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 -75.0

--LETFILLB

Gi.e to"onome blook.

TEMP

WAITUNTILLEVEL> --LETFILLA -DFF

Ho" ooen CI.- ..,.. B Sto" mi..,

LEVEL,

LET FILL A -DN

CHARGE

~ ~~

:==

S«ond,..., i. ~oo... fhon

-OFF

0,""uolto'5" lull

LETMIXER .ON SET(TEMP,"SP:' 95.0il WAITUNTIL TEMP> 94 5 -1

Svotemouto moti'ol'V

1200 CALL SET (TEMP, "SP," O)

;:~:~;t~::t ,... pointl

Ho"..th..tem

~~..,.tu.. lo' 20m;nul" "200 _ondo'

LETMIXER =OFF LETPUMP"ON

Tonkel'~"..,v

Tum

WAIT

TumhAto,on --CALL wt ""i'," tom u..

hA",

Olf ~

Tummi.., olf Stan di""

~~~WAIT

~ ~~~;:::::

wo"fo'm"tu"'O 'N,h tempe'otu..

~:;::/'~ pump

::::

LET

UNTIL PUMP

LEVEL

Instrumentation for Process Measurement and Control, Third Editon - PDF Free Download (2024)