatureMeasuringSystems ComparisonFactors Purchase cost Long distance transmission Change or replacement oí components lnstallation costs Maintenance Averaging measurement Surface measurement Time constant (bare bulb and no well) Temperature difference Sensitivity

Accuracy Operating costs

Least Favorable

Most Favorable

lntermediate

F E

p p

EandP F P T T

F P E

F F R

T R

E R F

Key: F Filled system. P PneumaticaIly transmitted filled system. T ElectricaI thermocouple system.

F F P F E

F R

T F P and T P

R Electrical RTD system. E Electrical thermocouple and RTD systems equally rated. oGeneral purpose wiring only. Explosion-proof electrical systems cost considerably more than other types.

128 FEEDBACK PROCESSCONTROL

(rather than complete systems) in the event of failure, fast response, and ability to measure higher temperatures.

Filled Thermal

Systems

Filled thermal systems, which traditionally bave been used most in the food, paper, and textile industries, consist of sensors (bulbs) connected through capillary tubing to pressure or volume sensitive elements (Figure 5-1). These systems are simple and inexpensive and generally bave fast dynamic responses. Their use with pneumatic and electronic transmitters has removed inherent distance limitations of filled systems and has minimized the danger of capillary damage. Moreover, transmitter amplification has made narrow spans practical and has improved linearity and response. Application specifications of several types of filled systems are listed in Table 5-2. These include the Scientific Apparatus Makers Association (SAMA) Classes I (liquid-expansion), 11(vapor-pressure), III (gas-pressure), and V (mercury-expansion). The SAMA Class 11 classifications also include alphabetical designations, by which A and B indicate sensorabove and below case ambient, respectively; C indicates a system in which the sensorcan cross ambient; and D denotes a system which can operate at ambient conditions. Liquid-expansion systems are characterized by narrow spans, small sensors, uniform scales, high accuracy, and capability for difIerential measurements. Class lA devices bave an auxiliary capillary and

Fig. 5-1. Filled measurement systemsgenerallyare the mostinexpensiveway or measuringandcontrollingtemperature.

TEMPERATURE AND HUMIDITY

MEASUREMENTS

129

Table5-2. Instrumentsfor Filled ThermalSystemSensors Gas

Type Principie SAMA Class

Liquid Volumechange

fluids Lower range limit Upper range limit

Organic liquido (Hydro-carbons) -200"F (- I3IY'C) +6OO"F(+315°C)

Narrowest span (b) Widest span

40°F (25°C) 600'F (33IY'C)

71Y'F (4IY'C) (c)

Ambient temperature

lA Full

Not required

Compensation Sensor size

IB Case

Smallest

Medium

Largest

Typical sensor size for 1000Cspan

9.5mm (0.375 in.) 00 x 48mm (1.9 in.) long

9.5mm (0.375 in.) OD x 50mm (2 in.) loog

22mm (,. ÍD.) OD x 70mm (6 ín.) lang

Overrange capabiJity Sensor elevation elfect

Medium

Least

None

Class llA, Ves Class lIB, NODe

Greatest None

Barometric pressure effect (altitude)

None

Slightly (greatest on smaIl spans)

Scale uniformity

Unifonn "'°.5 to "'1.0% ofopan

Non-Uniform

Uniform

;:0.5to;:I.0%ofspan upper % of scaIe

;:O.5to;:I.0%of

spon

#1-ClasslIA

Accuracy

Response (d) #1 Fastest

Vapor (a) Pressure change 11

Pressure change III

arganic liquido

Puregases

(Hydro-carbons), water -425°F

(-2SS"C)

+6OO'F (+3IS0C)

400'F (215°C)

-45SOF (-2700C) +l,4OO'F(+7ro'C) 1200F(700C) 1.000'F (5500C)

IIIB case

#3-Class

Slightly (greatest o small spans)

lIB

#4 Slowest Cost Maximum CapiIlary

standard length

Highe.1

Lowest

Medium

Clos. lA 30m or 100fI.

30m or 100 fi.

30m or 100I

Clas. IB 6mor 20fi.

(a) Class 11 systems are supplied as either SAMA Class llA or lIB. In Class llA, sensor is aIways hotter than tubing or instrument case. In Class lIB, sensor is always cooler than tubing or case. (b) Narrowest spans vary at elevated temperatures. (c) Smaller spans available in cryogenic regions. (d) Actual values depend on range, capillary length, sensor dimensions, and type of instrument used.

element to provide ambient temperature compensation and IB systems often utilize bimetallic techniques. However, fully compensated liquid-expansion systems are complex and, therefore, expensive. Vapor-pressure systems are reliable, inherently accurate, and require no compensation for ambient temperature effects. Instruments follow the vapor-pressure curves ofthe filled fluid, and associated dials and charts are thus nonunifonn, featuring more widely spaced increments at high temperatures. Measurements occur at the interface between liquid and va,porphases of the filling medium. If the temperatufe in the sensorexceeds that in the capillary and indicating element, the sensoris filled with vaporwhile the capillary and indicatorcontain liquido

130 FEEDBACK PROCESSCONTROL

The converse is true when the relative temperature polarity is reversed. A transition between liquid and vapor can cause erratic operation, so that vapor systems mar be unsuitable for ranges that cross the element and capillary temperatures. Systems mar also be unacceptable if uniform recording or indicating scales are desired. Gas-pressure systems, which rank second to the vapor-pressure devices in simplicity and cost, ofIer the widest range of all filled systems. Conventional designs use large-volume sensors, which mar be shaped to suit particular applications. For example, in duct-temperature averaging, the sensor mar be constructed of a long length of tubing of small cross section. Conventional recorders are Dot recommended for temperature spans of less than 200°F or 110°C, but transmitters operating on force-balance principIes can be utilized with spans as narrow as 50°F or 28°C. With gas-filled systems, it is difficult to compensate for ambienttemperature errors, but a sufficiently large sensor size mar reduce efIects to acceptable limits. Mercury-expansion systems are classified separately from other liquid-filled systems because of the unique properties of the fluid. For example, mercury is toxic and harmful to some industrial processes and products, and high-liquid density places limitations on sensor-toinstrument elevation difIerences. Sensors used in mercury-expansion systems are generally larger in diameter and more expensive than those used in either liquid or vapor systems. For these reasons, mercury is frequently bypassed in favor of other filling media.

Electrical

Systems

Electrical temperature sensorsbave long been popular in the metal and paper industries, but increasing use of ele<òtronicdevices has stimulated application in a variety of other areas. Thermocouples and resistance temperature detectors (RlDs) are most widely used, and representative application data are given in Table 5-3. Thermocouples

Thermoelectricity was discovered by Seebeck in 1821.He observed an electromotive force (emt) generated in a closed circuit oftwo dissimilar metals when their junctions were at different temperatures. This electricity, produced by the direct action of beat, is used today to measure temperatures from subzero to high ranges.

TEMPERATURE AND HUMIDITY

MEASUREMENTS

131

Table5.3. Quick-ReferenceSelectorChart for Standard Thermocouples& RTDs TEMPERATURE LIMITS Sensor

Calibration

r -°F oc

RTDs

Nickel Platinum

SAMA Type 11 SAMA 100 ohm, or

-200 to 315

-320

DIN 43760

-200 to O to -210 to -270 to -270 to -270 to -50 to

-320 to 1,200 32 to 300

Copper SAMA Thermocouples Iron-Constantan, ISA Type J Copper-Constantan, ISA Type T Chromel-Alumel, ISA Type K Chromel-Constantan, ISA Type E Platinum-Platinum Rhodium, ISA Types R & S ISA Type B

650 150 760 370 1,260 870 1,480

o to 1,700

to 600

-350 -455 -455 -455 -55

to to to to to

1,400 700 2,000 1,600 2,700

o to 3,100

A thermocouple consists basically of two dissimiliar metals, such as iron and constantan wires,joined to produce a thermal electromotive force when thejunctions are at different temperatures (Figure 5-2). The measuring, or bot, junction is inserted into themedium where the temperature is to be measured. The reference, or cold, junction is the open end that is normally connected to the measuring instrument terminals. The emf of a thermocouple increases as the difference in junction temperatures increases. Therefore, a sensitive instrument, capable of measuring emf, can be calibrated and úsed to read temperature directly.

< MEASURING JUNCTION

Fi2. 5-2. Thennocouple.

THERMOCOUPLE [JINSTRUMENT REFERENCE JUNCTION

132 FEEDBACK PROCESSCONTROL

Figure 5-3 indicates the approximate emf-millivolt output versus temperature relationship for the most popular thermocouple types. Deviation from the essentially linear relationship is generally less than 1

percent. Introduction of intermediate metals into a thermocouple circuit will Dot affect the emf of the circuit, provided the new junctions remain at the same temperature as the originaljunction. The algebraic sum ofthe emf' s in a circuit consisting of any number of dissimilar metals is zero, if all of the circuit is at a uniform temperature. Repeating the law, if in any circuit of solid conductors the temperature is uniform from Point 1 through all the conducting material to Point 2, the algebraic sum ofthe emf' s in the entire circuit is totally independent of the intermediate material and is the same as if Points 1 and 2 were put in contact. If the individual metals betweenjunctions ofthe circuit are hom*ogeneous,the

Fig. 5-3. Temperature-emf valuesapproximatethe relationshipof six standard thermocouples.The conditionsof a particularinstallationmar requireloweringthe maximumtemperatureto avalue belowthat listed. Temperature/millivolt curvesare availablein the appendix.

TEMPERATUREAND HUMIDITY MEASUREMENTS 133

sum ofthe thermal emf's will be zero, provided only that thejunctions of the metals are all at the same temperature. The emf in a thermoelectric circuit is independent of the method employed in forming the functions as long as all the junction is at a uniform temperature and the two wires make good electrical contact. The junction mar be made directly, by welding, or by soldering. Furthermore, an instrument for measuring the emf mar be introduced into a circuit at any point without altering the resultant emf, provided the junctions that are added to the circuit by introducing the instrument are all at the same temperature. If the temperatures of the new junctions are DOt uniform, the effect is that of introducing additional thermocouples into the circuit. Reference Junction To make accurate temperature measurements with thermocouples, the reference junction temperature must remain constant; if it varies, suitable compensation for these variations must be provided. Should there be an uncompensated variation in the reference junction temperature, there will be a corresponding change in the millivoltage with a resultant error in temperature measurement (Table 5-4). When used in the laboratory and for other checking and testing purposes, the thermocouple reference junction can be placed in a vacuum bottle filled with shaved ice saturated with water. This method provides close temperature control (within a fraction of a degree) and permits accurate reading. Table5-4. StandardLimits or Error Coupleor Wire

Range

Limits

Copper-constantan

-300 to -75°F -75 to +2000F 200 to 700°F -100 to + 530"F

:t2% oCreading :tl~oF:t~ % oCreading :t4°F

Chromel-alumel

530 to l ,400"F Oto 530°F 530 to 2,300"F

:t~% oCreading :t4°F

Platinumrhodiumplatinum

Oto 1,000°F 1,000to 2,700"F

Iron-constantan

:t~% oCreading :tJoF :tO.J% oCreading

75 KX

134 FEEDBACK PROCESSCONTROL

~~ WIRE~[]

THERMOCOUPLE

MEASURING JUNCTION

EXTENSION

INSTRUMENT

CONNECTION HEAD

REFERENCE JUNCTION

Fig. 5-4. Typical thermocoupleand extensionleads.

To ensure accurate readings, most thermocouples are now installed with instruments thai provide automatic reference junction compensation. In most instruments, ibis is accomplished by passing current through a temperature-responsive resistor, which measures the variations in reference temperature and automatically provides the necessary compensating emf by means of the voltage drop produced across

it. An industrial installation generally consists of a thermocouple with its connection head, the necessary length of extension wire, and an indicating, recording, or controlling instrument with internal and automatic reference junction compensation. The extension wires generally consist of the same materials as the thermocouple elements, or mar be composed of other materials and alloy wires that generate essentially the same millivoltage as the thermocouple for application temperatures up to approximately 400°F or 200°C(Figure 5-4). The ISA symbols and color codes for thermocouple lead wires are given in Table 5-5.

Table 5.5. Extension Wire Type Designations and Standard Limits of Error [SA

Extension

Type

Wire

Color Code

Copperconstantan Ironconstantan Ironcupronel Chromelalumel CopperCuNi alloy

+ (blue) -(red) + (white) -(red) + (green) -(red) + (yellow) -(red) + (black) -(red)

Limits 01 TemperatureRange F Error -75 to +200

:t 1~F

Oto

400

:t4 F

75 to

400

:6 F

400

:t4 F

75 to

400

:10 F

Couple UsedWith Copperconstantan Ironconstantan Chromelalumel Chromelalumel Platinum Rhodiumplatinum

Fig. <

TEMPERATURE AND HUMIDITY

MEASUREMENTS

135

5-5. Thermocouplesin para11el.

A verage Temperatures To measure the average temperature across a large duct or vessel, or around a retort, any number of thermocouples mar be used in parallel connections. The voltage at the instrument, or at the point of parallel connection, is the average of that developed by the number of thermocouples used. This voltage is equal to the sum of the individual voltages divided by the number of thermocouples. For accurate measurement, the resistances of aU thermocouples and extension wire circuits should be identical. Since the resistance of the actual thermocouple wiU vary with temperature, and since the lengths of extension wires mar also vary, the efIect of these variations can be minimized by using swamping resistors. The values of the swamping resistors should be high in comparison with the change or difIerence in resistances encountered. A resistor value of 1,500 ohms generaUy works weU. In order to prevent the flow of current through a ground loop, the thermocouples should not be grounded. AU thermocouples must be of the same type and must be connected by the correct extension wires (Figures 5-5 and 5-6). ParaUel connection of thermocouples for average temperature measurement is advantageous because the instrument construction and

Fig. 5-6. Parallelthennocoupleswith swampingresistors.

136 FEEDBACK PROCESSCONTROL

calibration can be the .sameas that for a single thermocouple. Two or more thermocouples mar be connected in series to measure average temperatures; however, this circuit requires that the instrument bave special reference junction compensation to provide the increased compensating emf for the specific number of thermocouples in the circuit. The instrument also must be calibrated for the total millivoltage output of the number of thermocouples used in series. Extension wires Crom each thermocouple must be extended back to the actual reference junction at the instrument. Differential Temperatures Two thermocouples may be used for measuring differential temperatures between two points. Two similar thermocouples are connected with extension wire of the same material as is used in the thermocouples. The connections are made in such a way that the emf's developed oppose each other. Thus, if the temperatures of both thermocouples are equal, regardless of the magnitude, the net emf will be zero. When different temperatures exist, the voltage generated will correspond to this temperature difference, and the actual difference may be determined Cromthe proper calibration curve. An instrument calibrated either for Omillivolts at midscale or Omillivolts at the end of the scale, depending upon whether thermocouples are operated at high or low temperatures with respect to each other, may be fumished and used to read temperature difference directly. Copper leads may be used between the instrument and the connection box that links the instrument to the thermocouple or extension wires (Figure 5-7). The instrument should Dot bave the reference junction compensation normally fumished when measuring temperatures with thermocouples. As in the case of parallel thermocouple connections, the thermocouples should Dot be grounded and the resistance of both thermocouple circuits should be the same.

Fig. 5-7. Two thermocouplesusedto measuretemperaturedifference.

TEMPERATUREAND HUMIDITY MEASUREMENTS 137

Thermocouple Calibration Curves Thermocouples develop an extremely small dc voltage, measured in thousandths of a volt. The millivolt output falls within a range of -11 to + 75 millivolts, depending on the type of thermocouple and its temperatufe working range. Calibration curves for thermocouples are included in the Appendix. Now let us consider some typical thermocouple instruments and investigate their functions.

PotentiometricRecorder Figure 5-8 shows a simplified circuit diagram of the Foxboro potentiometric recorder (Figure 5-9). An emf input (Ex) is derived Croma thermocouple or other measuring element. A constant emf (Ez) is supplied by a Zener diode regulated power supply. As Ex varies, an error signal is developed, and the circuit becomes unbalanced. The error signal is converted to an ac voltage by a field effect transistor chopper and amplified by the integrated circuit amplifier. The amplified output drives a two-phase balancing motor. The direction of rotation depends on whether Ex has become greater or smaller. The motor moves the wiper contact on the slidewire Rsto a position where the circuit is rebalanced. The slidewire coritact is mechanically con-nected to the recorder pen, and both are positioned simultaneously. With a thermocouple input, a temperature sensitive resistor (Rc) automatically compensates for referencè junction ambient temperature variations. This resistor changes the balance of the circuit to cancel

138 FEEDBACK PROCESSCONTROL

Fig. 5-9. Foxboro stripchart recorder.

changes in Ex with reference junction temperature variations. For straight millivolt inputs, Rc is a temperature-stable resistor. The slidewire is characterized to allow the use of uniform charts and"scales with thermocouple and certain other nonlinear measurements. Thisis accomplished by varying the resistance per unit length along the slidewire. lf the temperature measurement is used in conjunction with an electrical control system, a thermocouple-to-current transmitter mar be used. A typical transmitter is shown in Figure 5-10. The transmitter provides a two-wire output; the same wiring 'is used for both power and output. The load resistance is connected in series with a dc power supply (approximately 25 volts), and the current drawn Cromthe supply is the 4 to 20 mA dc output signal. Field mounting the transmitter at or near the actual measurement point eliminates the installation of special thermocouple extension wires to the receiver. ln some cases, this procedure can also improve the performapce of the measurement loop, since the possibility of extension wire error is avoided. As shown in Figure 5-10, the thermocouple/millivolt bridge circuit consists of a precision-constant current source, a reference-junction compensator, a bum-out detection current source, and associatedresistors. The amplifier is a very high gain, chopper-stabilized

TEMPERATURE, AND HUMIDITY MEASUREMENTS 139

Fig. 5-10. Simplifiedcircuit diagramof the Foxboro thermocoupletransmitter. (Bottom)Foxborothermocoupletransmitter.

amplifier. It functions as a null detector by controlling the 4 to 20 mA dc output corrent to maintain a null between the compensated thermocouple and feedback volt3;ges. The transmitter is protected from reverse polarity connection ofthe power supply by means ora diode in the negative lead of the output circuit. The maximum error for this transmitter is approximately :t0.25 percent of span. Many control instruments, such as this transmitter, feature thermocouple bum-out protection. In the event of an open thermocouple, a s mall voltage applied to the instrument causes it to read full-scale output. This causes the control system to shut off. the beat and prevent damage. Resístance Thermal

Detectors

Resistancethermometry is based on the change of electrical conductivitv with temperature.Therefore.a coil of wire can act as a tem-

140 FEEDBACK PROCESSCONTROL

perature sensor, with 'a direct relationship established between resistance and temperature. Standard curves are available, with certified accuracies within O.I°F or oC. Platinum RTDs used as laboratory standards can be obtained with tolerances well within this límit, and are capable of precise temperature measurement up to l,650°F or 900°C. If an RTD is adjusted to conform to its curve, it may be interchanged with other RTDs calibrated according to the same curve.

Resistance-thermaldetector temperature measurementmay be read out on many different types of instruments. If the measurement of temperature were to be used in conjunction with a pneumatic control system, the RTD could be attached to a resistance-to-pneumatic convertor, such as the Foxboro Model 34B (Figure 5-11). The resistance-to-pneumatic convertor converts the temperature measured by a resistance-temperature element into a proportional 3 to 15 psi or 20 to 100kPa pneumatic output signal. This signal is suitable for use with many types of pneumatic receiving instruments, such as controllers, recorders, and vario us computing instruments. This transmitter has several features. For example, when used with

Fig. 5-11. Foxboro 34BSeriesresistancepneumatictransmitter.

TEMPERATURF;AND HUMIDITY MEASUREMENTS 141

Fig. 5-12. Simplified circuit diagram of 34B Series nickel RTD transmitter.

the appropriate nickel bulb, the converter has an output that is linear with temperature. Spans as low as 5°F or 3°C can easily be achieved. An adjustable range allows a simple field calibration procedure to change the temperature input range required for a 3 to 15 psi or 20 to 100kPa output. It also operates on all normal supply voltages. This transmitter is an electromechanical device consisting of a solid-state, integrated circuit amplifier and an output transducer. Figure 5-12 isa simplified circuit diagram of the nickel RTD version of the transmitter. The transd ucer is shown in Figure 5-13. The RTD is wired into a measurement bridge and excited Croma regulated direct current power supply. The change in resistance of the RTD causes a bridge output change that is proportional to temperature. Negative feedback is obtained Cromthe output current and applied to the opposite side of the measurement bridge. A change in feedback by the span adjustment changes the gain of the amplifier and thereby changes the span of measurement.

Fig. 5-13. Outputtransducer.

142 FEEDBACK PROCESSCONTROL

The platinum RTD transmitter incorporates a negative impedance,integrated circuit amplifier that shunts the platinum RTD to linearizethe temperature versus the RTD characteristic. The amplifier section provides the high input impedance and gainrequired to amplify the low-input signal. The input signal is first converted to ac by an FET (used as a chopper) and then applied to a high-gain ac amplifier. Thè signal is next demodulated and applied to a voltage follower. The output of this amplifier is applied to a power transistor to supply the 10to 50 mA dc required by the transducer coil. A functional diagram applying to the output transducer is shown in Figure 5-13. The direct current input signal is converted into a proportional air output signal as follows: A coil is positioned in the field of a fixed, permanent magnet. When a direct current flows through the coil, the electromagnet and permanent magnet forces are in opposition. Any increase in the current, which causes a proportional increase in the force on the coil, tends to close the flapper against the nozzle. The air output pressure from the pneumatic relay is thereby increased. This increased pressure is fed to the feedback bellows to exert a force on the force beam to rebalance the force from the coil. All ofthe forces which act upon the force beam are balanced in this manner, and the pneumatic output tracks the current input. The capacity tank (C2) and the associated restrictor provide dynamic compensation to the circuit. During rapid input changes, the restrictor will effectively keep the capacity tank out of the circuit for faster feedback response through the relay. For slow changes, the capacity tank acts to damp pressure fluctuations and to provide a smoother output. The small capacity tank (C.) in the output circuit provides necessary constant damping. During alignment or calibration of the output transducer, zero adjustment is made by tuming a screw to advance or retract a spring which bears on the force beam. Coarse span adjustments are made by repositioning the feedback bellows with respect to the pivot. Wheatstone Bridge Recorder One of the most popular instruments used with RTDs is the slidewire type Wheatstone bridge recorder. This instrument is almost identical to the potentiometric recorder previously described and shown in Figure 5-9. Figure 5-14 shows a simplified circuit diagram of the Wheatstone bridge recorder. The resistance temperature detector (RTD) is one arm of a Wheatstone bridge excited by a Zener diode regulated dc power supply. Point A (the slidewire contact) and roini B form the input to the amplifier. When the temperature changes, the resistance of the RTD

TEMPERATURE AND HUMIDITY

MEASUREMENTS

143

Fig. 5-14. SimpIified Wheatstone bridge recorder circuit.

changes. This unbalances the bridge and creates an error signal between Points A and B. As in the potentiometric recorder, the error signal is converted to art ac voltage by a field-effect transistor chopper and amplified by the transistorized amplifier. The output drives a two-phase balancing motor. The direction of rotation depends on the polarity of the error signal. The motor moves the wiper contact on the slidewire until the bridge is rebalanced and no error signal exists. The pen and slidewire contact are mechanically connected and therefore positioned simultaneously. With all resistance-temperature measurements, the use of threeconductor RTD cable is recommended. The effect of ambient temperatufe variations on the cable is thereby minimized. If the cable connecting the RTD to the instrument has only two conductors, these conductors become part of the resistance being measured. The result then is an error that will vary with ambient temperature. Remember, with all resistance temperature measurements, three-conductor RTD cable is recommended. The purpose of the threeconductor cable is to stretch out the measuring bridge. Note the threeconductor cable in Figure 5-14. One of the conductors is common to both sides ofthe bridge while the other two connect one to each side of the bridge. Any change in cable temperature will be canceled as both sides of the bridge are changed a like amount. Occasionally RTD sensors use a four-wire cable. This is generally in conjunction with a Kelvin double bridge. The four-wire method does an excellent job of reducing temperature effects on the cable. The improve ment over the three-wire method, however, is minimal. In practice, an RTD may be used with as much as 500 feet of threeconductor cable without the cable creating a perceptible error.

Thermistors

144 FEEDBACK PROCESSCONTROL

Thermistors are made of heat-treated metallic oxides, and most thermistors differ from ordinary resistors by having a negative coefficient of resistance. Thermistors are available with a nearly linear temperature resistance relationship, and other types are available with a sharp change in slope at some characteristic temperature. A thermistor can replace an RTD as a temperature sensor. The difficulty lies in obtaining units that fit the desired characteristic curve within acceptable límits of accuracy. When this is accomplished and the thermistor is mounted so as to stand up under process conditions, it performs the same function as the conventional RTD. One advantage of the thermistor is that it has a greater resistance change for a given temperature change than that of the conventional wire RTD. A disadvantage is that the accuracy available, although good, is slightly inferior to that of the conventional RTD. This presumably accounts for the thermistor's limited application in the process

instrumentationfield. Radiation pyrometers utilize an optical system to focus energy radiat~d from a body onto a sensing system. Manual devices are often l:I~ed;'in which energy at infrared or visible wavelengths is focused on a tar~t'aridcompared with the light output of a calibrated optical filamentJ9automated devices, the energy (usually in the infrared band) is focusedori a series arcar ofthermocouples. This thermopile produces a millivolt output related to the temperature of the source. Pyrometers are used where high temperatures are to be measured or where contact with the object is impossible. Accuracy is influenced by such factors as reflections, gases present in the radiation path, and surface emissivity of the body under measurement. Humidity

Measurements

Humidity, or the amount of moisture in gases,is expressedin several differentways, including: 1. Relativehumidity-the actual quantity of water vapor presentin a given spaceexpressedas a percentageof the quantity of water vapor that would be presentin the same space under saturated conditions at the existingtemperature. 2. Absolute humidity-mass of vapor per unit magsof dry gas. 3. Dew point-the saturationtemperatureof the mixture at the correspondingvapor pressure.If the gasis cooled at constantpressure to the dew point, condensationof vapor will begin.

TEMPERATUREAND HUMIDITY MEASUREMENTS 145

A list of the methodsusedto measurehumidity would include the following: RelativeHumidity Measurement Mechanical(hair, wood, skin) Wet and dry bulb thermometers Surfaceresistivity devices(including Dunmore) Crystal frequencychange AbsoluteMoistureMeasurement Gravimetry Electrolysis Infrared Conductivity Capacitance Color change Karl Fischer titration RF power absorption Neutron reftection Heat of absorptionor desorption Nuclear magneticresonance Dew Point Measurement Chilled mirrar Lithium chloride (including DEWCEL) Wet bulb thermometer Direct measurement of relati ve humidity may be accomplished by equating the change in dimension of a hygroscopic substance with the variation in the moisture content of the air. The hair element (Figure 5-15) consists of a band composed of a number of selected and treated human hairs. The membrane element consists of a strip of treated animal membrane. The instrument will record relative humidity between 20 and 90 percent with a maximum error of :t 5 percent. The calibration should be adjusted initially by means of a psychrometer. If the hair element is exposed to humidities over 90 percent or to free moisture, the calibration should be checked. .Hair elements can be used at temperatures as high as 160°For 70°C

146 FEEDBACK PROCESSCONTROL

Fig. 5-15. Hair element.

without damage. However, in this event, they should be calibrated under these temperature conditions. The hair element is extremely responsive to changes in humidity, and will follow gradual or small changes with good speed. However, following a sudden large change, at least 30 minutes should be allowed for the measuring element to reach a state of equilibrium. The psychrometer consists of two temperature measurements. One, called the dry bulb, measures the ambient temperature, while the second, the wet bulb, is provided with a wick or sleeve saturated with water that is evaporating. The wet bulb temperature will normally be lower than that of the dry bulb. The lowering of this wet bulb temperatufe (wet bulb depression) is an indication ofthe moisture content ofthe surrounding air, or of its humidity. See Appendix for convenient conversions of wet and dry bulb readings into relati ve humidity. Example: dry bulb reads 90oP; wet bulb 80oP; difference is 10oP. Pollowing the coordinates to their intersection, we find the relative humidity to be 65 percent. A portable version of this instrument, called a sling psychrometer, provides a convenient way to check the calibration of relative humidity instruments. Their air velocity past the bulb should be 15 feet (4.6 metres) per second or higher for accurate results.

'-+'2.

TEMPERATURE AND HUMlDffY

MEASUREMENTS

147

.'0 .]

.."

I l

, 1001

t, , ,

.. E

~ ~ 2 00" ~ ~ C E

.,~f-.#"

I I

2 C

.fH-~

1--

--'

"- -17' I --/

-fi

-:eo

-40

-00

00 OEW POINT

10 TEMPERATURE

100

140

.F.

Fig. 5-16. Dewceloperatingcharacteristics.

The Foxboro dew point measuring system consists of an element, the DEWCEL, a source of power to energize it, and a temperature instrument to sensethe dew point temperature. The dew point element consists of a cylinder of woven gIass fabric with two windings of carefully spaced gold wires. The two windings do Dot contact each other. The fabric is impregnated with lithium chloride. The windings carry low-voltage power applied through an incandescent lamp ballast resis-

tor. Moisture determination by this lithium chloride element is based on the fact that, for every water vapor pressure in contact with a saturated salt solution, there is an equilibrium temperature at which this solution neither absorbs noc yields moisture to the surrounding atmosphere. This equilibrium temperature is shown in Figure 5-16 as the "DEW-

148 FEEDBACK PROCESSCONTROL

CEL@ Characteristic'Line." Below this equilibrium temperature, the salt solution absorbs moisture. Above this equilibrium temperature, the saturated salt solution dries out until only dry crystals are left. The temperature thus determined may be used as a measure of dew point temperature, absolute humidity, or vapor pressure. The relative humidity of the atmosphere can be determined from a knowledge of the dew point and reference to a vapor pressure curve or chart (see Appendix, Table A-29). Absolute measurements are less common in process applications than relative humidity or dew point determinations, but blast fumace control is one common application of absolute humidity measurement.

Questions

5.1. To obtainthe mostaccuratetemperaturerecord for the range 100°to 150°F,the filled thermal systemselectedwould be: 8. ClassI c. ClassIII b. Class11 d. ClassV 5-2. A resistancethermometerwould be chosenbecauseof: 8. Ability to measurehightemperatures b. Economy c. Higher accuracy d. Simplicity 5-3. Thermocouplesare often chosenbecauseof: 8. High accuracy b. Ability to measurehightemperatures c. Economy d. Ability to measurean extremelynarrow spanof temperature 5.4. The Class11(vapor-pressure) thermometeremploysa nonlinearscale because: 8. It is easierto read b. It maybe ratioedto ftow measurements c. The vaporpressurecurve is nonlinear d. The mechanismemployedcausesnonlinearity 5-5. Which filled thermal system,or systems,would you selectfor measuringthe room temperaturein your house? 8. ClassI c. ClassIII b. Class11 d. ClassV 5.6. A ClassIIIB (gas-filled)systememploysa large bulb to: 8. Minimize the ambienteffectson the connectingcapillary b. Obtainthe optimumdynamicperformance

TEMPERATURE AND HUMIDITY

MEASUREMENTS

149

c. Make a maximumbulb areaavailablefor measurement d. Reducethe powerproducedin the element 5-7. A temperaturerangebetween300°Fand 310°For 149°Cto 154°Cmusi be measuredwith the greatestpossibleaccuracy.The besichoiceof system would be: a. A copper-constantan thermocouple b. A copperRTD c. A nickel RTD d. A ClasslA filled thermalsystem 5.8. a. b. c. d.

A hair elementis usedbecauseit: Measuresabsolutehumidity Is the mostaccuratetype of humidity measurement Is simpleand inexpensive Measuresdew point

5-9. A lithium chloride elementis usuallycalibratedto read: a. Relative humidity c. Absolutehumidity b. Wet bulb temperature d. Dew point 5-10. Lithium chloride is usedbecause: a. It is nonpoisonous b. It is inexpensive c. It is extremelyhygroscopic d. It does noi corrodethe equipment 5-11. Whena wet and dry bulb psychrometeris readto determinerelative humidity: a. The dry bulb will read lower thanthe wet bulb b. The two thermometersmayreadthe same c. The wet bulb will read lower thanthe dry bulb d. A formula maybe employedto relatethe wet bulbreadingto relative humidity 5-12. The purposeof using extensionleadwires thai havethe samethermoelectric characteristicsas the thermocoupleis to: a. Preventcorrosionat all junctions b. Extend the referencejunction backto the instrument c. Preventcreatingan unwantedreferencejunction d. Make the thermocouplesystemoperatein standardfashion5-13. Relative humidity is: a. The moisture presentin a bodyof air expressedas a percentageof saturationat the existingtemperature b. The moisturein a body of air, in gramspercubic meter c. The temperatureat which moisture will condenseCroma bodyof air d. The ratio of actualmoisturein a volumeof air to the moisturethai would exist at optimumcomfort in a similarvolume

150 FEEDBACK PROCESSCONTROL

5-14. A psychrometeris: a. A hair elementinstrument b. A "wet and dry bulb" humidity instrument c. An instrumentthat sensespsychologicaldisturbances d. An instrumentthat readsdirectly in dew point 5-15. A hygrometeris: a. Convenientfor measuringspecificgravity b. An instrumentthat measuresgas weight c. Any instrumentthat measuresmoisturecontent d. Anothernamefor psychrometer 5-16. A certainthermocouplehasa specifiedtime constantof 2 seconds.If the processtemperaturechangesabruptly from 800°to 900°C,the temperature readouton the indicatorattachedto the thermocouplearter6 secondselapse will be approximately: a. 860°C c. 900°C b.835°C d. 895°C 5-17. The air velocity pastthe sensorsof a "wet and dry" bulb instrument shouldbe: a. 50 feet per second,minimum b. 2 metresper second,maximum c. Approximately4.6 metresper second d. Any value 5-18. The advantageof usinga three-wirecableto connectan RTD to its associatedinstrumentis that: a. Referencejunction errors are eliminated b. The effectof ambienttemperatureon the cablewill be minimized c. Potentialfailures will be minimal d. Resistancein the externalcircuit is reduced 5-19. A thermocoupleinstrumenthas an input resistanceof 50,000ohmsand is usedwith an IC Type J couple.The leadwire is #18 gauge,120feet long. What is the approximateerror contributedby the leadwire? a. :t5.0 percent c. :t0.05 percent b. :t0.5 percent d. :tO.1 percent 5-20. The differencebetweenanRTD calibratedto the NR 226curve and one calibratedto the NR 227curve is: a. A differentresistance-to-temperature relationship b. Nonexistent c. Greateraccuracywith the NR 226curve d. Greateraccuracywith the NR 227curve

Analytical measurements seek to define the contents of a process stream and thus enable control of its composition. Some analytical measurements are physical; others are electrochemical. The physical types include humidity, density, differential vapor pressure, boiling point rise, chromotography, ultraviolet, infrared, and turbidity, some of which bave been discussed previously. Still others, such as spectroscopy, osmometry, and polarography, are laboratory techniques and Dot usually associated with automatic control. Some are occasionally used, bot are beyond the scope of this book. Many other analytical measurements, such as conductivity, pH (hydrogen iODconcentration), ORP (oxidation-reduction potential), and specific iODconcentration, are electrochemical. These measurements, along with capacitance, will be covered in this chapter.

Electrical

Conductivity

While dissociation into ions and the resulting iOD concentration bave been adequate concepts in the past, the fact is that DOt all the ions present are necessarily effective. Some ofthem mar be "complexed," 151

152 FEEDBACK PROCESSCONTROL

that is, "tied up" to'other ions and unavailable for reaçtion. The concept of activity covers this situation. In short, a given compound will dissociate to some degree, described by the dissociation constant, into ions, and some portion of these ions will be active, described by the activity coefficient. However, in many common reactions, the activity coefficient is so near unity that concentration and activity mar be used interchangeably. In a growing number of processes, the actual ion activity is different enough Cromthe ion concentration to make it necessary to use the proper term. In general, electrochemical measurements measure activity rather than concentration, and it is always desirable to refer to the measurements as ion activity rather than ion concentration. Electrochemical measurements all rely upon the current-carrying property of solutions containing ions. Some techniques measure all ions present (electrolytic conductivity). Others respond mainly to particular types of ions-hydrogen ions (pH); oxidizing/reducing ions (ORP); selected ions (ion-selective). These will be discussed separately below. The ability to conduct electricity, or the reciprocal of electrical resistance, is called conductance.The unit in which it is measured is the reciprocal ohm, commonly called mho. The conductance of any conductor depends on the nature of the material, the shape of the conducting path, and the temperature. In analytical work, only the nature ofthe material, in this case the type and activity of the ions present, is important. Thus, the term conductivity, the conductance of a volume of the material of unit length and area, is generally used. (Conductivity has largely replaced an earlier term, specific conductance.) In actual measurement, a conductivity cell of known geometry is immersed in the material, and the resistance (or conductance) across the cell is measured. This gives a measurement that can be calibrated directly in conductivity due to the known shape of the cell. Conductance and conductivity are related as follows: the greater the length of a material of given conductivity, the higher its resistance (the lower the tonductance); but the greater the aTeaofthe material, the lower the resistante (the greater the conductance). That is, aTea conductance= conductivity iength

(6-1)

Sincethe unit of conductanceis mho, the unit of conductivity mustbe conductivity =mho x

centimeters squarecentimeters

(6-2)

ANALYTICAL MEASUREMENTS 153

or, conductivity = mho. cm-1 It is unfortunately common practice to omit the dimensional unit, so that conductivity is then referred to as mhos. This practice leads to confusion with conductance, and should be avoided. The conductivity of most electrolytes at the concentrations and the temperature ranges normally encountered fall well below unity. For this reason, the micromho per centímetre, the millionth part of the mho per centímetre, is normally used. In the SI system of units, the siemens replaces the mho. One mho equals one siemens. In conductivity units, one micro mho per centimetre (¡J.mho/cm)equals one microsiemen per centímetre (¡J.S/cm). However, the actual SI unit is the microsiemens per metre, since the unit of length in the SI system is the metre rather than the centímetre. One ¡J.S/cmequals 100 ¡J.S/m. The conductivity of material of unit length and area which has a resistance of 1,000ohms is 0.001 mho. cm-Ior 1,000micromho .cm-1 (sometimes called simply 1,000 micromhos). Since the measurement depends on the geometry ofthe cell used, a cell constant (F) has been defined to describe this geometry simply:

F = length (cm) aTea(cm2)

(6.3)

When the length is I centimetre and the area I square centimetre, F = 1.0 cm-I. Here, also, the dimensional unit is omitted in common use, so that the cell is said to bave a cell constant of 1.0. Note that the critica! dimensions are length and area, Dot volume. Thus while the above example has a volume of 1 cubic centimetre ifthe length were 0.5 centimetre and the area were 0.5 square centimetre, the cell constant would still be 1.0. But the volume would only be 0.25 cubic centimetres. Thus it is Dot correct to say that the resistivity is the resistance of unit volume, but only of unit length and cross-sectional area. A cell with greater area and the same length will bave a lower cell constant. But for the same solution (that is, for a given conductivity) the conductance will be greater with this cell. If we solve Equation 6-1 for conductivity,

(6-4)

154 FEEDBACK PROCESSCONTROL

and substituting Equation 6-2,

conductivity = conductancex cell constant A given measuring instrument will bave a certain conductance (resistance) range. But it may bave a variety of conductivity ranges by simply using cells of different cell constants. For example, an instrument with a range of O to 100 micromhos per centimeter with a cell having a constant ofO.Ol will bave a range oro to 1,000micromhos per centimeter if a cell with a constant of 0.1 is substituted.

Types

ot Calibration

Conductivity instruments can normally be furnished with 1. Calibration in conductivity (,LLSx cm-! or ,LLmhox cm-!) 2. Calibration in terms of concentration of electrolyte 3. Calibration in terms of conductivity difference Calibration

in Conductivity

Instruments of this type are measured in absolute units, ohms, mhos, siemens, or microsiemens. Such instruments can be used to measure the conductivity of any electrolyte at any solution temperature using a measuring cell with known cell factor. The conductivity of most solutions increases as the temperature increases. Therefore, if a conductivity instrument calibrated in ¡J-mhox cm-r is used with a solution of given concentration, the instrument reading will change if the temperature of the solution changes. Compensation for this effect of temperature on the conductivity of the solution is possible only if the solution's conductivity temperature coefficient is known. For example, if an instrument calibrated CromOto 1,000¡J-mhox cm-r were provided with temperature compensation for sodium chloride (NaCI), the instrument would Dot correctly compensate in any other solution. For this reason, instruments calibrated in absolute units are generally Dot furnished with temperature compensation. Instruments ofthis kind are generally the simplest to calibrate and lend themselves to more ftexibility of application, since they are Dot limited to any particular electrolyte. If compensation is desired, it can be supplied, bot only for one particular solution.

ANALYTICAL MEASUREMENTS 155

Calibration in Terms ot Concentration ot Electrolyte Instruments calibrated in terms of concentration of electrolyte read percent concentration, grams per litre, parts per million, and the like, for the range specified. 'This type of calibration is made to the conductivity values within the specified range of concentration, and at a specified temperature of a given electrotyte. The instrument can therefore be used only under the conditions for which it was calibrated. However, special cases exist which sometimes make conductivity useful in multiple-electrolyte solutions. If the material of interest is much more conductive than others in solution, the contaminants mar bave a negligible effect on readings. For example, contaminants slowly build up in a sulphuric acid (H2SO4)bath for treating textiles. The conductance of the contaminants is very low compared with thai of the acido Thus, the instrument mar read directly in concentration of sulfuric acido Laboratory tests determine when concentration of contaminants is too high and a new bath is then made up. Figures 6-1 and 6-2 show typical conductivity curves ofNaCl and H2SO4.Note thai the H2SO4curve reverses itself in the region of 30 to

Fig. 6-1. Percent concentration. Conductivity oCNaCl at lOO"C(212°F) and 1SOC(64.4°F).

156

FEEDBACK PROCESSCONTROl

Fig. 6-2. PercentConcentration.Conductivityof H2SO.at 70oP(21.IOC)and 40"P (4.4°C).

32 percent concentration and again in the vicinity of 84 percent and 93 percent. Obviously, it is impossible to calibrate for ranges that include these points of inflection. However, in electrolytes having such maxima they shift with temperature. By controlling sample temperature to a different value, certain ranges mar sometimes be measured which would be impossible to measure at process temperature. Polarization

When an electric current is passed through a solution, electrochemical etfects known as polarization occur. These etfects, if Dot minimized, wiU res uit in inaccurate measurement. One of the polarization etfects is electrolysis. Electrolysis generaUy produces a gaseous layer at the electrode surface, increasing the apparent resistance of the solution. For tros reason, direct current voltage is Dot practical in conductivity measurements. If the current is reversed, the layer wiU tend to go back into solution. Thus, if an altemating current is applied, the polarization etfect decreases, since the gases and other polarization etfects produced on one-half of the cycle are dissipated on the other half cycle. Cell Construction

The sensitive portion of the cells shown i~ Figure 6-3 consists of two platinum electrodes mounted in an H-shaped structure of Pyrex glass tubing. The electrodes, located in separate sections of the tubing, are

ANALYTICAL MEASUREMENTS 157

Fig. 6-3. Type H conductivityassembly.

concentrically mounted platinum rings and are ftush with the inside surface of the tubing. Fouling or damaging the electrodes is thus minimized, and the cells mar easily be cleaned chemically or with a bottle brush. The platinum electrodes in these cells are coated with platinum black to minimize polarization etfects. The cell shown in Figure 6-4 employs graphite, rathèr than metallic electrodes. The type of graphite used has the same surface properties with respect to polarization as metallic electrodes. These cells require no platinization. They are cleaned chemically or by wiping the surface of the electrode with a cloth or brush. Conductivity cells (Figure 6-5) are used for detecting impurities in boiler feedwater, for concentration of black liquor (in a pulp digester for kraft paper), for determination of washing etfectiveness by measurement ofpulp wash, and in many other applications where the presence and concentration of a known salt, base, or acid must be deter-

mined. Electrodeless

Conductivity

Measurements

In addition to the conventionalconductivity measurementsjust described another approachcalled an electrodelesstechnique mar be employed.This techniquediffers from conventionalconductivity measurementin that no electrodescontactthe processstream.Instead,two

158 FEEDBACK PROCESS CONTRO~

Fig. 6-4. Conductivitycells.

toroidally wound coils encircle an electrically nonconductive tube that carries the liquid sample. The first coil is energized by an ultrasonic oscillator (approximately 20 kHz) which induces an altemating current in the liquido This current in turo induces a current in the second coil.

Fig. 6-5. Gatevalve insertiontype conductivitycell.

~ ~ ~. ~

ANALYTICAL MEASUREMENTS 159

The induced current in the second coil is directly proportional to the electrical conductivity ofthe líquid carried by the tube. No direct contact between the coils and the solution is required, thus eliminating potential maintenance problems. Figure 6-6 shows a typical electrodeless conductivity measuring system which transmits a 4 to 20 mA dc signallinearly related to the measured conductivity. Electrodeless conductivity is especially applicable to the higher conductivity ranges such as 50 to 1,000 millimhos per centímetre. Lower conductivity ranges such as 0.01 to 200,000 micromhos per centímetre are best handled by the conventional techniques previously described.

Hydrogen The

term

solution. of

means is,

vary

from

any

tion

the

hydrogen

degree amo

unt

ofthat

percent).

of of ion.

The

potentiometric

ions

acidity a

(H+)

given Activity

alkalinity

ion

actually

values

measurement

can

ofpH,

measurement

that

as obeys

explanatech-

to with

ofthe

This

measurement

along

activity

1 (100 is

equation.

employed

the

effective

called

chapter,

contains

nique

The

percent)

this

a measure

time

Nemst

chapter

a measure

solution.

O (O

discussed

(pH)

therefore,

aqueous

present

the

lon Activity

determine the

Nemst

equation. To

aid

further

understanding surement, of the properties some

a thorough

of pH meafundamentals of aqueous

,---TOROIO

SECONOARY

!'RI MARY TOROIO CELL BORE

~~, solutions

most

understood.

CELL

lonization

or Dissociation

;\)' .1

Stable chemical compounds are electrically neutral. When th . d Wlthsolution, ter to ey forro areanmlxe aqueous wa o

:;\ \"' ~

!~~ "",,' -' ELECTRIC ./ "~~~~

they dissociate into positively Fig.6-6. Electrodeless conductivity measuring and negatively charged parsystemo

160 FEEDBACK PROCESSCONTROL

ticles. These charged particles are called ions. Ions travel from one electrode to the other if a voltage is impressed across electrodes immersed in the solution. Positive ions, such as H+, Na+, and so on migrate toward the cathode, or negative terminal, when a voltage is impressed across the electrodes. Similarly, negative ions, such as OH-, CI-, S04-2, and so on, migrate toward the anode, or positive terminal. The freedom of ions to migrate through a solution is measured as the electrical conductivity of the solution. Chemical compounds that produce conducting solutions are called electrolytes. Not all electrolytes completely dissociate into ions. Those that do (strong acids, strong bases, and salts) are strong electrolytes. Others dissociate, but produce fewer than one ion for every element or radical in the molecule. These are poor electrical conductors, and, hence, weak electrolytes. All weak acids and weak bases fall into this class. At a specified temperature, a fixed relationship exists between the activity of the ions and undissociated molecules. This relationship is called the dissociation constant (or the ionization constant). For hydrochloric acid (HCI), the dissociation constant is virtually infinite, which means that for all practical purposes, the HCI is completely composed of positively charged hydrogen ions and negatively charged chloride ions. Because of the essentially complete dissociation into ions, hydrochloric acid is a strong acid: HCl -+- H+ + Cl-

Conversely,acetic acid has a low-dissociationconstant. It breaks up in the following way: CH3COOH~ H+ + CH3COOFew hydrogen ions show up in the solution-less than one for every 100undissociated molecules-therefore, acetic acid is a weak acido It follows that the strength of an acid solution depends on the number of hydrogen ions available (the hydrogen ion activity). This depends not only on the concentration of the compound in water, but also on the dissociation constant of the particular compound. When free OH- ions predominate, the solution is basic, or alkaline. The dissociation of such a compound is illustrated below. NaOH -+ Na+ + OH-

ANALYTICAL MEASUREMENTS 161

Sodium hydroxide is, for all practical purposes, completely dissociated and is a strong base. Conversely, ammonium hydroxide, NH4OH, dissociates very little into NH4+ ions and OH- ions, and is a weak base. The OH- iODactivity, or strength, of a base depends on the number of dissociated OH- ions in the solution. The w\mber available depends, again, DOtonly on the concentration of the compound in water, but also on the dissociation constant of the particular compound. Pure water dissociates into H+ and OH- ions, but is very weak in the senseused above. That is, very little ofthe HOH breaks up into H+ ions and OH- ions. The number of water molecules dissociated is so small in comparison to those undissociated that the activity of (HOH) can be considered 1 (100 percent).

HOH ~ H+ + OHAt 77°F or 25°C, the dissociation constant or water has been determined to bave a value or 10-14. The product or the activities (aH+)(aOH-) is then 10-14. If the activities or hydrogen ions and hydroxyl ions are the same, the solution is neutral; the H+ and OH- activities must both be 10-7 mols per litre. It must be remembered that, no matter what compounds are present in an aqueous solution, the prJduct or the activities or the H+ ions and the OH- ions is always 10-14at 77°F or 25°C. If a strong acid, such as HC1, is added to water, many hydrogen ions are added. This must reduce the number or hydroxyl ions. For example, if HCl at 25°C is added until the H+ activity becomes 10-2,the OH- activity must become 10-12. The pH Scale

It is inconvenient to use terms as 10-7, 10-12and 10-2. Therefore, it has become common to use a special term to represent degree of acidity, or activity of hydrogen ions. This term is pH, originally derived from the phrase "the power of hydrogen." The pH is defined as the negative of the logarithm of the hydrogen ion activity, or as the log ofthe reciprocat ofthe hydrogen ion activity. pH = -log aH+ = log

(-:¡: aH

(6-5)

162 FEEDBACK PROCESSCONTROL

Table 6-1

Temperature oC

-Log

(aH+)(80H-)

14.94 14.00 13.26 12.69 12.26

25 50 75 100

Neutral pH

7.47 7.00 6.63 6.35 6.13

If the hydrogen iOD activity is lO-x, the pH is said to be x. For example, in pure water (at 25°C), the activity of hydrogen iODis 10-7. Therefore, the pH of pure water is 7 at 25°C. A point frequently overlooked is thai the pH for neutrality varies as the solution temperature changes due to a change in the dissociation constant for pure water, as shown in Table 6-1. An acid solution contains more hydrogen ions than hydroxyl ions. Table 6-2 Hydrogen [on

Activity Mols/Litre

Hydroxyl Jan Activity Mols/Litre

10.1

0.00000000000001

1 2

0.01

0.001

0.0001

O.0000 1

0.000000001

0.000001

0.00000001

0.0000001

0.00000001

0.000001

Neutral

9 10 11 12 13 14

0.0000000000001

0.000000001 0.0000000001 0.00000000001 0.000000000001 0.0000000000001 0.00000000000001

0.000000000001

0.0000000000I 0.0000000001

0.00001 0.0001 0.001

0.01

0.1 I

ANALynCAL MEASUREMENTS 163

Therefore, the activity of hydrogen ions will be greater than 10-1, that is, 10-6, 10-5,10-4. The pH of an acid solution then, by definition, must be lower than 7, that is 6, 5, 4. If the number of OH- exceeds H+ ions, the hydrogen iODactivity must be less than 10-1, that is, lO-s, 10-9,10-1°. Therefore, the pH will be higher than 7, that is, 8, 9, 10. Table 6-2 demonstrates that a change of just one pH unit means a tenfold change in strength ofthe acid or base. The reason for this is that there is an exponential relationship between pH numbers and hydrogen iODactivity. With so large a change in acidity or alkalinity taking place with a change ofjust one pH unit, the need for sensiti ve pH measuring and control equipment cannot be overemphasized. Table 6-3 shows the nominal pH values for a number of common solutions.

Table 6-3 pH 14 ~ Caustic soda 4% (I.ON) --Calcium hydroxide (sat'd sol.) (Iime) 12 --Caustic soda 0.04% (O.OIN)11 --Ammonia 1.7% (I.ON) --Ammonia 0.017% (O.OIN) 9 +- Potassium acetate ~.98% (O.lN) 8 +- Sodium bicarbonate 0.84% (O.lN)

6 5 ~ Hydrocyanic acid 0.27% (O.lN) 3 ~ Acetic acid 0.6%

"' 1 +- Hydrochloric acid 0.37% (O.IN) +- Sulfuric acid 4.9% (I.ON) O +- Hydrochloric acid 3.7% (I.ON) -1 +- Hydrochloric acid 37% (lON)

d -~---~ )LASrIC

164 FEEDBACK PROCESSCONTROL

Fig. 6.7. Schematicdiagramor glass-tippedpH measurement electrode. Measurement

ot pH-The

Glass Electrode

A number of different methods for measuring pH are available for laboratory use, but only one has proved sufficiently accurate and universal for industrial use: the pH glass electrode measuring system. A special kind of glass, sensitive to hydrogen ions, has been found to be the most useful medium for measuring pH. Figure 6-7 shows a INTEGRAL CABLE

( r--y= MOISTURE

SEAL CAl

SILVERSILVER CHLORIDE COLUMN

SHIELDED !LECTRODE

CABLE

GLASS-TO-METAL SEAL ; "TOTAL GLASS" CONSTRUCTION) NTERNAL

SOLUTION

,H-SENSITIVE

Fig. 6-8. Actual measuringelectrode.

MEMBRANE

ANALYTICAL MEASUREMENTS 165

schematic diagram of the measuring electrode in which this special glass is used. A thin layer of the special glass covers the tip of the electrode. Figure 6-8 shows an actual measuring electrode. This glass contains a chamber filled with a solution of constant pH. An internal electrode conductor element immersed in the internal solution is connected to the electrode lead. The conductor element is discussed in the section on temperature compensation. If the hydrogen iODactivity is greater in the process solution than inside the electrode, a positive potential difference will exist across the glass tip. That is, the external side of the glass will bave a higher positive potential, and the internal a lower positive potential. If the process is lesser in hydrogen iODactivity, a negative potential difference will exist. The relationship between the potential difference and the hydrogen iODactivity follows the Nernst equation. E

lo nF

aH+o~ts~de aH+ mslde

(6-6)

where: E = potential difference measured Eo = a constant for a given electrode system at a specified temR = T = n = F = aH+ =

perature (25°C) the gas law constant Absolute temperature charge on iOD(+ 1) Faraday's number, a constant hydrogen iODactivity

In the most common type of pH electrode, that with an internal buffer solution of7 pH, the voltage across the membrane will be zero at 7pH. Reference

Electrode

The potential inside the glass is the output oí the measuring electrode. It must be compared to the potential in the solution outside the giassto determine potential difference and, hence, pH. The sensing oí the potential in the solution must be independent oí changes in solution composition. Platinum or carbon would act as aRP, or redox-measuring electrodes. They would be responsive to oxidants or reductants in the solution. They would Dot yield a true solution potential with solution composition changes.

166 FEEDBACK PROCESSCONTROL

A reference electrode is the answer. Figure 6-9 is a schematic diagram of a typical reference electrode. The connecting wire is in contact with silver that is coated with silver chloride. This, in turn, is in contact with a solution of potassium chloride saturated with silver chloride (AgCI). The saturated KCI, called the salt bridge, in turn, contacts the process solution. Because the concentration of all of the components Cromthe connecting wire to the KCI solution is fixed, the potential Cromwire to KCI is fixed. The potential between the KCI and the process solution (called the liquid junction potential) is normally small, and will vary only insignificantly with process changes. The overall potential of the reference electrode is thus essentially constant, virtually independent of process solution changes, to meet the requirement mentioned earlier. As the need for high accuracy or repeatability becomes greater, protection of the reference electrode's internal environment becomes more important. AIso, prevention of coatings over the electrode tip becomes more critical. Leaking in of process solution must be prevented. Noxious chemicals, or even distilled water, would change the concentration, contaminating the electrolyte. The resuIt would be an unpredictable change in the reference potential. Conductive coatings

Fig. 6-9. Schematicdiagramofreferenceelectrode.

ANALYTICAL MEASUREMENTS 167

on the electrode tip mar cause spurious potentials, and nonconductive coatings mar literally open the measurement circuit. Two types of reference electrodes are available-ftowing and nonftowing. The ftowing version (Figure 6-10) is usually selected when the highest possible accuracy or repeatability is needed. To prevent electrolyte contamination and to minimize coatings or deposits on the tip, there is provision for a ftow of KCl electrolyte out through the paTOllS electrode tip. Instrument air is applied inside the electrode. It maintains a pressure on the electrolyte slightly higher than thai of the process liquido A 3 psi (20 kPa) differential pressure forces a trickle of 1 or 2 ml per dar of electrolyte out into the process solution. The nonftowing version (Figure 6-11)of a reference electrode is often considered standard. No external pressure is applied to ibis type of electrode. The electrolyte is a paste of KCl and water thai actually does ftow, or diffuse, into the process solution. The ftow rate mar be as low as 0.01 ml per dar; ibis is a function of diffusion properties. After

Fig. 6-10. Flowing referenceelectrode.

168 FEEDBACK PROCESSCONTROL

Plastlc

Body

Internal Electrode Element AgAgCI

Fig. 6 -11. Construction details of nonfiowing reference electrode.

depletion of the electrolyte, the nonflowing electrode is usually either recharged or replaced. Tem peratu re Com pensati on

The major potential difference exists in the reference electrode, between the metallic silver and the silver ions in the AgCI solution. It follows from the Nemst equation: (6-7) Because R, n, and F are constants, and aAgoand AAg+ are fixed, this potential (E) will vary only with the absolute temperature of the electrode. Since there is a definite chemical relationship between the ionic silver and the activity of chloride in the KCl electrolyte, the above expression mar also be written as: E = Eo -kT

log aCl-

(6-8)

To compensate for ibis temperature sensitivity, another silversilver chloride electrode is inserted into the top of the glass measuring electrode, the internal conductor element mentioned previously. As the temperature of the electrode changes, the potentials of the reference electrode and the conductor element will vary, but will effectively cancel each other, assuming similar values for aAg+ (or aCI-) in each electrode as is usually the case.

ANAl..YT!CAL MEASUREMENTS 169

A remaining temperature effect influences the potential across the membrane of the glass measuring electrode. This will vary with the absolute temperature and is greatest at high- and 10w-pH values. At values around 7, the variation with temperature is zero. This paint is called the isopotential paint. Figure 6-12 shows the magnitude of the temperature error, away from the isopotential paint, with glass electractes. In general, some type of temperature compensation is essential for accurate, repeatable pH measurement. If the process temperature is constant, or ifthe measured pH is close to avalue of7, manual temperature compensation mar be used. Otherwise, for good results, automatic temperature compensation will be required. Reading the Output

ot the pH Electrodes

The high resistance of the giass measuring electrode results in the need for a millivolt meter with very high internal resistance or sensitivity to measure the cell output. The pH electrodes mar be compared to a pair of ftashlight cells in series, but unlike the ftashlight cell, the electrodes

Fig. 6-12. Graph oCpH measurement errors versus pH values at various solution temperatures due to temperature differences across the measurementelectrode tip.

170 FEEDBACK PROCESSCONTROL

are characterized by èxtremely high internal resistance (as high as a billion ohms). Unless the millivolt meter employed to measure the voltage created by the electrodes has almost infinite resistance, the available voltage drop will occur across the internal resistance and result in no reading, plus possible damage to the electrodes. In addition to high impedance or sensitivity, the instrument must bave some provision for temperature compensation. It must also bave available adjustments that provide for calibration and standardization. The Foxboro pH transmitter shown in Figures 6-13 and 6-14 is typical of an instrument designed to make this measurement. Its output is typically 4 to 20 mA dc which can be fed to a control system. When pH is measured in the process plant, it is generally for the purpose of control. pH Control

Experience has shown that it is virtually impossible to control pH without considering the process composition as well as more obvious parameters offtow rate, pressure, temperature, and so on. This consideration is frequently even more critical where plant waste neutralization is being controlled; in such applications, there are usually wide, relatively uncontrolled variations in composition as opposed to the normally better defined, and controlled, process stream. A pH control system can be a relatively simple on/off controlloop in some batch processes. At the other extreme, it can be a complex, feedforward/feedback system with multiple sequenced valves for continuous neutralization over a wide, dynamic pH range.

Fig. 6.13. Block diagrarnoftypical transmitter.

ANALYTICAL MEASUREMENTS 171

Fig. 6-14. Actualtransmitter.

The rate of change of inlet pH and fiow is a major consideration in determining whether feedforward control is necessary. Since changes in pH refiect logarithmic changes in composition, they can atrect reagent demands tremendously and rapidly. Since reagent addition varies directly and linearly with fiow, doubling the fiow requires twice as much reagent at a given pH. But a change of one pH unit at a given fiow requires a tenfold change in reagent. Flow rate compensation is often required in complex pH control loops, but usuany only when fiow changes are greater than 3 : 1. The amount of reagent addition for butrered and unbutrered solutions, as seen on conventional acid-base titration curves (Figure 6-15), is also an extremely important consideration in the design of a pH control system. Reaction time of the various reagents musi also be

,;,

172 FEEDBACK PROCESSCONTROL

005 BASE

001

REAGENT

001

005 AtiO

REAGENT

MOLS REAGENTREQUIRED/LlTER INFLUENT

Fig. 6-15. Typical neutralization curves for unbuffered solutions (strong acid or strong base) and buffered solutions. Examples of buffered solutions are (I) weak acid and its sale with the addition of a strong base, and (2) strong acid or base, concentrated, 0.01

given serious considerationin designingboth the processand the control system. A pH measurementand control system, in conjunction with a well-designedprocess,canbe a mostsuccessful,reliable systemwhen proper considerationhas beengivento the various designparameters. Summary Continuous pH measurement is avaluable tool for industry and gives information thai cannot be obtained economically in any other fashion. It is generally more complex than, say, temperature or pressure measurements, but with constant use, it becomes a routine analytical tool.

Oxidation-Reduction

Potential

Oxidation-reduction potential or redox measurements determine the oxidizing or reducing properties of a chemical reaction. In this application, the term oxidation is used in its electrochemical senseand applies to any material which loses electrons in a chemical reaction. By definition, a reduction is the opposite of oxidation, or the gaining of external electrons. There can be no oxidation without an attending reduction.

ANAL YTICAL MEASUREMENTS 173

For example, a ferrous iODmar lose an electron and become a ferric iOD (gaining increased positive charge) if a reduction, say, of stannic to stannous ions (which is the reverse ofthis operation) occurs at the same time. This measurement uses electrodes similar to those in pH measurement (except that metal is used instead of glass), but the two types of measurement should DOtbe confused. The measurement depends on the oxidizing and reducing chemical properties of reactants (not necessarily oxygen). The inert metal electrode versus the reference electrode will produce a voltage that is related to the ratio of oxidized to reduced ions in solution. This measurement is similar to that of pH in the requirements that it places on the voltmeter used with it. It is useful for determinations in waste treatment, bleach production, pulp and paper bleaching, and

others. The application of ORP measurement or control depends on a knowledge of what goes on within the particular process reaction. The ORP measurement can be applied to a reaction only under the following conditions: 1. There are present in the solution two reacting substances: one that is being oxidized and one that is being reduced. 2. The speed of reaction, following an addition of one of the substances above, is sufficiently fast for good measurement or control. 3. Contaminating substances are held to a minimum, especially those capable of causing gide reactions of oxidation or reduction. 4. The pH ofthe solution is controlled in those areas ofthe applicable curve where variations in pH can affect the ORP measurement.

lon-Selective

Measurement

Certain applications require that the activity of a particular iODin solution be measured. This can be accomplisehd with an electrode designed to be sensitive to the particular iODwhose concentration is being measured. These electrodes are similar in appearanceto those employed to

measure pH, but are constructed as glass-membraneelectrodes, solid-membrane electrodes, liquid-ion-exchange-membrane electrodes, and silicone-rubber-impregnated electrodes. A common example ofion-selective measurementis found in many municipal water treatment plants. In this application, a measurement of

174 FEEDBACK PROCESSCONTROL

ftuoride iOD activity can be related to concentration. The measuring electrode is made of plastic and holds a crystal of lanthanum ftuoride through which ftuoride ions are conducted. The reference electrode is the same as thai used for pH. The electrode output is read on a high impedance voltmeter very similar to thai used with pH electrodes. Many applications are possible using the ion-selective technique. At present, measurements in water treatment include hardness, chlorine content, waste, and pollution. Many other industrial applications bave been suggested and many bave proven effective.

Chromatography

The original application of chromatography consisted of studying the migration of liquid chemicals through porous material, usually paper. The word chromatography means color writing, which occurs when certain extracts or dyes applied to paper produced colored bands. Modem gas chromatography dates from 1952,when James and Martin first used the principIe to separate a mixture of volatile fatty acids having nothing to do with color. The modem chromatograph is generally used for gas analysis. It consists of a column, a tube or pipe packed with materials that will absorb the gases being analyzed at different rates. The gas to be analyzed is carried through the columns by an inert carrier gas, usually helium. As the gas mixture passes through the column, different components are delayed for varying increments of time. Thus, as the gas stream leaves the column and is passed through a gas detector, a chromatogram, or "fingerprint," is formed which mar be used to determine the components in the gas as well as the quantity present. The packing material for the column must be properly selected to provide the separation desired for the sample under analysis. The operating parameters, such as temperature, carrier gas flow and pressure, sample valve timing and detector sensitivity, all influence output. Therefore, in a working chromatograph, these factors must be carefully controlled. Chromatographs are widely used in process work; in fact, they are among the most popular analytical tools. They are used for both liquids and vapors, and adaptations are available to provi de an output in conventional analog form such as a 3 to 15 psi (20 to 100 kPa) pneumatic signal. The details ofthis instrument' s operations are beyond the scope of this book. Several references suitable for further study are listed at the end of this chapter.

cable

ANALYTICAL MEASUREMENTS 175

Table6-4. ComparisonofCapaèitance,Conductivity,pH, andORPTechniques

Specificity Sensitivity Conducting fluids Nonconducting fluids

Maintenance InstalIation problems Cost

Capacitance

Conductivity

pH or ion-selective

ORP

Poor Pair Not applicable Good

Poor Good Good

Excellent Excellent Good

Poor Excellent Good

Not

applil

appIiI

Low Low

High High

Not applicable Medium Low

Low

Medium

Low

Capacitance

Capacitance is Dot, as applied, an electrochemical measurement. However, a measurement of some characteristic in a nonconducting liquid is frequently required, and in these applications, capacitance mar provide the answer. Electrical capacitance exists between any two conductors separated by an insulator (dielectric). The amount of capacitance depends on the physical dimensions of the conductors and the dielectric constant of the insulating material. The dielectric constant (K) for a vacllum is 1; all other dielectric materials bave a K greater than 1. For example, for air, K = 1.00588; for dry paper, K = 2 to 3; for pure water, K = 80. The Table of Dielectric Constants of Pure Liquids (NBS Circular 514), available Crom the U.S. Govemment Printing Office, lists the dielectric constants of nearly all common liquids. Mixtures of materials bave a composite value of K that can be directly related to composition. This approach is readily applied to the determination of water content in materials such as paper and crude oil. Capacitance is also applicable to level, interface, octane, and other measurement problems. In general, the capacitance technique has provided a solution to many measurement problems that cannot be solved easily by more conventional means. Table 6-4 compares the application of pH, ORP, ion-selective, conductivity, and capacitance measurements to process situations.

176 FEEDBACK PROCESSCONTROL

References Conductivity cells. Technical Information Sheet 43-10a. Foxboro, MA., The Foxboro Company. Fluoride measuring systems-potable water. Technical Information Sheet 43-21a. Foxboro, MA., The Foxboro Company. Fundamentals of pH measurement. Technical Infor~{ltion Sheet 1-90a. Foxboro, MA., The Foxboro Company. pH e1ectrodesand ho1ders. Technical Information Sheet43-11a. Foxboro, MA., The Foxboro Company. Theory and app1icationof oxidation-reduction potentials. Technical Information Sheet 1-61a. Foxboro, MA., The Foxboro Company. Pneumatic composition transmitter. Technical Information Sheet 37-1.30a. Foxboro, MA., The Foxboro Company. Lipták, B. G. Instrument Engineer's Handbook, Sec. 81, Volume I. Radnor, PA: Chilton. Shinskey, F. G. pH and pION Control in Process and Waste Streams. New York: John E. Wiley and Sons, 1973.

Questions

6-1. Conductivityand pH measurements are: a. Two differenttechniques b. Similar in operation c. ldentical but given differentnames d. Two techniquesthat usethe sameequipment 6.2. a. b. c. d.

The three factors that control the conductivityof an electrolyteare: Specificgravity, density,and volume Concentration,material in solution,and temperature Color index, turbidity, and temperature Hydrogenion concentration,temperature,and pressure

6-3. pH is a measureor: a. Effective acidity or alkalinity of a liquid b. The oxidationor reductionpropertiesof a solution c. Specificconductanceof an electrolyteor total ionic activity d. Purity in an aqueoussolution 6.4. a. b. c. d.

A buffer solutionis usedwith pH-measuringinstrumentsto: Standardizethe equipment Protectthe equipment Cleanthe electrodes Platinizethe referenceelectrode

6-5. Oxidation-reductionpotential (ORP)is a measurement or:

ANALYTICAL MEASUREMENTS 177

8. b. c. d.

The oxidizing or reducingchemicalpropertiesof a solution The oxygenpresentin any quantityof a givengasmixture The hydrogenion concentrationin a given solution The degreeof ionizationfor a particularsolution

6-6. Capacitancemeasurements are usuallyappliedto: 8. Conductingliquids c. Gasmeasurements b. Nonconductingliquids d. lonized gases 6.7. 8. b. c. d.

Which of the following are electrochemicalmeasurements: Humidity and density Turbidity and differentialvaporpressure pH and ORP Dew point and boiling point rise

6-8. A salt (NaCl)solutionmustbe controlled at a concentrationof 12 percent.The bestchoiceof measurement for the control systemwould be: 8. Conductivity c. ORP b. pH do Capacitance 6-9. An industrial effluentstreamis to be neutralizedby addinga sodium hydroxide solution.The bestchoiceof analyticalmeasurement for the control systemwould be: 8. Conductivity c. ORP b. pH d. Capacitance 6-10. lon-selectivemeasurements: 8. Are similar to conductivity in operationbut usea differentcell b. Are similarto capacitancemeasurements but usea differentinstrument c. Are similarto pH measurements but use differentelectrodes d. Are similarto densitybut usemore exacttechniques 6-11. A pH control systemis usedto neutralizea chemicalwastestream beingdumpedinto a municipalsewagesystem.The desiredpH is 7 or completeneutrality. An unfortunateaccidentshortcircuits the cable connectingthe electrodesto the measuringtransmitter.The result will be: 8. b. c. d.

The control valve admittingthe neutralizingagentwill fully open The control valve will close The control valve will remainapproximatelyat its halí openposition The systemwill cycle

6-12. The concentrationof salt in a liquid usedto carry a slurry niust be monitored.The bestchoice of measurementwill be: 8. Electrodelessconductivity c. ORP b. pH d. An ion-selectivesystem 6-13. A pH systemis to be selected.It is requiredthat the systemfunction with little or no maintenance.The referenceelectrodeselectedwould be:

178 FEEDBACK PROCESSCONTROL

8. A ftowingtype b. A pressurizedftowing type

c. A nonftowingtype d. A pressurizednonftowing type 6-14. The pH of 8 streamis to be monitoredaccurately.It is discoveredthat the temperatureof this streamvariesfrom 40 to 60°F: 8. A measuringsystemwith automatictemperaturecompensation is indicated b. Temperaturecompensationis not necessary c. A manualtemperaturecompensationwill be adequate d. The pH rangewill determinethe needfor temperaturecompensation 6-15. The most popularcarriergasusedin gaschromatographs is: 8. Helium c. Hydrogen b. Air d. Oxygen

SECTION

II PNEUMATIC

AND ELECTRONIC

CONTROL

SYSTEMS

The feedback controlloop, introduced in Chapter 1, requires further discussion. This chapter is devoted to a more detailed description of loop operation and its implicit mathematical relationships. ln the feedback loop, the variable to be controlled is measured and compared with the desired value-the set point. The difference between the desired and actual values is called error, and the automatic controller is designed to make the correction required to reduce or eliminate this error. WitQin the controller, an algebraic "summing point" accepts two inputs-one from measurement, the other from set. The resulting output represents the difference between these two pieces of information. The algebraic summing point is shown symbolically in Figure 7-1, where c represents measurement; r represents set point; and e represents error. Both rand c must be gi ven their proper signs (+ or -) if the value of e is to be correct. A typical closed-loop feedback control system is shown in Figure 7-2. Assume that the algebraic summing point is contained within the feedback controller (FBC). ln order to select the proper type of feedback controller for a s~cific process application, two factors-time and gain-must be considered. Time consists of dead time, capacity, 179

180 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

e~r e=r-c Fig. 7-1. Algebraic summing point.

and resistance. These factors cause phase changes that will be described in this chapter. Gain appears in two forms-static and dynamic. Gain is a number that equals the change in a unit's output divided by the change in input which caused il. Gain = AAoutput input The static gain of an amplifier is easily computed if, for a given step change in input, the resulting change in output can be monitored. Case A in Figure 7-3 shows an amplifier with a static gain of one. In Case B, the output is magnified when compared with the input by a factor greater than one. In Case C, the output change is less than the input. Rere, the input has been multiplied by a number less than one. The dynamic gain of an amplifier mar be computed by inducing a giDewave on the input and observing the resulting output. Figure 7-4 illustrates this procedure with an amplifier that has no time lag between its input and output. If the amplitude of the output is only hali as high as

Fig. 7-2. Closed-loopcontrolsystem.

TUE FEEDBACK CONTROLLOOP 181

Case

20% 5% 10% [ 10%

Output change

10% 10%

Static gain

!Q=1 10

22 10=2

Inputchange

1.--1 10-2

Fig. 7-3. Static gain.

the amplitude of the input giDe wave, the amplifier is said to bave a dynamic gain of 0.5 for the particular frequency of the input wave, for example, 1 Hz. By monitoring the output amplitude for many different input frequencies, a series of dynamic gain numbers mar be found. A plot of the amplitude ratio (gain) as a function of frequency of the input giDewave is the gain portion of a Bode diagram, or a frequency-response curve (Figure 7-4). Note that the higher the frequency, the lower the gain.

Fig. 7-4. Dynamicgain.

)(

182 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

This is true for nearly all processes and instruments. The frequency scale is normally a logarithmic scale. Gain or amplitude ratio is also normally expressed in decibels, where l decibel equals 20 times the logarithm to the base 10 of the amplitude ratio. As the frequency becomes lower and lower, and finally approaches zero, a measure of the amplifier's static gain can be obtained. Just as the static or dynamic gain of an individual amplifier can be computed, so can the static or dynamic gain of a process controlloop. Figure 7-5 shows a temperature controlloop. The static loop gain has been computed by multiplying the static gains of each of the individual components of the loop. Likewise, the dynamic loop gain could be calculated by multiplying the dynamic gains of each element at a particular frequency. Pure dead time has a gain of 1. Each element in the controlloop contributes gain to the totalloop. Increasing the size of a control valve or narrowing the span of a transmitter has exactly the same effect as increasing the gain of a controller.

Fig. 7-5. ResponsecharacteristicsoCeachelementin a Ceedback controlloop-heat, exchangerprocesso TT Transmittergain = psif'F TC Controllergain = psi/psi Diaphragmactuatorgain = inches/psi Valve gain = Btu/inches(lift) Reat exchangergain = °F/Btu F Si ~' " ., -., . ¡~ .~ Static loop gain = l' ~

)(

PS! ,

PS!

)(

mches

)( ~

Btu

)

The

THE FEEDBACK CONTROLLOOP 183

Proper selection of valve size and transmitter span is as important as selecting the gain range in the controller. In practice, the gain of the components in the loop mar nat be uniform throughout their operating range. For example, control valves having several characteristics will exhibit linear, equal-percentage (logarithmic), or other types of gain curves. Unless special precautions are taken, the gain of many control loops will change if the operating level shifts. The gain most then be readjusted at the controller to provide satisfactory control. Let us investigate how a feedback control system functions under closed-loop conditions. The Closed-Loop

Control

System

process consists of multiple capacitances (to store energy) andresistances (to energy flow), as shown in Figure 7-6. Similarly, the measuring system generally contains multiple capacitances and resis-tances. The controller also consists of capacitance and resistance net-works. The final operator, or valve motor, likewise contains capacitance and resistance, and the control valve is essentially a "variable resistance." Thus, the analysis of the system is simply an analysis of how signals change as they pass through resistance-capacitance and dead time networks of various types.

Fig. 7.6. Closed-loopprocesscontrol systemillustratestheRC combinationsthat could exist arounda feedbackloop. Eachatfectsprocessstability.

184 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Phase Shift Through

RC Networks

Figure 7-7 illustrates the phase shifts that occur when a sine wave is applied to a network ofresistances and capacitances. Each succeeding RC combination contributes its own phase shift and attenuation. In Figure 7-7, bottom, a phase shift of 180degrees (a full half cycle) takes place. That is, the output (eRa)is 180degrees out of phase with the input (e applied). The signal has also been attenuated because each resistor causes a loss in the energy level in the system. This phase change can lead to instability in a closed-loop system. Oscillation In a physical system employing feedback, instability will occur if energy is fed back in such direction (phase) as to sustain the instability or oscillation. Oscillators are often divided into two major categories, those thai utilize a resonant device and those thai do noto The resonant oscillator uses a device thai requires a minimum of added energy each cycle to maintain oscillation. On the other hand, the nonresonant oscillator is simply an amplifier with some type of phase-shifting network between output and input. A public address system with the gain so high thai it howls is a nonresonating type.

I -" I SIMPLIFIEO PHASE SHIFTER

Fig. 7-7. Phase ofsigna! acrossR¡, R2' andRa is different. At one frequency, the output signa! can be exact!y 180degrees out of phase with the input signa!, as shown in the

graph.

THE FEEDBACK CONTROLLOOP 185

Academically, both the resonant and nonresonant oscillators follow the same mathematicallaw, but the amplifier gain requirements are quite different for the two categories. With a nonresonant circuit, oscillation will occur (1) if the feedback is positive (inphase) and (2) if the gain is unity or greater. These two conditions are necessary for sustained oscillation. Figure 7-8 shows a simple mechanical oscillator. ln ibis system, energy stored in the spring is transferred to the weight, back to the spring, to the weight again, and so on. The oscillations soon die Dut because some ofthe energy is dissipated in each cycle. lfthe oscillation is to be continuous, energy musi be added to make up the losses. ln the bottom part ofthe figure, ibis energy is added by depressing and releasing the weight. If the energy is to enforce the oscillation, it musi be in the proper phase with the motion. That is, enforcing energy musi be added at a time when both the energy and the oscillation are moving in the same direction. Figure 7-9 shows a free-running oscillator in which the required energy is introduced through feedback. This circuit is called a phase shift oscillator. lt consists of a transistor amplifier and a feedback path comprised of three resistance-capacitance combinations. This circuit is important because it is a simple illustration of the manner in which an ordinary amplifier can be made to oscillate simply by use of feedback.

l@~ Fig. 7-8. At top, the magson the spring received a single downward displacement and the oscillation is delayed. Below, arter the initial displacement, the magsreceives periodic small displacements and the oscillation is continuous.

186

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

The transistor amplifier Dot only makes up for circuit losses, but also contributes a phase shift of 180degrees; that is, the collector is 180 degrees out of phase with the base signal. EachRC element contributes additional phase shift, depending on the values of the components and the frequency involved. If each RC combination contribute s a phase shift of 60 degrees, the three together will result in a 180-degreephase shift. This, added to the 180-degreephase shift through the amplifier, results in 360 degrees of phase shift. The feedback signal is now in phase with the input signal. This inphase feedback produces continuous oscillation. Since only one frequency will be shifted in phase exactly 360 degrees by the RC networks, the oscillator output is of this one fre-

quency. The closed-loop control system (Figure 7-6) also has phase-shifting networks, made up of all process and controller <:omponents,together with an amplifier capable of contributing sufficient gain to overcome the system's losses. This closed-loop system contains the same basic ingredients as the phase-shift oscillator. Each resistance-capacitance combination will shift the phase of the energy flowing around the controlloop in the same manner as in Figure 7-9. Oscillation (instability) will occur whenever (1) the phase relationships through the vario us resistance-capacitance combinations provide feedback in proper phase, and (2) the system gain is unity, or greater at the frequency at which the phase shift is 360 degrees. Figure 7-10 illustrates a plot of system gain (output/input signalBode diagram) and output/input phase shift versus frequency for a three-mode controller. The phase shift (expressed in degrees of lead or

Fig. 7-9. Shift of phasein threeRC sectionsmaintainsoscillationin phase-shift oscillator.

THE FEEDBACK CONTROLLOOP 187

o ~

'"o ~ Z ~ c 2

10 " 100 1000 LOGARITHM FREOUENCY-~AOIANS PER SECONO

10000

Fig. 7-10. Bode diagram shows gain of system (top) and phase change (bottom) .at various frequencies. The gain (output signal/input signal) and phase (output/input) are measured with the system in open-loop operation.

lag) is plotted linearly against the logarithm of frequency. Note that the integral is phase lagging and the derivative is phase leading. The proportional adjustment in the controller adjusts its overall gain and hence the loop gain. The integral adjustment governs the low-frequency response, and the derivative adjustment governs the high-frequency gain of the control mechanism. In addition to controlling gain, these adjustments also affect the phase shifts. Thus, an improper setting of any one of the three control modes can cause the control system to satisfy the two criteria for oscillation and become unstable, Stability in the Closed-Loop System Under normal operating conditions, the control system should produce stable operation. That is, the controller should retum the system to set point, in the event oí an upset, with mínimum overshoot and oscilla-

tion. Too much overall gain(too narrow a proportionalband)can cause

188 PNEUMAT1CAND ELECTRON1CCONTROL SYSTEMS

the system to oscillate if the feedback reinforces the oscillation. Too little gain can cause the system to deviate too far Cromthe desired set point. The damped oscillation shown in Figure 7-11 is characteristic ofthe curve a closed-loop control system will produce when it is subjected to a step change. If the phase and gain relationships are proper, energy is Dot fed back to sustain the oscillation, and the cycles die out. The pattem of decay generally can be controlled by the adjustments available in the control mechanism. Engineering judgment and skill are required to select the recovery curve best suited to the process being

controlled. A high-gain setting is desired because this gives the fastest and most accurate control action. However, too much gain produces oscillation. The best compromise is to use enough gain to produce a damped oscillation, as shown in the middle of Figure 7-11 (0.25 damping ratio). Nonlinearities

Thus far it has been assumed that the capacitances and resistances found in the process control loop bave a fixed value that does not change with process conditions. This is not always true in practice. Frequently, process conditions vary the value of the resistances and capacitances involved and, as a result, the phase and gain relationships are in constant transition Crom one value to another. At other times, these values change, limiting or restricting the natural behavior of the '-PERIOO~ GAI!

MEASURED DR CDNTRDLLED VARIABLE (CLDSED LODP SYSTEM)

GAIN',

TIMEFig. 7-11. Closed-loopresponseto an upsetdependson gainofloop.

THE FEEDBACK CONTROLLOOP 189

system. Such changes are often considered as a group and are called

nonlinearities. A thorough understanding of the operation of the linear system is a prerequisite to an understanding of the nonlinear type. It is common practice to assume a system is linear for the purpose of basic control, and then deal with the nonlinear characteristics as problems anse.

Controllers

and Control

Modes

A wide variety of responsecharacteristics involving gain and time create the different modes of process control. The controller mode selectedfor a givenprocesswill dependon: Economics Precisionof control required Time responseof the process Processgaincharacteristics Safety Now let us investigatethe most commoncontrol modes. Two-Position Control Within this classification there exist several specific methods-on/off, differential gap, and time-cycle control. On/off control is the most common. As soon as the measured variable differs from the desired control point, the final operator is driven to one extreme or the other. In the usual sequence (Figure 7-12), as soon as the measured variable exceeds the control point, the final operator is closed. It will remain closed until the measured variable drops below the control point, at which time the operator will open fully. The measured variable will oscillate about the control point with an amplitude and frequency that depend on the capacity and time response of the processo As the process lag approaches zero, the curve will tend to become a straight line. Then the frequency of the final operator open/close cycle will become high. The response curve will remain constant (amplitude and frequency) as long as the load on the system does Dot change. On/off control is found in many household applications, such as the refrigerator, heating system, and air-conditioning system. A simple

190 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

MEASURED VARIA BLE FINAL OPERATOR POSITION

riME'" FINAL OPERATOR POSIT/ON

MEASURED

VARIABLE

TIME -+

Fig. 7-12. Two-positioncontrolacts on operator.

thermostaticallycontrolledelectric heateris anotherfamiliar example. The room in which the heateris placeddeterminesthe capacityof the process,and, hence,the responsecurve. The following requirementsare necessaryfor on/off control to produce satisfactoryresults: 1. Precisecontrol must Dotbe needed. 2. Processmustbave sufficientcapacityto allow the final operatorto keep up with the measurementcycle. 3. Energy inflow is smallrelative to the energyalreadyexistingin the processo

Differential-gapcontrol is similar to on/off except that a band, or gap, is createdaroundthe controlpoint. In Figure7-12,notethat, when

THE FEEDBACK C~TROL LOOP 191

the measured variable exceeds the upper boundary of the gap, the final operator is closed and remains closed until the measured variable drops below the lower boundary. It now opens and remains open until the measured variable again exceeds the upper boundary. In a process plant, differential-gap control might be used for controlling noncritical levels or temperatures. A time-cycle controller is normally set up so thai when the measured variable equals the desired control point, the final operator will be open for halí the time cycle, and closed the other halí. As the measured variable drops below the control point, the final operator will remain open longer than it is closed. Two-position control is nearly always the simplest and least expensive form of automatic control. Any of the forms discussed can be implemented with commercially available mechanical, pneumatic, or electronic instrumentation. On the other hand, two-position control mar Dot meet the requirements often demanded by today's sophisticated processes. Now let us investigate a typical on/otI controlloop. Assume we bave a liquid-Ievel process as shown in Figure 7-13. Throttling

Control

Proportional or throttling control was developed to meet the demand for a more precise regulation ofthe controlled variable. Throttling control indicates any type of control system in which the final operator is purposely positioned to achieve a balance between supply to and demand from the processo The basic type of throttling control is proportional-only control. This term applied to a control action wherein the position of the final operator is determined by the relationship between the measured variable and a reference or set point. The basic equation for a proportional only controller is:

m = Gain (Error) + Bias

(7-1)

where: m = controller output or valve position Error = difference between set (r) and measurement (c)

e=r-c

(7-2)

Fig. 7-13. PROBLEM: DIFFERENTIAL

GAP CONTROL, CALCULATE PERIOD.

Question I: What is the period of oscillation ofthe controlloop? Given: Controller: on/otI with 7 percent differentia! gap. lnstrumentation response: assume instantaneous. Load = Q = 60 gpm. Manipulated Variable = M = O gpm or 90 gpm. Tank: 6 feet diameter, 12 feet high. Level transmitter: Oto 8 feet. Set Point = 50 percent Question 2: What is the period of oscillation ifthe load is 50 gpm? Question 3: At which load will the period be shortest? So/ution: 1. Volume oftransmitted signa! = area x height 1TD2

xH=

2. Volume within 7 percent differential (0.07)(1692) = 118.4gal. 3. Level cycle: 3a. Rate of rise = (90 -60)

TlIne " to nse .118.4gal. = 30

gpm = 30 gpm

gpm

3b. Rate offall = (O-60)

395

mm.

gpm = -60 gpm

Tirne to fall =

-118.4 gal. = 1.973min. -60 gpm 3c. Total tirne = (3.95 + 1.973)min. = 5.92 min. Solution to no. 2:

3.lD1e T ' to nse , = (90118,4 , -40) gal, gpm = 2.96 mm. TlD1e ' -118.4gal. ' to "la11 = (O -50) gpm = 2. 37 mm. Period oCoscillation = 5.33 min,

Solutionto no. 3: When Q = Mon + Moll = 90 gpm + O gpm = 45 gpm 2 2

m= Application

THE FEEDBACK CONTROLLOOP 193

Bias = usually adjusted to p-lacethe valve in its 50 percent open position with zero error. The term proportional band is simply another way oí expressing

gain. % ProportionalBand =

100

Controller Gain

or Controller Gain =

100

% Proportional Band

Substituting the error formula (e = r -c), proportionalband formula ( % PB = ~),

Equation 7-2, and the Equation7-3, into Equa-

tion 7-1, it mar be expressedas: 100

%PB (r -c)

+ 50%

Another approach to visualizing the effect of varying the proportional band is shown in Figure 7-14. Each position in the proportional band dictates a controller output. The wider the band, the greater the input signal (set point -measurement) musi change in order to cause the output to swing from O to 100percent. Manual adjustment of the bias shifts the proportional band so thai a given input signat will cause a different output level. ot Proportional

Control

Proportional control attempts to retum a measurement to the set point arter a load upset has occurred. However, it is impossible for a proportional controller to retum the measurement exactly to the set point, since, by definition (Equation 7-4), the output must equal the bias setting (normally, 50 percent) when measurement equals the set point. If the loading conditions require a difIerent output, a difIerence between measurement and set point must exist for this output level. Proportional control mar reduce the efIect of a load change, but it cannot eliminate it. The resulting difIerence between measurement and set point, arter a new equilibrium level has be en reached, is called ofIset. Equation 7-5

194 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

SET POINT MINUS MEASUREMENT

GAIN. 1

OUTPUT

TIME-.. OPEN-LOOP

GAIN RESPONSES

1001

CONTROLLER

OUTPUT

MEA5UREMENT,I

"I.

PROPORTIONAL BANO

OUTPUT 50%

100%

0% CONTROLLER

PROPORTIONAL

BANO

-SET

POINT

OUTPUT

.!~°I:,_C2~~R2!;~E~ OUTPUT BIAS (MANUALLY EFFECT -

CHANGES

PROPORTIONAL

SET)

= 50% BAND

Fig. 7-14. Outputresponsereactsto changein gain.

indicatesproportionalresponseto a load upset,and the resultingoffset. The amount of offset may be calculatedfrom: Ae =% Proportional Band AM 100

(7-5)

where ~e is changein offset, and ~M is changein measurementrequired by load upset. From Equation 7-5, it is obvious that, as the proportional band approacheszero (gainapproachesinfinity), offset will approachzero. This seemslogical, becausea controller with infinite gain is by definition an on-otI controller that cannot permit a sustainedoffset. Conversely, as the proportional band increases(gain decreases),propor-

___!_'22-:_C2~~~~~!~

THE FEEDBACK CONTROLLOOP 195

tionately more and more offset will exist. Offset mar be eliminated by manually adjusting the bias until the measured variable equals the set point. Narrow-band proportional-only controllers are often used in noncritical, simple temperature loops, such as in maintaining a temperature in a tank to prevent boiling or freezing. A low, dynamic gain allows a narrow band to be used. Controllers of ibis nature are typically fieldmounted and pneumatically operated. Many noncritical, level-control applications having long time constants also use proportional-only control. Now let us apply proportional-only control to the level problem shown in Figure 7-15. Proportional-Plus-lntegral

Control

If offset cannot be tolerated, another control mode must be added. Integral action will integrate any difference between measurement and set point, and cause the controller's output to change until the difference between measurement and set point is zero. The response of a pure integral controller to a step change in either the measurement or the set point is shown in Figure 7-16. The controller output changes until it reaches O or 100 percent of scale, or the measurement is retumed to the set point. Figure 7-16 assumesan openloop condition where the controller's output is dead-ended in a measuring device, and is Dot connected to the processo Figure 7-16 also shows an open-loop proportional-plus-integral response to a step change. Integral time is the amount oftime required to repeat the amount of change caused by the error or proportional action. In Figure 7-16, integral time equals t r, or the amount of time required to repeat the amount of output change (xJ. (Some instrument manufacturers define integral as the inverse of the above, or the number of times per minute the amount of change caused by proportional action is repeated.) Another way of visualizing integral action is shown in Figure 7-17. In this example, a 50 percent proportional band is centered about the set point. If all elements in the controlloop bave been properly chosen, the controller's output should be approximately 50 percent. If a load upset is introduced into the system, the measurement will deviate from the set point. Proportional response will be immediately seen in the output, followed by integral action. Integral action mar be thought of as forcing the proportional band to shift, and, hence, causing a new controller output for a given rela-

196 PNEUMATIC AND ELECTRON1CCONTROL SYSTEMS

Fig. 7-15. Sample problem: PROPORTIONAL CONTROL, CALCULATE MEASUREMENT. Question: What is the level under steady-state control? Given: Range of level transmitter: Oto 70 inches Level controller: Proportional only, PB = 75 percent, bias = 50 percent, Set Point = 40 inches Load, q: Fixed at 3.5 gpm Valve: Pressure drop, ~P, is constant, Linear characteristic, delivers 6 gpm at 100 percent stroke. Solution: I. Under steady state, inftow must equal outftow. 6 - 0 gpm = 58.3% 2. Inftow = 3.5 .gpm

3. Inftow % = Controller output m = 58.3% .40 4. Set pomt = r= 70 inches . h = 57.1%

mc es

5. Equation (7-4) for proportional control: 100 m = -(r

%PB

-c)

+ 50%

100(57.1 -c) + 50 58.3 = 75 Solving for c: c = 50.9% Converting to inches: 0.509 x 70 = 35.6 inches

tionship between rneasurernentand set point. Integral action will continue to shift the proportional band as long as a difference exists between rneasurernentand set point. Integral action has the sarne function as an operator adjusting the bias in the proportional-only controller. The width of the proportional band rernains constant, and is shifted in a

THE FEEDBACK CONTROLLOOP 197

MEASUREMENT

CONTROLLER OUTPUT

TIME-'

Fig. 7-16. Outputrespondsto stepchangein input.

direction opposite to the measurement change. Thus, an increasing measurement signal results in a decreasing output, and vice versa. If the controller is lloable to retum the measurement to the set point, integral action will drive the proportional band until its lower edge coincides with the set point (see Figure 7-17); hence, a 100 percent output. Ifthe measurement should then start to corne back within control range, it must cross the set point to enter the proportioning range, and cause the output to begin throttling. If the system has any substantial capacity, the measurement will overshoot the set point, as shown on the right gide of Figure 7-17. This basic limitation is called integral windup. It must be seriously considered on discontinuous or batch processes where it is common for the controller output to become saturated and overshoot. A pneumatic mechanism called a batch switch designed to prevent this overshoot is described in Chapter 8.

~ .=

LOAD

198 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

MEASUREMENT % OF SPAN

-~"--""

~;;;;",

','~ ,

SET paiNT

CHANGE

Fig. 7.17. Integral actionshiftsproportionalband in referenceto differencebetween input signa!and setpoint.

Integral setting is a function of the dead time associated with the process and other elements in the controlloop. Integral time should Dot be set faster than the process dead time. If it is set too fast, the controller's output will be capable of changing faster than the rate at which the process can respond. Overshoot and cycling will resuIt. An altemate definition of integral action is the fastest rate at which the process can respond in astable manner. Proportional-plus-integral controllers are by far the most common type used in industrial process control. Pneumatic and electronic analog, and digital hardware are available with proportional-plusintegral action. The classical equation or expression for a proportional-plusintegral controller is:

(7-6)

%PB

= gam

e = error (deviation)R = integraltime If rou compare this equation with Equation 7-4, the proportionalonly expression, rou will find the bias term replaced by the integral

term. Fig.

rHE FEEDBACK CONTROLLOOP 199

In operation, then, the output of this controller will continuously change in the presence of an error signat. Once the error has been reduced to zero, the output will stop changing and star fixed until an error redevelops. At this time, the output again will change in such direction as to eliminate the error once again. Adding

Derivative

ln controlling

(Rate)

multiple-capacity

processes, a third mode of controls is

often desirable. . By definition, derivative is the time interval by which derivative action will advance the effect of proportional action on the final operator. lt is the time difference required to get to a specified level of output with proportional-only action as compared to proportionalplus-derivative action. Figure 7-18 illustrates derivative response to a camp change; where td equals the controller's derivative time. Derivative action occurs whenever the measurement si~nal changes. On a measurement change, derivative action differentiates the change and maintains a level as long as the measurement continues to change at the given rate. Under steady-state conditions, the derivative acts as a 1 to 1 repeater. lt has no inftuence on a controller's output..By reacting to a rate of input change, derivative action allows the controller to inject more corrective action than is initially necessary in order to overcome system inertia. Temperature presents the most common application for derivative. Derivative action should Dot be used on processes that are characterized by predominant dead times, or processes that bave a high noise content, that is, high-frequenéY extraneous signaIs such as are present in the typical ftow application.

MEASUREMENT

, PROPORTIONAL

-ONLY

ACTION

PROPORTIONAL PLUS DERIVATIVE ACTION

TIME-

7.18. -Derivative

action increases rate oCcorrection.

DERIVATIVE TIME, td

Selecting

200 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

The equationor expressionfor the proportional-plus-integral-plus derivative controller is: (7-7) where: e = error R = integral time D = derivative time Question: How long will it take for the output to change 5 percent if the measurement remains constant?

Given: Proportionalband = 50 percent Integral time = 3 minutes Derivative time = 3 minutes Set point = 45 percent Measurement= 35 percent Control action: increase-decrease So/ution: 1. Error staysconstant,thereforeno output changedue to derivative. 2. No output changedueto proportionalaction. However, the proportional action affectsthe integralresponse. 3. Error = r -c = 45% -35% = 10% 4. R = 3 minutes = time to changean amountequalto the error 5. Becausethe proportionalband = 50%,the output in Step4 is multiplied by

= 2.

Therefore 2(10%)= 20%changein 3 minutes or

5% changein 3/4minute. the Controller

Now that the variety of available control modes has been described,the next logical question is: which should be selected to control a particular process? Table 7-1 relates process characteristics to the common control modes. Let us apply the chart to the beat exchanger processo The beat exchanger acts as a small-capacity process; that is, a small change in steam can cause a large change in temperature. Accu-

THE FEEDBACK CONTROLLOOP 201

Table 7-1. Process Characteristics Control Mode On/OlI Floating Prop.

Transfer Lag Min

Small Small

Dead Time

Capacitance

Reaction Load Rate Changes

SelfRegulation

Min Min

High Low Moderate

Slow High Slow

Any

Slow Slow

Must bave

SmaIl

Sma11

Prop. + Integral

Moderate

Any

Prop. + Integral +

Deriv.

rate regulation of processes such as this calls for proportional rather than onloff control. Variations in water rate cause load changes that produce offset, as described previously. Thus, the integral mode should also be used. Whether to include the derivative mode requires additional investigation ofthe process characteristic. Referring to the reaction curve (Figure 7-19), notice that the straight line tangent to the curve at the point of inftection is continued back to the 150°F (starting) level. The time interval between the start of the upset and the intersection of the tangentialline is marked TA(in Figure 7-12, this was dead time); the time interval Crom this point to the point of inftection is TB' If time T B exceeds time TA,some derivative action will prove advantageous. 1fT B is less than TA, derivative action mar lead to instability because of the lags involved.

Fig. 7-19. The process reaction curve is obtained by imposing a step change at input.

7-1. 7.3. 7-4.

202

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

Table 7-2.

OFFSET CA. BEy

~'ES

USE

TO'ERATEO?

P-O."

-'+1

USE

The reaction curve of Figure 7-19 clearly indicates that some derivative action will improve control action. Thus a three-mode controller with proportional, integral, and derivative modes satisfies the needs of the beat exchanger processoTable 7-2, as applied to this problem, will yield the same resulto Ouestions With adequate gain and inphase feedback. any system will: 8. Drift c. Increase amplitude b. Oscillate d. Degenerate 7-2. The natural frequency at which a closed-loop system will cycle depends

upon: 3. The amplifier gain b. The attenuation provided by the process c. The phase shift provided by the resistance-capacitanceand dead time networks that exist in the system

d. Resonance 8. b. c. d.

The Bode diagram describes: Gain and phase shift through the usable frequency range The system's linearity The reaction to a step change The recovery curve that will result from a load change

All systems may be assumed to be: a. Linear b. Nonlinear

THE FEEDBACK CONTROLLOOP 203

c. Linear for the purpose ofinitial consideration but with full knowledge that this may not be the case d. Nonlinear for purposes of analysis with rhe exception that the system may prove to be linear 7-5. A closed-loop control system that employs a three-mode controller: a. Can oscillate or cycle at only one frequency b. Can oscillate or cycle at several frequencies. depending on controller adjustment c. Will not oscillate because of the stability provided by derivative d. Will produce only damped oscillations with a 0.25 damping ratio 7-6. We have a closed-loop control system which is cycling. We should: a. Increase the proportional band c. Check and adjust both b. Increase integral action d. Immediately shut it down 7-7. A proportional controller is being used to control a process. and the offset between set point and control point must be held to a minimum. This would dictate that rhe proportional band: 3. Be as narrow as possible b. Be as wide as possible c. Be of moderate value d. Does not relate to the problem 7-H. The system gain ofthe closed-loop control system: 3. Refers to the process gain b. Refers to the gain of the measurement and control devices c. Refers to total gain of all components. including measurement, controller, val ve operator, valve, and process d. Relates only to the gain ofthe controller 7-9. If a closed-loop control system employs a straight proportional controller and is under good control. offset: 3. Will vary in magnitude b. Will not exceed one-half of the proportional band width c. Will exceed the deviation d. Is repeated with each reset7-10. Any closed-loop system with inphase feedback and a gain of one or more will: a. Degenerate c. Exhibit a 0.25 damping ratio b. Cycle or oscillate d. Produce square waves7-11. How long will it take for the Otltput to change 5 percent if the measurement remains constant? Gil 'l'li :

Proportional band '" 50 percent Integral time '" 3 minutes Derivative time '" 3 minutes

204 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Set paint = 45 percent Measurement = 35 percent Control action = increase/decrease7.12. If a closed-loop control system is adjustèd to produce aO.25 damping ratio when subjected to a step change, the system gain is: 3. 0.1 c. 0.5 b. 0.25 d. 1.07-13. A straight proportional controller is employed to control a processo Narrowing the proportional band will: 3. Not change the offset c. Always cause cycling b. Decrease the offset d. Never cause cycling7-14. The type of process that most often can benefit from derivative is: 3. Flow c. Temperature b. Level d. Pressure 7-15. Pure dead time ina process contributes a gain or: 3. Zero c. Depends upon dynamics d. Infinite d. One 7-16. RefeITing to Figure 7-5, the transmitter span is 200°F; the controller proportional band is adjusted to 150 percent; the equal percentage valve delivers saturated steam containing 40,000 Btu per minute at full open; and water enters the exchanger at 50°F and is heated to 2000Fat a 40 gpm maxirnum flow rate. The static gain of this control loop is approximately: 3. 0.5 c. 1.5 b. 1.0 d. 2.0 7-17. Ifthe flow rate ofheated water in Problem 7-16 is reduced to 5 gpm, you would expect the gain to: 3. Increase c. Remain the same b. Decrease 7-18. The integral control mode is: 3. Phase-Ieading b. Phase-Iagging

c. Inphase d. Phase-reversing

7-19. The derivative control mode is: 8. Phase-Ieading b. Phase-Iagging

c. Inphase d. Phase-reversing

7-20. The most common combination of control modes found in the typical process plant is: 8. Proportional-only b. Proportional, integral, and derivative c. Proportional-plus-integral d. On/off

Pneumatic Control Mechanisms

The basic pneumatic control mechanism is the ftapper-nozzle unit. This unit, with amplifying relay and feedback bellows, is a simple, rapidacting control mechanism. The basic pneumatic mechanism converts a small motion (position) or force into an equivalent (proportional) pneumatic signal. Since pneumatic systems mar use a signal of 3 to 15 psi (20 to 100kPa) (3 psi or 20 kPa at O percent and 15 psi or 100kPa at 100 percent scale), the instrument must bave the ability to convert a position or small force into a proportional pneumatic span of 12 psi (3 to 15 psi or 20 to 100kPa).

The Flapper-Nozzle

Unit

Figure 8-1 shows the principIe of the ftapper-nozzIe device. Input air (reguIated at 20 psi or 138 kPa) is fed to the nozzIe through a reducing tube. The opening of the nozzIe is Iarger than the tube constriction. Hence, when the ftapper is moved away from the nozzIe, the pressure at the nozzIe falls to a Iow vaIue (typicalIy 2 or 3 psi, or 10 or 20 kPa); when the ftapper is moved cIose to the nozzle, the pressure at the 205

206 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Fig. 8-1. Flapper-nozzleis the basicpneumaticcontrolelement.Flappercan be positionedby temperature(as shown),pressureelement,or any sensor.

nozzle rises to the supply pressure (20 psi or 138 kPa). Flapper movement of only a few thousandths of an inch (Figure 8-2) produces a proportional pneumatic signal that mar vary from near zero to the supply pressure. Some pneumatic control mechanisms use the air at the nozzle (nozzle pressure) to operate a control valve. The simple ftapper-nozzle unit shown in Figure 8-1 has several basic limitations. The output air must all corne through the input constriction if it is used directly to operate a control valve. Hence, the output pressure can change only slowly, causing sluggish action. Just as the rate of increase in pressure is limited by the input constriction, the rate of decrease in pressure is similarly limited by the slow rate of air passage through the nozzle to the atmosphere.

Fig. 8-2. Flapperneedmove only a fewthousandthsof an inch for full rangeof output (nozzle)pressure.

The Fig.

PNEUMATICCONTROLMECHANISMS 207

AIso, the measuring element that positions the ftapper must be strong enough to overcome the blast of air leaving the nozzle. Since many measuring sensors are relatively low-force elements, they could Dot be used to position the ftapper accurately and positively if the nozzle were made large enough to pass sufficient air to overcome this limitation. A second limitation is that the ftapper moves only a few thousandths of an inch for complete action from minimum to maximum nozzle pressure. This small trave I for a change in output from zero to full value makes the entire element susceptible to vibration and instability. All these limitations are overcome by employing (1) a relay, or other amplifier, which amplifies the nozzle pressure; and (2) a feedback system which repositions the ftapper or nozzle. Valve Relay or Pneumatic

Amplifier

Figure 8-3 shows a celar connected to a nozzle. The nozzle pressure is applied to the pneumatic relay, which contains a diaphragm operating a

small ball valve. Because the diaphragm has a large area, small pressure changes on its surface res uit in a significant force to move the ball valve. The ball valve, when open, permits the full air supply to reach the output; when closed, it permits the nozzle pressure to bleed to atmosphere. If the ftapper position is changed with respect to the nozzle, the air pressure acting on the celar diaphragm changes and either opens or closes the celar ball valve, thus either increasing or decreasingthe ftow of supply air, which now can ftow directly from the supply to the output, overcoming the first deficiency (slow action) of the ftapper noz-

zle. relay is often called a pneumatic amplifier becausea small

8-3. Relay is an arnplifier. That is, small change in nozzle pressure (the input to the relay) causes a large change in output pressure (to the control valve).

The

208 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

change in nozzle pressure causes a large change in output pressure and flow. The pneumatic relay shown in Figure 8-3 (used in the Foxboro Type 12A temperature transmitter and the Model 130 controller) amplifies the nozzle pressure by a factor of 16; that is, a change in flapper position of 0.0006 inch, which produces a change in nozzle pressure of3/4psi, and results in a change arrelar output of 12 psi (from 3 to 15 psi). The relay shown in Figure 8-3 increases output pressure as nozzle

pressureincreases.Relays can also be constructedto decreasethe output pressure as nozzle pressure increases. Linear Aspirating

Relay or Pneumatic

Amplifier

Flapper-nozzle detectors employed in the set-point transmitter and derivative sections of the Model 130 controller use a different type of pneumatic amplifier. If the flow or volume output requirements are small, an aspirating relay mar be employed. The pneumatic amplifier, shown in Figure 8-4, makes use of the Venturi tube principIe and resembles a small Venturi tube. With a 20 psi supply, the throat pressure of the Venturi can vary 3 to 15 psi or 20 to 100 kPa for a change in flapper position with respect to the nozzle of less than 0.001 inch. The aspirating relay accomplishes ibis with almost perfect linearity and does Dot require parts thai are subject to wear. This recent develop-

.,.SUPP" ,

FLAPPERtNO'

Fig. 8-4. Aspirating cone, showingVenturitube principIe.

Fig.

PNEUMAT1CCONTROLMECHANISMS 209

ment offers advantages over conventional pneumatic amplifiers, provided that a high volume output is Dot required. Proportional Action If a controller had only the units described thus"far, ~apper-nozzle and relay, it would only bave on/otI action. On/otI control is satisfactory for many applications, such as large-capacity processes. However, if on/otI action does Dot meet the control requirements, as in low-capacity systems, the ftapper-nozzle unit can easily be converted into astable, wide-band proportional device by a feedback positioning system that repositions the moving ftapper. An example of a proportional action mechanism is the Foxboro 12A pneumatic temperature transmitter (Figure 8-5). This device, called a "force-balance pneumatic transmitter," develops a 3 to 15 psi (20 to 100kPa) output signal proportional to the measured temperature. Thus, it is functionally a proportional controller.

8-5. Pneumatic temperature transmitter. with tubing and sensor.

210

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

Figure 8-6 shows .the principIe of the Model 12A transmitter. The forces created by the bellows are automatically balanced as follows. When the temperature sensor is subjected to an increase in temperatufe: 1. The increased temperature expands the gas contained in the sensor and increases the force exerted by its bellows. This increases the moment of force, tending to rotate the force bar clockwise. 2. The flapper now approaches the nozzle and the nozzle pressure increases. This pressure is applied to the pneumatic relay (Figure 8-3), increasing its output and the pressure applied to the feedback bellows, thus increasing the counterclockwise moment of force sufficiently to restore the force bar to equilibrium. The force bar (flapper) is now repositioned slightly closer (less than 0.001 inch) to the nozzle, and the output pressure has reached a new levellinearly related to the measured temperature. In the actual unit, two additional forces act on the force bar. One is thai applied by the zero elevation spring. Adjustment of tbis spring determines the constant force it adds to thai supplied by the feedback bellows. This allows a given span of temperature measurement to be raised or lowered. The other force is applied by the ambienttemperature- and barometric-pressure-compensating bellows. This force compensates for ambient temperature or atmospheric pressure changes acting on the gas-filled thermal system, thus minimizing errors caJ¡lsedby these changes.

Fig. 8-6. PrincipIeoCpneurnatictemperaturetransmitter.Forcescreatedin bellowsare balanced.

PNEUMAnc CONTROLMECHANISMS 211

Fig. 8.7. Generalpurposecontroller.

The Model 12A temperature transmitter produces an output proportional to measurement and is a proportional control mechanism. However, a useful general purpose controller should incorporate additional modes, and also bave the ability to adjust the parameters of the mechanism along with other convenient features. For these reasons the unit described, although a proportional controller, is used primarily as a transmitter to send an input signal to a generalpurpose controller (such as the 130 Series), as shown in Figure 8-7.

Control

Mechanism

Requirements

A control mechanismshouldbe ableto controlthe processandeasethe job of the operator. To achievethesegoals, it must meetthe following requirements: 1. The required control modesmustbe availableand easilyadjustable throughthe required range.

212

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

2. The controller shouldhave an easilyadjustedset point. 3. The mechanismshould clearly display what is going on for the benefitof the operator. 4. It shouldbe convenientfor the operatorto switch over to manual control either for the purpose of operatingthe processmanually during startupor in otherunusualsituations,or to performmaintellance or adjustmentson the automaticcontrol unit. 5. After manualoperation,it shouldbe a simplematterto switch back to automatic control smoothly without shockingor bumping the processo

6. If for any reasonthe unit requires maintenanceor adjustment,it shouldbe simpleto remove it for this purposewithout interfering with the processo 7. In manysituations,it mar alsobe convenientand practicalto bave a continuousrecord of the controllervariableand an alarm system to signalthe operatorwhensomepredeterminedlímit is exceeded. Figure 8-8showsthe completeModel 130controller in block diagramformo The total control mechanismconsistsof the following functionalparts: 1. A set-point unit that produces a 3 to 15 psi or 20 to 100kPa pneumaticsignalto be fed into the controllermechanism.This unit is generallylocated within the controller, but it mar be remote. 2. Thederivative unit that acts directly on the measurementsignal. 3. The automatic controller itself-headquarters for the control action. 4. The manualcontrol unit, whichperformstwo functions-switching Cromautomatic to manual and Crommanual to automatic, and manualadjustmentof the control valve (regulatedvariable). 5. The automatic balancingunit, consistingof a simple floating controller through which the operator can switch Cromautomaticto manualand back without any balancingadjustmentsand ret without causinga bump or suddenvalve change. 6. A measurementindicator that displays with pointersand scalethe measurementbeingfed into the controller, and the set point. 7. An output indicator-a display of controller output that mar be interpreted in terms of valve position. The Automatic

Controller

Figure 8-9 develops the mechanism of a proportional controller in schematic formo This controller, like the Model 12A shown in Figure 8-7, has measurement and feedback bellows and a flapper-nozzle relay

~ ~ unit. Fig.

PNEUMATICCONTROLMECHANISMS 213

Fig. 8-8. Block diagramoCFoxboropneumaticConsotrol130Mcontroller.

The basic added features are a set bellows, which permits adjustment of the set point; and an integral (R) bellows. ln the actual Model 130 controller (Figure 8-10), a ftoating disk actsas the ftapper of the ftapper-nozzle system. The resultant moments offorce due to the four bellows determine the position of the disk with

0f?5Ç!)@ OUTPUT

b=ooa

obOR b B P

b.40

OUTPUT

: o. o bM P b.lo 4

OUTPUT

8.9. Schematicdevelopmentofproportionalcontroller.

PROPORTIONAL ~ =1

214 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

('=I--~ --.

REDUCING TUBE-

~ ~

BAND DIAL REVERSING SWITCH

~.-

ADJUSTING ARM AND FULCRUM BAR

NU~~LI:

SET (B) OR MEASUREMENT (A) BELLOWS --

FORCE BALANCING FLOATING DISC

-INTEGRAL BELLDWS PROPORTIONING BELLOWS --'I

-MEASUREMENT (B) OR SET (A) BELLOWS CONTROLLER ACTION REVERSING SWITCH

=! , r~1 '=--,~_f=

INTEGRAL RESTRICTOR

Fig. 8-10. Control unit with floating disk flapper nozzle.

respect to the nozzle. Therefore, the relay output pressure varies with changes in pressure in any ofthe bellows. The mechanism is aligned to produce a midrange output of9 psi (60 kPa) when the error signal is O. This is called bias. The width of the proportional band is adjusted by the position of the proportional-band-adjusting lever. (The term gain is also used in place of proportional band. Gain is the reciprocal of proportional band.) This lever positions the fulcrum abolli which the moments of force created by the pressure in the four bellows act. These moments of force tilt the floating disk upward or downward, thereby causing a change in nozzle pressure. The reguli is an increased or decreased output pressure Crom the controller. This output pressure, which is proportional to changes in measurement or set pressure, acts to reposition the control valve, thus influencing the process and bringing abolli a change in the measurement bellows to establish a new equilibrium in

the system.

PNEUMATICCONTROLMECHANISMS 215

Derivative and Integral The general purpose controUer needs derivative and integral action, as described in Chapter 1. These are added to the pneumatic controUer. The derivative function is added to the measurement signal before it reaches the controUer (block 4, Figure 8-8). This eliminates derivative response to set-point change and practicaUy eliminates any interaction between derivative and the other control modes. During steady-state conditions, the unit acts as al: 1 repeater, but upon a change in the measurement the unit adds a derivative inftuence to the measurement change. In the derivative unit (Figure 8-11), the force moment (beUows area times distance from fulcrum) ofbeUows A is 16 times that ofbeUows B, and the force moment of beUows B plus beUows C equals that of bellows A. As the measurement signal increases, the immediate change in feedback pressure in B is 16 times the change in pressure in beUows A. Simultaneously, air starts to ftow through the restrictor to beUows C, graduaUy reducing the pressure needed in beUows B to restore equilibrium. Thus, the output ofthe derivative unit, which is the signal to the automatic control unit measurement beUows, reftects the change in

measurementplus a derivative responseadded to that change. The graph at the bottom of Figure 8-11 shows the signal that the measure-

TIME

Fig. 8-11. Derivative unit, schematicdiagramand responsecurve.

216

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

ment bellows in the automatic control unit receives from the derivative unit at the measurement change shown. The integral function takes place within the automatic control unit itself. The integral bellows opposes the feedback bellows; thus, if the feedback bellows introduces negative feedback, the force created by the feedback bellows will act like positive feedback; that is, it tends to move the flapper in the same direction as error. This would lead to instability if the integral restriction were Dot used. anly very slow signals (minutes in duration) can affect the integral bellows because of the very small integral restriction. The integral action occurs only arter the proportional and rate actions h~ve affected the processoIf an error remains (such as offset due to load change), the integral action takes place slowly. Because integral action will continue in the presence of a continuous error, such as we mar find in a batch process, it can cause the output to go to an extreme. This is called integral windup. Integral time is adjusted by setting an adjustable restrictor, or needle valve. The dial on this pneumatic val ve is calibrated in minutes of integral time. Figure 8-12 illustrates the Foxboro Model 130controller. The control rnodes-proportional, integral, and derivative-are in the controller shown. The signal level with respect to time mar be changed by appropriate adjustments of proportional, integral, and derivative modes. The proportional band adjustment is calibrated from 5 to 500 percent, while the integral and derivative dials are calibrated from 0.01 to 50 minutes. These adjustments are calibrated in "normal" times. The effective times are somewhat different. In any controller, some interaction between control actions mar exist because change in one action (proportional, integral, or derivative) can create change in the others. This unavoidable interaction, even if small, should be kept in mind when adjusting or tuning a control ler. Manual Control

Unit

Manual operation is achieved by using the manual control unit shown schematically in Figure 8-13 and depicted in Figure 8-14. With the transfer switch in the manual position, the thumbwheel is engaged, and by its action the flapper-nozzle relationship governs the pneumatic output. The operation of the manual control unit is similar to that of any pneumatic transmitter in that it employs a feedback bellows. Full-scale manipulation of the thumbwheel corresponds to a 3 to 15 psi (20 to 100 kPa) pneumatic output.

PNEUMATICCONTROLMECHANISMS 217

Fig. 8-12. Pneumatic Consotrol130M controller. (Top) right sicle cover removed and manual controls. (Battam) the leCtsicle cover is removed to show pneumatic printed circuit board.

Transfer

Automatic to Manual With the transfer switch in the automatic position, the thumbwheel in the manual control unit is disengaged and the automatic controller's pneumatic output is fed into the manual control unit bellows. The manual control unit remains balanced at this output. At the time of transfer to manual, the manual unitinstantfy starts transmitting this same output. Thus, the response record of the transfer from automatic to manual (Figure 8-15) is smooth and bumpless. Manual to Automatic The transfer Crom manual to automatic requires the use of an automatic-balancing unit, which consists of a singie-pivoted diaphragm with four air pressure compartments. This is shown in schematic Corm

AIR SWITCH SUPPLY SIGNAL

OUTPUT

Fig. 8-13. Schematicof manualcontrolunit.

Fig. 8-14. Manual controlunit; TRANSFER

TIME-Fig. 8-15. Responserecord oftransfer Cromautomaticto manual. 218

PNEUMATICCONTROLMECHANISMS 219

in Figure 8-16. At the left, the unit is in the automatic position; at the right, it is in manual. It will act as a simple proportional controller with a fixed proportional band of approximately 30 percent. The basic probIem in transferring from manual to automatic lies in the fact that the output of the automatic controller must equal that of the manual unit at the moment of transfer, and then a change at a predetermined integral rate is necessaryto bring the measurement to the set paint. The output ofthe manual station is the control unit' s output. Full air supply is sent to the three pneumatic switches, closing two and opening one, as shown in Figure 8-16. The proportional bellows of the automatic control unit is disconnected from the output of the controller. The integral restrictor is bypassed, and the integral bellows is disconnected from the proportional bellows. The input signals to the automatic balancing unit shown represent the automatic control unit proportional bellows pressure in bellows D, and the manual control output in bellows A. Bellows B is the balancing pressure and bellows C is the output to the integral bel-

lows. If either the measurement or the set paint to the automatic control unit changes, the pressure in the proportional bellows must also change, because it is operating as a proportional-only control unit. When the change in pressure in the proportional bellows is sensed by the balancing unit, the unit' s output will change the pressure in the controller's integral bellows. This, in turo, will cause the proportional bellows pressure to change in the opposite direction until it once again equals the output of the manual control relay, or until the supply pressure limits are reached. Any diiference between the set and measurement bellows is thus balanced by the difference between the integral and proportional bel-

lows. If the output of the manual control unit changes, a similar action occurs, forcing the proportional bellows pressure to equal the manual control unit output. When transferring from manual to automatic (Figure 8-17), the output will remain at the level determined by the operator when the controller is in manual. If the measurement input is equal to the set paint, the output remains constant until corrective action is required. If the measurement does Dot equal the set paint at the moment of transfer , the output will camp from the level of manual operation to the level necessary to make the measurement equal to set paint a function of the controller's integral rate.

220

PNEUMATIC ANDELECTRONIC CONTROLSYSTEMS

Fig. 8-16. Schematic of auto-manual mechanism with transfer switch in automatic position (above) and manual position (opposite page).

Set Poí nt

The set-point knob is attachedto a pneumatictransmitter, which relates the transmitter's output positionor the set-pointpointer (Figures 8-18and 8-19).The output or the transmitteris applied to the set bellows or the controller. If the automaticcontroller is operating, normal

PNEUMATICCONTROLMECHANISMS 221

changes can be made by turning the set-paint knob. Proportional-plusintegral action will occur. Since the derivative amplifier exists only in the measurementcircuit, derivative action will nat occur. If it is desired to bring the process slowly to the new set paint with integral action only, the controller is simply switched to manual, the set-paint change is made, and the controller is switched back to automatic. Now the measurement will approach the new set paint, with integral action only, and no overshoot will occur.

222

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

SET paiNT

LTIME-i

TIME-

Fig. 8-17. TransCerCrommanual to automatic ([eft) when measurementequals set point and (right) when measurement does not equal set point.

Fig. 8-18. FoxboropneumaticConsotrol130Mcontrolletpulled out to show access-to-mode adjustments.

PNEUMATICCONTROLMECHANISMS 223

LlNEARIZING ASPIRATOR RELAY

TO REVERSE FROMREMOTE SWITCH AND SET POINT AUTOMATIC SIGNAL L.A.R. CONTROL U 1T .L

LOCAL I ~. SETPOINT1n-"1 TRANS

AlS \~~-. r-rr

REMOTE SET POINT

RECEIVERI

SET KNOB

Fig. 8-19. Schematicoflocal and remote set-pointmechanisms.

The Closed-Loop

Pneumatic

Controlled

System

Now let us apply the pneumatic controller to a process controlloop. The objective of a control system is to maintain a balance between supply and demand over time. (See Chapter 1 for a discussion of supply and demand.) The closed-loop control system achieves this balance by measuring the demand and regulating the supply to maintain the desired balance. Figure 8-20 illustrates a typical and familiar controlled system in which the temperature of heated water (controlled variable) is regulated by control of i~put steam. The control system comprises a

IIPULATED

224

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

VARIABLE 1

Fig. 8.20. The processto becontrolledoccursin a beatexchanger.All elementsofthe pneumaticcontrol systemare shown-transmitter, controller, valve, input water, output water, and steam.

pneumatic temperature transmitter (Foxboro Model 12A), a forcebalance pneumatic controller (Foxboro 130 Series), a pneumatic (diaphragm) valve actuator, and a control val ve (wide-range V-port). Figure 8-21 shows an accepted manner of representing a system in a block diagram. All the elements of the actual system are included.

CONTROLLER

:.--J ERROR 1 fAMPLIFIER'

iDETECTORM (RELAY)t=l

L-

-INTERNALFEEDBACKLOOPjI

SET

¡-

II M~.A_S.u.~.!.NG II MEANS ~EXTERNAL

CONTROLLED

FEEDBACK

LOOP

MANIPULATEO

Fig. 8-21. Block diagramshowingall the elementsor Figure8-20.

PNEUMATICCONTROLMECHANISMS 225

The Process

The process to be controlled is a shell-and-tube beat exchanger. Lowpressure steam applied to the shell beats water flowing through the tubes. The exchanger has 33.5 square feet ofheat-transfer surface, and the time required for the beat exchange to take place across this surface causes the exchanger to bave a delayed response. The response characteristic is that of a multiple-capacitance, multiple-resi&tance circuit. ¡ The response or reaction curve of the beat exchanger was 'obtained by (1) allowing the beat exchanger to stabilize with a constant flow of both steam and water, (2) holding the water flow constant, (3) increasing the steam flow suddenly by opening the control valve, and (4) plotting the increase in water temperature. The resulting curve is the reaction curve illustrated in Figure 8-22. ' Since the water temperature was measured with the pneumatie temperature transmitter, the transmitter output depends nat only on the response of the beat exchanger, but also on the response of the transmitter, which is nat instantaneous. The Controller

Set Point

The set point oí the controller is established by setting an air pressure in a "set" bellows by means oí an air regulator. The setting dial (Figure 8-23) is spread over the span oí the measured (controlled) variable.

Fig. 8-22. Responseof outlet temperatureto stepsin steamvalve positiontest results.

226 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

OUTPUT

SET KNOB

Fig. 8-23. Schematic of set-point mechanism.

Valve and Actuator

The controller output positions a control valve which, in turn, governs the energy or material inflow to the processoThe speed of response of the valve depends on the type of valve actuator, that is, the device that transduces the controller output signal into a valve position. The actuator can be pneumatic or electric. The system under study uses a familiar pneumatic actuator, which consists of a large diaphragm (110 square inches) to which the pneumatic signal is-applied. When 3 psi (20 kPa) is applied to an area of 110 square inches, a force of 330 pounds is developed; when 15 psi (100 kPa) is applied, the thrust will be 1,650 pounds. This downward diaphragm force is opposed by a large coil spring that pushes upward with a force of 330 to 1,650 pounds. Increasing or decreasing the pneumatic signat to the diaphragm will cause the diaphragm to move until it reaches a position where diaphragm force and spring force are in equilibrium. Since the relationship between spring thrust and excursion is a linear one (Hooke's law), valve trave} is related linearly to controller output. Valve actuators mar be arranged either to open the valve or close it on increasing air pressure. The choice of action is usually dictated by the process being controlled. For a beat exchanger process, the air-toopen valve usually is selected because the spring will close the val ve and cause the temperature to drop in event of air failure. This is called fail-safe action. If the process were one that became hazardous when the valve closed, the action would be reversed to make the valve open on air failure. The valve actuator has a response time because it has the capacity

PNEUMATICCONTROLMECHANISMS 227

to hold air and the connectingtubing offers resistanceto air ftow. The time constant for a pneumatic operator is typically several seconds with normallengths of connectingtubing. Adding tubing lengthensthe time constant.Thus, the valve actuatorcontributestime lag or phase shift to the controlloop, dependingon the lengthof connectingtubing

used. Final Control

Element

The function of the pneumaticvalve actuatoris to positionthe control valve. The valve canbe one of manytypes, dependinguponthe process to be controlled. For the beat exchangerprocessbeing discussed,a single-seatwide-rangeequalpercentagevalve is used (Figure 8-24). The single-seatequalpercentagevalve hasa contouredinner valve that provides an exponentialrelationship betweenvalve stroke and valve capacity.

Fig. 8-24. Cutawayview of single-seat,wide-range,equalpercentvalve.

228 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Fig. 8-25. Closed-loopcontrol system,showingall basiccomponents.

Dynamic Behavior ot Closed-Loop Control Systems When all components are connected to form the closed-loop control system (Figure 8-25), each component contributes to control system operation. For example, the total gain (output signal/input signal) is affected by the gain of every one ofthe loop components. However, the only loop component that has an adjustable gain is the controller. Adjustment ofthe proportional band results in adjustment ofthe totalloop or system gain. Let us assume that the control system has stabilized with the outftow temperature at 1500F,66°C and that the system is subjected to an upset by raising the set paint suddenly to 1600F(71°C).

~SE

PNEUMATICCONTROLMECHANISMS 229

".,3."CON.'.,. '" ,. 6.

The action around the controlloop (Figure 8-26) will be as follows: 1. Increasing the set point increases air pressure in the set bellows, thereby causing the ftapper to approach the nozzle. 2. Increased nozzle pressure is amplified and becomes output to the control valve. Because the valve actuator is a resistancecapacitance element, the actual change in valve position will be delayed behind the change in output signal.

230 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

3. The addedbeat (Btu) will be nearly in stepor phasewith the valve position. 4. The added beat causesthe temperatureof the beat exchangerto rise, and as it Tises,the pressurein the measurement bellows will increase. 5. Any unbalanceof the momentsof force contributed by the measurementand set bellows will causethe integral bellows to continue to change through the integral restricter, and the output pressureto increaseuntil the temperaturereachesthe set point. The momentsof force are now balanced,and the ftapperis within its throttling range(a band of travelless than0.001 inch wide). 6. After approximately2 minutesbaveelapsed,the forcesexertedby the various bellows will be in equilibrium; the ftapperis within its throttling range; and the processhas stabilized at 160°F,71°C. Thesestepsare illustrated in Figure 8-26. (Note: If the upsetwere causedby a load change,derivative action would bave beenaddedto the functions described.) Adjusting the Controller To accomplish effective control and cause the process to feaci in an optimum fashion, the controller behavior, with respect to time, musi be matched to thai of the processoThis is done by adjusting the proportional band, integral time, and derivative time. Thning or adjusting the controller for optimum performance can be achieved either by trial-and-error, or by more exacting methods. The usual trial-and-error procedure in adjusting the controller settings to the process conditions is to set the integral restrictor at maximum and the derivative restrictor at minimum, and then to adjust the proportional band to produce the minimum process stabilization time. Then the derivative restrictor is increased gradually, and the proportional band narrowed, until a combination of proportional and derivative action is obtained which produces a shorter stabilization time than normal proportional, and with less upset to the processo To eliminate offset, the integral restrictor is then set to avalue thai will bring the control point to the set point in a minimal time without upsetting the stability of the system. Other methods of adjustment by mathematical and analog analysis are discussed in Chapter 12. Suppose a set point of 20 percent scale change is made in the Foxboro 130 Series controller with the controller on automatic. Note

PNEUMATICCONTROLMECHANISMS 231

OUTFLOW

WATER TEMPERATUREI

Fig. 8-27. Controlled set-point change made in automatic mode (top) and in manual mode, then switched to automatic (bottom).

the damped oscillations that occur as the system Testabilizes (Figure 8-27, top). The instability lasts for several minutes. If the controller is first switched to manual for the set-point change, a reaction will occur when switched back to automatic. This is shown in the lower part of Figure 8-27 and discussed previously. The controlled variable retums to the new set point at the integral rate. Any adjustments tend to cause a temporary upset; therefore, the technique of switching to manual, making any required adjustments and switching back to automatic, can be used to advantage with the Foxboro 130Series controller.

Batch Controli er

In Chapter 7, reference was made to integral saturation or integral windup. This occurs when the integral mode is used on a batch or discontinuous processo During the time the process is shut down, the integral circuit of a conventional two- or three-mode controller will saturate at the supply pressure. After the process is restarted, measurement overshoot of the set point can occur unless precautions are taken. The batch switch is a special pneumatic mechanism designed to prevent this overshoot. During the time a process is otI control, the measurement will be

-Fig.

232 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

riME

CuRVE

8-28. (Left) Recovery from sustained deviation; proportional plus integral controller without batch feature. (Right) With batch feature.

below the set point and the controller's output will be at its maximum value. Ifthe time oftbis deviation is long enough, the integral circuit of a conventional controller will also reach ibis value. When process conditions retum to normal, no change in controller output can occur until the measurementreaches the set point. Figure 8-28, curve A illustrates ibis control action. The batch switch eliminates tbis integral circuit saturation and conditions the integral bellows to permit output to start to change before the measurement reaches theset point. If the controller output starts to change before the measurement reaches the set point, overshoot can be prevented and the measurement can retum to the set point smoothly. Figure 8-28, curve B illustrates tbis control action. Principie

ot Operation

A schematic diagram of a proportional-plus-integral batch controller is shown in Figure 8-29. The only addition to a conventional two-mode controller is a specially designed pressure switch between the relay output and the integral circuit. The switch is actuated by the output pressure of the controller relay. Its trip point is adjusted by a spring, or an external pneumatic signal, to trigger at 15 psi (100 kPa). When the controller's output is below this pressure, the ball valve closes the vent port and permits passage of the relay output to the integral circuit. This allows normal integral response as long as the measurement remains within the proportional band (below 15 psi or 100 kPa). Should the measurement reach the 15 psi or 100 kPa limit of the proportional band throttling range, the force on the batch switch diaphragm will seat the ball valve in the opposite direction. This cuts off the relay output pressure to the integral circuit and simultaneously vents the circuit to the atmosphere.

PNEUMATICCONTROLMECHANISMS 233

Fig. 8-29. SchematicoCproportional-plus-integraJ batchcontroller.

This causes the pressure in the circuit to dropo As long as the relay output pressure is above the trip point, the integral circuit pressure will drop until there is no longer any pressure in the integral bellows. At this point, the proportional band throttling range will have shifted completely below the set point as indicated in Figure 8-28B, curve B. During this operation, the controller's output pressure is at 15 psi or 100 kPa (or more) and the valve is wide open. When the batch process is restarted, the control valve will begin to throttle as soon as the measurement reaches the 15 psi or 100kPa límit of the proportional band throttling range. Note that as soon asthe controller output drops below 15 psi or 100kPa, normal integral response is restored. This overcomes the tendency to overshoot the set point. Load Bias (Preload)

Due to the time characteristics of certain processes, shifting the proportional band completely below the set point will cause an intolerable delay in bringing the batch to the set point. In such cases, an adjustable back pressure mar be applied to the vent port to "bias" the batch switch. Thus, the pressure in the integral circuit mar be prevented from dropping below a preselected amount and the proportional band throttling range will shift only partially below the set point. Although this will allow faster recovery, a slight overshoot will occur if the "bias" is

234 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

increased too much. Increasing the bias to 15 psi or 100 kPa would obviously completely eliminate batch action. One limitation thai applies to all pneumatic control systems is the distance thai mar be accommodated between components. The maximum distance depends on two major factors: the pneumatic signal travels at the speed of sound, and the loop components along with the tubing all bave capacity and resistance. Thus, an RC time constant musi exist. Volume boosters often are applied to lengthen ibis working distance. Unfortunately, a volume booster will do nothing to speed up signal velocity. A booster will help if a large volume, such as thai found in a pneumatic valve actuator, is involved. The distance límit for pneumatic control systems is approximately 200 feet (60 meters). Iftbis distance factor is ignored, the dynamics ofthe control system will suffer and reguli in poor control operation. If it becomes necessary to lengthen these distances substantially, the only practical solution is to utilize electrical signals thai mar work over an almost unlimited distance. Questions

8.1. The integraldial in a pneumaticcontrolleris calibratedin: 8. Minutes or repeats d. Percentage b. Integralunits e. OtIset

c. Gain 8-2. True or false: In a proportional-onlycontroller,ifthe measurement equals the set point the output will equalthe bias. 8-3. True or false: In an integralcontroller,the rate of changeof the output is proportionalto the error. 8.4. True or false: The largerthe numberon the integraldial the greaterthe effectof the integralaction. 8-5. True or false: In a batchoperation,if a controllerhaswound up, it is quite possiblethat the valve may stay in an extremepositionuntil the measurementactuallygoesbeyondthe set point beforethe valve beginsto changeits position. 8-6. True or false: What somemanufacturerscall rate others call derivative. 8-7. Indicate all the correctstatements: 8. Gainis the reciprocatof the proportionalband. b. The proportionalbandis the reciprocatof gain.

PNEUMATICCONTROLMECHANISMS 235

c. d. e. f.

The The The The

proportional band times the gain equals 1. gain divided by the proportional band equals 1. narrower the proportional band, the higher the gain. wider the proportional band, the lower the gain.

8-8. In a process controlled by a proportional-plus-integral controller, the measurement was at the set point and the output was 9 psi (60 kPa). The measurement then quickly decreased to a certain value below the set point and leveled out there. The output responded by changing to 8 psi (55 kPa). As time progresses, what would you expect of the output pressure? a. Increase to 9 psi (60 kPa) to bring the measurement back to the set

point. b. Remain at 8 psi (55 kPa) as long as the measurement stays where it is. c. Decrease and continue to decrease to 3 psi (20 kPa). d. Continue to decrease until the measurementreaches the set point, or if it does not retum to the set point, decrease to Opsi. 8-9. The range of the temperature measuring system used in conjunction with a Model 130proportional-only contro1ler is O to 150oP(66°C). The output is 9 psi (60 kPa) when the set point and indicator are both at 75°P (24°C). If the proportional band is 200 percent, what is the output when the measurement is 150oP(66°C)? a. 9 psi (60 kPa) c. 12 psi (83 kPa) b. 3 psi (20 kPa) d. 15 psi (100 kPa)8-10. If the span of a measuring transmitter in a control system is made one-half of its value, the proportional-band adjustment in the controller must be -to maintain the same quality of control. a. Cut in half d. Narrowed b. Doubled e. None of the above.

c. Squared 8-11. With a proportional-plus-integral controller, a sustained error will result

in: a. b. c. d. e.

Windup A fixed offset A temporarynarrowingof the proportionalband A delay in the process None of the above

8-12. By locating the derivative function in the input measurement circuit, which of the following advantagescanbe realized? a. Smoothbumplesstransfer b. No derivative bump with a set-pointchange c. No proportionalresponseto a set-pointchange d. Integral adjustmentis isolated from response

8-13.

236 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

a. b. c. d.

If proportional-plus-integral controlis good,the additionof derivative: Will anticipatechangesand speedup corrections Will alwaysimprove control Will makethe controlleradjustmentseasierto accomplish May create stability problemsin somesystems

8-14. The advantageof addingderivativeto a controlleris always: a. Increasedstability b. The ability to overcomea big pure deadtime lag c. The ability to reactmore quickly to measurement change d. A decreasein the pure deadtime of the process 8-15. For fail-safeactionthe control valve should,uponenergy(air)failure: a. Open b. Close c. Move in suchdirectionas to makethe processnonhazardous d. Stay in its previous position 8-16. If the closed-loopcontrol systemhastoo muchgain, it will cycle. The only loop componentthat hasconvenientlyadjustablegainis the: a. Measuringtransmitter c. Process b. Valve operator d. Controller 8-17. Adjusting the controller for optimumperformance: a. Is not required,becauseit adjustsitself b. Requiresa specialtool c. Is usuallydone by trial and error d. Always requiresa very involved mathematicalanalysisof the process 8-18. A processis to be controlledusingan all pneumaticsystem.The maximumdistancebetweenloop componentswill be: a. 1,000feet c. 200feet b. 500feet d. 20 feet 8-19. If the distancebetweenloop componentsin the all pneumaticcontrol systemmustbe increasedit will require: a. A pneumaticvolume booster b. Largersizedtubing c. Smallersizedtubing d. Conversionto an electricalsignal 8-20. PneumaticsignalstraveI throughthe signaltubing al: a. 100feet per second b. Approximatelythe speedof sound c. A rate that dependson tubing size d. Approximatelythe speedof light

237

Electronic control systems,already widely accepted,are gainingrapidly in popularity for a numberof reasons: 1. Electrical signalsoperateover greatdistanceswithout contributing time lags. 2. Electrical signals can easily be made compatible with a digital computer. 3. Electronic units can easily handle multiple-signalinputs. 4. Electronic devices can be designedto be essentiallymaintenance free. s. Intrinsic safety techniques bave virtually eliminated electrical hazards. 6. Generally, electricalsystemsare lessexpensiveto install, take up less space,and can handle almost all processmeasurements. 7. Electronic devices are more energy efficient than comparable pneumatic equipment.

8. Specialpurposedevices suchas nonlinearcontrollers and analogcomputingunits are simplified. This chapter will describethe electronic instrumentcomponents that make up a typical multiloop system. The processis one found within the boiler room of most processplants-a feedwater control systemfor a boiler drum.

238 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Feedwater

Control

Systems

A sample electronic control system is shown in Figure 9-1. The water level in the drum is to be controlled. This is accomplished by measuring Dot only the water level, but the steam ftow out of the boiler and the water ftow into the drum. The three measured variables are fed to an electronic control system, which controls the water to the drum. Transm itters

Two ditIerential pressure transmitters (Fig. 9-2) are used, one to measure water flow; the other to measure drum water level. Referring to Fig. 9-3, in operation the ditIerence in pressure between the high and low gide of the transmitter body is sensed by a twin diaphragm capsule (1) which transforms the ditIerential pressure into a force equal to the ditIerential pressure times the etIective area of the diaphragm. The resultant force is transferred through the C-flexure (2) to the lower end of the force bar (3). Attached to the force bar is a cobalt-nickel alloy diaphragm which serves as a fulcrum point for the force bar and also as a seal to the process in the low-pressure cavity gide of the transmitter body. As a result of the force generated, the

Fig. 9-1. Peedwater control system. (I) Drum water level (2) Steam ftow from boiler, via turbine steam pressure. and (3) Water ftow into drum.

Fig. 9-2. Differentialpressuretransmitter.

Fig. 9-3. Operationof electronicforce balancedifIerentialpressuretransmitter. 239

force

240 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

bar pivots abolli the CoNi alloyseal, transferring a force to the vector mechanism (5). The force transmitted by the vector mechanism to the lever system (11) is dependent on the adjustable angle. Changing the angle adjuststhe span of the instrument. At point (6), the lever system pivots and moves a femte disk, part ora differential transformer (7) which serves as a detector. Any position change of the ferrite disk changes the output of the differential transformer determining the amplitude output of an oscillator (8). The oscillator output is rectified to a d-c signat and amplified, resulting in a,4-20 mA d-c transmitter output signal. A feedback motor (9) in series with the output signal, exerts a force proportional to the error signal generated by the differential transformer. This force re balances the lever system. Accordingly, the output signal ofthe transmitter is directly proportional to the applied differential pressure at the capsule. Any given applied differential pressure within the calibrated measurement range will result in the positioning of the detector' s femte disk, which, in turn, will maintain an output signal from the amplifier proportional to measurement, thus keeping the force balance in equilibrium. A simplified schematic of the electronic circuitry is shown in Fig.

9-4. Steam ftow out ofthe drum is measured in terms of steam pressure, which is measured with a pressure transmitter. The operation of the pressure transmitter is similar to the operation of the differential

Fig. 9-4. Working schematic oCelectronic transmitter.

ELECTRONIC(ANALOG) CONTROLSYSTEMS 241

pressure transmitter_,The same feedback technique used in the differential pressure transmitter is employed in the pressure transmitter. The major difference lies in the size and construction of the sensor. The pressure transmitter measures the pressure in the first stage of the power turbine. Since there is a linear relationship between first stage turbine pressure and steam flow, the output signal from the pressure transmitter is linear with steam flow out of the boiler, A variety of electronic differential pressure transmitters are available from a number of manufacturers. Some of these make use of strain gauge detectors, capacitive detectors, resonant wire detectors, and inductive detectors. Many are motion or open loop devices which are still capable of accuracies within a fraction of a percent. In the application of any electronic transmitter, the user must guard against subjecting the electronics to temperatures which might result in damage. This probIem generally can be avoided by observing the precautions recommended by the manufacturer.

The Controllers

The controllers described befe are the Foxboro SPEC 200 type. The SPEC 200 is generally a split-architecture system. In this system two areas may be used, a display area and a oest area. Field equipment, such as measuring transmitters, electrical valve actuators, and the like, generally operates on 4 to 20 mA dc. Within the oest, SPEC 200 operates on O to 10 volts. The display area contains control stations, manual stations, recorders, and indicators to provide the necessary operator displays and controls. These units are shelf-mounted and contain only the electronic circuitry required to communicate the display and adjustments necessary for an operator to control and monitor a processo The nest area contains the analog control, computing, alarm, signal conditioning, and input and output signal converter units. These units are in the form of "modules" and "circuit cards." The oest itself is basically an enclosure provided for the mounting of "modules." System power is supplied to the oest. This power supply must deli ver + 15 and -15 V dc for operation of the display and nestmounted instruments. Recorder chart drives and alarm lights require 24 V ac. When a single location is required, the oest and display areas may

242 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

Fig. 9-5. Basic arrangementof SPEC200loop.

be combined iota one unit. In faci, a single-unit controller with display, controUer card, and power supply mar be combined iota a single case. This is caUed a SPEC 200/SS (single-station) controUer. The basic arrangement ofthe conventional SPEC 200 system is shown in Figures 9-5 and 9-6. In the single-station unit (Figure 9-7), aUcomponents shown in Figure 9-5 are contained in the single unit. For the boiler drum level control, either the single-unit construction or the split system could be used. TypicaUy, the choice would be to split the system iota oest and display areas. This wiU provide added ftexibility. The typical boiler room would bave many control loops in addition to the boiler drum level. This could aU be combined iota one oest and display area.

Fig. 9-6. Displayand nestareas.

ELECTRONIC (ANALOG) CONTROL SYSTEMS

243

Fig. 9-7. Single station control unit. Electronic display: The measured variable and set point are continuously displayed as vertical bar graphs on a dual gas-discharge unit. The right-hand bar represents the measured variable; the left-hand bar represents the set point. Transparent scales are easily changed without recalibration.

Whether the controller is nest-mounted or case-mounted, it is essentially the same controller. Now let us take a closer look at its opera-

tion. Principie

of Operation

A SPEC 200card-tuned control component consists of a printed wiring assembly (circuit card) in a module. The component operates in conjunction with a control station in the system display area. The basic circuits of the proportional-plus-integral-plus-derivative control action model is shown in Figure 9-8. This diagram, with the

Fig. 9-8. FoxboroPID control componentcircuit diagram.

244 PNEUMATIC ANP ELECTRONICCONTROL SYSTEMS

derivative action circuits removed, also applies to the proportional-mode plus-integral control action. is a function primarily of the The output signat in automatic measurement arid set-point inputs. The output and control action are,e also affected by the increase/decrea~ switch on the control component and by the manual/automatic switcltl on the display station. Increase/Decrease

Switch

An INC/DEC switch on the front panel provides polarity reversing of both the set point and measurement signal inputs. Reversing the polarity of these input signals effectively reverses the action of the control component. With ibis switch in the INC position, control action is a function of measurement minus set point (an increase in output is caused by an increase in measurement). In DEC, control action is a function of set point minus measurement (a decrease in output is caused by an increase in measurement). Deviation

Signal

Generation

The o to 10 V dc measurement and set-point signals are applied to the input of differential amplifier UI. The amplifier has a gain of 1 and high common mode rejection. An output signal is produced by the amplifier any time the measurement differs from the set point. The output signa! from amplifier UI passes through a resistive adder to the proportiona! band amplifier as the deviation (error) signal. The resistive adder allows combination of the amplifier output with the derivative signal (in P + I + D control components). In proportionalplus-integral control components, this adder is part of the input resistance of the proportional band amplifier. Derivative

Action

When derivative action is included in the control component, the measurement signal from the INC/DEC switch is applied in parallel to the deviation signal generator amplifier and derivative amplifier U5. Derivative action occurs in proportion to the rate-of-change of the measurement signa!. Derivative amplifier U5 has a fixed gain of9. AIso included in these circuits are integrating amplifer U6 (in the feedback loop of U5) and solid-state (J-FET) switch U7. The input network to the integrator consists of fixed resistors and a Dotentiometer. The effective resis-

ELECTRONIC (ANALOG) CONTROL SYSTEMS

245

tance, and, hence, the deriva:tive action time, can be controlled by the potentiometer. Derivative action can be switched ofI by rotating the derivative potentiometer fully counterclockwise. Both derivative and integral time constants are adjustable from 0.01 to 60 minutes in three ranges (determined by card jumper). Proportional

Band ActionThe

proportional band stage consists of potentiometric amplifier U2arranged so that the output is proportional to the input. The gain of the amplifier is determined by the P control on the front panel. Final Summing

and Switching

Signal summing and switching is provided at the input of the output amplifier by a resistive adder and by solid-state switch U3. The external integral/summing and deviation signals, and also the output signal, are connected to the summing junction of the output amplifier through separate capacitors and field effect transistors (FET). These three signals are connected together through separate resistors at a point caUedthe resistor junction. The resistor junction is separated Cromthe summing junction by a field effect transistor. The field effect transistor is turned otI when the control component is in manual mode. This disconnects the deviation signal Crom the summing junction, and connects the dc voltage to the input of the output amplifier. Releasing the manual drive thumbwheel Crom the slow change position causes a spring return to the center position. As a result, the FET is turned otI to open the integrating input, and the component is placed in the "hold" condition. The output stage of the control component is integrating amplifier U4. The amplifier drives the composite signal produced by the final summing and switching element. High and Low Limits

High and low límits are established for the O to 10 V output signal by appropriate circuits. Bach límit circuit consists of comparator amplifiers VII and V12 with associated potentiometers, R77 (HI) and R87 (LO) on the front panel. The output signal from each comparator amplifier is applied to solid-state switch V3. The signal serves as a clamp on the manual or automatic signal input to the output amplifier.

246 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

When summed with either the automatic or manual signal, the comparator amplifier outputs prevent the control component output from exceeding the limit referençe voltages. Test jacks on the front panel allow monitoring of the limit adjustments for setting. Externallntegral

(-R)

Opti on

DifIerential amplifier UB is added to the standard control component card for an external signal to reset the output. Amplifier UB accepts external signats and sums them with the control component deviation signal. This provides an integral input to solid-state switch U3. Anytime the external integral input and the control component areunequal, an error signal is generated. The error signat biases the output in proportion to the external input value, and windup is thus prevented. As long as the control component output tracks the external integral signat, normal integral action takes place. The control component output is biased by the external integral signal in all other conditions, and only proportional action of the control component deviation signal is obtained. This option is used in this application. External

5umming

(-5)

Option

Externa! summing allows biasing the output directly with an external signal. Differentia! amplifier US is inserted into the "proportional path" solid-state switch U3. The proportional signa! is summed with the external bias signal in amplifier US. The control component output responds directly to changes in the external summing signa! in addition to the ordinary control functions. Power Supply

Fault Protection

Circuit

This circuit preserves the control component output during short periods of power failure. After such a failure, the output will be essentially at the last value prior to the power failure. The maximum duration of the fault condition for which this preservation will hold is I second. In the manual mode, the drift is less than 1 percent for this 1 second maximum duration. In the automatic mode, additional considerations will dictate the control component output if the fault is corrected within 1 second. Principally, there can be a new measurement signal value when power is restored. This, coupled with the tuning adjustments, will determine the output.

ELECTRONIC(ANALOG) CONTROL SYSTEMS 247

The power supply fault. protection circuit can be bypassedby jumper selection. Automatic/Manual

Switch

When the automatic/manual switch in the display area is moved to the MAN position, dc voltages are applied to the solid-state switch (high impedance module U3). This atIects the circuitry in two ways. First, the output amplifier is disconnected Cromall "automatic" signals, and the output remains at the last value. Second, the output amplifier is connected to dc voltages that cause a ramp up or ramp down output. Releasing the manual drive (thumbwheel) will cause a spring retum to center position, thereby opening a I-FET switch on the integrating input. This places the circuit in a "hold" condition. When the automatic/manual switch is transferred to the AUTO position, the solid-state switch connects the deviation signal to the output amplifier. Normal control action then begins. This switch Crom the manual to the automatic mode occurs without a "bump" (drastic change) in output signal due to the action of the balance circuits. Controller

Adjustments

This controller has a proportional band adjustable Crom2 to 500 percent, integral adjustable Crom0.01 to 60 minutes (equal to 100to 0.017 repeats per minute integral rate) and available, but Dotrequired for this application, derivative adjustable Crom0.01 to 60 minutes.

General

Description

ot the Feedwater

Control

System

The purpose of tros electronic control system is to maintain drum level at a manually set value with mínimum ftuctuation. The system continuously matches feedwater ftow (supply) to steam ftow (demand) to maintron the proper relationship of these variables. This relationship is trimmed by the drum level control unit to maintain drum level at any desired, manually set value over the load range of this unit. This control system is a three-element electronic cascade system in which the primary or master control unit functions to control drum level and the secondary, or slave control unit, functions to maintain the balance between feedwater and steam ftow. The primary control unit positions the set point of the secondary control unit, which functions to control the feedwater valve.

248 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

The primary control unit compares a measurement of drum level with its manually adjusted set point to develop an output signal that feeds to the external set point input of the secondary control unit. The output of the primary control unit trims the demand for feedwater to maintain the drum level at the set point. The secondary control unit compares the feedwater/steam ftow relationship with its set point to develop an output signal to regulate the feedwater valve. To maintain drum level, feedwater ftow must essentially equal steamftow. For tros condition, the measurement input to the secondary control unit is at midscale. Whenever the drum level is Dot at the control set point, the primary control unit will alter this secondary control unit set point to trim the ftow of feedwater to the drum. Trimming action will continue until the drum level returns to the control set point. Any change in steam or feedwater ftow is immediately sensedas a discrepancy in the actual feedwater/steam ftow relationship by the secondary control unit. This control unit, tuned to the response of the feedwater loop, will correct the feedwater ftow to restore the feedwater/steam ftow relationship. The measurement input to the secondary control unit is fed to the integral circuit ofthe primary control unit to prevent integral windup of the primary control unit when the control station is in manual control, or when the secondary measurement cannot follow its set point. Control Station The Foxboro Model 230SW cascade set control station is used with a module (Figure 9-9) containing two electronic control units to provide a O to 10 volt valve control signal in a single station three-element cascade feedwater control. The control station is a shelf-mounted display instrument located in the display panel of the SPEC 200 system. The control station contains two nitinol drive units for indicating the primary and secondary measurements of a cascadesystem. A SET knob on the front plate positions the set-point index on the scale and provides the set-point signal from the drive unit to the control unit. A front panel cascade/secondary switch allows the operator to select cascade or secondary operation. The set-point and valve control output signals are adjustable. In cascade (transfer switch in CAS position) operation, this station

indicates

ELECTRONIC (ANALOG) CONTROL SYSTEMS

249

TO CONTROLSTATION

I~I

G" o

SECONDARYI CONTROL CARD

CASCADE TRACI

--, c.

'-1-0 CX»IT

00 000000000 00 00 O O O O ,

00 O O

y CASCADE

CDNTRCX- MODULE

) 2AC-C

Fig. 9-9. Cascadecontrolmodule.This is a dual unit modulethat providesthe circuitry to configurea dual unit cascadefeedwatercontrolsubsystem.This moduleis wired internallyto providetracking by externalreset.

drum level set point (B/W pointer), valve control output sig-nat (black pointer), drum level measurement (red pointer), and feedwater steam ftow relationship (green pointer). In secondary operation (transfer switch in secondary position) the function ofthe set knob is transferred from the drum level (primary) tothe feedwater (secondary) control unit. The secondary switch position allows tuning of the secondary loop with only the feedwater control unit active. The switch should normally be in the CAS position. Either of two operating modes, automatic or manual, may be operator selected. In either mode, the control station indicates the selected set point (PRIor CAS), valve control signal, and both measure ment values. M/2AX + A4-R Drum Level Control Unit This is the primary or drum level control unit with circuitry to provide for the secondary measurement (feedwater/steam flow balance) to reset the drum level control unit output. This prevents the drum level control

250 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

unit from winding up when the secondary control unit is in secondary or manual control. The secondary measurementdrives the drum level control unit output to follow. As long as the secondary measurement tracks the secondary set point, normal integral action takes place. In all other conditions the drum level control unit output is driven (biased) bythe external secondary measurement signal. M/2AX + A4 Feedwater

Control

Unit

This is the secondary, or feedwater control unit. Measurement input to this unit is from the feedwater/steam flow computing unit. When feedwater flow matches steam flow, the measurement input signal is midscale. In cascade operation, the midscale set point is received from the drum level control unit. In secondary operation, the set point is received from the control station set-point circuit. M/2AP + SUM Feedwater/Steam

Flow Computing

Unit

Steam ftow is compared with feedwater ftow in the feedwater/steam ftow computing unit. When feedwater ftow and steam ftow are equal, the output of this computing unit is midscale. The summing unit is a function card that slides into a module located in the oest. Its output mar be the algebraic sum of two, three, or four signals scaled to achieve the proper relationship. In this application, only two inputssteam ftow and feedwater ftow-are used. In this application, the summing unit is adjusted to accept two Oto 10 volt signals, one representing feedwater ftow (A) and the other steam ftow (B). The summer also has an adjustable bias, which is set to produce 50 percent scale or 5 volts output when A = B. This output becomes the measurement input to the feedwater ftow controller and is indicated on the control station by the green measurement pointer (Figure 9-1OA). It should be emphasized that aU analog computing devices deli ver scaled values. This is a major advantage of working with the Oto 10 volt signallevel within the oest. For example, if the summer were to add two 10 volt signals, the output would Dot be 20 volts, since 10 volts is the maximum output. Depending on the calibration, the output signal wiU be between Oand 10volts, but wiU represent the addition of the two applied signals. Square

Root Extractor

The square root extractor is a nest-mounted card that accepts a signa} input from the differential pressure transmitter and produces a O to 10

ELECTRONIC (ANALOG) CONTROL SYSTEMS

251

Fig.9-10A. Foxboro SPEC 200 control station. All operating controls and indicators are located at the front.

Fig. 9-10B. The diagramis a simplifiedblock diagramofthe control stationusingthe nitinol drive units, the CAS/SECswitchand the manualcontrolstation.

volt output signal proportional to the square root ofthe input. It is used primarily in conjunction with difIerential pressure transmitters to produce an output directly proportional to ftow. Another version of the square root extractor can be part of the difIerential pressure transmitter's electronics. In either case, the square root extractor is designed to

252 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

create an inputJoutput characteristic such that the output represents the square root of the input. In Chapter 4, it was established that any restriction flowmeter has qüestionable accuracy at very low flow rates. Making the signallinear does Dot solve this problem. Therefore, this device features a lowsigna! cutoff circuit that automatically forces the output to zero scale level when the input signa! falls below 0.75 percent of input span. The square root extractor is employed in this application to translate water flow into linear units that can be compared with linear units of steam flow. If the summer received one linear signa! and one square root signa!, the difference would be meaningless. Feedwater Control Figure 9-1 illustrates how the three signals-steam flow, feedwater flow, and water level-are combined. The first two (steam flow and feedwater flow) are introduced directly into the sum-computing unit. The drum water level comes from a level controller. The measurement signal to the flow controller is the difference between steam flow out and water flow in. The resultant error signal is fed through the feedwater controller to provide the feedwater flow signal to the final operator on thefeedwater control valve. The output from the feedwater flow controller is 4 to 20 mA dc. This is converted into a pneumatic signal capable of operating the control valve by means of a current-to-air valve transducer operating on the signal received from the controller. The operation of this transducer is covered in Chapter 10. The transducer provid~s 3 to 15 psi (20 to 100kPa) pneumatic output linearly related to a 4 to 20 mA dc input. This pneumatic output is used to position the control valve, thus goveming the inflow of feedwater to the boiler. Valves are discussed in

Chapter 11.

Closed-Loop

Operation

Theoretically, the automatic control system need only balance steam from the boiler (demand) against feedwater iota the boiler (supply). If the measurements and control were perfect, such a system would meet all requirements. However, in practice, the drum water level must be used as an overriding control signal, Dot only for safety, but also because there is always some loss of water through blowdown. (Blow-

ELECfRONIC (ANALOG) CONTROLSYSTEMS 253

clown is a continuous removal of contaminated water from the drum.) Variation in blowdown rate requires a change in the drum-Ievel controller output to maintain correct level. The blowdown compensation readjusts the drum level. Thus, a measurement ofboiler drum level is made. This information, used to enforce a more perfect balance between supply and demand, is called feedback trim. Assume that the drum level can vary :!: 15 inches from the desired level. The differential pressure transmitter is calibrated -15 to + 15 inches ofwater head (span = 30 inches) and creates an output of4 mA dc at -15 inches, 12 mA dc at O,and 20 mA dc at + 15 inches. Assume also that the level control set dial is graduated -15 to Oto + 15(Figure 9-10A). If the dial is set at O, optimum level would be desired in the

drum. The usual procedure for adjustment of a multiple-control loop, such as the one described, is to isolate the loops and adjust them one at a time. The feedwater flow controller will normally bave a wide proportional band (typically 250 percent) and a fast integral (1/10 minute). Having adjusted the flow controller, the level controller proportional band and integral are adjusted to give maximum response with full stability. No derivative is employed on the feedwater flow controller .-8-9 DEC

~ :-I~f-~c~-(~C 6+

DEC

INC

FOxBORO

136-5-30 FEEDWATER STEAM FLOW COMPUTER

FOXBOAO

557

,.. ~;;~=~;;~.

/ ,,I

FEEDWATER

FDXBDRO

M/130

MC'¡'PRD

CASCADE SET FEEDWATER CONTROLLER

Fig. 9-11. Drum level control-pneumatic.

DRUM

LEVEL SET

Limited

254

PNEUMATIC AND ELECTRONIC CONTROL SYSTEMS

because derivative creates high-frequency response, and flow "noise" would upset the controller. A large number of power plants bave been instrumented in the manner shown and are currently working satisfactorily.

Comparison

ot Electronic

and Pneumatic

Systems

Figure 9-11 shows a pneumatic drum level control system. You will note the pneumatic system is essentially identical to the electronic system. Both systems use panel control stations that look and operate alike-occasionally the systems are combined in the same panel. In the drum level control process, the electronic system proves advantageous over a pneumatic system for several reasons. First, it is possible to mix the multi ple signats easily. Second, the installation cost is greater for pneumatic because of piping. The pneumatic system also has less flexibility. The two systems are compared in detail in Table 9-1.

Table 9.1. Comparisonof Pneumaticand Electronic Control Systems Feature

Pneumatic

Transmissiondistance Standardtransmission

3-15 psi practically universal

Practically unlimited 4-20 mAdc practically

Compatibilitybetween instrumentssuppliedby differentmanufacturers

No difficulty

universal Occasionallynonstandard

Controlvalve compatibility

Controlleroutputoperates control valve operator direct

Compatibility with digital computer or data logger

Pneumatic-to-electric converters required for all inputs Superior if energized with clean dry air Inferior unless air supply is

to a few hundred feet

signa!

Reliability Reaction to very low (freezing) temperatures Reaction to electrical interference (pickup)

E/ectroni

signals mar require special consideration and mar not be compatible Pneumatic operators with electropneumatic converters or electrohydraulic or electric motor operator required Easily arranged with minimuro added equipment Excellent under usual environmental conditions Superior

completelydry No reaction possible

No reaction with dc system if properly installed

ELECTRONIC(ANALOG) CONTROLSYSTEMS 255

Table9-1. Comparisonof Pneumaticand Electronic Control Systems (continued) Feature

Pneumatic

Operationin hazardous locations(explosive atmosphere)

Completelysafe

Reactionto suddenfailure of energysupply

Ease and cost oC instalIation

Electronic

Intrinsically safe equipmentavailable-equipmentmustbe removedfor mostmaintenance Inferior-electrical failure Superior-capacity of systemprovides mar disruptplant; backup safety marginexpensive,battery backupinexpensive backupavailable Inferior Superior

System compatibility

Fair-requires considerable auxiliary equipment

Good-conditioning and auxiliary equipment morecompatible to systems

Instrumentcosts

Lower if installation costs are not considered

Higher-becomes competitive when total including installation is considered

Ease and cost oC maintenance

Fair-procedures more readily mastered by people with minimum of training Slower but adequate for most situations

Good-depends upon training and capability of personnel

approach

Dynamic response

Excellent-frequently valve becomes limiting

factor Operation in corrosive

atmospheres

Superior-air supply becomes a purge for most

instruments Measurementof allprocess A few measurements are difficult but can be made variables

Perlonnance of overall control systems Politics (the unmentioned factor that frequently pops up)

Inferior, unless special consideration is given and suitable steps taken

Excellent

available Excellent, if transmission distances are reasonable Generally regarded as acceptable but not the

Excellent-no restrictions on transmission distance Often regarded as the latest and most modem

latestthing

approach

256 PNEUMATIC AND ELECTRONICCONTROLSYSTEMS

Questions

9.1. The SPEC200 control unit (2AC + A4) hasa deviationand is in the manualposition; whenthe transferswitchis movedto automaticthe controller reactsto the deviation: 8. With an initiallarge changeand thena gradualrecovery b. Withouta bump c. At the rate at which the deviationoccurred d. At a rate determinedby the proportionalband 9.2. Performanceparametersof mosttransmittersare rated as a functionor: 8. Full-scalerange c. Span b. Upperrangelimit d. Reading 9.3. The greatestadvantageof an electricalover a pneumaticcontrol system is: a. Price c. No transmissionlag b. Safety d. Accuracy 9-4. The electronictype of controller maybe consideredto be: a. An analogof a pneumatictype b. An entirely differentconceptof control c. A more economicalway to obtainautomaticcontrol d. A moreaccuratemethodof providing control 9.5. First stageturbine pressure: a. Is linearly relatedto steamflow b. Is a measureof efficiency c. Fluctuatesonly with temperature d. Does not relateto load 9-6. Both the pneumaticand electricalsystemsusea live zero because: a. It makesit possibleto tell the differencebetweena dead instrumentand one readingzero b. Zero is the most importantpoint on the scale c. A live zerofacilitates calibration d. It is importantto havethe line energizedat all times 9-7. Whenwe adjustderivativetime in a controller: a. WedetermineanRC time constantin the controller's controlled variableinput b. We adjustthe time it will take for integralto equalderivative c. We setthe processtime constantso that it will alwaysequal I d. What happensspecificallydependson the type of controller,pneumatic or electronic 9-8. If the control valve in anelectroniccontrol systemmovesin the wrong direction, it may be easilyreversedby:

ELECTRONIC (ANALOG) CONTROL SYSTEMS

a. b. c. d.

257

Reversingthe ac line connectionsat the controller Reversingthe signalleads Changingthe reversingswitch position Adjustingthe valve

9-9. A plant is beingdesignedfor an area that hastremendoustemperature extremes.The processis spreadout and requiresthat most instrumentlines run both indoorsand outdoorsto and Cromthe controlroom. The bestchoice of instrumentationtype would be: a. Pneumatic b. Electronic c. A combinationof electronicoutsideand pneumaticinside d. A combinationof pneumaticoutsideand electronicinside 9-10. In the electronicboiler drum level systemdescribed,measurement input to the secondarycontrol unit is fed to the integralcircuit of the primary control unit. a. To lock the two control actionstogether b. Only when in manualcontrolto preventintegralwindup c. To provide bumplesstransfer d. Statementis incorrect 9-11. The 4-20mA dc output Cromthe electronicditIerentialpressure transmitteris: a. Linear with ditIerential pressure b. Linear with flow c. Unrelatedto the frequencyof oscillation d. None ofthe above 9-12. Assumethe d/p Cell signalof feedwaterflowrate measurement was acutally5 percentlow. The boiler drum: a. Would overfill b. Wouldgo dry c. Feedbacktrim would correct for the error d. Level would be correctif the steamflow was adjustedto compensate for the error 9-13. The pneumaticboiler drum level control systemshownin Figure9-11 usesa squareroot extractor on the feedwaterflow controlloop. If the signal Cromthe ditIerentialpressuretransmitterto the squareroot extractoris 9 psi (60 kPa),the output Cromthe squareroot extractorshouldbe: a. 3 psi c. 6 psi b.11.5psi d.15psi 9-14. In the SPEC200boiler drum level control systemthere is a summing unit. If two inputs A = 6 volts and B = 3 volts are applied,the output will be: a. 3 volts b. 9 volts

258 PNEUMATIC AND ELECTRONICCONTROL SYSTEMS

c. 18 volts d. A voltage between O and 10, representing the scaled value of the inputs 9-15. A boiler delivers 50,000pounds of steam per hour. The steam pressure is 750 psi (5,171 kPa) and the temperature is 5100F(266°C). The feedwater pump delivers water at 900 psi (6,206 kPa). The size of the linear globe valve controlling feedwater should be: (Hint: A pound of water makes a pound of steam.) a. 4 inches c. 1 inch b. 2 inches d. 3/4inch

SECTION

III ACTUATORS

AND VALVES

Operation of the closed-loop control system depends on the perforfiance of each loop component, including the final control element, whether it be damper, variable speed pump, motor relay, saturable reactor, or valve. Each of these elements requires an actuator that will make the necessary conversion from controller output signal to element input. This controller output mar be pneumatic or electric and in some cases hydraulic or mechanical. The first need, then, is a device, an actuator, that will convert this control signal into a force that will position the final control element. From economic and performance standpoints, the most popular final operator is the pneumatic diaphragm actuator. A typical actuator is shown in Figure 10-1.

Valve Actuator

The pneumatic signal is applied to a large flexible diaphragm backed by a rígid diaphragm plate. The force created is opposed by a coil spring with a fixed spring rate. Thus, the stem position is an equilibrium of forces thai depends on diaphragm aTea,pneumatic pressure, and spring characteristic. The spring tension is adjusted to compensate for line

Actuators

259

260

ACTUATORS AND VALVES

Fig. 10-1. Cutaway of valve actuator showing diaphragm.

pressure on the valve and to produce a full valve stroke with signal changes from bottom to top scale value. The mechanical designs employed vary from one manufacturer to another. Figure 10-1 illustrates the Foxboro Series P actuator. Pneumatic spring-diaphragm actuators bave many applications, the most common of which is the operation of a control valve. They bave been adapted to globe, Saunders-patent, butterfly, and ball valves. Spring-diaphragm actuators convert air signal pressure to force and motion and can be adapted to a large number of industrial requirements when precise loading or positioning is required. On loss of air signal, the spring will cause the actuator to retum to the zero pressure position. This feature provides fail-safe action. First, in order to provide maximum safety, the function of the valve is determined. Sècond, the action-air-to-open or air-to-close-that will allow the spring to put the valve in that position if the energy supply (air pressure) should rail is selected. The actuator shown can be reversed for either air-to-open or air-to-close action by simply removing the cap, tuming over the actuator, and replacing the cap. The motion ofthe valve stem positioned by a diaphragm actuator is Dot exactly linear for uniform changes in air pressure (pneumatic signal). The nonlinearity is caused by the diaphragm material, variations

FREQUENCYRESPONSEANALYSIS 331

pone~ntscan be added graphically to produce the gain of the entire system. This is the same as multiplying the individual gains (since both scales are based on logarithms), and the product of these gains is the gain of the entire system. Although the frequency response technique is theoretically restricted to linear systems, nonlinear systems also can be tested if the amplitude of the input signal is kept sufficiently small, and provided there are no discontinuities. Finding

the Time Constant

tram the Bade Diagram

The Bode diagram ofthe valve shown in Figure 14-3is similar to thai of a single-capacity single-resistance system. The time constant of a system is the time it takes to develop one radian (one cycle divided by 211) at the so-called corner or break frequency. Gain (G) = 1/(1 + j Cl)T);at high CI),G = l!jCl)1;'where G = 1, Cl)T= 1; T = l/CI).The corner frequency lies at the intersection of the unity-amplitude-ratio line (gain = 1, db = O)and the line which is asymptotic to the downward slope of the curve. lt is a measure of system response; the higher the break frequency, the faster the response. ln other words, as the flat (horizontal) portion of the curve extends farther to the right, higher frequency disturbances can be handled. ln Figure 14-3, the corner frequency f c is 0.2 cycle per second; therefore, the time constant is (14-1)

Testing

a System

Figure 14-4is a block diagramof a heat-exchangercontrol system. lf the transfer function of eachcomponentor block is known, actualtests are unnecessarybecausea mathematicalapproachcanbe usedto obiaio the responsecurves. ln somecases,curvesfor componentssuchas

SET

3-MOOE

CONTROL

PNEU. TUBING

(100FT.)

VALVE MOTOR FEEDBACK

HEAT

EXCH'G'R

TEMP. MEAS.

SYSTEM

LOOP

Fig. 14.4. Block diagramof beat exchangercontrol system

PNEU. TUBING

(100FT.)

332 CONTROL LOOP ADJUSTMENTAND ANALYSIS

transmitters, receivers, and valve motors are available from the instrument manufacturer or from the technical literature. An entire process and its control system can sometimes be simulated wholly on paper with no equipment necessary. If a step-response test has been performed, and the time constants determined, the frequency response curves can be constructed by using the time constants-because the response curves for a first-order system bave a characteristic shape. Since the time constant is known, the corner frequency can be calculated from Equation 14-1 and the decibel curve can be fitted to the corner frequency valve, using a slope of -6 db/octave (gain decreases by a factor of 2 as frequency increases by a factor of 2). Location of the phase curve for a single time constant system also depends on the corner frequency-this is where the 45-degree phase shift occurs. At corner frequency (CJJT = 1), G = 1/(1 + jCJJ1)= 1/(1 + n, representing a vector at an angle of 45 degrees, with length I/Y2, or 3 db down. This curve is shown at bottom in Figure 14-3. However, a frequency test must be run if response data are Dot available for all components. Although each system component could be tested individually, it is easier to group several components and test the group. For instance, the heat-exchanger, valve motor, and temperature-measuring system can be tested simultaneously to yield the frequency response curves (gain and phase) for the three compo-

nents. The test could be expanded to include the two lengths of pneumatic tubing. However, since tubing length might be changed at some later date, it is best to obtain tubing data separately. If the length does change, new response curves can be graphically added to the curves for the other components. Once the response data bave been gathered, the gaiG and phase curves are plotted (Figures 14-5 and 14-6). In the beat exchanger example, it will be assumed that the steadystate gaiG of each component, and thus the entire process, is unity. In Figure 14-5, the gaiG curve for the three components (heat exchanger, valve, and temperature-measuring system) is added to the curve for the pneumatic tubing to produce the curve for thc entire processo Since there are two 100-foot lengths of tubing, the tubing curve is added twice. (For simplification, this curve is an average of two curves, one for a pneumatic line terminating in a valve motor and the other for a line terminating at the controller.) Measurements are made from the zero-db line, and points on the same side of the line are additive. A controller has a response curve for each combination of control-

FREQUENCYRESPONSEANALYSIS 333

Fig. 14.5. Gaincurves.

ler settings. However, this family of curves can be simplified into a single curve for each control mode because the integral action affects the low-frequency response, the derivative action affects the highfrequency response, and the proportional action is simply a horizontal line. A set of the simplified curves is shown in Figure 14-7. All curves are shifted up or down as the proportional band is changed; the integral line is shifted to the left as the integral time is increased, and the derivative curves also are shifted to the left as the rate action is in-

creased. For continuous cycling to occur, the system must simultaneously bave a gain equal to or greater than zero db (gain ofunity or more) at a

Fig. 14-6. Phasecurves.

334 CONTROL LOOP ADIUSTMENT AND ANALYSIS

d ~ +10'

r INTEGRAL

CORNERFREQ.AT +3DB'

PROPORTIONAL BAND

FREQ.AT +3DB

+50-

~ ~ c

--I

--BAND

-' I-

INTEGRAL

~ -501

DERIVATIVE

""~

/-PRDPDRTIONAL

-- -- ---

DERIVATIVE '",

~ -1001

LOG FREQUENCY

Fig. 14.7. Simplifiedcontrol-moderesponsecurves.

phase shift of -180 degrees. The proportional band that results in a gain of unity at this -180-degree point is called the ultimate proportional band. The ultimate proportional band is the one which, when added to the process curve, produces a gain of unity at the critical -180-degree phase point. In Figure 14-6, the -180 degree phase shift occurs at a frequency of 1.4 cpm. At this frequency, the gain is -11 db, or an amplitude ratio of 0.28. To raise the process curve to zero db at 1.4cpm, the proportional band (PB) curve would be a horizontalline at + 11 db or 3.55 amplitude ratio. Since PB is (l/amplitude ratio) x 100, the ultimate proportional band (PBJ is, therefore, --u = 3.55 x 100 = 28% PR.. ~ A second factor of interest, calledfrequency ratio, is a measure of the system response beyond the -180-degree phase point. The ratio of the frequency at -270-degree phase change to the frequency at -1800 phase change gives this. For the beat exchanger, this ratio (fr) is 2.8 cpm/l.4 cpm, or 2.0.

FREQUENCYRESPONSEANALYSIS 335

Dead time is another factor to consider. Dead time increases phase lag without affecting the gain curve. If the total dead time for the system is greater than about 0.1 of the largest system time constant, there will tend to be overshoot with three-mode control. The PB u tells much about the processo A rough estimate of offset (with straight proportional action) is PBu/2. In the beat exchanger this would mean an offset of approximately 28/2, or 14percent. Therefore, ifthe span ofthe temperature measuring instrument were 100degrees, offset would be in the neighborhood of 14 degrees. If this amount of offset proved to be troublesome, the integral mode should be considered, keeping in mind that the addition of integral action can cause overshoot on startup. Another rough indicator can be used to point out the necessity for derivative action. Itthe 270 degree/180 degree frequency ratio (f r) is two or greater, derivative can be used to advantage. Derivative action raises the high-frequency end of the process curve to increase the -180-degree frequency. For the beat exchanger, all three control modes were selected.

Control

Objectives

Since cycling occurs when a process plus its control has a gain of one or greater at the same time that its phase is -180 degrees, the major control objective is to separate this phase and gain by as large a frequency spread as practical. To ensure this spread, two quantities are defined-gain margin and phase margin (Figure 14-8). Gain margin is the amo unt that the gain curve differs from unity (O db) at the -180degree frequency. Phase margin is the amo unt by which the phase curve differs from -180 degrees at the O-dbfrequency. When one of the margins is set at a desired value, the other margin is fixed. Widening either the phase or gain margin reduces the settlingout time (after a change in set point) until, in the ultimate, all overshoot is eliminated. In general, the gain margin does Dot fall below -5 db nor exceed + 10 db. When the phase margin is used as the controlling factor, it usually lies between 40 degrees and 60 degrees, with 50 degrees as a good compromise. Control mode curves must be added in sequence-derivative first, followed by integral and proportional band. The proportional band must be added last because it adjusts the process gain without affecting the phase; the other modes affect both gain and phase simultaneously.

336 CONTROL LOOP ADIUSTMENT AND ANALYSIS

LOG FREOUENCY--

Fig. 14-8. Gainand phasemargindescribedgraphically.

Adding

Derivative

Although place ment of the derivative curve is somewhat arbitrary, one successful method is to align the + 50-degree point of the derivative curve with the -180-degree point of the process curve (Figure 14-9). When these two curves are added graphically, the -180-degree fre-.

Fig. 14-9. Phase curve oCprocess plus derivative.

FREQUENCYRESPONSEANALYSIS 337

quency shifts to the right. The position of the derivative phase curve determines the position of the derivative gain curve. Adding the derivative gain curve to the process curve (Figure 14-10)raises the process gain curve. At the new -180-degree frequency of 2.2 cpm, the gain of process plus derivative becomes -11 db. The derivative time is also a function ofthe corner frequency ofthe derivative gain curve; it is the frequency at which the gain of the curve is + 3 db.

derivative time =

217"x derivative-curve corner frequency

From Figure 12-10,the corner frequencyis 1.1 cpm; therefore, derivative

Adding

time

~ ~ 1 1 = 0.142 minute 21T X

Integral

The next control mode to be added to the process-plus-derivative curve is the integral (Figure 14-11). Here the -IO-degree point ofthe integral

Fig. 14-10. Gain oCprocess plus derivative.

338

CONTROL LOOP ADJUSTMENT AND ANALYSIS

Fig. 14.11. Phase oCprocess plus derivative plus integral showing phase margino

curve is aligned with the -170 degree point of the process-plusderivative curve. This shifts the -180 degree slightly left to a frequency of 2.0 cpm. In general, adding integral lowers the total phase curve since the integral phase curve lies entirely below zero. Adding the integral gain to the process-plus-derivative curve (Figure 14-12) raises the low-frequency response. Note that the highfrequency end of the curve does Dot change.

Fig. 14-12. Gainor processplus derivativeplus integral.

21T

FREQUENCYRESPONSEANALYSIS 339

integraltime =

x integral-curve corner frequency

The corner frequencybefe is also at the 3-dbpoint and is equalto 0.26 cpm. Therefore, integral time =

21T x 0.26

= 0.615minute/repeat

If the controller is calibrated in repeats per minute, the reciproca} of this number is used. Adjusting the Proportional Band Adjusting the proportional band moves the gain curve vertically but has no effect on phase. From Figure 14-11,the -180-degree frequency of process-plus-derivative-plus-integral curve is 2.0 cpm. From Figure 14-12, the gain of process plus two control modes (corresponding to 2.0 cpm) is -10 db, or the gain margin without proportional band is 10db. To obtain a gain margin of 5 db, the curve can be raised 5 db. This is accomplished by adding a proportional band of + 5 db to the process-plus-derivative-plus-integral curve. Since + 5 db = 1.78 amplitude ratio,

The final gain curve is shown in Figure 14-13. The phase margin is íound by first noting the írequency oí the gain curve oí the process plus the three control modes at O-dbgain. From Figure 14-13 this is 1.0 cpm. Since at 1.0 cpm the phase is -125degrees, the phase margin (Figure 14-11)is 55 degrees (180 degrees -125 degrees). The curve oí process plus derivative plus integral (PB = O) in Figure 14-11, and the gain curve oí the process plus all three control modes in Figure 14-13,are the open-loop response curves oí the process plus its control.

Closed-Loop

Response

Using data from the open-loop response curves, closed-loop response can be found from a NichoLs diagram. The Nichols diagram, or phase

340 CONTROL LOOP ADJUSTMENTAND ANALYSIS

Fig. 14-13. Gain of process plus all three control modes. A controlling gain margin of 5 db determines the value ofthe proportional band.

marginplot, mar be usedto define systemperformance.It is a plot of magnitudeversusphase.The magnitudeis plotted vertically, and the phaseis plotted horizontally. For a more detaileddescription, refer to an advancedtext on frequencyresponsetechniques.Closed-loopresponseis automaticcontrol; manual control is openloop. If the openand closed-loopresponsesare plotted on a singleBode dlagram,much interestinginformationcanbe obtained.For instance,a plot of the ratio of closed-loopto open-loopmagnituderatios revealsthe effectiveness of the controller in handlingvarious disturbancefrequencies.AIso, if the processplus its control resemblesthat of a second-ordersystem (this is valid in manycases),suchquantitiesasthe naturalfrequencyof the system, dampingfactor, and settlingtime can be estimated.AIso calculableis the peak deviation arter a set-pointchange. Conclusion The frequencyresponsemethodis botha testanda graphicaltechnique to obtain informationaboutthe controlloop. The instrumentmanufacturer can put thesetests to goodadvantagein evaluatinginstruments. However, few plants would allow the processdisruptionscaused.by frequency response testing. Perhaps the greatest benefits are the

FREQUENCYRESPONSEANALYSIS 341

graphical solutions of rather. complex problems and the simultaneous understanding of the system that is developed.

Questions

14-1. The frequencyresponsetechniqueis theoreticallyrestrictedto: 8. Nonlinearsystems c. Closed-loopsystems b. Resonantsystems d. Linear systems 14-2. The frequencyresponseanalysistechniqueis: a. A test that canbe quickly conductedwithout specialequipment b. A test that does not upsetthe processin any way c. A test that will revealcontrollersettings.processtime constants,etc. d. Not suitablefor large-capacitysystems 14-3. The first-ordertime constantor singletime constantoccurs at a phase shift or: a. 90.0degrees c.45.0degrees b. 63.2degrees d. 36.8degrees 14-4. In constructinga Bode diagramon linear graphpaperthe gain (vertical)axis shouldbe expressedin terms or: a. Decibels c. Linear gain b. Gainratio d. Maximumgain 14-5. In usingthe frequencyresponsemethodas a graphicalanalysis technique,the only componentthat usuallyrequiresactualtestingis the: a. Controller c. Closed-loopcombination b. Process d. Control valve operator 14-6. The frequencyresponseof a three-.mode controller: a. Displaysthe quality of the controller b. Variesaccordingto the manufacturer c. Canbe manipulatedto a desiredcurve shapethroughmode adjustment d. Is fixed and alwaysremainsrígid 14-7. The frequencyresponsegaincurve is nat affectedby: a. Proportionalband c. Integral b. Deadtime d. Derivative 14-8. Whencontrol modecurvesare added,the following order mustbe observed: a. Proportional,integral,and derivative b. Derivative, proportional,and integral c. Integral, proportional,and derivative d. Derivative, integral,and proportional

342 CONTROL LOOP ADJUSTMENTAND ANALYSIS

14-9. Whenthe frequencyresponsecurvesof allloop componentsare added,the resultantcurve becomes: 8. The closed-loopcurve b. Useful in that the Nichols diagramwill then reveal closed-loop response c. InterestingCroman academicstandpointonly d. A measureof controllereffectiveness 14-10.Perhapsthe greatestbenefitof the frequencyresponsetechniqueis that it: 8. Providesa methodof controller adjustment b. Makes it possibleto predict stability c. Providesa methodof measuringtime constants d. Providesthe studentof automaticcontrol with a clearerinsightas to what occurs within the controlloop

SECTION

V COMBINATION

CONTROL

SYSTEMS

Although conventional controllers satisfy most process control requirements, improvements can be achieved in some situations by combining automatic controllers (duplex, cascade, ratio). All of the combination controller actions to be described can be achieved with either pneumatic or electronic equipment.

Duplex

or Split-Range

Control

A duplex controller has one input and two outputs. It mar bave two control mechanisms, each with an output, or a single-control mechanism operating two control valves by m.eansof relays or positioners. The need for such a system is apparent in a process such as electroplating. For example, the quality of bright chromium plating depends largely on proper temperature control ofthe bath. With a given current density and bath composition, variations in temperature Dot only affect the final appearance, but also the rate of chromium deposi-

tion. Temperaturesa few degreestoo high producedull, lusterlessplating. When tools are being plated with a bard chromium finish, low 343

344 COMBINATIONCONTROLSYSTEMS

temperatures can cause hydrogen embrittlement of the steel, resulting in cracking and tool failure. Desired thicknesses and tinishes can only be produced on successive jobs if the operating conditions are duplicated exactly (Figure 15-1). Plating current ftowing through the electrolyte generales beat that is normally dissipated by a controlled ftow of cooling water through the tank coils. Frequently, however, when large, cold metal pieces are introduced, the solution becomes too cool for good plating. AIso, on startup, the temperature must be brought up to the operating level or the initial batch will be below specitications. The problem is solved by a duplex controller that adds cooling water when the temperature is too high, and steam to the heating coils when the temperature is too low. If the temperature is within acceptable limits, neither cooling water nor steam is admitted. The control action is pneumatically produced by a conventional controller with proportional action (left in Figure 15-1). Controller output is simultaneously fed to (1) the receiver bellows in a val ve positioner, located on the water (cooling) valve, and (2) a similar bellows in a second positioner located on the steam (heating) valve. If the controller proportional band is adjusted to 10 percent, the response will be as shown in Figure 15-2. The positioner on the steam valve is adjusted to stroke the valve through its full travel when the air signal on the valve positioner receiver bellows goes from 3 to 9 psi (20 to 60kPa); the valve is closed with 9 psi (60 kPa) applied to the positioner and wide open with 3 psi (20 kPa) applied. The positioner on the water valve is adjusted to operate in the opposite direction; it opens the valve fully with

Fig. 15.1. Platingprocessrequiresa duplexcontrol1er.one with one input but two outputs.

SPLIT-RANGE,"~UTO-SELECTOR. RATIO. AND CASCADESYSTEMS 345

Fig. 15-2. Response ofproportional controller with a proportional band setting of 10 percent.

15 psi (100 kPa) applied and closes it when the signal pressure is 9 psi (20 kPa). A properly aligned pneumatic proportional controller produces an output of 9 psi (60 kPa) when meas9rement and set point agree. In this example, both valves would beclosed with a signal pressure of9 psi (60 kPa). If measured temperature rises above, or falls below, the set point, water or steam would be circulated in proportion to the measurement's deviation from the set point. Integral and derivative action could be incorporated in the electroplating control system. However, neither one is required normally because a system of this type usually is required to control only within a narrQWband of temperature (say 10 percent band) between heating and cooling. Thus, integral and derivative modes are unnecessary. On/off control sometimes proves to be the most economical and satisfactory solution to the same problem-provided the process can tolerate the cyclic operation that will occur.

Auto-Selector

or Cutback

Control

Auto-selector control is the opposite of duplex in that it allows the automatic selection between two or more measurement inputs and provides a single output to control a single valve. The auto-selector-

346 COMBINAllON CONTROL SYSTEMS

Fig. 15-3. Pipelineoperatessafelyon auto-select/cutback control.

control system continuously senses all measurements applied to it and provides control action to the valve based on the value of the measurement closest to its particular set point. All measurements musi be interdependent, thai is, directly related to each other, for successful auto-selector application. While control mar be either pneumatic or electronic, the electronic type is ideal for tbis technique. A simple selector system, often found in pipeline control, will be used as an illustration (Figure 15-3). In attempting to operate a pumping station efficiently on a pipeline, it is desirable to operate the control valve wide open at all stations except one. One station will then become the limiting or throttling unit and will pace the line based on the delivery requirements. However, if any of the following conditions occur, it is necessary to cut back on the position of the control valve:

SPLIT-RANGE,AUTO-SELECTOR,RATIO, AND CASCADESYSTEMS 347

1. Suction pressure draps too low. 2. Motor load rises too high. 3. Discharge pressure rises too high. If the suction pressure drops below a predetermined level, there is danger of causing the pump to cavitate. If motor load rises above a predetermined level, there is danger of overloading the motor and burning it auto If discharge pressure rises too high, there is danger of causing problems downstream. Cutting back on the position of the final operator will cause each of these variables to return to a safe operating

level. Consider the operating parameters in the following example for a pumping station: 1. All variables are on the "safe" gide oftheir respective set points. Suction is sufficiently high; motor load and discharge pressure are sufficiently low. 2. A decreasing suction pressure will cause the output of the suctionpressure controller to decrease. 3. An increasing motor load will cause the output of the motor-load

controllerto decrease. 4. An increasing discharge pressure will cause the output of the discharge-pressure controller to decrease. 5. A low-signal selector is used. Its output will be equal to the lowest input. 6. A decreasing input to the low-signal selector will cause its output

to decrease. 7. The control valve opens as its input increases (air-to-open). Since all variables are operating in their "safe" zones, all controllers will have a maximum output, that is, 100percent, and the control valve will be wide open. Assume that the suction pressure drops below the predetermined low limit, as will be indicated on the suction-pressure controller's setpaint dial. Output of the suction-pressure controller will start to decrease. This decreasing output will be selected by the low-signal selector and transmitted to the control valve. The control valve will close until the suction pressure is brought equal to the preset limito Assume this condition is met with a 50 percent valve position. If all of the controllers in a cutback system contain proportionalplus-integral action, integral windup should be anticipated. In order to prevent this condition, a special type of "external feedback" is employed. The selected output is fed back to each controller's integral circuit. This feedback (rather than conventional feedback, where a con-

348 COMBINATIONCONTROL SYSTEMS

troller's output is fed to its own integral circuit) conditions all of the controllers whose outputs are Dot being selected. Assume one of the other variables, for example motor load, approaches its limito As soon as the load exceeds the limit, the output of the motor-load controller will begin immediately to decrease from 50 percent (the output of the low selector) and Dot from 100 percent as would be the case if externat feedback had Dot been provided. If the control valve must start to move before the motor load reaches the límit, a batch-cutback (auto-selector) controller should be used. A slow, ramping-open of the control valve is a common requirement in starting up a pumping-station pipeline-control system. A ramp generator providing a constantly increasing signal (commencing on operator command) will smoothly open the valve at a controlled rate. This generator simply becomes another input to the low-signal selector. Provisions for switching the entire system to the manual mode of control are normally incorporated into the system as an integral part of the signat selector, or sometimes as a separate unit. If an air-to-close valve is required, a high-signal selector should be specified. The switch on each controller that determines whether an increasing measurement will cause an increasing or decreasing output should be changed to the action opposite to that used in the preceding example. Nonpipeline

Application

ot Auto-Select/Cutback

Control

Systems

A nonpipeline application of a cutback system is shown in Figure 15-4. In this system, the outlet temperature of the product is sacrificed if the oil pressure drops below a preset low límit. In normal operation, the temperature controller will regulate the oil pressure, and thus the beat input, in order to maintain the product temperature at the desired controllevel. If the demand for oil by the exchanger should start to diminish the main oil supply (indicated by a falling oil-header pressure), the oilpressure controller will cut back the control valve, reducing the product temperature and, at the same time, the consumption of oil. The header pressure will now be allowed to reco ver and remain at the predetermined low límit. Should other process demands for oil be reduced, the oil-pressure controller will gradually open the oil valve until complete control is returned to the temperature controller. The one major requirement for auto-selector application is that all of the measured variables must be interdependent, that is, regulated by the single manipulated variable.

SPLIT-RANGE,AUTO-SELECTOR,RATIO, AND CASCADESYSTEMS 349

Fig. 15-4. Temperatureadjuststo reduceoil pressure.

Flow-RatioControl Assume a fixed ratio between two flow rates is to be controlled. This would suggesta flow-ratio control. Acid-to-water ratio for a continuous pickling process found in certain planis working on metal would be typical. An acid-water-ratio control system for continous pickling automatically controls the addition of fresh acid in correct proportion to the water used. The accurate flow control and proportioning ofthe acid results in a stricter adherence to pickling specifications, and, therefore, a minimum consumption of acido The system records and integrates the cons umption of both water and acido Control of solution level by the operator is also simplified since he need adjust only the water valve. An installation is schematically shown in Figure 15-5. Normally, variation of the flow of water, either to fill the pickling tank or maintain the operating solution level, is accomplished by pneumatically positioning a control valve in the water line by means of a pneumatic manual setting station. This is a typical ratio control system; however, it does bave a limitation. It is assumed thai the instrument components are selectedsized to provide the desired ratio of acid to water, and thai ibis ratio

350 COMBINAllON CONTROL SYSTEMS

will never need to change. Unfortunately, this is seldom the case, making a method of ratio adjustment necessary. The ratio factor is set by a ratio relay or multiplying unit. This unit would be located between the wild ftow transmitter and the ftowcontroller set point (Figure 15-5). It is desired to control Flow B in a preset rati o to Flow A. Flow transmitter A sensesthe wild ftow. The

(o)

RATIO

RELAY

Ib) RATIO CONTROLLER

SPLIT-RANGE,AUTO-SELECTOR,RATIO, AND CASCADESYSTEMS 351

~~J

(8)

RATIO

CONTROLLER

Fig. 15-5. (continued)

ratio relay multiplies the output (Oto 100 percent) of the flow transmitter by a manually set factor: (Flow output A) x (Preset factor) = Output of ratio relay

This output becomesthe set point of the controller that regulates Flow B. At equilibrium, Flow B equalsthe set point of the controller, or: Flow B = (Flow A) x (Ratio factor) Ratio factor = Flow B/Flow A The following example mar help in understanding a ratio-control system. Assume that the range of Flow A is Oto 100gpm, the range of Flow B is Oto 100; the output oftransmitters A and B changes linearly from O to 100 percent as the ftow changes from O to 100percent. The ratio Telar has a factor adjustment ranging from 0.3: 1 to 3: 1. If the ratio factor is set at 1 (meaning al: 1 ratio), for every mea-

352 COMBINATIONCONTROLSYSTEMS

sured gallon of A, the controller will allow 1 gallon of B to flow. If 50 gpm of A flow, then 50 gpm orB will flow. Ifthe ratio factorchanp,esto 2, then 2 gallons of B will flow for every gallon of A. If 50 gpm of A flow, 100 gpm of B will flow. If the range of flow transmitter B is changed to range from O to 10 gpm, while A remains Oto 100gpm, al: 10ratio factor is built into the system. In other words, if the factor set on the ratio relay is 1, then for every gallon of A that flows, 0.1 gallon of B will flow. Hence, the range of the transmitters, as well as the multiplying factor set into the ratio relay, determines the ratio factor for the system. Therefore, c~re should be taken in selecting transmitter range in order to allow ri1a:x:imum system flexibility. Try to choose a range so that the ratio factor is normally in the middle. However, make sure that the transmitter range will cover all process conditions. Flowmeters used in a ratio control system are often orifice metecs or other constriction metecs with differential-pressure transmitters. Thus, transmitter output is proportional to the square of flow, rather than being proportional to a linear relationship as in the above example. (The transmitters in the example cQuld bè magnetic flowmeters, turbine flowmeters, rotameters, and so on.) In this case, the ratio relay provides the same 0.3: 1 to 3.0: 1 ratios between transmitter outputs, that is betweendifferential pressures. Since flow is proportional to the square root of differential pressure, the actual flow ratios will be (0.3: 1)1/2to (3.0: 1)1/2,or about 0.6: 1 to 1.7: 1. The ratio dial will bave a square root layout and indicate flow ratios of 0.6: 1 to 1.7: 1. This rati o range is the square root of the gain range. A transmitter with a linear output cannot be used with another having a square root output unless one or the other output is passed through a converter to obtain its square or square root, as required. More complicated systems may involve ratioing two or more flows to the wild flow. A ratio control system may be implemented in several different ways with pneumatic or electronic hardware. The ratio delay may be incorporated in the controller, and a ratio dial replaces the normal set-point dial. This is normally called a single-station ratio controller (Figure 15-5).

Cascade

Controller

A cascade-control system consists of one controller (primary, or master) controlling the variable that is to be kept at a constant value, and a

SPLIT-RANGE, AUTO-SELECTOR, RATIO, AND CASCADE SYSTEMS

353

second controller (the secondary, or siave) controlling another variable that can cause ftuctuations in the first variable. The primary controller positions the set point of the secondary, and it, in turo, manipulates the control valve. The objective of the cascade-control system is the same as that of any single-loop controller. Its function is sirrply to achieve a balance between supply and demand and thereby maintain the controlled variable at its required constant value. However, the secondary loop is introduced to reduce lags, thus stabilizing inftow to make the whole operation more accurate. The cascade-control technique is shown in schematic form in Figure 15-6. Two feedback controllers are used but only one process variable (m) is manipulated. The primary controller maintains the primary variable (C J at its set point (rJ by automatically adjusting (r2)the set point ofthe secondary controller. The secondary controller controls the secondary loop responding to both its set point (r 2)and the secondary measurement (C2). The secondary controller mar be regarded as an elaborate final control element, positioned by the primary controller in the same way as a single controller would ordinarily position the control valve. The secondary variable is Dotcontrolled in the same senseas the primary; it is manipulated just like any control medium. If, for example, the secondary controller is a ftow controller, then the primary controller will Dot be dictating a valve position, but will, instead, be dictating the prescribed ftow. A simple, single-loop temperature-control system is shown in Figure 15-7, wherein the temperature of the liquid in the vessel is controlled by regulating the steam pressure in the jacket around the vessel. Since such a process normally involves a longtime constant, a threemode controller having a long integral time is required. This will provide satisfactory control as long as the supply of steam is constant, that is, the upstream pressure does not change.

Fig. 15-6. Cascadecontroltechnique.

354 COMBINAnON CONTROL SYSTEMS

Fig. 15.7. Temperaturecontrollerprovides set paint for stearnvalve or stearn-pressure controller.

However, if the supply steam is subject to upsets, a different control scheme is needed. The temperature controller will Dot know that the beat input (steam pressure) has changed until the temperature ofthe liquid in the vessel starts to change. Since the time constant of the temperature loop is long, the temperature controller will take a long time to return the process to an equilibrium (a new steam-valve position corresponding to the new level of beat input). Therefore, it is desirable to correct for the change in beat input before it affects the temperature of the liquido The cascade control system shown in Figure 15-7 will both control the temperature in the vessel and correct for changes in the supply steam pressure. The steam-pressurecontroller, called the secondary or slave controller, monitors the jacket inlet steam pressure. Any changes in supplypressure will be quickly corrected for by readjusting the valve because this loop has a fast time constant, and, hence, a short integral time. The temperature controller, normally called the primary or master controller, adjusts the set point of the pressure controller as dictated by the beat requirements of the incoming reed. Thus, the secondary controller has its set point set by another controller rather than by a manually adjusted dial. These secondary devices are termed remote-set

controllers. For the cascade control system in the above example, the time constant of the secondary controlloop must be significantly faster than that ofthe primary loop. Ifthe time constant ofthe secondary loop is too

SPLlT-RANGE, AUTO-SELECTOR, RATIO, AND CASCADE SYSTEMS

355

long-equal to or even greater than the primary loop-cascade control will provide no benefits. It may, in fact, cause stability problems. An example of this occurs when a valve positioner, described in Chapter 10, is used for ftow control. The ftow process is faster than the valve positioner and this produces a continuous cycle. Stating it another way, the slave controller will Dot accept orders from the master controller faster than it can carry them out. Typical secondary loops or inner loops and primary loops mar be generally classified as follows: Types01 Inner Loops

Set By Anything bot ftow

Valve position Flow Temperature

Anything Temperature (with longer time constant)

Inner (Secondary)Loops

Control Modes

Valve position Flow

Proportional only Proportional plus integral

Temperature

Proportional only

Mathematically, it could be demonstrated that a cascade system wiU increase the natural frequency and reduce the magnitude of some of the time constants in the system, both beneficial results. However, the more evident benefits are reduced effect from disturbances, more exact adjustment in the presence of disturbances, and the possibility of incorporating high and low limits into the secondary control. Saturation in Cascaded Loops Integral windup or saturation, mentioned in Chapter 11, can become a problem in cascade control. Assume, for example, the process load demands more than the control valve can deliver. This would result in a sustained deviation of the secondary measurement from its set point. The primary measurement will then change and result in a change of the primary controller' s output. This will readjust the set point of the secondary controller. In practice we do Dot want the primary controller to change its output. A simple way to accomplish this in a pneumatic system is to use the secondary measurement as the integral to the primary controller

356 COMBINATIONCONTROL SYSTEMS

(Figure 1.5-8).In a conventional controller, as in Chapter 1.1.,the integral input is the output. In the cascade system this is the secondary set point. As long as the secondary measurement and set point are equal, integral actionofthe primary controller proceeds in normal.fashiOD. If the secondary measurement can DOtfollow its set point, integral action in the primary controller will stop. It will resume only when the secondary measurementonce again can follow set point. To accomplish this, both primary and secondary controllers must bave integral action and the primary controller must be equipped with an external integral connection. This arrange ment also simpl.ifies transfer Crom automatic to manual. With conventional integral action, the primary controller would saturate if the secondary were placed in the manual position. With the arrange ment described, this cannot happen as the primary controller's integral bellows will track the process (secondary) mea-

surement. In the electronic system (SPEC 200), a similar arrangement mar be employed to prevent saturation ofthe primary controller. Just as in the pneumatic system described, secondary measurement is used as the integral input to the primary controller resulting in operation similar to the pneumatic system.

Fig. 15-8. Prirnary and secondary controllel

SPLIT-RANGE,AUTO-SELECTOR,RATIO, AND CASCADESYSTEMS 357

Logical use of cascadecontrol systemsrequiresnothingmore than standardcontrolinstruments.A standardunit canprovide indicationor recordingand control of both the primary andthe secondaryvariables, plus output indicationand manual-automatictransfer. That is all that is neededfor normal operation. To tune a cascade-controlsystem,the following procedureis suggested: 1. Place both controllers in manual. 2. Adjust proportional and integral settings to conservativevalues (wide proportional band and long integral time) on the secondary controller. 3. Placesecondarycontroller in automaticand thentune, usingany of the proceduresoutlined in Chapter12. 4. Adjust the proportional, integral, and derivative settings on the primary controller to conservativestartingvalues. 5. Placethe primary controller in automaticand thentune, using any of the proceduresin Chapter12. Always tune the secondarycontroller first (with the primary controller in manual),and then the primary controller. Summarizingthe major advantagesof cascadecontrol: 1. Disturbancesaffecting the secondaryloop are corrected by the secondarycontroller before they are sensedin the primary loop. 2. Closingthe secondaryloop reducesthe lags sensedby the primary controller, thus increasingthe speedof response.

Questions

15-1. A duplex controllerhasthe following numberof inputs: a. Gne c. Gne for eachoutput b. Two d. As manyas required 15-2. The duplex controllerprovidesthe following numberof control valve signals: a. Gne c. Gne for eachinput b. Two d. As manyas required 15-3. An auto-selectorcontrol systemshouldbe consideredwhen: a. The processhas more controlledvariablesthan manipulatedvariables b. The processhasmore manipulatedvariablesthancontrolledvariables c. Two independentcontrol systemsare Doteconomical d. Two or more measuredvariablesmustbe isolated

358 COMBINAnONCONTROL SYSTEMS

15-4. The auto-selectorcontroller will function only whenthe measurement inputs are: 8. Interdependent c. Isolatedfrom one another b. Independent d. Flow measurements IS-S. The ratio controller: 8. Canbe usedwith any combinationof relatedprocessvariables b. Has one measurement input and two outputs c. Canbe used for even-numbered ratios d. Must always employthe derivativemode in the controller 15-6. Two ftows are to be ratio controlled,the first is measuredwith an orifice and the secondwith a sheddingvortex ftowmeter.The signalsmustbe: 8. Both madelinear by usinga squareroot extractoron the orifice signal b. U sedas if a 1 percenterror canbe tolerated c. Both madelinear by usinga squareroot extractor on the shedding vortex transmitter d. Flow-calibrated 15-7. A cascadecontrol systemwill increasethe naturalfrequencyofthe controlloop alongwith havingthe following inftuenceon the magnitudesof the associatedtime constants: 8. Reducethem c. Not affectthem b. Increasethem d. Have an unpredictableeffect 15-8. In a cascadecontrol systemthe secondarymaybe regardedas: 8. A valve actuator b. An elabomtefinal control element c. A meansof slowing down regulationof the manipulatedvariable d. A sophisticatednoisefilter 15-9. If two squareroot ftow signalsareto be mtio-controlledand the ratio factor adjusted,the maximumpracticalfactor is: 8. 0.6 to 1.7 c. 1.0to 10 b.0.3t03.0 d.l.0tol.0 lS-lO. A very commonsecondaryloop that maybe usedwith almostany processexceptftow is: 8. Flow c. Pressure b. Temperature d. Valve position IS-Il. A cascadecontrol systemis to be adjusted.You shouldfirst: 8. Placethe primary controller on manualand adjustthe secondary controller b. Placethe secondarycontroller on manualand adjustthe primary controller c. Place both controllers on automatic and go through the conventional adjustment routine '

SPLIT-RANGE.AUTO-SELECTOR.RATIO. AND CASCADESYSTEMS 359

d. Bypass the secondary controller and adjust the primary controller by the conventional method 15-12. If the time constant of the secondary loop is greater than the time constant of the primary loop, cascade control will: 8. Shorten the period of the total system b. Lengthen the period of the total system c. Improve the operation of the system d. Provide no benefits

Feedforward Control Definition

The term feedforward control applies to a system in which a balance between supply and demand is achieved by measuring both demand potential and demand load and using this information to govern supply. History

The first feedforward control system was used in abolli 1925to control boiler drum level. In ibis type of feedforward control, which is described in Chapter 9, water iriflow is directly regulated by steam outflow. Feedback iri the form of bias, or trim, corrects for any cumulative measurement or other error in the system. This system, which is still in everyday use, met an urgent need for better level control. It was applied to a process thai was completely understood and required no special iristrumentation. Many years passed before feedforward techniques were applied to other process applications. Advantages

The potential applications of feedforward techniques are virtually endless, but they usually involve a distillation processo Severa! improve360

FEEDFORWARDCONTROL 371

Ouestions

16-1. The feedbackcontrol system: a. Cannotmakecorrectionsuntil a measurableerror exists b. Makesa changein output which is the ditferentiatederror c. Is always superiorto a feedforwardsystemin operation d. Is theoreticallycapableof perfectcontrol 16-2. The feedforwardcontrol system: a. Cannotmakecorrectionsuntil a measurableerror exists b. Makesa changein output that is the integratederror c. Requireslittle knowledgeof the processbefore installation d. Is theoreticallycapableof perfectcontrol 16-3. The original boiler drum level applicationof feedforwardcontrol, developedin 1925: a. Is still being applied every dar b. Wasabandonedbecauseof poor measuringtechniques c. Worked well only with the particular boiler for which it was originally designed d. Was immediatelyrecognizedas the ultimate control system 16-4. A properlydesignedfeedforwardcontrol system: a. Shouldbe appliedto everyprocess b. Shouldbe employedwhenits use canbejustified economicallyand technologically c. Is always easierto adjustthana feedbacksystem d. Will always result in more economicalprocessoperation 16-5. The mostdramatic applicationof feedforwardtechniqueshasoccurred in their applicationto: a. Heat exchangers c. Flow processes b. Level processes d. Distillation columns

SECTION

VI PROCESS COMPUTERS

AND SIMULATION

Computer Interface and Hardware

For many years the slide rule, an analogdevice, was a universally popular and usefulcalculator. ln recentyears,the slide rule has been replaced by the pocket calculator, or electronic slide rule-a digital device. The advantagesof the calculatorare obvious. Similar advantages,proportionalto the requiredinvestment,are possiblefrom properly applied digital control systems. A digital computer cannot reasonfor itself. Therefore, it must be provided with all the relevantdata and told exactly how to solve the problem.This is calledthe program,or "software." Essentialto a basic understandingof softwareand its operationis the identificationof its functionalcomponents-the hardware.This chapterwill be devotedto a discussionof hardware. Basic Elements

ot the Computer

Computers are designed to perform the particular varied tasks assigned to them. For example, a computer designed for machine control would Dot make a very good filing system. Nevertheless, there are several basic elements common to all computers. These elements are shown in Figure 17-1. 372

COMPUTERINTERFACEAND HARDWARE 373

Fig. 17-1. Computerelements. Input

In its simplest form, the input system translates the input information prepared by people into a form to which the machine can respond. Generally, the source of computer input information includes punched cards, punched or magnetic tape, or a special typewriter. The input system converts information into a series of signals. Each signal is merely the presence or absence of a voltage or electrical current. A signal is either there or it is Dot there at any particular time. Just as the 26 symbols of the Engiish alphabet can be combined into many different words to convey information, so can the two symbols of the computer alphabet (signal and no signal) be combined to form words, phrases, and sentences in computer language. When the information Ïs put into this form, the computer is able to work with the information and process it through a series of logical operations. The input information, now in the form of signals, is next sent to the computer memory. Central Processing Unit (CPU) The combination of the working memory, control, and arithmetic elements IS often called the CPU. The CPU has a bus for transmitting and receiving signats, and the controllers, or modules, which are tied directly to thai bus. At the "head" ofthe bus is the central processor, which decodes and executes instructions, a series of which are stored in memory as programs. The central processor controls the activity of its bus, performs the computations with the data it obtains from various devices connected to its bus, and stores the results of these computations in its memory, alternatively transmitting them to the appropriate bulk storage device or controller.

Memory

This element stores information until it is needed. Just as people store in their memories multiplication tables, phone numbers, addresses,

374 PROCESSCOMPUTERSAND SIMULATION

schedules of what they pIan to do, the computer memory stores information for future reference. The memory element is passive in that it merely receives data, stores them, and gives them up on demando Devices used as memory elements include magnetic cores, magnetic drums, tape recorders, disks, and solid-state devices. Control The next element, the control unit, is active. It selects information Crom the memory in the proper sequence and sends the information to other elements to be used. In addition, the control unit convers commands so that the next element down the line will perform the proper operations on the information when it arrives. Thus, the control element makes decisions. Arithmetic The arithmetic unit receives information and commands from the control unit. Here, the information, still in the form of symbolic words, is analyzed, broken down, combined, and rearranged in accordance with the basic fules of logic designed into the machine and according to the commands received from the control unit. The astonishing phenomenonis that there are so few fules of logic designed into the machine. The power ofthe digital computer lies in the fact that it can perform complex operations rapidly by breaking them down into a few simple operations that are repeated many, many times. By performing these few simple operations over and over again in many different combinations, immense problems can be solved a bit at a time, but at fantastic speed. Output When the signats bave passed completely through the arithmetic unit, they no longer take the form of a problem, but now assumethe form of an answer. This answer is passed back to the memory unit and along to an output element. The output element reverses the process, converting the new train of signats back into a form thai can be undestood by the operator or by other machines. Types

ot Memory

Core This is the main memory associated with the computer. The basic unit of storage within main memorv is called a word. Process computer

COMPUTER INTERFACE AND HARDWARE

375

systems typically bave maiG memories with storage capacities between 24,000 and 64,000 words. Memory sizes are usually expressed as multipIes of 1,024words, for example, 24K, 64K, and so on, where K equals 1,024. (A 24K memory actually contains 24,576 words). Since maiG memory is essentially part of the basic computer, access to it is ex-

tremely rapid. Drum

A drum is essentiaUya continuous loop of magnetic tape. A cylinder is coated with a ferrous material similar to that used on tape. The cylinder is then kept in rotation and read/write heads are positioned around its circumference. Each head writes only on that track (band) of the drum with which it is aligned. Heads are energized by addressing circuits that select the desired track and are synchronized by the output of a prerecorded timing track, which generates pulses at bit and word time intervals. In this fashion, computer words can be written on any track and at any word position of that track. In either writing or reading a word into a given position, the longest wait encountered is the time of one complete drum revolution. Drums typically rotate at speeds of up to 6,000 RPM. Figure 17-2 shows the basic elements of drum memory. Disk

A disk is similar to a drum. Data are stored on the magnetic surface of a flat circular plate, like a phonograph record. The disk material is somewhat similar to that used in magnetic tape. Stored information is divided into tracks, or sectors, as with a drum. The primary difference is that the disk has only one read/write head that moves Cromtrack to track. The advantage to this design is that it is less expensive than ,

TRACKS -4 CLOSE-UP OF SECTION OF ONE TRACK

~~ñi=J1J!J

---~~3~~~ ~ ' .'

,~~

DIRECTIDN

Fig. 17.2. Magnetic drum memory.

~-;::c

c::J-0-..

C=:J-o-.

c=I--O~ C)--o ":I5'AMPLIFIERS

DF RDTATIDN

HEAD

376

PROCESS COMPUTERS AND SIMULATION

multiple heads. However, the mechanical movement oí the head causesdata accessto be slower than with drums (Figure 17-3). Semiconductor

(Solid-State)

The semiconductor memory, like the others, is simply an information storage device. These memories are classified into a number of types according to such variables as manufacturing technique, how information is put in and taken out, permanence of storage, and other characteristics. In any memory, the binary bit storage location must be addressable. Further, it must be possible to read the state of every binary word. If the binary words can be read but nat changed, the memory is called a read-only memory (ROM). If the contents of the memory can be changed as well as read, it is called a read/write memory. Read/write memories are commonly called random-access memories (RAM). A memory is said to be randomly accessible if individual binary words within the memory can be accesseddirectly. Solid-state memories are also divided into two categories-static and dynamic. Static memories are bistable. Information is stored in either of the two stable states. It remains in a state until changed by an external signal. A flip flap is a common form of static memory. A dynamic memory circuit uses logic absence or presence, zero or one, in the form of a capacitar charge, as a storage element. Because a capacitar charge can leak ofr, it must be periodically recharged or refreshed. The specifications for the memory used in the FOX 3 computer are as follows: N-channel MOS, 4K by 1 bit RAM. This translates into N-type material, manufactured by meta! oxide semiconductor (MOS) technology, 40% bits on each chip, and 16 chips per array for a total of 4096words with 16bits per word. One logic board contains two arrays, which provides 8192addresses per board. The unit can accommodate from three to eight boards or 24to 64K words capacity of random-access memory. The FOX 3 also contains a diskette (small disk) which is used

Fig. 17-3.Magneticdisk memory.

COMPUTERINTERFACEAND HARDWARE 377

diskette (small disk) which isused for both bulk storageand for initiating programsinto the working solid-statememory. Operator Communication

Devices

The process computer system supports various operator communication devices that enable the process operator to observe process measurements, enter control set points and tuning parameters, request logs and summaries, and trend critical process variables. These devices include operator's consoles, auxiliary special-function keyboards, alarm and messagetypers, trend recorders, Teletype@and CRT terminals, and remote CRT monitors.

Process

Interface

Equipment

Process parameters thai are monitored by the control system are called inputs. Voltage or current signats from measurement sensors are classified as analog inputs, since the voltage, or current value, is analogOllSto the value of the measured process parameter over the entire parameter range. Some process parameters, such as ftow rates measured using turbine ftowmeters, are monitored by pulse-generating devices and are classified as pulse inputs. Limit switches and other contact sensedevices indicate which oftwo possible states a parameter is in, such as pump (on or oir) and pressure (high or low). This type of process measurement is called a digital input. Since the FOX 3 is a digital system, there musi be some means of converting the analog signats from the field devices into equivalent form before it can be used in the computer. This conversion is done by an analog to digital convector which, when activated, converts the input voltage to some equivalent digital number. The key phrase is "when activated." Since there could be alarge number ofinputs to any computer system, it would be wasteful to bave one AID convector for each input. Therefore, one convector will function for a number of inputs, and each time any of these inputs is sampled the AID convector is also activated. The input/output (l/O) module reads the current process signal, converts it to a number thai can be read and processed by the control computer, and notifies the computer thai the value is available by sending it an interrupt. The computer reads the converted parameter value and stores it in its memory for further processing.

378 PROCESSCOMPUTERSAND SIMULATION

There are severaltypes of computersystems.The most common type is the businessor data-processingsystem. Next is the scientific type, and last-but most important to the processindustry-is the processcontrol computersystem. A processcontrol computersystemis anon-line computersystem. Measurementsand other indicationsfrom the processare sentdirectly to the computer system. The computer systemchangesthe analog signalsto digital words, and then performs the proper control equations. Resultsof controlcalculationsare sentto the computersystem's output circuits, which changedigital words to analogsignals, which then return to the processoMany loops are controlled by this means. Since data for each loop reside somewherein the computersystem, occasionallythesesystemsmar alsobe used simplyto collectinformation for the operator. However, this is simply an extensionof the conventional analogsystem. The true processcomputer, when used for control, is part of the closedloop. The outputs from the computer connectto the controller via the analogoutput subsystem.In this closed-loopconfiguration,the computer will take the measurement and performcalculationsbasedon the measurementand other processparameters.The computedresults, or control strategy, will be sentto the selectedcontroller to update the controller set point or to changethe controller output directly, thereby driving the valve. If the computerdeterminesthe set point of an analogcontroller, it is called a set-point control system.Set-point, or supervisorycontrol systems,usethe computerto determinenew setpoints. Measurements are sent to the computer and the analog controllers. The computer partially replacesthe operator by changingset points in responseto processchanges,production schedules,and supervisorycontrol programs while control is by conventionalanalogmeans.This frees the operator for more importanttasks. Direct digital control is a systemin which the manipulatedvariablesare controlled directly by the computer.A valve is drivenaccording to the result of computer calculation of the control equation or algorithm for that loop. (An algorithmis an equationthat is repeated manytimes. AIgorithmsare namedfor the control actionthey provide, i.e., Lead-Lag,Proportional-plus-lntegral,Ratio,etc. Thesealgorithms make up mostofthe control actuatingprogramofthe control software. Thus, the actual operationof the closed-loopcomputercontrol system can be subdividedinto DDC (direct-digitalcontrol) or SPC (set-point

Fig.

COMPUTERINTERFACE AND HARDWARE 379

control). The typical process computer has the capability of operating in either fashion. At times, a combination of these techniques mar be

employed.

Having explored the functions thai are carried out by a computer, let us look at an actual computer. Computer systems are available in many sizes with varying abilities. Since ibis presentation is simply an introduction, the computer selected is of modest size, but is used widely for monitoring and process control of planis such as the one shown in Figure 17-4. This computer system has a multiprogrammed operating system and utilizes modular equipment. The process interface is through SPEC 200/INTERSPEC (Foxboro multiplexing system). The INTERSPEC port plugs into the FOX 3 the same as any other peripheral device and accepts, converts, directs, and transmits the many signals thai flow between a SPEC 200/INTERSPEC system and the FOX 3, allowing the

17-4. Typical process plant.

380

PROCESS COMPUTERS AND SIMULAnON

Fig. 17-4.(continued)Analog/digitalinstruments.

FOX 3 to perform process monitoring, supervisory set-paint control, or direct-digital control of even the most complex loops. Standard software packages bave been developed and are available for process monitoring and control applications. Those discussed in the next chapter mar be employed to create video displays, as well as other support facilities. The FOX 3 system equipment provides the speed, storage, and l/O capabilities needed for real-time, on-line data acquisition and control

COMPUTERINTERFACEAND HARDWARE 381

Fig. 17-4. (continued) Fox 3 computer.

applications. It combinesthe reliability essentialto processapplications and the functional modularity necessaryfor economicalgrowth and easeof maintenance. Functional modularity meansthat the systemis composedof basic building blocks, suchas a completelyindependent,intrinsically safe, l/O subsystem.

382 PROCESSCOMPUTERSAND SIMULATION

Fig. 17-4.(continued)Parts of this figure showmajorcomponentsin a computersystem: processplant. instruments.computer,and operator.

The major hardware components of a FOX 3 system include: Processor cabinet (Figure 17-5) Peripheral equipment (Figure 17-6) Process l/O interface (Figure 17-7) All of the electronics necessary for system operation are housed in tros single cabinet, which contains the following elements:

Microprocessor The major functional elements are four microcontroller chips chosen for their high-speed characteristics and application flexibility. The mi-

crocontrollers form a 16-bit processorthat interprets the language statements stored in memory that directs the FOX 3 to perform its control functions. It can perform arithmetic calculations in both fixed and floating-point formats.

Fig. 17.5. Processorcabinet.

Fig. 17-6. Peripheraiequipment.

Fig. 17.7. Processinterfacethrough FoxboroSPEC200/INTERSPEC. 383

384 PROCESSCOMPUTERSAND SIMULATION

Diskette

The diskette provides a simple, fast, safe, and convenientmethodfor the user to save a permanentrecord of tasks, schemes,or the entire contentsof memory(Figure 17-8).Data canbe reloadedfrom diskette to memory at any time. ProcessorService Unit This unit is an integral part or the processor and performs off-line runctional testing or critical processor operating parameters. It is used in conjunction with a diagnostic diskette and eliminates the need or procuring separate processor test equipment. Just as the patient tells the doctor where it hurts, the diagnostic program tells the technician where the trouble ties. System Clock The line frequency clock provi des a time reference thai schedules many functions vital to accurate and effective control applications. It

Fig. 17.8. Diskette.

We 17.]

COMPUTERINTERFACEAND HARDWARE 385

can be used to generateinterrupts, provide referencesfor measuring elapsedtime, control programsequencing,and so on. Peripheral Interface Logic This logic provides a standard interface channel for easy interconnection with all keyboard/printers, alarm loggers, vídeo consoles, and so on. Each interface channel supports full-duple x operation. The FOX 3 provides up to eight channels for devices that mar be located up to 8 kilometres (5 miles) from the processor cabinet if optional models are

used. Other components located within the cabinet include a battery backup unit that provides power to system memory for up to 30 minutes (optionally for 24 hours) during power outages, power fail/restart circuits that assure continuous process control during power dips or outages, a service panel that monitors cabinet temperature and power, as well as the mode (normal/backup) of the process controllers and the system power supplies. Conclusion

should note thai the physical size of a computer in no way relates toits power or performance. Computers cannot be compared in terms ofthe sizes of memory banks or cycle times, since these factors do Dotindicate the power available to perform the required tasks. A reliable method for selecting a computer involves running the same higher language program on several types and sizes. Note the ease of development, the regulis in time of execution, the amount of storage consumed by each computer, and the potential ability to handle development of programs while the process is under computer control. A digital computer system mar or mar Dot be more economical than the equivalent analog system, depending upon the complexity of the system, performance requirements, projected long-term changes, and other relevant factors. For many applications, the digital system will prove to be more economical than an equivalent analog system. Ouestions

I. A digital computer a. Has the ability to solve problemsby reasoningb. Can only do the things it has beentaughtto do

:i.,.'-

386

PROCESS COMPUTERS AND SIMULAllON

c. Has all the answerson file in its memory d. Makesassumptionsand estimatesthe answer 17-2. The computer's memoryelementis 8. Passive c. Always a magneticdevice b. Aggressive d. Always a capacitivedevice 17-3. The arithmetic unit receivesinformationand commandsfrom 8. The operator'sconsole c. The control unit b. The memory d. A punchtape reader 17-4. The longestdelay in readinginformationfrom a drumis 8. One drum revolution b. 1 second c. 1/60second d. Dependenton track configuration 17-5. A disk recordingsurfaceis madeof 8. Aluminum b. Castiron c. Fiber d. Plasticcontainingmagneticmaterial 17-6. A processcontrol computersystemis 8. A real-timesystem b. An otf-line system c. Independentof the controlloop d. On-line until the operatorpressesthe releasekey 17-7. A processcontrol computersystem 8. Always costsmore than an equivalentanalogsystem b. Always costsless than an equivalentanalogsystem c. May prove cost effective if future changesand processefficiencyare considered d. Will always provide superiorcontrol 17-8. Most processinputs to the computercontrol systemare 8. Digital c. Pulses b. Analog d. On/otI 17-9. The inputloutputmodulereadsthe processsignaland notifiesthe computerit is availableby an 8. Interrupt c. Activating pulse b. Alarm d. Equivalentdigital number 17-10. A diagnosticprogramis usefulfor 8. Locating informationin memory b. Locating processmalfunctions

¡;ff~r

COMPUTERINTERFACEAND HARDWARE 387

c. Off-line functional testingof operatingparameters d. Indicating whenroutine maintenanceis needed 17-11. A systemclock a. Keepsthe operatorawareof the time b. Schedulesfunctions vital to control applications c. Programsthe rate at which memoryis searched d. Placesthe alarmson a periodicbasis 17-12.The powerof a processcontrol computer a. Is a direct functionof physicalsize b. Dependsonly on availablememory c. Canbe evaluatedonly by applyinga higherlanguageto the computers beingcompared d. Is measuredby the total numberof controlloops it canhandle

A Brief Introduction

By definition, software is the collection ofprograms and routines associated with a computer. The first working process computer became operational in 1958. These routines involve other programs such as compilers, library routines, inputJoutput (l/O) devic e handlers, plus vario us other devices shown in Figure 18-1. This figure is termed a software configuration. The computer performs many tasks in decimal parts of one thousandth of a second. While it is extremely fast, it can do only one thing at a time; therefore, an executive program is provided to control the order in which tasks will be accomplished. This is called a priority schedule. Under the control of the executive are process l/O service handler programs, terminal l/O handler programs, and applica-

tion programs such as scanning,alarming, controlling, and logging. Thus, the executive is both a manager and a traffic director. Computer systems also have on-line compilers and off-line compilers. The example shown in Figure 18-1is an on-line system. This means that, while the system is actively monitoring or controlling process routines, the engineer or programmer mar at the same time modify bis control scheme or compile new scan-and-alarm-logging pro grams. 388

Thus,

COMPUTERSOFTWAREAND OPERATION 389

Fig. 18-1. On-line system.

changes in the various application programs or the overall control scheme may be made without shutting down the computer or removing the plant from the control ofthe computer. The on-line capa-bilities of some computer systems bave been used to develop maintefiance programs that allow the computer to diagnose itself and to generate alarms when preventative maintenance is due. Onthe other hand, some computer systems require that compilers be loaded off-line, which meansthat the computer must be shut down for modification of programs. No process control is carried out during the modifications. With certain types of computers, program development must be carried out on a different machine altogether. To compare on-line with off-line operation, let us assume that a particular solenoid valve rails to energize as a result of a minor computer l/O failure. If the computer has on-line capabilities, a test program can be compiled immediately to determine the location of the problem. The maintenance man, using the test program, can isolate the specific point of failure and determine the proper action to take without affecting the rest of the processoHowever, with an off-line system, the computer would bave to be shut down to develop or load a test program into the compiler and

390

PROCESS COMPUTERS AND SIMULATION

isolate the problem. Some off-line computers will Dot even allow the tuning of control. loops without shutting down.

Basic Computer

Operation

The steps the computer negotiateswhen it follows the program are shownin a generalway in the following discussion.First, a programis written and converted iota a languagethe machine can understand. This is called machinelanguage. For our illustration, let us: calculate output No. 1 by solvingthe equation ~ where A = 25,B = 4 and C = 5. The programwill be stored in memory, beginningat location200. For the purpose of simplicity, these instructionsbave been shownbefe symbolically. lnstructions enterthe machinethrough sometype of input equipment (Figure 18-2).The input equipmentwould normally be used to convert these instructions iota electrical pulses that would represent the data. The controllogic sendscommandsignalsto the input equipment and the memory, causingdata to be transferredto memory for storage.The controllogic probablywould be initiated by an operator function. Once the programand its data bave beenstored in the memory, the programcanbe run. Again, this likely would be initiated by an operatorfunction. The operatorwould setthe startingaddresswherethe programhas beenstored on a set of computerconsole switches-in this case,ad-

Fig. 18-2. Instructionsenteringmemory.

COMPUTER SOFTWARE AND OPERATION

391

dress 200-then press a start button. As a result, the control logic would obtain or "fetch" the first instruction from the address that was provided by the operator through the console (Figure 18-3). After fetching this first instruction, the controllogic would bave to interpret and determine the type ofinstruction. In tros case, the control logic would establish tros as a MULTIPLY instruction. The control logic is capable of determining the type of instruction because of the way in which an instruction is coded. Each type of instruction has a particular operation code associated with it. Therefore, the control logic decodes that portion or field of the instruction that contains the operation code and, as a resuit, provides other pieces of logic that wiIl be needed for the execution of that instruction. To execute the MULTIPLY instruction, the controllogic must aIlow the two factors (A and B) to be obtained from memory and brought to the arithmetic unit. The addresses of these two factors (204 and 205) would also bave been provided in this hypothetical instruction. Upon entry iota the arithmetic unit, the two numbers wiIl be multiplied, resulting in a product of 100, which would reside in the arithmetic unit' s temporary storage register or accumulator. After executing the multiply instruction, the controllogic sets itself up to fetch the next instruction, which is located at Location 201 (Figure 18-4). After fetching this instruction from its memory location, the controllogic wiIl interpret it. This time, the controllogic establishes the operation code as a DIVIDE instruction. The controllogic wiIl be set up to perform the division using data from the address specified by the CONTROL

MEMORY

LOGIC ACTION

r-;:OCI CONTENTS I GET INSTRUCTION FROM

==::::!I~~~~I r,

OETERM1NE THE TYPE OF

INSTRUCTION MULT

I 201 I DIV. C

204

205

(B)

206

ARITHMETIC

Fig. 18-3. Fetchingthe first instruction.

UNIT

Fig.

392 PROCESSCOMPUTERSAND SIMULAnON

18-4. Performingthe divide operation.

DIVIDE instruction-Location 206. The divisor value (5) will then be brought to the arithmetic unit and the division process will be performed upon the accumulator contents and the data CromLocation 206. The of this contents. operation is the quotient of 20,' which becomes the new result accumulator The controllogic will now fetch the next instruction CromLocation 202, this time finding an output instruction (Figure 18-5). Since the

Fig. 18-5. Output ofdata.

FiE.

COMPUTERSOFTWAREAND OPERATION 393

output instruction is nat an arithmetic instruction, the controllogic will handle it somewhat differently than for the arithmetic MULTIPL Y and DIVIDE instructions. Instead of looking for an address where it can find other data words, the controllogic will look fora code thai will specify the devic e to which the contents ofthe arithmetic unit should be sent. In ibis case, the output instruction is specifying device No. 1, which we will call a line printer. The contents of the arithmetic unit will be sent to the line printer as a reguli of controllogic signals sent during the execution of the instruction. Finally, arter the output instruction has been completed, the controllogic will return to reich the next instruction, this time from Location 203 (Figure 18-6). When it determines thai it has fetched a HALT instruction, it will bring the memory and control unit timing circuits to an orderly shutdown. Many steps are necessaryto perform even an elementary problem. In some of the most complicated problems, the number of instructions necessary to define the problem completely mar require hundreds of instructions. However, it musi be kept in mind thai the computer can execute these programs at lightning speeds, since cycle or operating

18-6. Halting the programo

394 PROCESSCOMPUTERSAND SIMULATION

time of these instructions is in the order of microseconds (millionths of a second). Any problem or condition that can be represented logically or numerically, can be solved with the digital computer. In addition, once a program has been written, the computer is able to solve that problem repeatedly, using original or new data. Real-Time Clock and Power Fail/Restart Logic The real-rime (line frequency) clock interrupts the system at a high priority level every 1/60of a second so that the system can time events t9 this degree of accuracy. The clock "tick" is accumulated into seconds, minutes, and days so that user programs can respond to time-oriented events. The power fail/restart module continually senses system ac power. lf power drops below a predetermined threshold, the module interrupts the system, forcing it to corne to an orderly shutdown (before insufficient power is available to read and write memory). On the return of suitable operating power, a second interrupt forces the system to resume operations. The term "control system software" describes all programs that go into the making of a complete control system. On large systems, programs are placed in bulk storage (drum, disk, tape, etc.) and the operating system controls the transfer into cone or semiconductor memory for program execution. These programs are grouped into three basic categories: the operating system, control software, and support software. The operating system consists of programs that control system resources and do internal housekeeping. The control package consists of programs that interface with the process to accomplish some level of control. The support programs consist of programs that minimize the user' s effort in using the system.

Control

Software

The primary approach to process and plant control is to use a building block concept to complete control 100ps. Each block in this control loop represents a mathematical algorithm that is performed on some piece of information to achieve some other piece of useful information in the control scheme. These algorithms are performed at fixed periods to achieve the proper control. These periods, calIed scan periods, generally range from one second to several minutes. Every controlloop in

COMPUTERSOFTWAREAND OPERATION 395

a plant will be represented by a number of these control blocks. To minirnize the user's efforts in creating a control scheme, most control systems employ the standard algorithms currently used in analog control. These blocks are assembled in a file called the data base. The data base contains all the inforrnation necessary to define each controlloop, both internal to the computer and external to the user. Building the data base is the first task that the user must perforIn with the control system. This building effort is often accomplished by using fill-in-the-blank forms to describe the type of control and the type of control scheme that is to be accomplished. These forms ask such qüestions as: What is the name ofthe controlloop? What is the range of the measurement and the engineering units? It asks for such things as set-point and measurementlimits. It also asks for the hardware address of the measurement and the control valve. After all the qüestions are answered, these forms are converted into punch cards, paper tape, or other means and fed into one ofthe control programs called a data-base generator. The data-base generator converts this information into especially formatted words that are filed away and utilized by the control programo Having created the data base and, of course, having the operating system and the control program, the user can then load the data base into the system and start to control the processoSince data base modifications are frequently required, provision must be made for on-line data-base-modifying routines. This is a part of the control package. Data-base modifications would include simple set-point changes through more sophisticated modifications. As the level of control increases, the building block approach soon becomes inadequate to handle the special needs of individual plants. Therefore, rather than try to create standard algorithms that apply to all control needs, an interface is normally provided within the control package to allow user-written programs to assume some of the control. With the capability of user programs interfacing to the control package, either the engineer or the programmer, or both, can accomplish various sophisticated functions in terms of plant level control. Production scheduling, inventory control, and material tracking are just a few of the many powerful things that can be accomplished. The only limitation is the capability of the engineer/programmer and the time available to develop the control scheme. An important component is the support software, called the compiler. The compiler converts the language employed by the engineer/programmer into machine language the computer can understand.

396 PROCESSCOMPUTERSAND SIMULATION

Now let us demoristrate how atypical process computer, the FOX 3, is programmed to carry out its control assignments. The system language is called Foxboro Process Basic (FPB). This language has evolved from the American N ational Standard Basic with some modifications provided by Foxboro Process Language (FPL), which was developed originally as a programming tool for small computers. In FPB, tasks (programs) are written like operating instructions, using expressions (statements) familiar to process people. This FPB enables process engineers and operators to build, operate, and modify process monitoring and control tasks, using conventional process terminology. Within the computer' s memory there exists a program that will convert the FPB into so-called machine language that the computer can utilize. This function is called a compiler. Achieving

Process Control

The purpose of a language like FPB is to allow the user to tell the computer what to do and how to do it, in a concise andorderly way. To attain a control objective, the user first defines the problem in functional terms, then designs an appropriate solution. The next step is to express the solution as a structured set of statements. The supervisory portions of the solution are written as FPB tasks. These tasks are groups of FPB statements arranged so that they describe a set of procedures for the FOX 3 system to follow. Typically, these tasks describe supervisory functions, such as generating reports and controlling the sequence of process operations. To define a task, the user types FPB statements at the interactive device currently serving as the system terminal. Once entered, a task is ready to rUflo The illustrations below show a simple batch processo The task called CHARGE involves mixing two materials in a tank, heating the mixture, and holding it at a constant temperature for 20 minutes before draining the tank. Figure 18-7shows the process diagram. Figure 18-8 is the flow chart depicting the st~ps to be taken to control the processo Figure 18-9 is the FPBtask that performs those steps. When the user types the command: RUN CHARGE, the task will begin executing; that is, the materials will be mixed, heated, and held at the specified temperature, and, arter the designated interval, the tank will be drained. An important part of the FPB software is the control package, which is the means of describing the process interface and control structure to the FOX 3 system.

COMPUTERSOFTWAREAND OPERATION 397

Fig. 18-7. Processfor chargetask.

In a question-and-answer format, the user enters the specific characteristics of the process control and computational elements to be used. This description is called a "block." Blocks can be connected to forro a variety of control strategies, called "schemes," which tell the system how to control the processo A block is comparable to an analog device. It is a conceptual entity, identified by a name, for which certain monitoring and control functions (called "algorithms") are defined. By logically connecting blocks of various functions, the usercan create a block scheme in the computer which can replace or enhance an analog control scheme-

398 PROCESSCOMPUTERSAND SIMULAnON

Fig. 18.8. Flow chart for chargetask.

Hold

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K..ppumpm. Tumpumpoff .Stop

Fig. 18-9. Charge task written in FPB.

~ ~---~

--c I..k definilion 'ompleled

COMPUTER SOFTWAREAND OPERAnON 399

Fig. 18-10. Analog flow ¡oop.

receiving measurements from the plant, processing these signals, performing control or computational functions, and retuming control signaIs to the plant. In a simple analog flow loop (Figure 18-10),the signat from a differential flow loop is conditioned and transmitted by the square root element (f). The resulting flow signat is passed to a controller, where it is subtracted from a set point to produce an error value to be used in the control function. The control function, or algorithm, is two-mode proportionalintegral (PI) control, which calculates the new valve position. This is a building block approach to process control, since the process engineer selects standard "black boxes" thai perform defined functions and connects them into loops. The Foxboro Control Package (FCP) refers to the computer equivalent of an individual analog device as a "block." For every analog "black box," there is an equivalent computer "block." Using the control package, the process engineer logically connects blocks to achieve control schemes exactly as with analog devices. Figure 18-11 depicts a computer-based control scheme equivalent to thai in Figure 18-10.This

r -cDMPüTER"---~

Fig. IS. Il. Digital ftow loop.

l..

400 PROCESSCOMPUTERSAND SIMULATION

is a direct digital control (DDC) scheme because the computer is producing the valve position signal. In certain situations, flow control would be superior with an analog controller because of its speed. When tros is necessary, the computer would set the analog controller' s set point. FCP consists of standard control blocks that provide a wide range of process monitoring, control, and calculation functions. Each FCP Control Package block is a standard skeletal definition of one process function. The user completes the definition of a block by participating in a question-and-answer dialogue with the FOX 3 system. That is, the user signifies the kind of block to be defined, and the system asks qüestions about the alarm limits, engineering units, and so on. The user's answers, which define the characteristics ofthe block, are called the block parameters. As in the comparable analog control scheme, the block itself is called an algorithm. A wide variety of control block algorithms is available. These software blocks now replace analog components in the system. The user can define each block in the system by specifying all of the control parameter values that pertain to each block type. For example, all analog input blocks start with the samebasic block structure, ret each one can bave its own unique set of block parameter values such as the frequency of block execution, high and low limits, engineering units conversion, and so on. In addition to control functions, blocks are available to perform alarm functions, displays, monitoring calculations, and virtually every function an analog device would accomplish. The software for the modern process computer system has progressed considerably in recent years. When the first computer was applied to the control of a refinery in 1958, it was necessaryto program the computer in machine language. This was a long and extremely tedious job. Modern technology, combined with controller languages like FPB, makes the job much easier and infinitely more pleasant. Significant improve ments in computer technology continue to occur at a rate that staggers the imagination. Ouestions

18-1. A compiler a. Storesbulk data b. May be on-line or off-line

c. Establishespriorities d. Is an inoutJoutouthandler

COMPUTER SOFTWARE AND OPERATION

18-2. In computeroperationevena simple operation a. Requiresa sophisticatedCPU b. Takesmanysteps c. Must be scheduledby the real-timeclock d. Must be reprogrammedeachtime it is run 18-3. An algorithmis a. A sequenceof calculationsperformedto obtaina givenresult b. A formula c. Always a ditferential equation d. Determinedfrom a table 18-4. Every analogfunction a. Is duplicatedby digital hardware b. Shouldbe reviewedto confirmits usefulness c. Canbe duplicatedby digital software d. Canbe improved upon in a digital system 18-5. A major advantageof the digital systemis a. Energyefficiency b. The ease of makingchanges

c. Economy d. Its ability to control without feedback 18-6. The first working processcomputerbecameoperationalin a. 1976 c. 1968 b. 1948 d. 1958 18-7. The numberof tasks that a computersystemcan carry out depends mostly on a. Real-timeclock c. Its restartmodule b. Capacityof its memory d. Its data base 18-8. If the computeris examinedas a processcontrol tool, we conclude a. It hasreachedits full potential b. It hasthe potentialto becomevirtually anything you wish to make it c. Economicallyit cannotbejustified d. It is a more economicalmethodof control for any processo

401

In a programmed control system, the control point is automatically adjusted to follow a predetermined pattern with respect to time and process conditions. For example, assume that a food product is to be cooked and the cooking process requires the following sequence: 1. Raise the batch temperature uniformly up to the cooking temperature over a 1-hour period. 2. Cook the batch for 1 hour at the cooking temperature. 3. Allow the batch to cool to room temperature gradually and uniformly over a 2-hour period. This type of process can be satisfied by a programmed control station. Originally, most programmed controllers were cam-operated, and this technique is still widely used. In the cam-operated controller, the control setting movement is replaced by a follower, riding on a carn that has been cut to produce the desired schedule. The carn is frictiondriven by a clock. The carn can be laid out to provide any predetermined schedule of time-and-process requir.ements. The cam-operated, programmed controller ofIers the advantages of simplicity and ease of operation. The limitations are that it is only a single loop; and a program change requires a new carn layout, and, in some cases, a change in carn speed (motor). These limitations made the elapsed-time controller popular. 402

PROGRAMMEDCONTROLSYSTEMS 403

The elapsed-time controller is designed to bring the measurement up to a set point at the start of a preset period (holding period) and control it at thai point for the remainder of the period. At the end of theperiod, control ceasesand the process shuts down until another cycle is started. Elapsed-time controllers mar be either electronic or mechan-ical instruments for application on any process variable. On/otI or proportional control mar be used. The timer periods are adjustable and available to provide holdingperiods Crom minutes to hours. Figure 19-1 shows a typical process curve controlled by an elapsed time controller.

Description

01 Circuit

The Model 4OE-A elapsed-time controller consists of a conventional pneumatic controller with an additional ftapper-nozzle operated by an electrical circuit (Figure 19-2). With the elapsed time switch in the manual (M) position, the ftapper is held against the nozzle irrespective of the solenoid plunger position, and the pneumatic circuit functions in the usual manner. However, with the elapsed-time switch in the A (automatic) position, the ftapper is free to be operated by the solenoid, which, in turo, is controlled by the timer. When the timer is set to the desired value of the holding period, and the timer start button (14) is pressed, the timer circuits (1) and (3) are completed, as shown in Figure 19-2. The solenoid is energized, moving the plunger to the right in the diagram, covering the nozzle, and thereby starting pneumatic control. The control valve opens to raise the measurement to the holding value and maintain it there for the duration of

Iol

.. ~ m

TIME

Fig. 19.1. Typical process curve controlled by elapsed time controller.

Fig.

404

PROCESS COMPUTERS AND SIMULATION

19.2. Foxboro 4OE-Aelapsed time controllers.

the holding period. Electric circuits are also completed that operate the timer motor and the green holding light. At the end of the holding period, timer circuits 1 and 2 are connected, all previous circuits are broken, and the solenoid is deenergized. Air bleeds Crom the pneumatic circuit and the control valve (air-to-open) close to shut down the processo At the same time, the electric circuit through the "End-of-Cycle" light is completed. This type of elapsed-time controUer is, like the cam-operated controUer previously described, a single-controlloop device. If more than one controlloop is involved and additional functions are required, the control systems described are inadequate. The initial solution to the problem might be to use a cam-operated controUer for each loop, which has been done on occasion. This approach would bave limited success, since any required change in the program would be difficult to incorporate into the system. This type of problem can be resolved quite readily by the digital computer. A digital computer-oriented system provides versatile, preprogrammed sequentiallogic control functions. It is used to automate adjustments of analog set points and the check and inhibit actions of

Fig.

PROGRAMMEDCONTROLSYSTEMS 405

interlock logic. Also, the synchronized starts and stops of process equipment are completely automated with the use of a computer system. This computer-compatible logic system bridge s the gap between mechanical programmers and process computers. The sequential control program is designed with an easily understood ladder logic language. The logic operation is created by pushbutton, without wires or wiring, and is stored in the memory of a programmable controller. This programmable controller is capable of operating multiple, completely independent process units at the same time.

Sequential

Control

Systems

In addition to startups and shutdowns of continuous systems, batch processes are potential applications for computer-controlled systems. A stored control program is used to repeat all the events in an operation, step-by-step, throughout a production cycle. The program elements consist of on/off Telar logic, time-delay and elapsed-time periods, predetermined counts of pulses, and pulse outputs for set-point control. Elementary mathematical manipulations (addition, subtraction, multiplication, divisiott) can be performed within a step of the logic programo Each of the stepped phases of all operational events is controlled by input contacts and feedback. These contact inputs are from pushbuttons for manually initiated action or from limit switches for positional action. AIso, contact inputs can be derived from analog inputs for signal comparison or from other permissive interlock or inhibit actions. The memory and logic program, shown in Figure 19-3,controls

SEQUENTIAL CONTROLLER

19-3. Functional diagrarn oCsequential controller.

406 PROCESSCOMPUTERSAND SIMULATION

the conditionswhenafield output is turned ON or OFF for any of the following operations: Openingor closing individual valves Starting or stoppingpumps or agitators Operatingthe lights of communicationdisplays Programmable

Controllers

The programmable controller is a solid-state, sequential logic control system. It replaces mechanicallogic equipment, such as relays, stepping switches, and drum programmers. It is designed and packaged for operation in harsh industrial process environments and for high reliability and long-operating life. The logic sequence program, implemented by pushbuttons, simplifies the development, checkout, and maintefiance of the control system designo The programmable controller consists of four functional sections: a COfe memory, a logic processor, storage registers, and inputJoutput signa! conditioners. The size of the memory determines the logic storage capacity for individual programs. These programs are executed by the control routines of the logic processor and are used to generate signals to turo on or otI operating field outputs or to adjust set points of controllers. To communicate these inputJoutput signals, storage registers act as bridges between the signals at field levels and the high-speed circuit of the logic processor. The inputJoutput signal conditioners convert input signals at field levels for compatibility with the logic processor and control the output power for operation of field circuits.

Programming

Language

The language used to describe sequential on/otI logic is an electrical ladder diagram with logic line numbers and contact symbols. A logic control program closely resembles the format used for mechanical relay systems. A typicalladder diagram is illustrated in Figure 19-4. In this diagram, the source of power is indicated by the vertical uprights of the ladder. The horizontal rungs indicate switch contacts to control the ftow of power. The four contact symbols used in logic sequences are shown in Table 19-1.

-1.-;;;¡ Fig.

PROGRAMMEDCONTROLSYSTEMS 407

PRQGR_BLE CONTROLLER EQUIVALENT

CONVENTIONAL SCHEMATIC

19-4. Logic language (ladder diagrarn) format.

Generally, the logic program diagram elements use the same number designations as the conventional relay diagram. However, an individual rung is limited to a maximum of four contact elements. If a logic sequence requires more than the four elements, it mar be handled as follows: The originalline output number is used as the first contact input reference to the next line. For step-controlled events, a singleinput contact is used to control many contacts by assigning the same reference number as if it were a relay with unlimited poles.

Table 19-1. Logic Sequence Symbols TYPE OF CIRCUIT

NORMALLY OPEN (NO)

CLOSED (NC)

SERIES

PARALLEL

NORMALLY

-::¡ïr

408

PROCESS COMPUTERS AND SIMULAllON

Programming

The logic control program is created in memory by the use of a programming panel. A typical panel is shown in Figure 19-5. Logic is entered line by line. The programming panel is plugged into the service port of the programmable controller. A new program is manually entered into the memory by pushbuttons marked with the same symbols as the four Telar contact types. The line number and the individual contact reference number are dialed on a thumbwheel; one of the pushbuttons, marked with the logic symbol, is then selected and pushed. The programming panel contains other types of logic functions, including time delay or elapsed time, event counting, and calculation (addition, subtraction, multiplication, divisi on, and comparison of two numbers) for control of a logic line output.

Fig. 19-5. Programming panel.

PROGRAMMEDCONTROLSYSTEMS 409

The logic programlines are designedwith seatcircuits for momentary contact inputs or with latch relay circuits for retentive output action in caseof power failure. Logic System

Automation

Proper application of a programmable control system begins with an economic justification analysis. Savings are developed principally from reduced cycle time and scheduling. Cycle automation provides rigid control enforcement to eliminate human errors and to minimize necessary manual interventions. lncreased efficiency in scheduling is to be expected with maximum utilization of equipment and reduction of fluctuating demands on criticat equipment. Guidelines should be established to determine future plant goals and the direction for the analysis. For instance, in a limited production

Fig.

410

PROCESS COMPUTERS AND SIMULATI0N

plant, the economic incentives are immediate from increased throughput. In a plant that produces for a limited market, quality control, cost reductions, and future flexibility for change are more important. With this type of system, the many possible control schemes are as variable as the individual processing applications. System Control

Displays

The effectiveness of the programmed logic control system depends on cycle status communication. This, in turo, depends on the proper selection of compatible display hardware and an understanding of the needs of the operator for efficient performance of bis job in varying circ*mstances. The display task is to advise Dot only the correct information, but the most useful information. Table 19-2 lists typical displays that might be incorporated into the system. A good display technique simplifies the communication of the operation tasks. There should be no time lost while the operator waits for operating status and instructions. 'L" LO'I' S'ST"" l " D'TE2' SEPT' P'GE 'NO"E .NDDE 'NDDE D NDDE LI NEI REFERENCED IN LI'ES ,-" I

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1 RE'OY FOR TR'OSFER LIGHT I

PROGRAMMEDCONTROLSYSTEMS 411

TIMED HOLD PERIODS

RAMP

RATES

TIMEFig. 19-7. Typical prograrn cycle.

The outputs controlled by this program adjust the correct processing values by moving the set points of the analog controllers. The logic system can program the final set-point position by comparing the programmed set-point signal to the measurement signal from the processoThese signals are interlocked to prevent the sequence from advancing to the next step until the measurement has reached the preprogrammed set point. A typical program cycle is shown graphically in Figure 19-7.

Conclusion

The batch processesin the food, chemical,paper, and cementindustries are sequentialin nature, requiringtime-or-event-based decisions. Programmablecontrollers are beingusedmore and more as total solutions to a batch problem rather than just a tool. A process control computer systemgenerallyhasthe ability to perform a programmable controller function. lndustry's goal is to improve quality and cot costs. This can be done by increasingthroughputby minimizingcycle time per batch, and consistentproduction of on-specproducts.

Questions 19-1. A prograrnrnable control systern is 8. A single-carn set controller b. A digital cornputer prograrnrned to carry out a rnultiloop control

sequence

412

PROCESSCOMPUTERSAND SIMULATION

c. A data loggerattachedto a multiloop system d. Any digital computerthat performsset-pointcontrol 19-2. Programmablecontrol systemsare generallyusedwith 8. Flow loops c. Batchprocesses b. Pressureloops d. Large-capacitysystems 19-3. Cam-operatedcontrollersare programmedby 8. The layout of the carn c. Varyingthe timer settings b. Usingthe programmingpanel d. The operator 19-4. The effectivenessof the programmedlogic control systemdependson 8. Cycle status communication b. Economicjustificationanalysis c. The mathematicalmanipulationsrequired d. The computerit interfaces with 19-5. Properapplicationof a programmablecontrol systemshould beginwith 8. A difficult control problem b. A passiveprocess c. Properselectionof compatiblehardware d. An economicjustificationanalysis

A processcontrolloop can bestbe understoodwhenits componentsare combinedin a loop and studied in operation.This, or course,requires both the instrumentationand a processto be controlled. The process mar be real, or it mar be an analogyor a simulationor a real processo This chapterdescribeshow both simulatedand real processescan be constructed.In terms or operation,there is little differencebetweenthe real thing and the simulation,but in termsor beingableto visualizethe operation, the real processdefinitely has the advantage.First, let us considerthe simulatedprocesso Simulated

Processes

The axiom in plane geometry that "two things equal to the same thing are equal to each other" applies to the technique of simulating a process and its control. The axiom is applied by constructing a system, a simulator, which simulates the behavior of the physical system under study. The information from the simulator is applied to the actual sys-

tem. The technique is convenient because it is generally much easier to 413

414 PROCESSCOMPUTERSAND SIMULATION

manipulate the components of the simulator than it is to work with the actual system being investigated. It also is a great time-saver, because the simulator time base can be manipulated. For example, if a dynamic study of a process with a 30-minute time constant were made, it would take many hours to collect the necessarydata. However, an equivalent simulator with a time constant of a few seconds, or even milliseconds, could provide the same data in a few minutes. Still another area of effectiveness for the simulator is its application to the training of instrument engineers and operators. Frequently, it is desirable Dot only to demonstrate control action, but also to let the student make adjustments and observe the results. An actual process mar be expensive and unwieldy, and mar contain time constants that would make the demonstration too long to be practical. Both of these obstacles can be overcome by a suitable simulator. A process simulator mar be analog or digital; that is, it mar use voltages or pressures, currents or flows, or other continuous variables toiepresent the processoOr a digital computer mar be used to make a digital simulation of the processo Only the analog simulator will be considered befe. The process simulator mar be electric or pneumatic; the choice usually is dictated by the type of instrument mechanisms being investigated. The response of many process elements is similar to that of a single resistance-capacitance (RC) electric circuit. More complicated process elements usually bave a response similar to severa! RC elements in series. Thus, three RC groups can simulate a three-element processo Constructing

an Electric

Process Simulator

A three-element electric analog simulator for a process containing multiple capacitances and resistances, including an adjustment for gain and load changes, is shown in schematic Cormin Figure 20-1 and pictured in Figure 20-2. This simulator consists ofthreeRC networks whose resistance value-and hence the RC (time-constant) value-is adjustable. The middle capacitar in the series has an adjustable resistor in parallel with it to simulate process load changes. The output of the RC network P has an adjustable gain control, making it possible to simulate various process gajos. Output P is amplified, recorded, and brought to the controller input to close the loop. With the adjustments available, this analog simulator has the capability of simulating a wide variety of process types and operating conditions. It has the further advantage of being relatively inexpensive and easy to construct.

CONSTRUCTINGAND INSTRUMENTING REAL AND SIMULATED PROCESSES 415

Fig. 20-1. A three-element electronic simulator for a process containing multiple capacitances and resistances and used with Foxboro SPEC 200equipment.

Now let us examinea commerciallyavailableanalogsimulatorand the features it makesavailable. The Foxboro

Electronic

Process Simulator

The Foxboro Companyelectronic process simulator is a lightweight, portable,self-containedreal-time simulator(Figure20-3).A wide range of industrial processescanbe simulatedwith this device.

Fig. 20-2. Electronicanalog.

416 PROCESSCOMPUTERSAND SIMULATION

Fig. 20-3. Processsimulator.

The simulator consists of three serially connected special electronic circuits. One circuit simulates a final actuator-commonly valves or dampers of various sizes and characteristics. A second circuit (Process 1), simulates a fast-ftow processo The third circuit (Process 2), simulates a thermal processo Simulated final actuators (valves, dampers, and so on) mar be scaled to a range of sizes. The simulated final actuator characteristics mar be linear or nonlinear, with either a slow or fast response time. A hold position is provided to allow display of the controller output without the dynamic effect of measurement feedback. Process 1, the fast-ftow or materials feed process, is adjustable for process gain. Single or repeated load upsets, with or without noise, can be superimposed on the input to Process 1. Process 2, the slow heating, tank, and reactor process, is adjustable for total-process time lag and process load. In addition, the circuit allows the simulation of linear or nonlinear processes with three different sensor gains.

CONSTRUCTINGAND INSTRUMENTINGREAL AND SIMULATED PROCESSES 417

Fig. 20-4. A studentand the author at electronicprocesssimulator.

When using pneumatic instrumentation, controllers, and recorders, it is necessary to add only pneumatic-to-electric and electric-topneumatic converters between the simulator and the instruments. With such converters, useful and direct comparisons can be made between electric and pneumatic instruments. The process simulator input, the manipulated variable, is an analog signat either 10 to 50 mA dc, 4 to 20 mA dc, or O to 10 volts dc. The process simulator outputs (MEASUREMENT 1 and MEASUREMENT 2) from, respectively, Process 1 and Process 2, appear as the same type of signals.

418 PROCESSCOMPUTERSAND SIMULATION

"-f

ACTUATOA FINAL

PROCESS2 (TEMP.I

IVALVE)

INPUT

SIGNA L

OUTPUT SIGNAL RANGE SWITCH I

RANGE SWITCH I

MANIPULATED VAAIAfLE

CONTAOLLEA OUTPUT

L_.J

OUTPUT S'GNAl RANGE SWITCH

MEASUREMENT1

MEASUREMENT2

INTERNAL EXTERNAL

CONTAOLLEA1. I (SECONDAAVII

L (SINGLELDOP) J

~""

-1\ ' !+

CONTROLLEA INPUTI'

I IN':UT

\:eJ

,,'

r'-.-'-.

CONTADLLE~ -..CONTAOLLEA SETPOINT OUTPU:r1 IPAIMAAVI L J Input/DutputPo'a"ty As! Posit'," (CASCADEI Black.Nogat;..

;

l' .1ï '.

.J . . . -'+ SETP'DINT

Fig. 20-5. Connectionblock diagram.

Inside the simulator, special purpose solid-state electronic circuitry provides the features and characteristics to provide realistic simulation of a variety of processes. Circuit block diagram Figure 20-6 shows the internal arrangement. Assume that we wish to simulate a beat exchanger-a singleelement temperature control as shown in Figure 20-7.

Fig. 20-6. Circuit block diagram.

CONSTRUCTINGAND INSTRUMENTINGREAL AND SIMULATED PROCESSES419

Fig. 20-7. Heat exchanger-single-element temperaturecontrol.

In this single-element temperature control system, the controller compares a measurement of bot water temperature with its manually adjusted set point to develop an output signal. This output signal feeds to and controls a fast-acting equal percentage steam valve. The size of the beat exchanger, bot water load, steam pressure variations, and many other factors determine the successof the controller in its efforts to control the bot water temperature. As stated in Chapter 11, the final actuator or valve must be properly sized. To accomplish this, several steps must be taken. The valve characteristic linear or equal percentage also must be selected. The final actuator should be sized to bring the simulated process (1 or 2) measurement to 100 percent when the controller output (manipulated variable) is 100percent. To do this: 1. Adjust controller output to 100percent. 2. Adjust Process 2 load to the highest anticipated load. Low -0.2, High -5.0. 3. When using Process 1 but not Process 2, adjust to normal (1), center (up) position. 4. Adjust final actuator gain to bring Process 2 measurement to 100 percent. 5. Adjust Process 1 gain to bring Process 1 measurement to 100percent. Now we are ready to tune the controller to control the simulated beat exchanger process, using the procedures outlined in Chapter 12. The results would be similar to those shown in Figure 20-9. Once the simulator has been set, it should not be adjusted to get the desired results. The process is not tuned to match the controller, but rather the controller is adjusted to accommodate the processo

420 PROCESSCOMPUTERSAND SIMULATION

Fig. 20.8. Simulatorsetupfor single-element temperaturecontrol.

The variety of processes that can be simulated is virtually endless. The limitations are time-related. For example, a simulation of a distillation column with time constants of an hour could Dot be done in realtime with this simulator. Generally, this creates no problem, since shorter time periods are much more practical for leaming. Pneumatic

Process Simulator

The pneumatic-simulated process shown in schematic form in Figure 20-10 and pictured in Figure 20-11 consists of three capacitances (tanks) and three resistances (variable restrictions) altemately in series, and a method of simulating a change in process load. Components above the dotted line in the schematic provide simulated load changes. In order to simulate load changes, a simple proportional controller is

used.

CONSTRUCTINGAND INSTRUMENTING REAL AND SIMULATED PROCESSES 421

HEAT EXCHANGER WITH FAST-ACTING EQUAL PERCENTAGE VALVE

LOAO NORMAL SET paiNT

LOAD NORMAL SET POINT

55 PERCENT

LOAD

PERCENT

NORMAL SET

POINT

15 PERCENT

Fig. 20-9. Reat Exchanger-normalload, equalpercentagevalve.

The Foxboro Model 56-3 Telar is basically a proportional controller, that is, the output (bellows P, called the feedback bellows) has a signal proportional to the difference in signals in bellows A and C. Bellows C is normally called the "measurement bellows," and A is called the "set bellows." In this case bellows C is used as the measure ment input, but bellows A is used as a "simulated process." This analog demonstrator uses three standard Foxboro instruments (a Model122F [two-pen] recorder, a ModeI130-M-N5 [PR&D controller], a three-unit pneumatic control shelf #lOO-3N-RI-Cl, and a Model 56-3-9 computing Telar). The set-point transmitter, controller, and transfer switch are all in the same unit. The controlled variable (pressure) is recorded by the one pen (red in the Foxboro ModeI122F). Another pen (green) mar record any of several possible inputs, such as controller set point, controller output, or air pressure applied to the C bellows of the relay. The ability to record these factors provides ftexibility for demonstration. The set-point transmitter deli vers a signal to the controller corresponding to the desired operating level. The transfer switch permits

l ~ ~

J~.;---~ ¡;.Ir ~ g

422 PROCESSCOMPUTERSAND SIMULATION

C!c_-

TANK (CIO4AT) TANK (CIO4AT) r'

RESTRICTOR (UIOIBC)

r-J, ~ up

M56-3 ~

RELAY~ LI6LI :- ~

I !

Ii ~

I ~ I

REGULATOR~---~-~-=B=~~~: ~ z)

RESTRICTOR (UIOIBC)

_:~-:J

L~..I ) 'A

SUPPLY

30-PSI

..:~ .I

RECOROED

~ RESTRICTOR

(UIO! BCI

[

I TANK

'" CI)'"

i-J

§L

Q. I l

J(~I~~~T) l

:o . ."..RESTRICTOR

~ -'

.(UIOIBC)

/ ';;;:I.

,INSTRUMENT' IDENTIFICATION (AS SPECIFIED IN SALES ORDER)

/-~. -.,./

AIR SUPPLY.REGULATE 1/4" TUBING TO A FIXEOIPRESSURE OR BETWEEN I 3/B" PIPING IB ANO 22 PSI

Fig, 20-10. Sirnulation of a three-element system with pneumatic components.

switching control Crom manual to automatic, or Crom automatic to manual. The three-mode pneumatic controller has proportional, integral, and derivative functions. The recorder should bave a 3;:í-inchper minute chart drive.

CONSTRUCTINGAND INSTRUMENTING REAL AND SIMULATED PROCESSES 423

Fig. 20-11. Pneumatic Consotrol-lOO Line, three-unit shelf, and two-pen recorder.

Operation ot the Pneumatic Simulator Operation of the controlloop can be traced on the schematic of Figure 20-10. First assume that astable condition has been reached with the recorder pen on scale. A step change then is created by moving the set point. This results in a change in set-bellows pressure, and in the moment of force exerted by this bellows on the controller's floating disk. The controller immediately sets out to rebalance itself. The result is a change of controller output pressure, which is applied through the resistance-capacitance network to the A bellows of the relay. The three resistance-capacitance networks and their time constants establish the process time characteristics, or phase shift. It is by altering these vallles that the time constants of the process may be varied. The pressure change in the A bellows unbalances the moments of force in the computing relay. This unbalance is sensed by the flapper-nozzle detector, and the relay rebalances its elf by changing the pressure in bellows P. This pressure in bellows P becomes the controlled variable, and is fed back to the measurement bellows of the controller and the recorder. Within the controller, the moment of force created by the pressure in this bellows is concemed with that created by the set-bellows pressure.

424 PROCESSCOMPUTERSAND SIMULATION

When these moments are again in equilibrium, the controller has rebalanced and the system has returned to a steady state. The C bellows is the "measurement" bellows of a conventional transmitter. Load changes are simulated by feeding changes through a three-element RC circuit into the "measurement" bellows C of the Model 56-3 relay. Load changes mar be simulated by changing the pressure in the C bellows. The knob on the pressure regulator varies the process load. The resistance-capacitance network in series with the regulator adds delay time to the load-change signal and makes the operation more realistic. Many processes bave the characteristic of pure dead time. Pure dead time is the lapse between the instant a change occurs in the process and the time it is sensed by the control system. For example, assume that the outlet temperature of a beat exchanger is to be measured and controlled. If the temperature sensor is placed in the outlet line 200 feet Cromthe exchanger, and if the flow velocity through the line is 5 feet per second, then 40 seconds (200fe et per 5 feet per second) must elapse before any temperature change can be sensed by the sensor. This 40-second time delay would be pure dead time. Pure dead time is very difficult to simulate in any process analog. In the pneumatic process simulator, the pure delay is approached by substituting a lag for dead time. This is accomplished by introducing a resistance in series with the P signa!. Severa! feet of 0.007-inch bore capillary in this line will provide the lag. A bypass valve will eliminate it as desired. For demonstration purposes, the simulated process should be operated without dead time, and then dead time can be introduced as an additional complication or a greater challenge. A list of adjustments that will provide a starting point might be as follows: VR¡ = 60 percent; VR2 = 60 percent; VR3 = Min; C = 25; PB = 100 percent; integral = 0.5; derivative = 0.5; no dead time resistance (bypass open). Time Base

One advantage of the process simulator is its ability to operate on a faster time base. For example, assume that an actual open-loop process is subjected to a step upset and output is recorded on a chart having a %-inch per hour chart drive. If the simulator recorder chart moves at % inch per minute and we manipulate the RC values, we discover that the resulting curve has the

CONSTRUCTINGAND INSTRUMENTINGREAL AND SIMULATED PROCESSES425

Fig. 20-12. (Top) The response curve, the "signature" ofthe system, can bave its time axis changed by simuIation. Only the time base is different. One curve is the real system; the other is simulated.

same shape, though our time base is only 1/60ofthat ofthe real process (Figure 20-12). If the controlloop is now closed and the controller is manipulated, the general problems encountered with the simulated process are essentially the same as for the real process, but the speed of action has been increased by a factor of 60. If, arter a few trial-and-error adjustments, the controller modes are set to produce the recovery curve desired, these same settings can be used in the controllerattached to the actual process, but those factors

Fig. 20-13. Liquid-level processo

426 PROCESSCOMPUTERSAND SIMULATION

Fig. 20-14. Level/ftow processo

having time elements (derivative and integral) musi be changed by a factor of 60. Time scaling has perhaps been oversimplified in ibis illustration. If the analog is used in the solution of a differential equation, the time factor musi be introduced into the equation so thai the resultant solution will be in proper formo Proportional band has no time factor and would remain the same for either case. An open-loop step upset can be simulated by switching the controller to manual control. Using ibis technique, and the faster time base, the step upset or signature curve of the simulated process can be adjusted to correspond to the process under investigation.

CONSTRUCTINGAND INSTRUMENTlNG REAL AND SIMULATED PROCESSES 427

Real Processes

Simplicity and economics are major considerations in the construction of a process for instructional purposes. After investigating many possibilities, the logical choice became a simple level processoThe process and instrumentation are shown schematically in Figure 20-13 and pictured in Figure 20-14. The process consists of a tall cylindrical main tank which empties into a short tank large enough in diameter to contain the contents of the tanks above il. A small tank is placed in the flow line between the bottom tank and the main tank to provide a realistic lag. Liquid (colored water) is pumped by a submergible pump from the bottom tank through an orifice plate-mounted within a difIerential pressure transmitter-a control valve, the small-capacity tank, and then back into the main tank. Level in the main tank is measured by a Foxboro Model 17B buoyancy transmitter. The lisi of material required to construct the system follows. The materials employed cost approximately $7,000 in 1980. 1 Foxboro 1 Foxboro 1 Foxboro 1 Foxboro 1 Foxboro valve 1 Foxboro 1 Foxboro

Model 130-M-N5 PR&D controller Model 130F-N4 P&R controller Model 123, three variables Mode1102-4N, four-unit mounting shelf Model V 4A 3/4-inchbody, H needle, C v = 0.56 control Model 17B4-K41 pneumatic buoyancy transmitter Model 17B displacer A0100WM, 14-inch, rod = 8 in-

ches 1 Foxboro Model 13A d/p Cell transmitter 1 Foxboro Model 13A d/p Cell transmitter with integral orifice, 0.159-inc,h-diameter 1 Little Giant submergible pump; Little Giant Corp., Oklahoma City, OK 20 feet of Imperial plastic tubing, 3/s-inch 50 feet of Imperial plastic tubing, !/4-inch Assorted Imperial fittings 1 pressure regulator and manifold Wire and junction boxes

428 PROCESSCOMPUTERSAND SIMULATION

1 plywood 2 x 6 feet mounting panel and 2 x 6 feet instrument panel 1 plastic tank, 4-inch inside diameter x 42 inches high 1 plastic tank, 4-inch inside diameter x 13 inches high 1 plastic pail Use all nonferrous materials to prevent rusty water. The combinations thai mar be arranged with ibis equipment are many and can demonstrate a variety of control actions. Figures 20-15 through 20-20 show some of these arrangements. If rou pIan to do the feedforward loops Figure 20-19 and Figure 20-20, two square root extractors, such as Foxboro Model 557 and an analog computer, Foxboro Model 136-1, will be required. Now let us examine a more deluxe real-time process designed for training. Figure 20-21 presents a picture of a process designed for use in educational activity at Foxboro. It is shown in schematic form in Figure 20-22. This process unitfeatures a graphic panel to which all instrument inputs and outputs are terminated. It is possible, then, with pneumatic patch cords, to make an almost endless number of loop configurations. The dead time unit is a form of hydraulic screw. The colored water

Fig. 20-15. Flow measurement-head-meter using d/p Cell transmitter. (A) Mark one gallon on large tank. (B) Calibrate d/p Cell Oto 1h.gpm. (C) With stopwatch, run for 2 minutes and compare reading with actual flow arter adjusting control valve to aIlow full-scale 1h.-gpmflow. (D) Calculate error, ifany. (E) Repeat at several flow rates.

CONSTRUCnNG AND INSTRUMENTING REAL AND SIMULATED PROCE~SES 429

Fig. 20-16. Flow control usingheadmeasurement.

enters one end and is delayed for a number of seconds-depending on speed of rotation-before it exits at the other end. This unit makes it possible to simulate dead time and capacity as it occurs in many actual process situations. This device represents perhaps the ultimate in educational process units. It does represent a substantial investment. From a practicat point of view, building a unit similar to that shown in Figure 20-14 and making use of available instruments around the plant will provide an adequate teaching tool. A school engagedin teach-

Fig. 20-17. Level control.

430 PROCESSCOMPUTERSAND SIMULATION

Fig. 20-18. Cascadecontrol.

Fig. 20-19. Feedforwardwithout trim.

CONSTRUCTING AND INSTRUMENTING

REAL AND SIMULATED PROCESSES 431

Fig. 20-20. Feedforwardwith trim.

ing process instrumentationand control will find a working loop a most valuable tool. The following problems are intended to stimulate possible uses of a process unit. ProblemI Figure 20-15. Flow measurement-head-meter using d/p Cell transmitter. (A) Mark 1 gallon on large tank. (B) Calibrate d/p Cell Oto 1/2gpm. (C) With stopwatch, rull for 2 minutes and compare reading with actual flow arter adjusting control valve to allow full-scale (1/2gpm) flow. (D) Calculate error, if any. (E) Repeat at several flow rates. Problem2 Having calibrated the flowmeter, put the controller whose output positions the control valve on manual. With the system operating manually, position the valve at 10 percent increments from Oto 100 percent and record the flow rate at each step. Now plot the characteristic curve for the valve and compare the results with those shown in

Chapter 11. Problem3 Bypass the small tank as suggested in Question 20-7 and verify your answer.

432 PROCESSCOMPUTERSAND SIMULATION

Fig. 20-21.Educationalprocesssimulatorunit.

Problem4 Connect the system as shown in Figure 20-17 and carefully adjust the controller. Now use the cascade arrangement shown in Figure 20-18 and repeat the proper adjustment procedure. Explain any differences in results. Problem5 Create a feedforward system as shown in Figure 20-19. Once it is operating properly, adjust the zero on the ftow transmitter to introduce an error. Observe the resulto Repeat the same procedure using the

CONSTRUCTINGAND INSTRUMENTINGREAL AND SIMULATED PROCESSES 433

Fig. 20-22. Schematic-educationalprocessunit.

system shown in Figure 20-20. Note the results and carefully explain any difference. Questions

20-I. A big advantagein simulatinga processis a. Puredeadtime canbe clearly demonstrated b. The noisefactor is eliminated

434 PROCESSCOMPUTERSAND SIMULATION

c. That it is relatively inexpensive and mar be performed on a faster time

base d. That one mar witness every detail of cause and effect 20-2. The major difference between the pneumatic process simulator and the one that is electrically energized is that a. The pneumatic type outperforms the electrical type b. The electrical type outperforms the pneumatic type c. The pneumatic type operates much faster than the electrical d. The electrical type is physically smaller and easier to construct 20-3. The academic basis of all simulation techniques is a. All physical systems behave in essentially the same way with respect to time b. Electrical systems react faster than pneumatic systems c. Pneumatic systems are 3 to 15 times faster than real-time systems d. Electrical simulators react in a square root relationship to an equivalent pneumatic system 20-4. Proportional band has the following scaling factor for almost any process

a. 1 b. O

20-5. a. b. c. d.

c. 10 d. 100

The integral orifice d/p Cell flowmeter has the greatest readability At midscale Within Oto 25 percent of scale Within 25 to 60 percent of scale On the upper 40 percent of scale

20-6. Assuming a properly adjusted controller is controlling a flow process, changes in load-flow rate mar cause instability because a. The loop gain varies with flow rate b. The loop gain varies with valve position c. The location of the flow sensor is incorrect d. Not true. The loop remains stable. 20-7. If the small tank between the control valve and the main tank is bypassed, it becomes impossible to create oscillations or cycling. Why? a. It is similar to a flow process b. It does llot bave enough capacity and resistance elements to create sufficient phase shift c. The gain of the large tank is so small in value that the controller gain is inadequate for oscillation d. The statement is llot true; the system will oscillate vigorously 20-8.. The cascade control system exhibits several advantages,one of which is

CONSTRUCllNG

a. b. c. d.

AND INSTRUMENTING

REAL AND SIMULATED

PROCESSES 435

More efficiency Greaterstability No possibilityof cycling or oscillation Greatereasein adjustment

20-9. The disadvantageof feedforwardwithout feedbacktrim control is a. Nonexistent b. Poor stability c. The errors accumulateand eventuallythe tank eithergoesdry or overflows d. Difficulty in makingadjustments 20-10.The processemployingfeedforwardcontrol with feedbacktrim provides excellentresults but a. Is very difficult to adjust b. Cannotcorrect for bad upsets c. Is very sluggishin its operation d. Must in practicebe a processthat canjustify the expenserequiredto provide this sophisticatedcontrol system

APPENDIX

TableA-I. Unit Conversions ATMOSPHERES-atm x 101.325 x 14.696 x 76.00 x 29.92 x 33.96 x 1.01325 x 1.0332 x 1.0581 x 760

(Standard at sea-Ievel pressure) = Kilopascals (kPa) absolute = Pounds-force per square inch absolute (psia) = Centímetres of mercury (cmHg) at OOC = Inches of mercury (inHg) at O°C = Feet of water (ftH2O) at 68°F = Bars (bar) absolute = Kilograms-force per square centímetre (kg/cm2) absolute = Tons-force per square foot (tonf/ft2) absolute = Torr (torr) (= mmHg at O°C)

BARRELS, LIQUID, U.S.-bbl x 0.11924 = Cubic metres (ma) x 31.5 = U.S. gallons (U.S. gal) líquid BARRELS, PETROLEUM-bbl x 0.15899 = Cubic metres (ma) x 42 = U.S. gallons (U.S. gal) oilBARS-bar x x x x

100 14.504 33.52 29.53

= = = =

Kilopascals (kPa) Pounds-force per square inch (psi) Feet of water (ftH2O) at 6SOF Inches of mercury (inHg) at OOC 436

APPENDlX 437

Table A-I. Unit Conversions (continued) x x x x

1.0197 0.98692 1.0443 750.06

= = = =

Kilograms-force per square centimetre (kg/cm2) Atmospheres (atm) sea-level standard Tons-force per square foot (tonf/fi2) Torr (torr) (= mmHg at O°C)

BRITISH THERMAL x 1055 x 778 x 0.252 x 107.6 x 2.93 x 10-4 x 3.93 X 10-4

UNITS-Btu (See note) = Joules (J) = Foot-pounds-force (fi .Ibt) = Kilocalories (kcal) = Kilogram-force-metres (kgf. m) = Kilowatt-hours (kW .h) = Horsepower-hours (hp .h)

BRITISH THERMAL x 17.58 x 12.97 x 0.02358

UNITS PER MINUTE-Btu/min (See note) = Watts (W) = Foot-pounds-force per second (fi .Ibf/s) = Horsepower (hp)

CENTARES x 1

= Square metres (m2)

CENTIMETRES-cm x 0.3937

= Inches (in)

CENTIMETRES OF MERCURY-cmHg, at O°C x 1.3332 = Kilopascals (kPa) x 0.013332 = Bars (bar) x 0.4468 = Feet of water (fiH2O) at 6SOF x 5.362 = Inches of water (inH2O) at 6SOF x 0.013595 = Kilograms-force per square centimetre (kg/cm2) x 27.85 = Pounds-force per square foot (lbf/fi2) x 0.19337 = Pounds-force per square inch (psi) x 0.013158 = Atmospheres (atm) standard x 10 = Torr (torr) (= mmHg at O°C) CENTIMETRES PER SECOND-crn/s x 1.9685 = Feet per minute (ft/min) x 0.03281 = Feet per second (ft/s) x 0.03600 = Kilometres per hour (km/h) x 0.6000 = Metres per minute (mImin) x 0.02237 = Miles per hour (mph) CUBIC CENTIMETRES-cm3 x 3.5315 x 10-5 = Cubic feet (fi3) x 6.1024 X 10-2 = Cubic inches (in3) x 1.308 x 10~ = Cubic yards (yd") x 2.642 x 10~ = U.S. gallons (U.S. gal) x 2.200 x 10-4 = Imperial gallons (imp gal) x 1.000 x 10-3 = Litres (I) CUBIC FEET-ft3 x 0.02832 x 2.832 x 104

= Cubic metres (m3) = Cubic centimetres (cm")

438 APPENDIX

Table A-I. Unit Conversions (continued) x x x x x

1728 0.03704 7.481 6.229 28.32

= = = = =

Cubic inches (in3) Cubic yards (yd3) U.S. gallons (U .S. gal) Imperial gallons (imp gal) Litres (I)

CUBIC FEET PER MINUTE-cfm x 472.0 = Cubic centímetres per second (cm3/s) x 1.699 = Cubic metres per hour (m3/h) x 0.4720 = Litres per second (l/s) x 0.1247 = U.S. gallons per second (U.S. gps) x 62.30 = Pounds of water per minute (lbH2O/min) at 6SOF CUBIC FEET PER SECON~fs x 0.02832 = Cubic metres per second (m3/s) x 1.699 = Cubic metres per minute (m3/min) x 448.8 = U.S. gallons per minute (U.S. gpm) x 0.6463 = Million U.S. gallons per dar (U .S. gpd) CUBIC INCHES-in3 x 1.6387 X 10-5 x 16.387 x 0.016387 x 5.787 x 10-4 x 2.143 x 10-5 x 4.329 x 10-3 x 3.605 x 10-3

= = = = = = =

Cubic metres (m3) Cubic centímetres (cm3) Litres (I) Cubic feet (ft3) Cubic yards (yd3) U.S. gallons (U.S. gal) Imperial gallons (ímp gal)

CUBIC METRES-m3 x 1000 x 35.315 x 61.024 x 10" x 1.3080 x 264.2 x 220.0

= = = = = =

Litres (I) Cubic feet (ft3) Cubic inches (in3) Cubic yards (yd3) U.S. gallons (U.S. gal) Imperial gallons (imp gal)

CUBIC METRES PER HOUR-m3/h x 0.2778 = Litres per second (l/s) x 2.778 x 10-4 = Cubic metres per second (m3/s) x 4.403 = U.S. gallons per minute (U.S. gpm) CUBIC METRES PER SECOND-m3/s x 3600 = Cubic metres per hour (m3/h) x 15.85 x 103 = U.S. gallons per minute (U.S. gpm) CUBIC YARDS-yd3 x 0.7646 x 764.6 x 7.646 x 105 x 27 x 46,656 x 201.97 x 168.17

= = = = = = =

Cubic metres (m3) Litres (I) Cubic centímetres (cm3) Cubic feet (ft3) Cubic inches (in3) U.S. gallons (U.S. gal) Imperial gallons (imp gal)

APPENDIX 439

Table A-I. Unit Conversions (cQntinued) DEGREES, ANGULAR (O) x 0.017453 = Radians (rad) x 60 = Minutes (') x 3600 = Seconds (") x 1.111 = Grade (gon) DEGREES PER SECOND, ANGULAR (OIs) x 0.017453 = Radians per second (rad/s) x 0.16667 = Revolutions per minute (rImin) x 2.7778 X 10-3 = Revolutions per second (rIs) DRAMS (dr) x 1.7718 x 27.344 x 0.0625

= Grams (g) = Grains (gr) = Ounces (oz)

FATHOMS x 1.8288 x 6

= Metres (m) = Feet (ft)

FEET-ft x x x x

0.3048 30.480 12 0.3333

= = = =

Metres (m) Centimetres (cm) Inches (in) Yards (yd)

FEET OF WATER-ftH2O, at 68°F x 2.984 = Kilopascals (kPa) x 0.02984 = Bars (bar) x 0.8811 = Inches of mercury (inHg) at O°C x 0.03042 = Kilograms-force per square centimetre (kg/cm2) x 62.32 = Pounds-force per square foot (lbt/ft2) x 0.4328 = Pounds-force per square inch (psi) x 0.02945 = Standard atmospheres FEET PER MINUTE-ft/min x 0.5080 = Centimetres per second (cm/s) x 0.01829 = Kilometres per hour (km/h) x 0.3048 = Metres per minute (mImin) x 0.016667 = Feet per second (ft/s) x 0.01136 = Miles per hour (mph) FEET PER SECOND PER SECOND-ft/S2 x 0.3048 = Metres per second per second (m/S2) x 30.48 = Centimetres per second per second (cm/s2) FOOT-POUNDS-FORCE-ft .lbf x 1.356 = Joules (J) x 1.285 x 10-3 = British thermal units (Btu) (see note) x 3.239 x 10-4 = Kilocalories (kcal) x 0.13825 = Kilogram-force-metres (kgf. m) x 5.050 x 10-7 = Horsepower-hours (hp .h) x 3.766 X 10-7 = Kilowatt-hours (kW .h)

440 APPENDIX

TableA-I. Unit Conv~rsions(continued) GALLONS, U.S.-U.S. x 3785.4 x 3.7854 x 3.7854 X 10-3 x 231 x 0.13368 x 4.951 x 10-3 x 8 x 4 x 0.8327 x 8.328 x 8.337

= = = = = = = = = = =

gal Cubic centirnetres (cm3) Litres (I) Cubic metres (m3) Cubic inches (in3) Cubic feet (ft3) Cubic yards (yd3) Pints (pt) Iiquid Quarts (qt) Iiquid Imperial gallons (imp gal) Pounds of water at 60"F in air Pounds of water at 60"F in vacuo

GALLONS, IMPERIAL-imp gal x 4546 = Cubic centimetres (cm3) x 4.546 = Litres (I) x 4.546 x 10-3 = Cubic metres (m3) x 0.16054 = Cubic feet (ft3) x 5.946 x 10-3 = Cubic yards (yd3) x 1.20094 = U.S. gallons (U.S. gal) x 10.000 = Pounds of water at 62°F in air GALLONS, PER MINUTE, U.S.-U.S. gpm x 0.22715 = Cubic metres per hour (m3/h) x 0.06309 = Litres per second (l/s) x 8.021 = Cubic fe et per hour (cfh) x 2.228 x 10-3 = Cubic feet per second (cfs) GRAINS-gr x 0.0648

av. or troy = Grams (g)

GRAINS PER U.S. GALLON-gr/U.S. gal at 60"F x 17.12 = Grams per cubic metre (g/m3) x 17.15 = Parts per million by weight in water x .142.9 = Pounds per million gallons GRAINS PER IMPERIAL GALLON-gr/imp gal at 62°F x 14.25 = Grams per cubic metre (g/m3) x 14.29 = Parts per milIion by weight in water

GRAMS-g x x x x

15.432 0.035274 0.032151 2.2046 x 10-3

GRAMS-FORCE-gf x 9.807 x 10-3

= = = =

Grains (gr) Ounces (oz) av. Ounces (oz) troy Pounds (Ib)

= Newtons (N)

GRAMS-FORCE PER CENTIMETRE-gf/cm x 98.07 = Newtons per metre (N/m) x 5.600 x 10-3 = Pounds-force per inch (Ibti'in)

APPENDIX 441

Table A-I. Unit Conversions (continued) GRAMS PER CUBIC CENTIMETRE-g/cm3 x 62.43 = Pounds per cubic foot (lb/ft3) x 0.03613 = Pounds per cubic inch (lb/in3) GRAMS PER LITRE-g/l x 58.42 = x 8.345 = x 0.06243 = x 1002 = HECTARES-ha x 1.000 x lO' x 1.0764 x 10'

HORSEPOWER-hp x x x x x x x

745.7 0.7457 33,000 550 42.43 10.69 1.0139

HORSEPOWER-hp x 33,480 x 9.809

Grains per U .S. gallon (grIU .S. gal) Pounds per 1000U.S. gallons Pounds per cubic foot (lb/ft3) Parts per million by mass (weight) in water at 600F

= Square metres (m2) = Square feet (ft2) = = = = = = =

Watts (W) Kilowatts (kW) Foot-pounds-force per minute (ft .Ibf/min) Foot-pounds-force per second (ft .Ibf/s) British thermal units per minute (Btu/min) (see note) Kilocalories per minute (kcal/min) Horsepower (metric)

boiler = British thermal units per hour (Btu/h) (see note) = Kilowatts (kW)

HORSEPOWER-HOURS-hp .h x 0.7457 = Kilowatt-hours (kW .h) x 1.976 x 106 = Foot-pounds-force (ft .Ibt) x 2545 = British thermal units (Btu) (see note) x 641.5 = Kilocalories (kcal) x 2.732 x 10' = Kilogram-force-metres (kgf. m) INCHES-in x 2.540

= Centimetres (cm)

INCHES OF MERCURY-inHg at O°C x 3.3864 = Kilopascals (kPa) x 0.03386 = Bars (bar) x 1.135 = Feet of water (ftH2O) at 6SOF x 13.62 = Inches of water (inH2O) at 6SOF x 0.03453 = Kilograms-force per square centimetre (kg/cm2) x 70.73 = Pounds-force per square foot (lbf/ft2) x 0.4912 = Pounds-force per square inch (psi) x 0.03342 = Standard atmospheres INCHES OF WATER-inH2O at 6SOF x 0.2487 = Kilopascals (kPa) x 2.487 x 10-3 = Bars (bar) x 0.07342 = Inches of mercury (inHg) at O°C x 2.535 X 10-3 = Kilograms-force per square centimetre (kg/cm2) x 0.5770 = Ounces-force per square inch (ozf/in2)

442 APPENDIX

Table A-I. Unit Conversions (continued) x 5.193 x 0.03606 x 2.454 x 10-3 JOULES-J x 0.9484 x 10-3 x 0.2390 x 0.7376 x 2.778 X 10-4

KILOGRAMS-kg

x 2.2046 x 1.102 x 10-3

= Pounds-force per square foot (lbf/ft2) = Pounds-force per square inch (psi) = Standard atmospheres = = = =

British thermal units (Btu) (see note) Calories (cal) thermochemical Foot-pounds-force (ft .Ibf) Watt-hours (W .h)

= Pounds (Ib) = Tons (ton) short

KILOGRAMS- FORCE-kgf x 9.807 = Newtons (N) x 2.205 = Pounds-force (Ibf) KILOGRAMS-FORCE PER METRE-kgf/m x 9.807 = Newtons per metre (N/m) x 0.6721 = Pounds-force per foot (Ibf/ft) KILOGRAMS-FORCE x 98.07 x 0.9807 x 32.87 x 28.96 x 2048 x 14.223 x 0.9678

PER SQUARE CENTIMETRE-kg/cm2 = Kilopascals (kPa) = Bars (bar) = Feet of water (ftH2O) at 6SOF = Inches of mercury (inHg) at O°C = Pounds-force per square foot (Ibf/ft2) = Pounds-force per square inch (psi) = Standard atmospheres

KILOGRAMS-FORCE PER SQUARE MILLIMETRE-kgf/mm2 x 9.807 = Megapascals (MPa) x 1.000 x 10. = Kilograms-force per square metre (kgf/m2) KILOMETRES x 27.78 x 0.9113 x 54.68 x 16.667 x 0.539% x 0.6214

PER HOUR-km/h = Centimetres per second (cm/s) = Feet per second (ft/s) = Feet per minute (ft/min) = Metres per minute (mImin) = Intemational knots (kn) = Miles per hour (mph)

KILOMETRES x 0.2778 x 27.78 x 0.9113

PER HOUR PER SECOND--km .h-1 .S-I = Metres per second per second (m/S2) = Centimetres per second per second (cm/s2) = Feet per second per second (ft/S2)

KILOMETRES x 37.28

PER SECOND--km/s = Miles per minute (mi/min)

KILOPASCALS-kPa x loa x 0.1450 x 0.010197

= Pascals (Pa) or newtons per square metre (N/m2) = Pounds-force per square inch (psi) = Kilograms-force per square centimetre (kg/cm2)

APPENDIX 443

Table A-I. Unit Conversions (continued) x 0.2953 x 0.3351 x 4.021

= Inches of mercury (inHg) at 32°F = Feet of water (ftH,O) at 6SOF = Inches of water (inH,O) at 6SOF

KILOWATTS-kW x x x x x

4.425 x 104 737.6 56.90 14.33 1.3410

= = = = =

KILOWATT-HOURS-kW' x 3.6 X 106 = x 2.655 X 106 = x 3413 = x 860 = x 3.671 x 10' = x 1.3410 = KNOTS-kn x 0.5144 x 1.151

Foot-pounds-force per minute (ft .Ibf/min) Foot-pounds-force per second (ft .Ibf/s) British thermal units per minute (Btu/min) (see note) Kilocalories per minute (kcal/min) Horsepower (hp) h Joules (J) Foot-pounds-force (ft .Ibi) British thermal units (Btu) (see note) Kilocalories (kcal) Kilogram-force metres (kgf' m) Horsepower-hours (hp .h)

(International) = Metres per second (mis) = Miles per hour (mph)

LITRES-I x x x x x x

1000 0.035315 61.024 1.308 x 10-3 0.2642 0.2200

= = = = = =

Cubic centimetres (cm3) Cubic feet (ft3) Cubic inches (in3) Cubic yards (yd3) U.S. gallons (U.S. gal) Imperial gallons (imp gal)

LITRES PER MINUTE-l/min x 0.01667 = Litres per second (l/s) x 5.885 x 10-4 = Cubic feet per second (cfs) x 4.403 x 10-3 = U.S. gallons per second (U.S. gal/s) x 3.666 x 10-3 = Imperial gallons per second (imp gal/s) LITRES PER SECOND-l/s x 10-3 = Cubic metres per second (m3/s) x 3.600 = Cubic metres per hour (m3/h) x 60 = Litres per minute (I/min) x 15.85 = U.S. gallons per minute (U.S. gpm) x 13.20 = Imperial gallons per minute (imp gpm)

MEGAPASCALS-MPa x x x x

106 lOS 145.0 0.1020

= = = =

Pascals (Pa) or newtons per square metre (NImI) Kilopascals (kPa) Pounds-force per square inch (psi) Kilograms-force per square millimetre (kgf/mm')

METRES-m x 3.281 x 39.37 x 1.0936

= Feet (ft) = Inches (in) = Yards (yd)

444 APPENDIX

Table A-I. Unit Conversions (continued) METRES PER MINUTE-m/min x 1.6667 = Centimetres per second (cm/s) x 0.0600 = Kilometres per hour (km/h) x 3.281 = Feet per minute (ft/min) x 0.05468 = Feet per second (ftls) x 0.03728 = Miles per hour (mph) METRES PER SECOND-m/s x 3.600 = Kilometres per hour (km/h) x 0.0600 = Kilometres per minute (km/min) x 196.8 = Feet per minute (ft/min) x 3.281 = Feet per second (ftls) x 2.237 = Miles per hour (mph) x 0.03728 = Miles per minute (mi/min) MICROMETRES-¡Jm x 10-8

formerly micron = Metres (m)

MILES-mi x x x x

1.6093 x 10-3 1.6093 5280 1760

= = = =

Metres (m) Kilometres (km) Feet (ft) Yards (yd)

MILES PER HOUR-mph x 44.70 = Centimetres per second (cm/s) x 1.6093 = Kilometres per hour (km/h) x 26.82 = Metres per minute (m/min) x 88 = Feet per minute (ft/min) x 1.4667 = Feet per second (ft/s) x 0.8690 = Intemational knots (kn) MILES PER MINUTE-mi/min x 1.6093 = Kilometres per minute (km/min) x 2682 = Centimetres per second (cm/s) x 88 = Feet per second (ft/s) x 60 = Miles per hour (mph) MINUTES, ANGULAR-(') x 2.909 x 10-4 = Radians (rad)

NEWTONS-N x x x x

0.10197 0.2248 7.233 lOS

= = = =

Kilograms-force (kgi) Pounds-force (Ibi) Poundals Dynes

OUNCES-oz av. x 28.35 x 2.835 x 10-5 x 16 x 437.5 x 0.06250

= = = = =

Grams (g) Tonnes (t) metric ton Drams (dr) av. Grains (gr) Pounds (Ib) av.

APPENDIX 445

Table A-I. Unit Conversions (continued) x 0.9115 x 2.790 X 10-5

= Ounces (oz) troy = Tons (ton) long

OUNCES-oz x 31.103 x 480 x 20 x 0.08333 x 0.06857 x 1.0971

troy

OUNCES-oz x 0.02957 x 1.8046

U.S. fluid = Litres (I) = Cubic inches (in)

= = = = = =

Grams (g) Grains (gr) Pennyweights (dwt) troy Pounds (Ib) troy Pounds (Ib) av. Ounces (oz) av.

OUNCES-FORCE PER SQUARE INCH-ozf/in2 x 43.1 = Pascals (Pa) x 0.06250 = Pounds-force per square inch (psi) x 4.395 = Grams-force per square centimetre (gf/cm2) PARTS PER MILLION BY MASS-mass (weight) in water x 0.9991 = Grams per cubic metre (g/m3) at 15°C x 0.0583 = Grains per U .S. gallon (griU .S. gal) at 600F x 0.0700 = Grains per imperial gallon (gr/imp gal) at 62°F x 8.328 = Pounds per million U.S. gallons at 60°F

PASCALS-PA x x x x

1 1.450 x 10-4 1.0197 x 10-5 10-3

= = = =

Newtons per square metre (N/m2) Pounds-force per square inch (psi) Ki1ograms-force per square centimetre (kg/cm2) Kilopascals (kPa)

PENNYWEIGHTS-dwt troy x 1.5552 = Grams (g) x 24 = Grains (gr) POISES-P x 0.1000 x 100 x 2.0886 X 10-3 x 0.06721

= = = =

Newton-seconds per square metre (N .s/m2) Centipoises (cP) Pound-force-seconds per square foot (Ibf. s/ft2) Pounds per foot second (Ib/fi .s)

POUNDS- FORCE-lbf av. x 4.448 = Newtons (N) x 0.4536 = Kilograms-force (kgt) POUNDS-lb av. x 453.6 x 16 x 256 x 7000 x 5 X 10-4 x 1.2153

= = = = = =

Grams (g) Ounces (oz) av. Drams (dr) av. Grains (gr) Tons (ton) short Pounds (Ib) troy

446 APPENDlX

Table A-I. Unit Conversions (continued) POUNDS-Ib x 373.2 x 12 x 240 x 5760 x 0.8229 x 13.166 x 3.6735 x x 4.1143 x x 3.7324 x

troy

10-' 10-' 10-'

= = = = = = = = =

Grams (g) Ounces (oz) troy Pennyweights (dwt) troy Grains (gr) Pounds (Ib) av. Ounces(oz) av. Tons (ton) lang Tons (ton) short Tonnes (t) metric tons

POUNDS-MASS OF WATER AT 60"F x 453.98 = Cubic centimetres (cm3) x 0.45398 = Litres (I) x 0.01603 = Cubic feet (ft3) x 27.70 = Cubic inches (in3) x 0.1199 = U.S. gallons (U.S. gal) POUNDS OF WATER PER MINUTE AT 60"F x 7.576 = Cubic centimetres per second (cm3/s) x 2.675 x 10-' = Cubic feet per second (cfs) POUNDS PER CUBIC x 16.018 x 0.016018 x 5.787 x 10-'

FOOT-Ib/ft3 = KiIograms per cubic metre (kg/m3) = Grams per cubic centimetre (g/cm3) = Pounds per cubic inch (lb/in3)

POUNDS PER CUBIC x 2.768 x 10' x 27.68 x 1728

INCH-Ib/in3 = KiIograms per cubic metre (kg/m3) = Grams per cubic centimetre (g/cm3) = Pounds per cubic foot (lb/ft3)

POUNDS-FORCE PER FOOT-Ibf/ft x 14.59 = Newtons per metre (N/m) x 1.488 = KiIograms-force per metre (kgf/m) x 14.88 = Grams-force per centimetre (gf/cm) POUNDS-FORCE PER SQUARE FOOT-Ibf/ft' x 47.88 = Pascals (Pa) x 0.01605 = Feet of water (ftH,O) at 68"F x 4.882 x 10-' = KiIograms-force per square centimetre (kg/cm') x 6.944 x 10-3 = Pounds-force per square inch (psi) POUNDS-FORCE PER SQUARE INCH-psi x 6.895 = KiIopascals (kPa) x 0.06805 = Standard atmospheres x 2.311 = Feet of water (ftH,O) at 68"F x 27.73 = Inches of water (inH,O) at 68"F x 2.036 = Inches of mercury (inHg) at O"C x 0.07031 = Kilograms-force per square centimetre (kg/cm")

QUARTS-qtdry x 1101 x 67.20

= Cubic centimetres (cm3) = Cubic inches (in3)

APPENDIX 447

Table A-I. Unit Conversions (còntinued) QUARTS-qt x 946.4 x 57.75

líquid

= Cubic centirnetres (cm3) = Cubic inches (in3)

QUINTALS-obsolete x 100 x 220.46 x 101.28 x 129.54 x 101.41 x 101.47 x 101.43

metric mass term = Kilograms (kg) = Pounds (Ib) U.S. av. = Pounds (Ib) Argentina = Pounds (Ib) Brazil = Pounds (Ib) Chile = Pounds (Ib) Mexico = Pounds (Ib) Pern

RADI ANS-rad x 57.30

= Degrees CO) angular

RADIANS PER SECOND-rad/s x 57.30 = Degrees per second (o/s)angular STANDARD CUBIC FEET PER MINUTE-scfm (at 14.696 psia and 60°F) x 0.4474 = Litres per second (Us) at standard conditions (760 mmHg and x 1.608

O°C) = Cubic metres per hour (m3/h) at standard conditions (760 mmHg and O"C)

STOKES-St x 10-4 x 1.076 x 10-3 TONS-MASS-tonm x 1016 x 2240 x 1.1200

= Square metres per second (mz/s) = Square feet per second (ftz/s) long = Kilograms (kg) = Pounds (Ib) av. = Tons (ton) short

TONNES-t metric ton, millier x 1000 = Kilograms (kg) x 2204.6 = Pounds (Ib) TONNES-FORCE-tf x 980.7

metric ton-force = Newtons (N)

TONS-ton short x 907.2 x 0.9072 x 2000 x 32000 x 2430.6 x 0.8929

= = = = = =

Kilograms (kg) Tonnes (t) Pounds (Ib) av. Ounces (oz) av. Pounds (Ib) troy Tons (ton) long

TONS OF WATER PER 24 HOURS AT 61Y'F x 0.03789 = Cubic metres per hour (m3/h) x 83.33 = Pounds of water per hour (Ib/h HzO) at 61Y'F x 0.1668 = U.S. gallons per minute (U.S. gpm) x 1.338 = Cubic feet per hour (cfh)

448 APPENDIX

Table A-I. Unit Conversions (continued) WATTS-W x 0.05690 x 44.25 x 0.7376 x 1.341 x 10-3 x 0.01433 WATT-HOURS-W' x 3600 x 3.413 x 2655 x 1.341 x 10-3 x 0.860 x 367.1

= = = = =

British thermal units per minute (Btu/min) (see note) Foot-pounds-force per minute (ft .Ibf/roin) Foot-pounds-force per second (ft .Ibf/s) Horsepower (hp) Kilocalories per minute (kcaJ/min)

= = = = = =

Joules (J) British thermal units (Btu) (see note) Foot-pounds-force (fi .Ib!) Horsepower-hours (hp .h) Kilocalories (kcal) Kilogram-force-metres (kgf. m)

NOTE: SIGNIFlCANT FlGURES The precision to which a given conversion factor is known. and its application, determine the number of significant figures which should be used. While many handbooks and standards give factors contained in this table to six or more significant figures, the fact that difIerent sources disagree, in many cases, in the fifth or further figure indicates that four or five significant figures represent the precision for these factors fairly. At present the accuracy of process instrumentation, analog or digital, is in the tenth percent region at best, thus needing only three significant figures. Hence this table is confined to four or five significant figures. The advent of the pocket calculator (and the use of digital computers in process instrumentation) tends to lead to use of as many figures as the calculator will handle. However, when this exceeds the precision of the data, or the accuracy of the application, such a practice is misleading and timewasting. NOTE: BRITISH THERMAL UNIT When making calculations involving Btu it must be remembered that there are several definitions of the Btu. The first three significant figures of the conversion factors given in this table are common to most definitions of the Btu. However, if four or more significant figures are needed in the calculation, the appropriate handbooks and standards should be consulted to be sure the proper definition and factor are being used.

APPENDIX 449

TableA-2. TemperatureConversions F -273.15 -268 -262 -257 -251

-459.67

-246 -240 -234 -229 -223

-410

-218 -212 -207 -201 -196

-360

-190 -184 -179 -173 -169

-310

-273

-459.4

-168 -162 -157 -151 -146

-270

-454 -436 -418 -400 -382

-140 -134 -129 -123 -118

-220

-112 -107 -101 -95.6

-90.0 -84.4 -78.9 -73.3 -67.8 -62.2

-450

-440 -430 -420

-400 -390 -380 -370

-350

-340 -330 -320

-300 -290 -280

-260 -250 -240 -230

-210

-200 -190 -180

-150 -140 -130

-184 -166 -148 -130 -112

-120 -110 -100

-90 -SO -70

-40.0

-40 -30

-28.9 -23.3 -17.8

-274 -256 -238 -220 -202

-170 -160

-56.7 -51.1 -45.6 -34.4

-364 -346 -328 -310 -292

-94 -76 -58 -40 -22

-60 -50

-4

-20

-10

-17.2 -16.7 -16.1 -15.6 -15.0 -14.4 -13.9 -13.3 -12.8 -12.2 -11.7 -11.1 -10.6 -10.0 -9.4 -8.9 -8.3 -7.8 -7.2 -6.7 -6.1 -5.6 -5.0 -4.4 -3.9 -3.3 -2.8 -2.2 -1.7 -1.) -0.6 O 0.6 1.1 1.7

I 1 3 4 5 6 7 8 9 10 11 JZ 13 14 15 16 17 18 19 ZO 11 11 13 14 15 16 17 Z8 29 30 31 31 33 34 35

33.8 35.6 37.4 39.2 41.0 42.8 44.6 46.4 48.2 50.0 51.8 53.6 55.4 57.2 59.0 60.8 62.6 64.4 66.2 68.0 69.8 71.6 73.4 75.2 77.0 78.8 80.6 82.4 84.2 86.0 87.8 89.6 91.4 93.2 95.0

2.2 2.8 3.3 3.9 4.4 5.0 5.6 6.1 6.7 7.2 7.8 8.3 8.9 9.4 10.0

36 37 38 39 40 41 42 43 44 45 46 47 48 49 50

96.8 98.6 100.4 102.2 104.0 105.8 107.6 109.4 111.2 113.0 114.8 116.6 118.4 120.2 ll.O

c 10.6 11.1 11.7 12.2 12.8 13.3 13.9 14.4 15.0 15.6

SI S2 S3 54 SS S6 S7 S8 S9 60

123.8 125.6 127.4 129.2 131.0 132.8 134.6 136.4 138.2 140.0

16.1 61 16.7 62 17.2 63 17.8 64 18.3 6S 18.9 66 19.4 67 20.0 68 20.6 69 21.1 70 21.7 71 22.2 72 22.8 73 23.3 74 23.9 7S 24.4 76 25.0 77 25.6 78 26.1 79 26.7 80 27.2 81 27.8 82 28.3 83 28.9 84 29.4 8S 30.0 86 30.6 87 31.1 88 31.7 89 32.2 90 32.8 91 33.3 92 33.9 93 34.4 94 35.0 9S 35.6 96 36.1 97 36.7 98 37.2 99 37.8 100

141.8 143.6 145.4 147.2 149.0 150.8 152.6 154.4 156.2 158.0 159.8 161.6 1.63.4 ]65.2 167.0 168.8 170.6 172.4 ]74.2 176.0 177.8 ]79.6 181.4 183.2 185.0 186.8 188.6 190.4 192.2 194.0 195.8 197.6 199.4 201.2 203.0 204.8 206.6 208.4 210.2 212.0

F 43

110

49 54

120 130 140 ISO 160 170 180 190 200 210

230 248 266 284 302 320 338 356 374 392 410

100

211

413

104

220

428 446 464 482

60 66 71

77 82 88 93

110 230 116 240 121

250

127 132 138 143 149

260 270 280 290 300

154 160 166 177

310 320 330 340 350

182 188 193 199 204

360 370 380 390 400

210 216 221 227 232

410 420 430

238 243 249 254 260

460 470 480 490 500

171

500 518 536 554 572 590 608 626 644 662 680 698 716 734 752 770 788 806

440

824

450

842 860 878 896 914 932

InterpolationValues

.ln the center column, find the temperature to beconverted. The equivalent temperature is in the left column, if converting to Celsius, and in the right column, if converting to Fahrenheit.

0.56 1.11 1.67 2.22 2.78

1 1 3 4 S

1.8 3.6 5.4 7.2 9.0

3.33 3.89 4.44 5.00 5.56

6 7 8 9 10

10.8 12.6 14.4 16.2 18.0

450 APPENDIX

Table A-2. Temperature Conversions (continued)

543 549 554 560 566

1010 1020 1030 1040 1050

571 577 582 588 593

1060 1070 1080 1090 1100

599 604 610 616 621

1110 1120 1130 1140 1150

627 632 638 643 649

1160 1170 1180 1190 1200

654 660 666 671 677

1210 1220 1230 1240 1250

682 688 693 699 704

1260 1270 1280 1290 1300

710 716 721 727 732

1310 1320 1330 1340 1350

738 743 749 754 760

1360 1370 1380 1390 1400

766 771 777 782 788

1410 1420 1430 1440 1450

793 799

1460 1470 1480 1490 1500

804 810 816

1850 1868 1886 1904 1922 1940 1958 1976 1994 2012 2030 2048 2066 2084 2102 2120 2138 2156 2174 2192 2210 2228 2246 2264 2282 2300 2318 2336 2354 2372 2390 2408 2426 2444 2462 2480 2498 2516 2534 2552 2570 2588 2606 2624 2642 2660 2678 2696 2714 2732

821 827 832 838 843

1510 1520 1530 1540 1550

849 854 860 866 871

1560 1570 1580 1590 1600

877 882 888 893 899

1610 1620 1630 1640 1650

904 910 916 921 927

1660 1670 1680 1690 1700

932 938 943 949 954

1710 1720 1730 1740 1750

960 966 971 977 982

1760 1770 1780 1790 1800

988 993

1010

1810 1820 1830 1840 1850

1016 1021" 1027 1032 1038

1860 1870 1880 1890 1900

1043 1049 1054 1060 1066

1910 1920 1930 1940 1950

1071 1077 1082 1088 1093

1960 1970 1980 1990 2000

999 1004

2750 2768 2786 2804 2822 2840 2858 2876 2894 2912 2930 2948 2966 2984 3002 3020 3038 3056 3074 3092

1099 1104 1110 1116 1121 1127 1132 1138 1143 1149 1154 1160 1166 1171 1177 1182 1188 1193 1199 1204 1210 1216 1221 1227 1232 1238 1243 1249 1254 1260 1266 1271 1277 1282 1288 1293 1299 1304 1310 1316 1321 1327 1332 1338 1343 1349 1354 1360 1366 1371

3110

3128 3146 3164 3182 3200 3218 3236 3254 3272 3290 3308 3326 3344 3362 3380 3398 3416 3434 3452 3470 3488 3506 3524 3542 3560 3578 3596 3614 3632

c 2010 2020 2030 2040 2050 2060 2070 2080 2090 2100 2110 2120 2130 2140 2150 2160 2170 2180 2190 2200 2210 2220 2230 2240 2250 2260 2270 2280 2290 2300 2310 2320 2330 2340 2350 2360 2370 2380 2390 2400 2410 2420 2430 2440 2450 2460 2470 2480 2490 2500

3650 3668 3686 3704 3722 3740 3758 3776 3794 3812 3830 3848 3866 3884 3902 3920 3938 3956 3974 3992 4010 4028 4046 4064 4082 4100 4118

4136 4154 4172 4190 4208 4226 4244 4262 4280 4298 4316 4334 4352 4370 4388 4406 4424 4442 4460 4478 4496 4514 4532

1377 1382 1388 1393 1399

2510 2520 2530 2540 2550

1404 1410 1416

2560 2570 2580 2590

1421 1427

2600

1432 1438 1443 1449 1454

2610 2620 2630 2640 2650

1460 1466

2660 2670 2680 2690 2700

1471 1477 1482 1488 1493 1499 1504

2710 2720 2730 2740 2750

1510 1516 1521 1527 1532 1538

2760 2770 2780 2790 2800

1543 1549 1554 1560 1566

2810 2820 2830 2840 2850

1571 1577 1582 1588 1593

2860 2870 2880 2890 2900

1599 1604 1610 1616

1621

2910 2920 2930 2940 2950

1627 1632 1638 1643 1649

2960 2970 2980 2990 3000

4550 4568 4586 4604 4622 4640 4658 4676 4694 4712 4730 4748 4766 4784 4802 4820 4838 4856 4874 4892 4910 4928 4946 4964 4982 5000 5018 5036 5054 5072 5090 5108 5126 5144 5162 5180 5198 5216 5234 5252 5270 5288 5306 5324 5342 5360 5378 5396 5414 5432

TEMPERATURECONVERS/ON FORMULAS DEGREESCELS/US

(FORMERLY CENT/GRAVE)C

DEGREES FAHRENHEIT-F

C + 273.15 = K Kelvin (C x 9/.,) + 32 = F Fahrenheit C x 4/, = R Réaumur

F + 459.67 = Rankine (F -32) x 'I, = C Celsius (F -32) x 'I, = R Réaumur

DEGREES

RÉAUMUR-R R x 'I. ~ C Celsius (R x '/.) + 32 = F Fahrenheit

APPENDIX 451

TableA-J. ApproximateSpecific Gravities of Some CommonLiquids under Normal Conditionsof Pressureand Temperature Specific

Liquid

Gravity

Acid Hydrochloric, 31.5% Muriatic, 40% Nitric,91% Sulphuric, 87% Sulphuric, 100% Alcohol Ethyl, 100% Methyl, 100% Benzine Chlorofonn Com Syrup Crude Oil

Ether Ethylene Glycol Fish and Animal Oils

Freon Fuel Oils

Gasoline Glycerine, 100%

Kerosene Lubricating Oils Milk

Mercury Molasses

Tar Vamish Vegetable Oils

Water Water at l00'C Water, Ice Water, Sea

1.05 1.20 1.50 1.80 1.83 0.79 0.80 0.73-0.75 1.50 1.40-1.47 0.78-0.92 0.74 1.125 0.88-0.96 1.37-1.49 0.82-0.95 0.68-0.75 1.26 0.78-0.82 0.88-0.94 1.02-1.05 13.546 1.40-1.49 1.07-1.30 0.9 0.90-0.98 1.0 0.96 0.88-0.92 1.02-1.03

ll~

452 APPENDIX

TableA-4. StandardDimensionsfor Weldedor SeamlessSteelPipe INTERNAL DIAMETER

Nominal Pipe Size

lnches

mm Sch lO

mm Sch 40

mm Sch 80

~ Y4

.405

10.29 .540 13.72 .675

17.15

* lV4

.840

21.34 1.050 26.67 1.315 33.40 1.660

42.16 1!12

2 21-2

3 4

1.900

.410

.269

6.83 .364

10.41

9.25

.545 13.84

.493 12.52

.674

.622

17.12

15.80

.884 22.45

20.93

1.097 27.86 1.442

36.63 1.682

.824

1.049 26.64 1.380 35.05

1.610

48.26 2.375

42.72

60.33

54.79

52.50

2.875

2.635 66.93

2.469 62.71 3.068

73.03 3.500 88.90 4.500 114.3 6.625

168.3

8.625

219.1 10.750

.307 7.80

273.1 12.750 323.9

2.157

3.260

82.80 4.260 108.2 6.357 161.5 8.329

211.6 10.420 264.7

12.390 314.7

40.89

2.067

77.93 4.026

102.3 6.065 154.1

7.981 202.7 10.020 254.5 11.938

303.2

.215 5.46 .302 7.67 .423 10.74 .546 13.87 .742 18.85 .957 24.31 1.278 32.46 1.500 38.10 1.939 49.25 2.323 59.00 2.900 73.66 3.826 97.18 5.761 146.3 7.625 193.7 9.564 242.9 11.376 289.0

Threads Per

Nominal

lnch

Ib 1ft

Weight

0.244

0..424

18 14

ll~

1.678

III-?

2.272

11\-7.

2.717 3.652

8 8

8 8 8

28.554

40.483

APPENDIX 453

TableA-S. Propertiesof SaturatedSteamand SaturatedWater

P,." ,,',

Tem, F

En.."B'"'lbm.' En'..'.Blo/lbmW,I,'

En'h,'p"B'w'bm

Vol.molt'/lbm

W...,

Sloom

---

W.,.,I "

"oa.' '00'.' '000.0 '70aO '500.0

705.'7 700.0 005." oao.o OOa.ll

0.0507a 0.0'00' o.o,.,a 0.0'037 0.O'a50

0.00000 0.O'a57 0.0507' o.oaoao 0.10'00

0.0507S 0.07510 0.OS500 0,11117 O.I'OOS

000.0 S22.' SOI.S 75S.5 7".7

'305.7 '050.0 '000.0 17aO.0 15'3.'

000.0 0'0.0 035.ao 0'0.0 000.0

0.O'70a 0.0'505 0.0'505 0.0"00 0.0'30'

0.11003 0.15"7 0.10'00 0.10015 0."3a.

0.1"31 0.IS021 0.ISS31 0.220S1 0.207'7

1500.0 "'0.17 "00.0 l133.3a 1000.0

500.'0 5ao.0 507.10 500.0 5".5a

0.0'3'0 0.0"70 0.0"3' 0.0"07 0.0"50

0.'537' 0.'0037 0."013 0.30507 0""30

00'.70 al'.53 aoo.o oao.ao 000.0

5'0.0 5'0.0 5la." 500.0 .ao.,o

0.0"'0 0.0'001 0.O'Oa7 0.0'0'3 0.0'013

500.15 500.0 '00.a7 '00.0 3al.5'

.ao.o '07.01 '00.0 "'.00 "0.0

'Oa.7aO 300.0 '50.0 "7.'50 '00.0

S",m

'I'I

0.0 172.7 2IS.' "0.' '01.0

000.0 005.2 1020.' I06S.5 100'.'

1.0012 0.0001 0.072S 0.0'05 0.0130

0.0000 0.1'00 O.ISOI 0.2720 0.3206

1.0012 1.1'00 1.1010 1.20S0 1.23'5

S75.0 S01.5 7S2.S 7".2 71S.5

S75.0 052.2 07'.1 1012.S 1032.0

71'.0 070.1 072.1 0'0.0 017.1

302.1 '5'.0 '00.2 500.3 550.0

1107.0 1133.7 113S.3 1153.2 1107.7

0.SO05 O.SOSO 0.S025 O.S'O' 0.SI3'

0.3502 0."3' 0.'250 O'OSO 0.5100

1.2'OS 1.2S21 1.2SSI 1.3002 '.3"0

702.S 000.2 002.0 O'S.S 0'0.'

10'3.0 1005.0 100S.0 IOSO.2 1001..

0.27710 0.32210 0.'02'5 0.'S71. 0."500

011.7 5S0.1 5710 502' 5'2.0

55S.' 5S0.0 013.0 025.' 050.'

1170.1 1170.0 IIS'.S IIS7.7 1102.0

0.SOS5 0.7S70 0771' 0.7025 0.7'"

0.52SS 0.507' 0.5000 0.01'2 0.0'70

1."7' 1.'550 ,..OS. 1.3757 1.'010

005.2 5S'.5 500.0 557.S 53S.0

100'.1 1000.0 IlO'.' 1100.5 1110"

0."307 0.53aO' 0.5.aoO 0.05..a 0.7'00'

0.'0513 0.55050 0.50S00 0.07'02 0.70075

530.S 512.0 500.S 'S7.0 '71.7

057.5 OS7.0 OSO.O 71'.3 732.0

110'.3 1100.0 llOO.' 1202.2 1203.7

0.737S 0.7133 0.7111 O.OSOO 0.0723

0.0577 0.7013 0.7051 0.7"3 0.773S

1.305' 1.".0 1."03 1.'333 1."01

532.0 50S.S 500.7 'S5.' '00.5

1111.' 1115.0 1115.2 1117.2 IIIS.2

0.0'000 0.01075 0.01001 0.0103' 0.010'0

0.70710 0.007a7 0.07'0' '.1"0 1.1070

0.S1717 0.02702 0.00'2' 1.010 1.2100

.0..5 "0.5 "'.5 .2..2 "0.0

730.. 755.1 703.2 7S0.' 7S5.'

120'.1 120'.7 120'.S 120'.0 120'.'

O.OO'S 0.0'00 0.0'05 0.0217 0.0101

0.7S71 O.S"S 0.S200 0.S030 0.S720

1.'5IS 1.'030 '.'70' 1.'S'7 I.'SOO

'02.' "7.7 '30.S '22.7 .,70

IIIS.5 IIIS.S IIIS.O IIIS.7 IIIS.5

"0.0 "7.'5 '00.07 '00.0 3al.aO

O.OlaO' o.olaao 0.01a05 O.OlaO' 0.01a30

I..aoa I.5'3a I.a,.5 I.a... '.,oao

1.'007 1.5'27 I.S'32 I.S030 2.2S73

300.0 30'.0 370.1 375.1 355.5

S06.2 SOS.O S25.0 S25.0 S'2S

1203.1 '202.0 1201.1 1201.0 IIOS.3

0.5015 0.5SS2 0.5070 0.5007 0.5'3S

0.0105 0.0223 005S5 0.0007 1.0010

1.50S0 1.5105 1.520' 1.527' 1.5.5.

305.S 302.0 375.3 37'.3 35'.S

1117.5 1117.2 11\5.S 1115.7 1113.7

105.7'0 153.010 150.0 "0.0 117.00'

3aO.0 300.0 35a." 3".'7 3'0.0

0.Ola30 o.olal l o.olaoo 0.017aO 0.017a7

'.3170 '030' '.005a 3.7007 3.7000

2.3353 2.0573 3.0130 3.7275 3.7S7S

3530 332.3 330.0 312.0 311.3

S".5 S02.1 S03.' S77S S7S.S

IIOS.O IlO'.' 110'.1 1190.' 1100.1

0.5"0 0.5101 0.51" 0.'010 0.'002

1.0057 1.05'7 1.055' 1.0000 1.0000

1.5'73 1.507S 1.5005 1.5S70 1.5S02

352.0 331.S 330.1 312.2 310.0

1113.5 1110.0 1110.' 1107.. 1107.'

100.0 aO.O'3 ao.o 70.0 07.005

3'7.a, 3'0.0 "'.0' 30'.03 300.0

0.0177' 0.01700 0.01757 0.Ol7.a 0.017'5

'."33 '.aool 5.'530 0.Ia7" 0...a3

'.'310 '.013S 5.'711 0.2050 0.'05S

20S.5 200.' 2S2.' 272.7 200.7

SSS.O SO'.S 000.0 007.S 010.0"

IIS7.2 IIS5.2 IIS3.1 IISO.O 170.7

0.'7'3 0..0.0 0.'53' 0."" 0.'372

1.12S' 1.1'77 1.1075 1.1005 1.1070

1.0027 1.0110 1.020S 1.0310 1.0351

20S.2 200.1 2SI.0 272.5 200.5

1105.2 1103.7 1102.1 1100.2 1000.0

00.0 50.0 '0.'00 '0.0 35."7

'0'.71 'al.o' 'ao.o '07.'5 '00.0

0.01 73a3 0.017'7' 0.017'0' 0.017151 0.0170aO

7.150' a.'007 a.O'07 10...0 11.7'5

7.1730 S.51'0 SO'30 10.'00 11.702

202.2 250.2 2'0.2 230.1 22S.S

015.' 023.0 02'.0 033.0 03S.0

1177.0 117'.1 1173.S IIOO.S 1107.'

0.'273 0."'2 O.'OOS 03021 0.3S10

1.2107 1.2.7. 1.2501 1.2S" 1.30'3

1.0"0 1.05S0 1.0500 1.0705 I.OS02

202.0 250.1 2'0.1 230.0 22S.0

100S.0 1005.3 1005.1 1002.1 1000.3

30.0 '5.0 ".ooa '0.0 l7.laO

'50.3' "0.07 "0.0 "7.00 "0.0

0.017000 0.0100'7 0.0100'0 0.OlOa3' 0.010775

13.7'7 lo.,a. 10.30' '0.070 '3.131

13"" 10.301 10.321 20.0S7 23.I'S

21S.0 20S.52 20S.'5 100.27 ISS..3

0'5.2 052.1 052.1 000.1 005.2

110'.1 1100.0 1100.0 1150.3 1153.'

0.30S2 0.3535 0.3533 0.335S 0.32"

1.3313 13007 1.3000 1.3002 1.'201

1.0005 '.71" 171'2 1.7320 1.7"2

2IS.S 20S.' 20S.3 100.21 ISS.IS

IOS7.0 IOS5.2 IOS5.2 "OS2.0 1070.S

15.0 ,...00 11.5'0 10.0 a.o

"3.03 "'.00 '00.0 103." la'.ao

0.0107'0 0.010710 0.010037 0.01050' 0.0105'7

'0.'7' 'O.7a' 33.0" 3a..0' '7."a

20.200 20.700 33.030 3S.'20 .7.3.5

ISI.21 ISO.17 10S.00 101.20 150.S7

000.7 070.3 077.0 OS2.1 OSS5

1150.0 1150.5 1"0.0 1"3.3 1130.3

0.3137 0.3121 0..0.0 0.2S30 0.2070

1."'5 1."'7 1.'S2' 150'3 I 53S'

1.7552 1.750S 1.770' 1.7S70 I.S060

ISI.IO ISOl2 IOS.05 10,...3 150.S'

1077.0 1077.0 107'.2 1072.3 1000.2

7.5110 0.0 5.0 ..7'" .."

lao.o 170.05 10'." 160.0 15'.00

0.010510 0.010'51 0.010'07 0.010305. 0.Ol035a

50.'Oa 01.007 73.515 77.'7 00.03

50.225 OI.OS' 73.532 77..0 00.0'

"S.OO 13S.03 130.20 127.00 120.02

000.2 000.2 1000.0 1002.2 IODO.'

113S.2 113... 1131.1 1130.2 1127.'

0.2031 0.2'7' 0.23'0 0.2313 0.2100

1.5'SO 1.5S20 1.000' 1.017' 1.0'2S

I.SIII IS20. I.S"3 I.S'S7 IS020

"7,OS 13S.01 130.IS 127.0' 120.00

100S.' 1005.' 1003.1 1002.' 1060.2

3.0 '.aao' '.0 1.00'7 1.0

"'..7 "0.0 "0.07 "0.0 101.7'

0.010300 0.010'0' 0.010'30 0.010'0' 0.010130

0.0'0" 0.500a3 0.'501' 0.1"03 0.oaa05

100.0 ao.o 00.0 '0.0 32.01 a

0.010130 0.01007' 0.010033 0.010010 0.0100"

lla.71 l ".oa 173.7' '03.'5 333.50 350.' 03'.3 "07.0 "'5.a 330'.'

IIS.73

100.'2

1013.2

1122.0

0.2000

1.0S5'

I.SSO'

100."

1050.7

123.00 173.70 203.20 333.00

107.05 0'.03 S7.07 00.732

1014.0 1022.1 1025.0 10'0.1

1122.0 1110.. 1113.0 1105.S

0.IOS5 0.1750 0.10'0 0.1320

1.0010 1.7'50 1.7003 I.S'55

I.SS05 1.0200 1.0330 1.07S'

107.0' 0'.03 S7.00 00.73

1050.2 I 1051.S; 10'0.0 I 10...1.1

1037.1 I04S.' 1050.7 1071.0 1075.5

1105.1 1000.' IOS7.7 1070.0 1075.5

0.1205 0.0032 0.0555 0.0102 0.0000

I.S530 1.0'20 2.0301 2.1'32 2.IS72

I.OS25 2.0350 2.00'0 2.!50' 2.IS72

350.' 033.3 1207.0 2..5.. 3302.'

07.000 'S.037 2S.000 S.027 0.0003

OS.OO 'S.030 2S.000 S.027 0.000

10'3.5 1037.0 1030.5 102'.0 1021.2

454 APPENDlX

Table A-6. Resistance Values of Copper Wire and Thennocouple Extension Wire RESISTANCEVALUESFOR SOLID ROUND ANNEALED COPPERWIRESAT 20 DEGREESCELSIUS Number Resistance American Ohms per Wire Gauge 1000 Feet 30

103.2

81.8 64.9 51.5 40.8 32.4 25.7 20.4 16.1 12.8 10.2 8.05 6.39 5.06 4.02 3.18 2.53

28 27 26 25 24 23

22 21 20 19 18 17 16 15 14

RES/STANCE CONVERS/ON R, = Ro[/ + a (t -to)] R, = Resistance at operating temperature, t Ro = Resistance at a known temperature, to t = Operating temperature to = Temperature for a known resistance and a a = Temperature coefficient of resistance at 10 (0.00393 per degree C)

fIC 282204

APPENDIX 455

TableA-6. (continued)ResistanceValuesof Thermocoupleand DuplexExtension Wire (Ohms/ftat 70°F) Gauge

(J)

CIA (K)

CRIC

CUIC

0.009

0.011 0.027 0.044 0.087

24 28

0.005 0.014 0.022 0.043 0.054 0.089 0.137 0.221 0.350 0.550 0.87 2.261

1.49 3.81

3.568

6.05

6 8 II 12

14 16

20 22

Diameter 0.020 0.022 0.024

0.023 0.037 0.074 0.095 0.147 0.234 0.380 0.586 0.940

0.112

(T)

0.047 0.074

0.175

0.279

0.117

0.448 0.706 1.120 1.77 4.55 7.23

0.190 0.297 0.457 0.754

1.92 3.04

PLT/PLT +

PLTIPLT + IO%RH. (5)

/3% RHo (R)

0.46 0.38 0.32.

0.48 0.39 0.33

TableA.7. Velocity and PressureDrop throughPipe (Air) FLOW RATE (cfm)

AP (PER /00 fI)

FLOW RATE (cfm)

[" Pipe

%" Pipe

0.769 1.282 2.563 3.204 4.486

5.767 7.690 10.25 12.82 19.22

AP (PER 100 fI)

0.037 0.094 0.345 0.526 1.0 1.62 2.85

12.8222 19.

4.96

28.84

7.69 17.0

35. 24

4.87 10.8 16.0

44.87

25.8

3. 4. 486408971 6.

0.029 0.156 0.293 0.578 1.10

2.21

456 APPENDIX

Table A-7. Velocity andPressure Drop through Pipe (Air) (continued) FLOW RATE (cim)

I1P (PER 100ft)

FLOW RATE (cim)

2" Pipe

J !;2" Pipe

4.486 7. 690 Il. 53

22.43 28.84 41. 65

54.4708 64. 89.71 115.3

0.035 0.094 0.203 0.727 1.19 2.42 4.09 5.61 10.9

121.8

18.0

166.6

25.63

38.45 48.06 60.88

1.40

76.90

2.21

54.47 70.49

96.12 121.8 166.6 230.7 448.6 769

166.6 205.1

384.5 576.7 897.1 1410 1794 2307 3332

5.47

10.1

57.67 76.9 102.5 128.2 179.4 256.3 512.6 897.1 1410 1794

6" Pipe

121.8

3.90

102.5

4" Pipe

0.045 0.090 0.151 0.248 0.451 0.715 1.32 2.50 9.23 27.1

41.65

0.036 0.107 0.264 0.573 0.887

8.971 16.02

3" Pipe 28.84

~P (PER 100 fI)

0.042 0.073 0.127 0.197 0.377 0.757 2.94 8.94 22.2 36.0 8" Pipe

0.023 0.041 0.061 0.204 0.450

1.07 2.62 4.21

6.% 14.5

256.3 448.6 576.7 897.1 1153 1538 1794

2307 2820 3588

0.023 0.068 0.111 0.262 0.427 0.753 1.02 1.68 2.50 4.04

FLOW 10"

APPENDIX 457

Table A-7. Velocity and Pressure Drop through Pipe (Air) (continued) ~P (PER 100 fI)

RATE (cfm)

FLOW RATE (cIm) /2" Pipe

Pipe

0.022 0.043 0.082 0.164 0.234 0.364 0.520 0.918 1.25 1.42

448.6 640.8 897.1 1282 1538 1922 2307 3076 3588 3845

AP (PER 100 fI)

640.8 769.0 1025 1282 1538 1794 2051 2563 3076 3588

0.018 0.025 0.044 0.067 0.096 0.129 0.167 0.260 0.371

0.505

STEAM OR VAPOR FLOW Determination of pressure loss through schedule-40 pipe for a steam or vapor can be accomplished by calculating the equivalent liquid velocity. Velocity (feet per second) = (4.245)(W)(v)

D' x 1000

W = Flow rate (pounds per botir) D = Nominal pipe diameter (inches) v = Specific volume (cubic feet per pound) By determining the velocity, pressure loss can be found by referring to the tables for liquid losses. E.g., if a 3-inch pipe is used, and the equivalent liquid velocity is 8.68 feet per second, the pressure loss is 3.7 psi/lOOfeet. A/R FLOW Following is a tabulation of pressure dropper 100feet of schedule-40 pipe for air at 100 psi and 6ffF. Note: lf air at temperatures other than 6ffF or pressure other than 100 psi is used, the pressure drop can be determined by multiplying the values given in the table by 100+14.7 P + 14.7

460+t -s;:o

where Pis the actual pressure in psi and t is the actual temperature in degreesFahrenheit. Likewise, if the fluid is Dot air and has a specific gravity other than 1.0, multiply the pressure drop by fo' where G is the actual specific gravity.

lill 35.

460 APPENDlX

Table A-lO. Thermocouple Temperature/mV Data For Platinum-6% Rhodium Ys. Platinum-30% Rhodium Thermocouples, Type B Based on International Practical Temperature Scale of 1968 (IPTS-68) Reference Junction: At 32°F, mV = O Temperature in Degrees Fahrenheit Ys. Absolute mV °F

o 10 20 JO

0.00' 0.004 0.002 0.000 I

-0.001

so .0

-0.002 -0.002

-0.003

-0.002

0.002

,'O '20

0.000

-0.002

'00

-0.00'

'30

0.00.

'.0

0.00.

'SO l

'.0

0.00. 0.0'2

'70

O.O'S

'SO

0.0"

0.023

0.027

22. 23' 2'. 25. 26. !

0.0'7 0.0.'

0.0.'

0.0'2

0.07S

'3..

520 5~g

530 5.0

550 5.0 I 570 5'0

O.OS'

3..

37.

O.O.S

0.0.'

O.OSS

27. 2R' 29'

5'" I

3'.

..,(;S

468 APPENDIX

Table A.18. Thermocouple Temperature/mV Data For Copper vs. Copper-Nickel (Copper-Constantan) Thermocouples, Type T Based on International Practical Temperature Scale of 1968 (IPfS-68) Reference Junction: At 32°F, mV = O Temperature in Degrees Fahrenheit vs. Absolute mV o, .V 50 0.301

-6.10S -6.0S3 -S.99S -S.930 -S..60

-'S. -140 -130 -320 -110 -30. -Z90

5.J"

_c - 5..240

."6. -

-4.' ;TJ -4.' -4.' _19

)10 )l.

7.775

)50

8.00l

)00 )7.

8.)50 8.0.1

18.

8.'))

)'.

'.ll7

.lO .). ..0

.50

-"-I l l

11.Ol7

.00

Il.)))

5.. Sl. .1.

ll.S7l l).l.. li

')0

l).SIO

.7. I.'".'.0" 11.0.. '.'0'S.SSO ,.360

Il.'.. ...ll.l~.

200 70.

,."

7..'.

..0 .10

. 1.067'.llS . ,, ;.01' , ,

,.7'0

O.'l. 7.l07

)). ).0

2.711 2.050 3.20" 3.05' 3.711

,..250 !,. 270 '

-"SO -4.''9'

5."

1).834

Reference Junction: At O°C, mV = o Temperature in Degrees Celsius vs. Absolute mV O( I

,-l''' _"" -l"

-3..'. -J"'J -3.7"

-lO' -3.'" -100

007 950

059

1.° 'OS

-4.'

1.510 1.752 1.0.' 2.2'" '.0.7

20. 210 '20 23. '00

5.1J5 5.025 '.912

-21.

100 1\0 120 130 '00 150 ,.0 170 \'0 100

-S.70' -S.70S -S.620 -S.S1Z -S.439

-".. -Z7.--Z40 -Z1. -"Z.

0.." 0..30 1.0.0 1.2.'

mV 0.0.7

0..20

-400 -190 .'.0 -170 -160

.0 70 .0 00

., .)00

0.120

mV -6.2S4 -6.240 -6.217 -6.1.7 -6.1S0

0.'2'O.T2'

°F -4S0 -.40 -430 -420 -410

-3.378

'OC

30 35

l.l'b 1.403

40 45 50

l.bll 1.822 2.035

IBO IB' lon lOS

5' bn b5 70 7'

2.250 2.4b7 2.b87 2.'0. 3.131

80 ., .n ., 100

3.357 3.584 3..13 4.044 4.277

105 110 li' 120 12'

4.512 4.74' 4."7 5.227 5.4b'

25" 12.291 ?o 12.512 265 Il..S. l10 13.131 l1S 13.4l\

130 135 140 145 l"

5.712 5."7 b.204 b.4'2 b.70i'

l.O 13.101 l.' 13.003 lOO 14.l01 lO' 1..510 30. 14...0

15' 160 lb5 170 175

b..54 7.207 7.4b2 7.71. 7.'75

305 IS.ISI 310 15..43 315 15.13. 320 1..030 3.5 16.3l5

B.l3S B.40S '.151 O.Oll

?no O.l.'

?OS 0.553 llO O.BlO lIS 10.000 ?lO 10'3.0 n, 10.63l I ,

?30 ío.oo, 23S l'.IB. ?4' 11.456 24' 11.133 250 12.011

\3. l

APPENDlX 469

Table A-19. Thermocouple Temperature/mV Data For Nickel-Chromiul:i1 vs. Copper-Nickel (Chromel-Constantan) Thermocouples, Type E Based on Intemational Practical Temperature Scale of 1968 (IPTS-68) Reference Junction: At DoC,m V = O Temperature in Degrees Celsius vs. Absolute mV ."

1\0 90 100

4.9.3 5,'4' '.311

l1Ò I?O

'.99' 1...3 '.0'0 0.3'" \..

'S. ".'8',.. )'. '..501 II.nZ ,.,

1 Il.oS' 1,.'" 13.'"

"" '""

?l. ll'

".'0' ".,"

l' U

IS...1

Z.. Z'O ZSO

17.17. 117.9'Z

'7'~ Z.O 200

/'O...' ZO.Z5.

)00

21.0),

)10

2'.."

)20

33.

2Z.S01

23.303 3'. 2'.17)35.

2..'61 36. 370

3eo 300 ..0 .10

25.75' 26.5"

1 .7.3.5 "e.l.3

.e.O.3

...30.5..

'0.7..

472 APPENDIX

Table A-22. Platinum RTD Temperature/ResistanceData Calculated from DIN 43760 Platinum RTD Curve Data (Foxboro PR 239) Degrees Fahrenheit vs. Absolute Ohms These tables show the value of resistance (in Absolute Ohms) between the black and white terminals or leads of RTD type sensors at different temperatures (in degrees Fahrenheit). "F

Ohm

-360

-330 -320 -310

1250 1260 1270 1280 1290

337.95 339.68 341.41 343.14 344.97

-300 -290 .280 -270 -260

1300 1310 1320 1330 1340

346.59 348.30 350.01 351.72 353.43

-250 -240 -230 -220 -210

1350 1360 1370 1380 1390

355.13 356.83 358.52 360.21 361.90

-200

1400 1410 1420 14301440

363.59 365.27 366.95 368.62 370.29

1450 1460 1470 1480 1490

371.95 373.62 375.28 376.94 378.59

1500 1510 1520 1530 1540

380.24 381.88 383.52 385.16 386.80

-350 -340

-190 -180 -170 -160 -150 -140 -130 -120 -110 -100

-90 -80 -70 -60

-50 -40 -30 -20 -10

O 10

20 30

115501388.421 11560 1390.051

APPENDIX 473

Table A-23 CURVE CR-228 FOR COPPER RTDs. FAHRENHEIT TEMPERATURE VS ABSOLUTE OHMS

Deg F

o 10

20 30 40

50 60 70 77

80 90 100

Deg C

o 5 10 15

20 25 30

35 40 45 50

Ohms

8.359 8.573 8.787 9.000 9.215 9.428 9.642 9.856 10.005 10.070 10.284 10.498

Deg F

Ohms

Deg F

Ohms

110 120 130 140

10.712 10.926 11.140 11.354 11.568 11.782 11.996

210 220 230 240 250 260 270

12.852 13.066 13.280 13.494 13.708 13.922 14.136

12.210 12.424 12.638

280 290 300

14.350 14.564 14.778

150 160 170

180 190

200

CURVECR-229FOR COPPERRTDs. CELSIUSTEMPERATURE VS ABSOLUTEOHMS Ohms Deg C Ohms Deg C 9.042 9.235 9.428 9.620 9.813 10.005

10.198 10.390 10.583 10.775 10.968

55 60

65 70

11.160 11.353 11.546 11.73911.931

105 110 115 120 125

13.086 13.279 13.472 13.665 13.857

12.124 12.316

130 135 140 145 150

14.050 14.242 14.435 14.627 14.820

75 80 85 90 95 100

One absolute Ohm equals 0.999505 international ohm.

Ohms

12.509 12.701 12.894

474

APPENDIX

Table A-24

-2IS.0 -212.S -210.0 -207.S -20S.0 -202.S -200.0 -197.S -19S.0 -192.S -190.0 -187.S -18S.0 -182.S -ISO.O -177.S -17S.0 -172.S -170.0 -167.S -16S.0 -162.S -160.0 -IS7.S -ISS.O -IS2.S -ISO.O -147.S -14S.0 -142.S -140.0 -137.S -13S.0 -132.S -130.0 -127.S -12S.0 -122.S -120.0 -¡17.S -IIS.O

155.297 156.047 156.802 157.560 158.322 159.087 159.856 160.629 161.405 162.186 162.970 163.757 164.549 165.344 166.144 166.947 167.754 168.565 169.380 170.199 171.022 171.848 172.679 173.514 174.353 175.196 176.042 176.893 177.749 178.608 179.471 180.339 181.211 182.087 182.967 183.851 184.740 185.633 186.531 187.433 188.339

-112,S

189.249

-110.0

190.164

-107.S -IOS.O -102.S

191.083

-100.0

193.868 194.805

-97.S -9S.0 -92.S -90.0 -87.S -8S.0 -82.S -80.0 -77.S -7S.0 -72.S -70.0 -67.S -6S.0 -62.S -60.0 -S7.S -SS.O -S2.S -SO.O -47.S -4S.0 -42.S -40.0 -37.S -3S.0 -32.S -30.0 -27.S -2S.0 -22.S -20.0 -17.S -IS.O -12.S -10.0 -7.S -S.O -2.S

235.116

+2.5 S.O

236.253 237.395 238.543 239.696 240.855 242.019 243.189 244.364 245.546 246.733 247.926 249.124 250.328 251.539 252.755 253.977 255.204 256.438 257.678 258.924 260.175 261.433 262.697 263.967 265.243 266.525 267.813 269.108 270.409 271.716 273.030 274.350 275.676 277.009 278.348 279.693 281.045 282.404 283.769 285.141

192.007 192.935

195.747 196.693 197.644 198.600 199.560

7.5

10.0 12.5

15.0 17.5

200.524 201.494 202.468

20.0

203.447

27.5

204.430

30.0 32.5 35.0

205.418 206.411 207.409

22.5 25.0

37.5

208.412 209.419 210.432 211.449

40.0 42.5 45.0

212.471

50.0

213.498 214.530 215.567

52.5 55.0 57.5

216.610

60.0 62.5 65.0

217.657 218.709 219.766 220.829

221.896 222.969 224.047 225.130 226.218 227.312

228.411 229.515

230.624 231.739 232.859 233.985

47.5

67.5 70.0 72.5 75.0 77.5 80.0 82.5 85.0 87.5 90.0 92.5 95.0

97.5 100.0

102.5 105.0 107.5 110.0 112.5 115.0 117.5 120.0 122.5 125.0 127.5 IJO.O 132.5 135.0 137.5 140.0 142.5 145.0 147.5 150.0 152.5 155.0 157.5 160.0 162.5 165.0 167.5 170.0

286.520 287.905 289.296 290.695 292.100 293.512 294.931 296.357 297.790 299.229 300.676 302.129 303.590 305.057 306.532 308.014 309.503 310.999 312.503 314.013 315.531 317.057 318.589 320.130 321.678 323.233 324.795 326.365 172.5 327.943 175.0 329.528 177.5 331.121 180.0 332.722 182.5 334.330 185.0 335.947 187.5 337.571 190.0 339.203 192.5 340.842 195.0 342.490 197.5 344.146 200.0 345.809 202.5205.0347.481 349.161 207.5 350.849 210.0 352.545 212.5 354.249

215.0

217.5 220.0 222.5 225.0 227.5 230.0 232.5

235.0 237.5 240.0 242.5 245.0 247.5

250.0 252.5 255.0 257.5 260.0 262.5

265.0 267.5 270.0 272.5 275.0 277.5

280.0 282.5 285.0 287.5 290.0 292.5

295.0 297.5 300.0

302.5 305.0 307.5 310.0

312.5 315.0 317.5

320.0

APPENDIX 475

TableA-lS CURVE NR-21ó FOR FOXBORO RTDs. FAHRENHEIT TEMPERATURE VS ABSOLUTE OHMS (ONE ABSOLUTE OHM ~ 0.999505INTERNATIONAL OHM)

D.gF

Ohms

-320 -31S -310 -30S

161.233 162.099 162.970 163.84.5 164.72.5 16.5.610 166..500 167.39.5 168.294 169.199 170,108 171.022 171.940

-300 -29S -290 -28S -280 -27S -270 -26S -260 -2SS -2S0 -24S -240 -23S -230 -22S -220 -21S -210 -20S -200

-19S -190 -18S -180 -17S -170 -16S -160 -ISS -ISO -14S -140 -13S -130

172.864 173.793 174.727 17.5.666 176.609 177..5.58

178..512 179.471 180.436 181.40.5 182.380 183.360 184.34.5 18.5.33.5 186.331 187.332 188.339 189.3.51 190.368 191.391 192.419 193.4.53 194.492 19.5..537 196..588 197.644

Deg F

Ohms

-12S -120 -liS

198.706 199.774 200.847 201.926 203.011 204.102 205.198 206.301 207.409 208.524 209.644 210.771 211.903 213.042 214.187 2]5.337 216.494 217.657 218.826 220.002 221.184 222.372 223.567 224.768 225.976

-1]0

-lOS -100 -9S

-90 -8S

-80 -7S -70 -6S

-60 -SS -SO -4S

-40 -3S -30 -2S

-20 -]S -10 -S

227,190

+ S

228.411 229.638 230.872 232.112

20 30

233.359 234.613

23S.111

Deg F

Ohms

95 100 105 110 115 120 125 130 135 140 145 150 155 160 165 170 175 ISO 185 190 195 200 205 210

235.874 237.141 238.415 239.696 240.984 242.279 243.580 244.889 246.205 247.527 248.857 250.194 251.539 252.890 254.249 255.615 256.988 258.369 259.757 261.153 262.556 263.967 265.385 266.811 268.244 269.685 271.134 272.591 274.056 275.528 277.009 278.497 279.993 281.498 283.010 284.531

212

285.141

35 40 45 50 55

60 65 70 75 80 85

Deg F

Ohms

Deg F

Ohms

215 220 225 230 235 240 245 250 255 260 265 270 275 280 285 290 295 300 305 310 315 320 325 330 335 340 345 350 355 360 365 370 375 380 385 390 395 400

286.059 287.596 289.142 290.695 292.257 293.827 295.406 296.993 298.589 300.193 301.806 303.428 305.057 306.696 308.344 310.001 311.667 313.341 315.025 316.717 318.419 320.130 321.850 323.579 325.318 327.066 328.823 330.590 332.366 334.152 335.947 337.752 339.566 341.391 343.225 345.069 346.923 348.787

405 410 415 420 425 430 435 440 445 450 455 4W 465 470 475 480 485 490 495 500 505 510 515 520 525 530 535 540 545 5SO 555 5&J 565 570 575 580 585 590 595 600

350.661 352.545 354.439 356.343 358.258 360.183 362.118 364.064 366.020 367.986 369.963 371.951 373.949 375.959 377.979 380.009 382.051 384.104 386.168 388.243 390.329 392.426 394.534 396.654 398.785 400.928 403.082 405.247 407.425 409.614 411.814 414.027 416.252 418.488 420.736 422.997 425.270 427.555 429.852 432.162

NOTE: For narrow span instruments or instruments with midscale values below -400F or -4Q"C a special value resistor is used jn place ofthe 217.657ohm resistor. Padder panels with these special value resistors are identified with a RED dot and the actual resistance value is marked on the end ofthe coiI. This special value should be used instead of 217.657ohms.

476

APPENDIX

TableA-26. FahrenheitTableof Relative Humidity or Per CelÍt of Saturation oI Wet .n'

D'7 BuJb, m

I .,

., o, ., ..,. """""62""""" ..Ofi 'O " ..., .. ,. ., .,

o lO U ui.

.. .. O. 70 7.

..O. ..O. ..O.

85 00

'OD

102

0 ...0

, ,

..'R

..'O

O .O

30..., ",.

..52

,. " 70se

, ..,.

,. ,.

..O,

tO ..RO ,. 'O ..., ta 00 ..., " ,.

O.O,

'o,.

'1 .,

1 .,

..30

SS 00

O .OO.

,. .O 'O l' .

.5 '10

30., ..I. 1. , ,

...,

'15

.. BO

,. ..,.. se 5330., ..., " U ,. " ..Il., .1 53" '0" ..., , " , ,. se..OQO,..52 .0 30..'1 , 30 'O..., .2 59 OI.0 , ..33 , O. 30..,. O,..53 .0., '0 30.. O.O.00 30..,. 53 52 0..'1 ., .. O.O.tO., sa30" ,. ,. 53 53., 32 '1 , ,.

00 OS

100 102 100 106 108

lOS

00 ..tO ., ..O. 00 .,

..., ...1

,. ,. ..'O " 'O "'0

se ..O, .,

"2'"

..O.

...1

..,.

tO .,

O, O. tO ., ..., O, ..00

12O

122 12' 120

128

,. 'O ,. ,. ,. ,.

" SO "

..O,

'O ,. ..,.

,. ,. ..'I ..60 ,.,.

"'I ..., ...,

" ...,

O. .,

30 ,.

..00

tO .,

O. tO

SO ,.

,.,.

SO,.

..00O.tO SO ,. ,. "2,., ..ta O.tOSO , 'O,. O. O, tO SO 1 tOSO 1 "8,.. ..O, tO ..SO sa ., ..77 ..O. ..tO SO SO ..., "O

,....O. ,.. ..O,

..53

.."

..O. ..O.

'70

'72'7'

..O,

..53

..SO

, ,

,. ,. 'O ,. 7'J'O " ..'" ," 'O ,. " ,. .."

..SO

O, O,

,. , ,.

..O,

'78

,. ..,.

..53

...,

..52

IlO

118 120

...

, 'O., "

"""'1'

,. U.,

30'.'.'"

...,

..'0"

..,. 52

O. ., O, O. ..., ,

..60

,'O ". "8

'40

..0..

..'"

...0'

, ., ..'0" ,

...0

.,..

..,

OI ,.. ..OI .0.

,.",. ,.

..O.

i88 iOO

!O.!'O ..O,

!OD

O, tO ..O. ..O.

" ,. ,.

" ,. ,. ,.

'0 SO ., ..SO 60 ..SO

'40

, '1

'08 'SO '52 '54 '56 '58

'00

" I.

,. ,.

,.,.

,.. '68

"10

'.2 'M

'0'

,...,.

"12 "10 1'1.

'0'

..,.

"18

00 68 68 53 ., , 0 O, ..., , 53 O ,.

80 , ..,. .0 1. ", ..'O .0 56 ..OI' ..., , 80,. ,. ,. ,. ..'0

'02 '44

'I ,.,.

",.

'M O. ..O, O. ..O, ..tO O,

.."

30...,. ,. 53.1 'O1. 'O,. , 'O lO ",. 32 lO",. ,. ,. , ..'1 1.,.

,. 53..59 , 6853 , ,..., ,...,.

" ,

...0

.0 .0 .."

'O'I

., .,

53 ..,.

, O,

,. ,. ,." 'O '0

'82 i86

1 'O'O

..O,

122 120 12. 128 "2

...0

68O,53'O..,. ., O,53 , OI ..O, ,. 1 , , , ..68 OI,. 68M O, ,

56 ,

O. 53 .0 ..,..

112

11.

...

.0" ,.

...0

O, ..68

110

,.'O ,.'O ., ...,.,

...,

.."

., ,

..53

0 ..O.

..SO

l' 1

6860 , ..'O ., 68 OI., ., '1 68O", ., .." "

O, ..53

,.. ..O, O, OISO sa...,,

'70

O..,

O.00..52

...,

O, O. O, ..53

..O,

33..

0 .1

1 O. 68 .,60 ..O. ..53

..30

02 MI ..., , ..OI ..,.

..O,

'08 ..tO

'02

,. ,. 'O..60 ,. ,. 'O..60 'O,. 70

138

., .,

OI ...,

..53 ,

..'O

,, ..,. ..,.

"2,..,..

..., ..53 'O O,

..'O

..SO ..~, ,...,., ..O. ..O. , SO ,

130

..O, O,

..'O

..., 0 .,

53 OI .0 ., ,'. .0 .0 .. 33O,

.0 .,

O, ..53

OI OI O.

..O, O,

..O,

"2 13'

..'O

O, 6(\ ..O, O, ..O,

,.,. ,...,. ,...,. ,.,',.

59 56...1 , ,.'O .. O,.. 'O ,.

'BO

'82 ,.. '86 '88 '00 !OO !OS

APPENDIX

477

TableA-27. CelsiusTable of Re1ativeHumidity or Per Centof Saturatión D'1

BuIb

D...

.. . .

" "

,. "

.. .. .. ..

",.,.,.

.. ., ..

.. 'O .0

",.,.

.."

.. ., .. ., 70

7' 7. 7. 7' SO

" .. .. li

,... ,...

100

.020

478 APPENDIX

TableA-28. SealFluids

Aquaseal'

002

Nujol orother highly refined neutral mineral oil Auorolube' FS-S

0002

S-JO HO-12S Mercury Halocarbon3 4-11

11-21 10-25

1.868

1.927 1.953 13.6 1.85 1.90 1.95

-60 P.P. 12 P.P. 60 P.P. -38.8

-110

P.P. O P.P. 3S P.P.

0.1

0.003 0.002 .005

0.18

<0.01 <0.01

1.2

100

004

0.6 0.02 0.01 .OS

1.7 0.12 <0.01

I.S 0.6 2.6 60

Hooker Industrial Chemicals

HIGH HIGH

1.2

190

Widely available Halocarbon Products Corp.

, Dibutylphthalate .Triftuorovinyl Chloride polymers 3 Chlorotriftuoroethylene ln the measurement of pressure and ftow, it is sometimes desirable to protect the instruments against dangerous and corrosive ftuid~uch as swphuric, hydrochloric, and nitric acids; strong sodium or potassium hydroxide; the halogens, and many of the halogenated hydrocarbons. ln these applications it is necessary to fill the connecting leads hetween the instrument and the saurce of measurement with a seal fluid which will remain stable under a wide range of operating conditions. Seal fluids showd bave the following characteristics:

I. Higher specitic gravity than the measured fluid. 2. Inert to attack by, immiscible with, and noI a solvent for, the measured fluid. 3. Stability at high ambient temperatures. 4. High boiling point, low vapor

pressure. 5. Low pour or freeze point, low viscosity and flat viscosity curve. 6. Nontoxic on contact or inhalation, freedom from obnoxious

odors.

No one fluid wiIl meet the wide variety of conditions imposed by many installatioDS, The seal fluids listed above have been reported by users or field service engineers as materials which have given satisfactorr service. The data pertaining to these materials was abstracted from manufacturers' publications or technical data, and is assumed to be reliable. Unless a user has had practical experience with any of these fluids, they sbould be considered on a quasiexperimental basis until the validity of their use is confirmed.

Table A-29. Psychrometric Chart BAROMETRIC

PRESSURE 29.92

in.

Hg .10

Legend 1 2 3 4 5 6 7

Dew Point Temperature Wet Bulb Temperature Cubic Feet Per Pound Relative Humidity Grains 01 Moisture Pounds 01 Water Dry Bulb Temperature

How to use chart Locatc point on chart at intersection 01 any two valucs. Obtain other valucs by hillowing chart lines Example: at a dry bulb tcmpcratufe 7 01 172"F and a wet bulb temperature 2 01 102 F, thc lollowing valucs mar bc obtaincd Irom the chart: dcw point tcmpcraturc 187.5 F; cubic Icct per pound 01 dry air 3 16.7; rclative humidity 4 10.3 pcrccnt; grains 01 moisturc per pound 01 dry air 5 201; pounds 01 water per pound 01 dry air 6.0287.

,cI

"OU

479

GLOSSARY

Accuracy. Confonnity to an indicated, standard, or true value, usually expressed as a percentage (of span, reading, or upper-range value) deviation Cromthe indicated, standard, or true value. Amplijication. The dimensionless ratio of output/input in a device intended by design to have this ratio greater than unity. Amplijier. A device whose output is, by design, an enlarged reproduction of the input signal and which is energized Croma source other than the signal. See Gain. Amplitude ratio. The ratio of the magnitude of a steady state sinusoïdal output relative to the input. Analog computer. A computer operating on continuous variables. Compare Digital computer. Analog simulator. An electronic, pneumatic, or mechanical device that solves problems by simulation of the physical system under study using electrical or physical variables to represent process variables. Attenuation. A decrease in signal magnitude-the reciprocal of gain. Automatic controller. A device, or combination of devices, which measures the value of a variable, quantity, or condition and operates to correct or limit deviation of this measured value Croma selected (set point)

reference. Automatic control system. An operable arrangement of one or more automatic 480

GLOSSARY 481

controllers along with their associated equipment connected in closed loops with one or more processes. Automation. The act or method of making a processing or manufacturing system perform without the necessity of operator intervention or supervision. The common word designating the state of being automatic. Block. A set of things, such as words, characters, dígits, or parameters handled as a unit. Bode diagram. A plot of log-gain and phase-angle values on a log-frequency base, for an element, loop, or output transfer function. lt also comprises similar functional plots of the complex variable. Breakpoint. Thejunction of two confluent straight line segmentsof a plotted

curve. Bulk storage. An auxiliary memory device with storage capacity many orders of magnitude greater than working memory; for example, disk file, drum, magnetic tape drives. Bus. One or more conductors used to transfer signats or power. Capacitance. The property that may be expressed as the time integral of flow rate (heat, electric current, and so on) to or from a storage divided by the associated potential change. Capacity. Measure of capability to store líquid volume, mass, beat, information, or any form of energy or matter. Cascade control system. A control system in which the output of one controller is the set point of another. Chip. An integrated circuit.. Closed loop (feedback loop). Several automatic control units and the process connected so as to provide a signal path that includes a forward path, a feedback path, and a summing point. The controlled variable is consistently measured, and if it deviates from that which has been prescribed, corrective action is applied to the final element in such direction as to return the controlled variable to the desired value. Compiler. A program that translates a higher levellanguage like "BASIC" or FORTRAN into assembly language or machine language, which the CPU

canexecute. Computer. A device that performs mathematical calculations. It may range from a simple device (such as a slide rule) to a very complicated one (such as a digital computer). In process control, the computer is either an analog mechanism set up to perform a continuous calculation on one or more input signals and to provide an output as a function of time without relying on external assistance (human prompting), or a digital device used in direct digital control (DDC). Control accuracy. The degree of correspondence between the controlled variable and the desired value arter stability has been achieved. Controlloop. Starts at the process in the form of a measurement or variable, is monitored, and returns to the process in the form of a manipulated variable or "valve position" being controlled by some means.

482 GLOSSARY

Control point. The value at which the controlled system or procèss settles out or stabilizes. It may or may Dot agree with the set point (instruction) applied to the controller. Control system. A system in which deliberate guidance or manipulation is used to achieve a prescribed value of a variable. Controlled system. That part of the system under control-the processo Controlling means. The elements in a control system that contribute to the required corrective action. CPU. Central processer unit-the portion of a computer that decodes the instructions, performs the actual computations, and keeps order in the execution of programs. Cycling. A periodic change in the factor under control, usually resulting in equal excursions above and below the control point of sinusoidal wave shape-o scillation. Damping. Progressive reduction in the amplitude of cycling of a system. Critically damped describes a system that is damped just enough to prevent overshoot following an abrupt stimulus. Data. A general term to denote any information that can be processed. Dead band. The change through which the input to an instrument can be varied without initiating instrument response. Dead time. instrument. The time that elapses while the input to an instrument varies sufficiently to pass through the dead band zone and causes the instrument to respond. Derivative action. Control action in which the rate of change of the error signal determines the amplitude of the corrective action applied. It is calibrated in time units. When subjected to a ramp change, the derivative output precedes the straight proportional action by this time. Deviation. The departure from a desired value. The system deviation that exists arter transients bave expired is synonymous with offset. Digital computer. A computer operating on data in the form of digits-discrete quantities of variable rather than continuous. Dynamic behavior. Behavior as a function of time. Equilibrium. The condition of a system when all inputs and outputs (supply and demand) bave steadied down and are in balance. Error. The difference between the actual and the true value, often expressed as a percentage of either span or upper-range value. Feedback. Information about the status of the controlled variable that may be compared with information that is desired in the interest of making them

coincide. Final control element. Component of a control system (such as a val ve) which directly regulates the ftow of energy or material to the processo Frequency. Occurrcnce of a periodic function (with time as the independent variable), generally specified as a certain number of cycles per unit time.

GLOSSARY483

Frequency corner. That frequency in the Bode diagram indicated by a breakpoint-the intersection of a straight line drawn asymptotically to the log-gain versus log-frequency curve and the unit log-gain abscissa. Frequency-responseanalysis. A system of dynamic analysis that consists of applying sinusoïdal changes to the input and recording both the input and output on the same time base using an oscillograph. By applying these data to the Bode diagram, the dynamic characteristics can be graphically determined. Gain (magnitude ratio). The ratio of change in output divided by the change in input that caused it. Both output and input must be expressed in the same units, making gRifi apure (dimensionless) number. Gain, loop. The combined outputJinput magnitude ratios of all the individual loop components multiplied to obtain the overall gRifi. Gain, margino The sinusoïdal frequency at which the outputJinput magnitude ratio equals unity and feedback achieves a phase angle of -180 degrees. Gain, static (zero-frequencygain). The outputJinput amplitude ratio of a component or system as frequency approaches zero. Handler. A small program that bandies data flow to and from specific pieces of hardware for use by the other software. Hardware. Physical equipment; for example, mechanical, magnetic, electrical, or electronic devices. Something that rou can touch with your finger. Hunting. Oscillation or cycling that mar be of appreciable amplitude caused by the system's persistent effort to achieve a prescribed level of control. Hysteresis. Difference between upscale and downscale results in instrument response when subjected to the same input approached from opposite directions. Input. Incoming signal to measuring instrument, control units, or system. Instrument. In process measurement and control; this term is used broadly to describe any device that performs a measuring or controlling function. Instrumentation. The application of instruments to an industrial process for the purpose of measuring or controlling its activity. The term is also applied tothe instruments themselves. Integral control action. Action in which the controller's output is proportional to the time integral of the error input. When used in combination with proportional action, it was previously called reset action. Integral time. The calibrated time on the controller integral (reset) dial which represents the time that will elapse while the open-loop controller repeats proportional action. Integral windup. The overcharging, in the presence of a continuous error, of the integral capacitor (bellows, in a pneumatic controller) which must discharge through a longtime constant discharge path and which prevents a quick return to the desired control point.

484 GLOSSARY

Integrator. Often used with a flowJ!leter to totalize the aTeaunder the flow record; (for example, gallons per minute x minutes = total gallons. It produces a digital readout of total flow. l/O. Input/Output: The interface between peripheral equipment and the digital

system. Lag. A delay in output change following a change in input. Laplace transformo A transfer function that is the operational equivalent of a complex mathematical function permitting solution by simple arithmetic techniques. Limiting. A boundary imposed on the upper or lower range of a variable (for example, the pressure in a steam boiler as limited by a safety valve). Linearity. The nearness with which the plot ora signal or other variable plotted against a prescribed linear scale approximates a straight line. Load. Level of material, force, torque, energy, power, or other variable applied to or removed Croma process or other component in the system. Log gain. Gain expressed on a logarithmic scale. Loop. A signal path. Manipulated variable. That which is altered by the automatic control equipment so as to change the variable under control and make it conform with the desired value. Measuring element. An element that conyerts any system activity or condition into a Cormor language that the controller can understand. Memory. Pertaining to that storage device in which programs and data are stored and easily obtained by the CPU for execution. Nichols diagram (Nichols chart). A plot of magnitude and phase conto urs of return-transfer function referred to ordinates of logarithmic loop gain and abscissae of loop phase angle. Noise. Unwanted signal components that obscure the genuine signal information that is being sought. Off-line. (1) Pertaining to equipment or programs not under control of the computer. (2) Pertaining to a computer that is not actively monitoring or controlling a processo Offset. The difference between what we get and what we want-the difference between the point at which the process stabilizes and the instruction introduced into the controller by the set point. On-line. (1) Pertaining to equipment or programs under control of the computer. (2) Pertaining to a computer that is actively monitoring or controlling a process or operation. Open loop. Control witoout feedback; for example, an automatic washer. Optimum. The highest obtainable proficiency of control; for example, supply equals demand, and offset has been reduced to a minimum (hopefully

zero). Oscillograph recorder. A device that makes a high-speed record of electrical variations with respect to time; for example, an ordinary recorder might

GLOSSARY 485

bave a chart speed of 3A inch per hour while an oscillograph could 'bave a chart speed of 3Ainch per second or faster. Output. The signal provided by an instrument; for example, the signal that the controller deli vers to the valve operator is the controller output. Overdamped. Damped so that overshoot cannot occur. Overshoot. The persistent effort of the control system to reach the desired level, which frequently results in going beyond (overshooting) the mark. Phase. The condition of a periodic function with respect to a reference time. Phase difference. The time, usually ex:pressedin electrical degrees, by which one wave leads or lags another. ProcessoThe equipment for which supply and demand must be balanced-the system under control, excluding the equipment that does the controlling. Programo A series of instructions that logically solve given problems and

manipulatedata. Proportional banJo The reciprocat of gain expressed as a percentage. Refers to the percentage of the controller' s span of measurement over which the full travel of the control valve occurs. Proportional control. Control action in which there is a fixed gain or attenuation between output and input. Ramp. An increase or decrease of the variable at a constant rate of change. Rate action. That portion of controller output that is proportional to the rate of change of input. See Derivative action. Reaction curve. In process control, a reaction curve is obtained by applying a step change (either in load or set point) and plotting the response of the controlled variable with respect to time. Real-time clock. A device that automatically maintains time in conventional timè units for use in program execution and event initiation. Reproducibility. The exactness with which ameasurement or other condition can be duplicated over time. Reset action. See Integral control action. Reset rime. See Integral rime. Reset windup. See Integral windup. Resistance. An opposition to flow that accounts for the dissipation of energy and límits flow. Flow Croma water tap, for example, is limited to what the available pressure can push through the tap opening ., reslstance (ohms) = potential {volts) electncal fl ow (amperes) Response. Reaction to a forcing function applied to the input; the variation in measured variables that occurs as the result of step sinusoidal, ramp, or other kind of input. Routine. A small program used by many other programs to perform a specific

task. Self-regulation. The ability of an open-loop process or other device to settle

486 GLOSSARY

out (stabilize) at some new operating plant arter a load change has taken

place. Servomechanism. An automatic control system that takes necessary corrective action as the res uit of feedback. The output may be mechanical position or something related to it as a function oftime. Servotechniques. The mathematical and graphical methods devised to analyze and optimize the behavior of control systems. Set point. The instruction given the automatic controller determining the point at which the controlled variable hopefully will stabilize. Signal. Information in the form of a pneumatic pressure, an electric current, or mechanical position that cames information from one controlloop component to another. Software. The collection ofprograms and routines associated with a computer. Stability. That desirable condition in which input and output are in balance and will remain so unless subjected to an external stimulus. Static behavior. Behavior which is either Dot a function of time or which takes place over a sufficient length of time that dynamic changes become of minor importance. Steady state. A state in which static conditions prevail and all dynamic changes may be assumed completed. Step change. A change from one level to another in supposedly zero time. Summing paint. A point at which several signals can be algebraically added. System. Generally refers to all control components, including process, measurement, controller, operator, and valves, along with any other additional equipment that may contribute to its operation. Terminal. A device for operator-machine interface; for example, CRT's, typewriters, teletypers with keyboard input, or telephone moderns. Thermocouple. A device constructed of two dissimilar metals that generales a small voltage as a function of temperature difference between a measuring and reference junction. This voltage can be measured and its magnitude used as a measure of the temperature in question. Time constant. The product of resistance x capacitance (T = RC), which becomes the time required for a first-order system to reach 63.2 percent of a total change when forced by a step. In so-called high-order systems there is a time constant for each of the first-order components. Transducer. A device that converts information of one physical form to another physical type in its output (e.g., a thermocouple converts temperature into millivoltage). Transfer function. A mathematical description of the output divided by input relationship which a component or a complete system exhibits. It often refers to the Laplace transform of output over the Laplace transform of input with zero initial conditions. Transportation lag. A delay caused by the time required for material to travel

GLOSSARY 487

Cromone point to another; for example, water flowing in a pipe at 10 feet per second requires 10.0 seconds to travel100 feet, and if this 100feet exists between manipulation and measurement, it would constitute at 10-secondlag. Ultimate period. The time period of one cycle at the natural frequency of the system where it is allowed to oscillate without damping. Value. The level of the signat being measured or controlled. Variable. A level, quantity, or other condition that is subject to change. This mar be regulated (the controlled variable) or simply measured (a barometer measuring atmospheric pressure). Zero frequency gain. Static gain or change in output divided by the change in input which caused it, arter sufficient time has elapsed to eliminate the dynamic behavior components. Zero shift. Change resulting Croman error that is the same throughout the

scale.

Note: A more complete setofdefinitions maybefoundin the ISApublication, "Process Instrumentation Terminology," ANSI/ISA 551:1, 1979.

ANSWERS TO QUESTIONS

l-I. c

2-3. a

1-2. c 1-3. c

2-4. c

1-4. b l-S. a 1-6. a 1-7. d b h e

g c

f 1-8. c 1-9. d 1-10. a l-Il. a 1-12. c 1-13. a 1-.14.b 1-15. c 2-1. b

2-2. c

2-5. b 2-6.c 2-7. c 2-8. 2-9. 2-10. 2-11. 2-12.

b c b b b

3-3. a 3-4. b 3-5. d 3-6. a 3-7. b 3-8. a' 3-9. c 3-10. c 4-1. d c

2-13. c 2-14.c 2-15.a 2-16. c 2-17. c 2-18. a

2-19.c 2-20. b 2-21. b

2-22.c 2-23.d 2-24. d

3-1. c 3-2. c

a b e

4-2. a 4-3. b 4-4. d 4-5. d 4-6. d 4-7. a 4-8. b

5-1. a 5-2. c 5-3. b 5-4. c 5-5. a 5-6. a 5-7. c 5-8. c 5-9. d 5-10. c 5-11. c 5-12. b 5-13. a 5-14. b 5-15. c 5-16. d 5-17. c 5-18. b 5-19. c 5-20. b

4-9. b 4-10. a 4-11. d 4-12. b 488

6-1. a

6-2. b

6-3. a

ANSWERSTO QUESTIONS 489

6-4. a 6-5. a 6-6. b 6-7. c 6-8. a

6-9. b 6-10. c 6-11.c 6-12. a 6-13. c 6-14. a 6-15. a 7-1. b

7-2. c 7-3. a 7-4. c

7-5. b 7-6. c 7-7. a 7-8. b 7-9. b 7-10. b 7-11.45 seconds 7-12. c

7-13. b 7-14. c 7-15. d 7-16.a 7-17.a 7-18. b

7-19.a 7-20. c

8-1. a 8-2. T 8-3. T 8-4. F 8-5. T 8-6. T 8-7. a. T b. T c. T d. F e. T f. T 8-8. d

8-9. c 8-10. b

8-11. a 8-12. b 8-13. d 8-14. c 8-15. c 8-16. d 8-17. c 8-18. c 8-19. d 8-20. b 9-1. b 9-2. c 9-3. c 9-4. a 9-5. a 9-6. a 9-7. a 9-8. c 9-9. b 9-10. b 9-11. a

~-12.c 9-13. b 9-14. d 9-15. d 10-1. b 10.2. a 10-3. b 10-4. b 10-5. b 10-6. c 10-7.b 10-8. a 10-9. b 10-10. c

11-1. Cv max = 4.57 Cv min = 0.355 ~ ball valve 11-2. Cvmax = 300 Cv min = 18.9 6-inch, equal percentage, globe val ve 11-3. Cv max = 41.3 Cvmin = 7.6 2-inch, equal percentage, globe valve 11-4. Cv max = 1407 Cv min = 56.3 S-inch butterfty11-5. Cv max = 3.43 ~-inch globe or ball valve 11-6. b11-7. b11-8. c11-9. a 12-1. c

12-2.d 12-3. a 12-4. b 12-5. d 13-1. d 13-2. a 13-3. b 13-4. b 13-5. a 13-6. d 13-7. a 13-8. b 13-9. d 13-10. d 13-11. b 13-12. d 14-1. d 14-2. c 14-3. a 14-4. a 14-5. b 14-6. c 14-7.b

17-10.

490 ANSWERSTO QUESTIONS

14-8. d 14-9. b 14-10. d 15-1. a 15-2. b 15-3. a 15-4. a 15-5. a 15-6. a 15-7. a 15-8. b 15-9. b15-10. a15-11. a15-12. d

16-1. a 16-2. d 16-3. a 16-4. b 16-5. d

17-1.b 17-2.a 17-3.c 17-4.a 17-5.d 17-6.a 17-7. c 17-8.b 17-9.a

c 17-11. b 17-12. c 18-1. b 18-2. b 18-3. a 18-4. c 18-5. b 18-6. d 18-7. d 18-8. b 19-1. b 19-2. c

19-3. a 19-4. a

19-5. d 20-1. c 20-2. d 20-3. a 20-4. a 20-5. d 20-6. c 20-7. b 20-8. b 20-9. c 20-10. d

BIBLlOGRAPHY

Books Lavigne, J. R. An Introduction to Paper Industry Instrumentation. San Francisco: Miller-Freeman Publications, 1972. Lipták, B. G. Instrument Engineers Handbook, vols. I and Il. Radnor, PA: Chilton Book Company, 1969, 1970. Shinskey, F. G. ProcessControl Systems. New York: McGraw-Hill Book Company, 1979. Shinskey, F. G. pH and pION Control in Process and Waste Streams. New York: John E. Wiley & Sons, 1973. Shinskey, F. G. Distillation Control for Productivity and Energy Conservation. New York: McGraw-Hill Book Company, 1977. Shinskey, F. G. Energy Conservation Through Control. New York: Academic Press, 1978. Spink, L. K. Principies and Practices of Flow Meter Engineering, ed. 9. Foxboro, MA: The Foxboro Company, 1967.

Periodicals Computerworld (W). Newton, MA: Computerworld, CW Communications,

Inc. Control Engineering. Barrington, ILL: Technical Publishing Company, Dun & Bradstreet. Instrumentation Technology(M). Pittsburgh, PA: Instrument Society of

America. Instruments and Control Systems (M). Raqnor, PA: Chilton Company. 491

INDEX

Absolute pressure, 34, 37 Absolute pressure transmitter, 64-65 Acidity. See pH measurement Actuators, 259-68 electrical signal conversion and, 263-

Bubbletubemethodof levelmeasurement, 73-74 Buoyancylevel transmitters,71-73

electric motor, 267-68 piston-and-cylinder, 263 valve, 226-67, 259-61 Algebraic summing point, 179, 180 Aspirating relay, 208-9 Atmospheric pressure, 34 Automatic controllers. See Controllers Auto-selector control, 345-48

Calibrator, portable pneumatic, 59-60 Capacitance, 78 Capacitance measurement, 175 Capacity oCcontrol valves, 272-73 oCa process, 14, 18 Cascade control system, 247-52, 352-57 Cavitation, 274-76 Cell constant, 153 Central processing unit (CPU), 373-74 CGS units oCpressure, 35, 37 .

Bar, 37 Batch controller, 231-34 Bell instrument,44, 45 Bellows, metallic,49-52 Bemoulli's theorem,91-92, 270 Blocks, 397, 399,400 Bode diagram,frequencyresponseanalysis and,329-31 Bourdontube, 46-48

Chromatographs, 174 Cippoletti weir, 110 Closed loop control system, 179-201. See a/so Controllers gain and, 180-83 nonlinearities in, 189 oscillation in, 184-87 phase shiCtsin, 184 pneumatic, 223-31 stability in, 187-88

492

INDEX

Computer hardware, 372-85 Computer input, 373 Computer interface equipment, 377-85 Computer memory, 373-77 Computer software and operation, 388-

400 analog fIow loop, 399 blocks, 397, 399, 400 control software, 394-400 Foxboro Control Package (FCP), 399400

Foxboro Process Basic (FPB) language, 396 otf-line system, 389-90 on-line system, 388-89 real-rime clock and power fail/restart logic, 394 Computer system process control, 378-85 Computers, basic elements or, 372-74 Conductance, 152-54 Conductivity level sensors, 79 Conductivity measurements, 151-59 applications or, 157 calibration of instruments for, 154-57 construction of cells for, 156-57 electrodeless, 157-59 polarization etfects and, 156 Controllers, 12-29 adjustment (tuning), 295-303 closed-loop cycIing method, 301-2 proportional-only controller, 295-96 proportional-plus-integral controller, 296-97 proportional- plus-integral- plusderivative controller, 297-301 reaction curve used to determine, 320-24

tuning maps, 298-99 auto-selector or cutback, 345-48 cascade, 352-57 control modes or, 189-200 proportional-plus-integral control, 196 throttling control (proportional-only control), 191, 193-95 two position control, 189-191 direct and reverse actions or, 16 duple x or split-range, 343-45 elapsed-time, 402-11 fIow-ratio, 349-52

493

pneumatic. See Pneumatic controllers programmed,402-11 responses or, 16-29 selection of, 200-1 selection of the action or, 16 sequential, 405-6 Control valves, 270-92 capacityof, 272-73 pressure drop across, 273-76 rangeabilityof, 276-79 selecting, 278-79 sequencing, 279-81 sizing or, 272, 278-80 viscosity corrections for, 281 Cofe memory, 374-75 Cutback control, 345-48 Dall tubes, 96 DDC (direct-digital control), 378 Dead time, 6-7, 17-18, 335 Dead weight testers, 42-44 as gravity dependent, 38-39 pneumatic, 43-44 Density measurement, 81-87 hydrostatic head, 82-84 radiation, 84 temperature etfects and, 84 vibration, 84 Derivative action, 25-29. See a/so Proportional-plus-derivative control action; Proportional-plusderivative-plus integral control frequency response analysis and, 335-37 of pneumatic controllers, 215-16 proportional control and, 199-200 in SPEC 200 system, 244-45 DEWCEL, 147-48 Diaphragm box, 74-75 Differential-gap control, 191 Ditferential pressure, 37 Ditferential pressure transmitter density measurement with, 85-87 electronic, 238-41 for level measurement, 75-78 Direct action, 16 Disk,375-76 Diskette, 384 Displacement level transmitters, 71-73 Dissociation, 159-61

494 INDEX

DistilIation, feedforward control of, 369-70 Drag body fIowmeter, 98-99 Droms, computer, 375 Dúplex controller, 343-45 Elapsed-time controller, 402-5 Elbow taps for flow measurement, 97-98 Electric motor actuators, 267-68 Electrolysis, 156 Electromotive force (emt) of thermocouples, 131-33 Electronic control systems, 237-255. See a/so Feedwater control system,

electronic pneumatic systems compared to, 254-55 Electronic process simulator, 414-20 Exponential-rise transient, 6 Feedback controlloop, 3, 179-201. See a/so Closed-loop control system basic characteristics or, 9, 12-14 Feedforward control, 360-70 advantages or, 360-61 defmition or, 360 of distillation process, 369-70 of beat exchanger, 361-69 history or, 360 Feedwater control system, electronic, 237-54. See a/so SPEC 200 system closed-loop operation or, 252-54 controllers in, 241-43 general description or, 247-52 principie of operation or, 243-47 transmitters in, 238-41 Filled thermal systems, 128-30 Final actuator, 13 Flapper-nozzle units, 205-14 Flashing, 274-76 Float-and-cable devices, 70 v-notch weir with, 116 Flow measurement, 90-124 constriction or differential head type devices, 91-92 elbow taps, 97-98 flow nozzle, 96-97 flow rates pressure relationship, 100-3 orifice plates, 94, 100

Pitot tube, 97 primary devices, 94-99 secondary devices, 99-100 target (drag force) device, 98-99 temperature and flow rate, 103, 105-8 variable aTeameters (rotameter), 109 Venturi tube, 95-96 displacement method of, 91 open-channel, 109-16 velocity flowmeters, 117-23 Flow nozzle, 96-97 Flow rate differential pressure reiated to, 100-3 temperature and, 103, 105-8 Flow-ratio control, 349-52 Flumes, 110-16 Force, 36 Force-balance pneumatic pressure transmitter, 60-65 Frequency ratio, 334 Frequency response analysis, 328-40 and Bode diagram, 329-31 closed-loop response and, 339-40 control objectives and, 335 and derivative action, 335-37 and integral action, 335, 337-39 and proportional band, 335, 339 testing a system with, 331-35 Gain, 183 frequency response analysis and,

329-31 Gain margin, 335 Galvanometric motor, 265 Gauge pressure, 34, 37 Gravity force and mass and, 36 pressure measurement and, 38-39 Hair element, 145-46 Head, 33-34, 39. See a/so Pressure Head level, measurement and, 73-78 Heat exchanger, 2, 3,12 Humidity, relative and absolute, 144 Humidity measurements, 144-48 Hydrogen ion activity (pH). See pH Instrument Society oCAmerica (ISA) symbols used by, 9, lO

INDEX

Integral action (reset), 23-25, 28-29.. See a/so Proportional-plus-derivativeplus-integral control; Proportional-plus-integral action frequency response analysis and, 335, 337-39 of pneumatic controllers, 215-16 proportional control and, 1%-98 Integral rime, 1%-97 Integral windup, 198, 216 Interface equipment, computer, 337-85 Ionization, 159-61 Ion-selective measurement, 173-74 Level measurement, 69-81 capacitance, 78 conductance, 79 displacement (buoyancy), 7"-73 float-and-cable, 70 head or pressure, 73-74 radiation, 79 thermal, 81 ultrasonic, 80-81 weight, 79-80 Limp or slack diaphragm instrument,

44-46 Liquid density. See Density measurement Líquid pressure measurement, 48 Lo-Loss tubes, % Magnetic flowmeter, 117-21 Manometers, 39-42 mercury, 99 Manual control unit of pneumatic controller, 216-19 Mass, 36 Measurement, 7-9, 13 Measuring transmitters, 8~9 Memory, computer, 373-77 Meniscus correction, 41 Metering pumps, 91 mho (reciprocal ohm), 152-53 Microprocessor, 382 Multicapacity system, 313-15 Newton (N), 36-37 Nichols diagram, 339 Otf-line system, 389-90 Otfset, 22, 28, 194-95

495

On-line system, 388, 89 On/off control, 19-20, 189-91 step-analysis method and, 316 Open-channel flow rate measurements, 109-16 Orifice plates, 94 tap locations for, 100 Oscillation, 184-87 Output transducer, resistance pneumatic transmitter used with, 141, 142 Oxidation-reduction potential measurements, 172-73 Parshall flume, 112-15 Pascal, 35-37, 39 Percent-incomplete method, 310-13 pH (hydrogen ion activity), definition or, 161

pH measurement, 159-72 control system, 170-72 glass electrode system, 164-65 ionization or dissociation and, 159-61 reading the output of pH electrodes, 169-70

reference electrodes and, 165-68 temperature compensation and, 168-69 Phase margin, 335 Phase shift, frequency response analysis and, 329 Piston-and-cylinder actuators, 263 Pitot tube, 97 Pneumatic amplifier, 207-9 Pneumatic calibrator, portable, 59-60 Pneumatic controllers, 205-34 batch controller, 231-34 closed-loop control system or, 223-31 derivative and integral action or, 215-16 electronic systems compared to, 254-55 flapper-nozzle units or, 205-14 manual control unit or, 216-19 requirements or, 211-12 set-point mechanism or, 220-23, 225-26 single-seat equal percentage valve or, 227

transferring Cromautomatic to manual, 217 transferring Crommanual to automatic, 217-19

valve actuators or, 226-27

496 INDEX

Pneumatic indicators, 53-55 Pneumatic process simulator, 420-26 Pneumatic recorders, 53-55 Pneumatic relay,62-63 Pneumatic transmitter, resistance, 140-42 Polarization, conductivity measurements anc;!,156 Portable pneumatic calibrator, 59-60 Positive displacement metecs, 91 Potentiometric recorder, 137-38 Pounds per square inch (psi), 38, 39 Power faiVrestart logic, 394

Pressure absolute, 34, 37 detinition of, 33-34 differential, 37 gauge, 34, 37 seals, 48, 55, 57-59 units of measurement for, 35-38 Pressure drop across control valve, 273-76 Pressure gauges, 34, 37, 46-48 Pressure level, measurement and, 73-78 Pressure-measuring instruments, 39-52 bell instrument, 44, 45 bellows, 49-52 calibration standards for, 39-40 calibration techniques for, 59-60 deadener or damper for, 48-49 dead weight testers, 42-44 gauges, 46-48 manometers, 39-42 seals and purges for, 48 slack or limp-diaphragm instrument, 44-46

Pressure recorders and indicators, 53-55 Pressure transmitters, 52-59 absolute, 64-65 differential, 238-41 force-balance pneumatic, 60-65 Process control computer system, 378-85

Processes controllabilityof, 17-18 types of, 5-9 Programmed control systems, 402-11 Proportional action, pneumatic transmitter and, 209-11 Proportional band, 20-23, 193 frequency response analysis and, 335,

339 ultimate, 334

Proportional control, 20-23, 28-29 offset and, 194-95 step-analysis method and, 316-18 Proportional-only control(ler), 191, 193-95 adjusting, 295-96 applications of, 195 Proportional-plus-derivative control step-analysis method and, 319-20 Pro po rtional-p 1us-de ri vati ve -pi us-integral

control step-analysis method and, 320 Proportional-plus-integral action step-analysis method and, 318 Proportional-plus-integral control(ler), 196-98 adjusting, 296-97 Pro po rti onal- p Iu s-in te gral- p Ius-de ri vati v e controller, 199-200 adjustment procedure for, 297-301 Psychrometer, 145, 146 Pulsation dampener, 48-49 Purges, 48 Pyrometers, radiation, 144 Radiation, density measurement, 84 Radiation level measurement, 79 Radiation pyrometers, 144 Rangeability of control valve, 276-79 Ratio control system, 349-52 Reaction curve, controller adjustments termined by using, 320-24 Real processes, 427-32 Real-time clock, 394

de-

Recorder potentiometric, 137-38 wheatstone bridge, 142-43 Redox measurements, 172-73 Relay, pneumatic, 62-63 Resistance thermal detectors (RTDs), 139-44 output transducer used with, 141, 142 wheatstone bridge recorder used with, 142-43 Resistance-to-pneumatic convertors, 140-42 Reverse action, 16 Reynolds number, 95 Rotameter (variable area meter), 109 Seal pressure system, 48, 55, 57-59 Semiconductor memory, 376-77

INDEX

Sequencing-control valves, 279-81 Sequential controllers, 405-6 Signal transmission system for pressure, 52-53 Simulated processes (simulators), 413-26 electronic, 414-20 pneumatic, 420-26 SÍngle-seal equal percentage valve, 227 SI units of pressure, 35-37, 39 Slack or limp-diaphragm instrument,

44-46 SIÍng psychrometer, 146 SPC (set-point control), 378 Specific gravity. See Density measurement SPEC 200 system, 241-52 automatic/manual switch in, 247 controller adjustments in, 247 derivative action in, 244-45 deviation signal generation Ín, 244 external integral (-R) option in, 246 external summing (-S) option in, 246 final summÍng and switching in, 245 high and low limits in, 245-46 increase/decrease switch in, 244 power supply fault protection circuit Ín,

246-47 proportional band action Ín, 245 Split-range control, 343-45 Square root extractor, 250-52 Steam pressure measurement, 48 Step-analysis method of fmdÍng time constant. See Time constant, stepanalysis method of finding SwampÍng resistors for average temperature measurement with thermocouples, 135-36 Symbols, 9-11 Target flowmeter, 98-99

Temperature flow rate and, 103, 105-8 pH measurement and, 168-69 Temperature measurement, 126-44 filled thermal systems, 128-30 resistance thermal detectors, 139-44 thermistors, 144 thermocouples, 130-39 average temperature measurement, 135-36 calibration curves, 137

497

differential temperature measurement with, 136 potentiometric recorders, 137-38 reference junction compensation, 133-34 transmitter, thermocouple-to-current, 138-39 Temperature transmitter, pneumatic, 209-11 Thermallevel measurement, 81 Thermistors, 144 Thermocouples, 130-39 average temperature measurement, 135-36 calibration curves for, 137 differential temperature measurement with, 136 potentiometric recorders used with, 137-38 reference junction compensation and, 133-34 Thermocouple-to-current transmitter, 138-39 Throttling control, proportional-only control, 191, 193-95 Time constant Bode diagram used for fmding, 331 step-analysis method of fmding, 304-24 block diagrams, 304-7 finding control modes, 315-20 multicapacity system, 313-15 on/oir control action, 316 percent-incomplete method, 310-13 proportional control action, 316-18 proportional-plus-derivative control action,319-20 propo rti onal-pIu s-derivat ive-pIusintegral control, 320 proportional-plus-integral action, 318 reaction curve used to determine controller adjustments, 320-24 single-time-constant system, 308-9 two-time-constant system, 309-10 Time-cycle control, 191 Transducer, output, 141, 142 Transmitters displacement (buoyancy), 71-73 pH, 170, 171 pneumatic, 140-42

498

INDEX

Transmitters, (cont'd.). pressure, 52-59 thermocoup1e-to-current, 138-39 Tuning maps, 298-99 Turbine flowmeter, 122-23 Ultrasonic level sensor, 80-81 Upsets, 17 Valve actuators, 226-27, 259-61 Valve positioners, 15, 261-63 Valve relay, 207-8

Valves control. See Control valves single-seat equal percentage, 227 Velocity flowmeters, 117-23 Venturi tube, 95-%, 208 Vibration, density measurement, 84 Viscosity corrections for control valves, 281 Vortex flowmeter, 121-22

Weightsystem,level measurement, 79-80 Weirs, IlO, III, 115-116

Wheatstonebridge recorder,142-43

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