Tyco Control Valve Manual

tyco FLOW CONTROL

CONTROL VALVE MANUAL

PROCESS CONTROL TERMINOLOGY

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What is a Control Valve? The most common final control element in the process industry is a control valve. The control valve manipulates flowing fluids such as gas, steam, water or chemical compounds to compensate for load disturbances and assist in regulating process variables to the desired set point. In achieving this within the desired operating range it ensures the quality of the end product that the particular industry is producing. To reduce the effect of load disturbances sensors and transmitters collect process information and their relationship to the desired set point. Controllers then process this information and decide how to adjust the control valve in order to move the variable back to set point. When all the measuring, comparing and calculating are complete, generally it is a control valve that must implement the adjustment within the process to achieve the set point. Generally control valves are really an assembly consisting of the valve, internal trim parts, an actuator to provide power to operate the valve and a variety of additional valve accessories which could include positioner, transducers, supply regulators or limit switches to name a few. This control valve manual is both a textbook and reference that we feel will be a useful tool to assist you in your daily sales efforts.

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Process Control Terminology Accessory: A device that is mounted on the actuator to complement the actuators function. Examples include positioners, solenoids and limit switches. Actuator: A pneumatic, hydraulic or electrically powered device that supplies force and motion to open or close a valve. Automated Valve: A valve and actuator package capable of responding to a remote signal. Position selection is usually fixed as opposed to the variable positioning capable in a control valve. Ball, V-Notch: The most common type of segmented ball control valve. The v-notch ball includes a partial sphere that rotates against the seat or seal ring. The v-shape notch permits wide rangeability and produces equal percentage flow characteristics. Bench Set: The calibration of the actuator spring range of a control valve to account for the in-service process forces. Capacity: Rate of flow through a valve under s s. Cascade Control: An arrangement utilizing twseries so as to increase the speed of response Consider that a system may have two sources ooperation, either of two inputs could vary:

In this system the control loop regulates the flowmixture caused by disturbances to either fluid Asensed, the controller acts to modify flow of fluidthat he control is too slow, causing loss of prod A Cascade Control system using two controllerswith any change in fluid A or the mixture.

tated conditiono conventional feedback controllers connected in of a closed loop system.

f disturbance. For example, in a mixing

CONTROLLER

of fluid A to compensate for changes in the or B. When a change in the mixture is A. There may be such a time lag however,

uct.

as shown can serve to initiate corrective action

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Here the M loop is the primary or outer loop. The F loop is secondary or inner loop. Disturbances in fluid A that would affect the mixture are now corrected by the secondary loop without having to wait for the mixture to change. If a change in fluid B occurs, the response of the system will be similar to what it would have been with single loop control. On the basis of response time, the secondary loop should be applied to the flow most likely to experience disturbances. For tuning, the secondary loop F is tuned first, followed by the primary. Otherwise tuning of each controller is similar to single loop controllers. Cavitation: Cavitation is a phenomenon that occurs inside of a piping system when a vapor implodes to a liquid due to an increase in fluid pressure. Normally, cavitation is a two-stage process where liquid is caused in the first stage to flash into vapor by a sudden drop in fluid pressure to some point less than the vapor pressure. This can occur, for instance, as the fluid experiences increased velocity and decreased pressure as it passes through a valve. In the second stage, as the fluid exits the valve, it experiences decreased velocity and increased pressures. If the increased pressures are above the fluids vapor pressure, the vapor implodes back to liquid. In its mildest form, cavitation is a minor, but somewhat noisy occurrence. At its worst, cavitation can cause rapid failure of the control valve, as well as the piping adjacent to the valve. In t his worst condition, cavitation produces very high sound levels, which are often compared to gravel flowing through the system. Cavitation is predictable and often preventable. Choked Flow (Gases): Choked flow is a term used to indicate a condition where maximum flow rate has been achieved through a valve for a given inlet pressure. Dependent upon the type of gas flowing, there exists for each inlet pressure, some maximum value of pressure differential at which maximum flow rate and velocity occur. When this maximum pressure differential exists, the flow is said to be Choked. The velocity through the valve is at sonic value and no additional flow can be forced through the valve except by increasing the inlet pressure or the valve travel position. Closed Loop System: A closed loop system is a control system capable of sensing values of a preselected variable and generating corrective action without interaction of human operator.

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CONTROLLER

Note: While the human operator may interact to modify the control desired, once modified, the

operator need not remain involved. Compression Set: Many materials such as elastomers, will deform when a load is applied. Compression set is the term used to define the amount by which the material fails to recover after the load is removed. For example, if a sample of elastomer was compressed by .060 inches under load and if it recovered only .040 of this amount upon load removal, it would be

said to have 060.020.

x 100, or 33% compression set.

Normally, compression set is measured after some number of hours of continual compression and immediately upon removal of the compressive forces. Thus compression set is given as X% compression after Y hours. Control Valve: A valve and actuator package capable of responding to a variable remote signal, resulting in modulation of the valve position and regulation of the flowing media. Control Characteristics: This term is generally employed to describe the relationship which exists between flow rate through a valve and the valve travel as the latter varies from full closed to full open. Control Characteristic is given as inherent or as installed. The Inherent Characteristic is the relationship which exists under a normal test situation where constant pressure differential is maintained across the valve at all travel positions. The Installed Characteristic is the relationship which occurs when the valve is installed in a working system, and where pressure differential may vary dependent upon valve travel and overall system characteristics. Control Range: The range of valve travel over which a control valve can maintain the installed valve gain between the normalized values of 0.5 and 2.0. Dead Band: The minimum change in input signal, which will rof the valve. Expressed in percent of full input signal span. Dead Time: The time which elapses between a change in inpchange.

esult in any detectable movement

ut and the initial response to that

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Derivative Control (Rate): An optional function available on controllers which causes the normal corrective proportional action to take effect more rapidly. Derivative action is proportional to the rate of change of the controlled process variable. When no change is occurring to the process variable, no derivative action occurs. Disc Conventional: The symmetrical flow-controlling member used in the most common varieties of butterfly rotary valves. High dynamic torques normally limits conventional discs to 60-degree maximum rotation in throttling service. Disc Eccentric: Common name for the valve design in which the positioning of the valve/disc connections causes the disc to take a slightly eccentric path on opening. This allows disengagement of the disc from the seat at a relatively slight rotation reducing wear and friction. Double Acting: An actuator in which power is supplied in either direction. Droop (Offset): The difference between the desired value of a controlled process variable and the actual value of that variable. Durometer: A measure of the hardness or stiffness of elastomeric materials. Fail Closed: A condition where the valve upon loss of power moves to the closed position. (Normally Closed Valve, reverse acting) Fail Open: A condition where the valve upon loss of power moves to the open position. (Normally Open Valve, direct acting) Fail Safe: A condition where the valve upon loss of power will move to either the fully closed, fully open or remain in the last position which has been defined as necessary to protect the process. Fail-safe action can involve the use of auxiliary controls connected to the actuator. Feedback Control: A control system which monitors system output and which modifies system input to maintain the output at the desired value.

Feed Forward Control: A control system which monitors input variables and which compensates for deviations in their values prior to their having an effect on the system output. This requires predictable corrective action for minimal disturbance to the system output.

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Final Control Element: The control valve (or variable speed pump, if control is achieved via this pump). Flashing: A liquid flashes in a control valve if it enters the valve as a liquid and exits as a vapor. The initial stages of flashing are identical to those of cavitation, in that the increased velocities internal to the valve create a lowering of pressure such that the pressure decreases to below the fluids vapor pressure. In flashing however, the fluid pressure does not recover sufficiently downstream of the valve to cause a return to the liquid state. Flow Characteristic: Relationship between flow through the valve and percent travel as the latter is varied from 0-100 percent. This term should always be designated as either the inherent flow characteristic or installed flow characteristic. Flow Coefficients: There are numerous coefficients used by industry to predict valve capacities. The most common is Cv, which is determined via test or analysis. Cv is defined as the number of U.S. gallons per minute of water at 60F that will flow through the valve with the 1 psi pressure differential. In order that consistency exist between valve manufacturers, standard means of Cv determination have been established. Values of Cv used in this manual are determined as described by ISA S39.2 for incompressible fluids and by ISA S39.4 for compressible fluids. Frequency Response: Refers to the ability of a device to respond to changes of input which occur at various frequencies. As the input signal varies, there is always some time lag before response. Normally this time lag is small. If the input is caused to change at constantly increasing frequencies, the time lag becomes significant as the time available for response is small. At some frequency, phase shift between input and response is noticeable. Attenuation of response also occurs as full response is not achieved prior to input reversal. Frequency response is expressed in units of Hertz and degrees of phase shift at the frequency where attenuation has decreased to 6db for a 5 percent sinusoidal change in input based upon full span. Friction Factor Piping: A factor used to determine pressure losses in piping systems due to frictional forces occurring between the pipe and the flowing media. Both the type of piping (size and surface finish) and fluid characteristics (Reynolds number) affect the resultant friction factors.

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Gain: Used to relate an incremental change in output to an incremental change in input. Gain may be used to describe individual components or the control system as a whole. Gain need not be constant at all inputs, and in fact, often is not constant. Examples:

The gain of a valve having a linear control characteristic is constant over the range of valve travel where the linear characteristic occurs.

The gain of a valve having an equal percentage control characteristic is greater at the more open travel positions of the valve.

The gain of a proportional controller is constant, but can be varied by modification of the selected proportional band.

Head, Static: The height of a body or column of liquid above a given point of reference. Used to express pressure as in feet of water. One foot of water is equal to .433 psi. High Recovery Valve: Used to describe a valve having little pressure loss at given flow rates, high internal velocities and low internal pressures. The pressure is said to recover from the low internal pressures to the relatively higher pressures of the downstream piping. Straight-through flow valves such as rotary-shaft ball valve and butterfly valves are typically high-recovery valves. Hydrostatic Testing: A shell test on a valve body using a liquid such as water to verify structural integrity of the part. Hydrostatic testing often serves the dual purpose of assuring that porosity is not present in the valve body. Verification of zero porosity is not always appropriate as certain valve types employ full surface liners which eliminate potential for leakage regardless of porosity presence. Hysteresis: The difference in valve position for a given input signal when approached from full closed position and the position for the same input when approached from the full open position. Hysteresis may apply to the system as a whole or to the valve/actuator only. Integral Control (Reset): An optional function available on controllers which provides the controller with the ability to reduce or eliminate droop (offset). Laminar Flow: A state of flow in which the fluid moves in unmixed parallel layers or laminae. This flow state exists in most applications having a Reynolds number value less than 2000 and rarely exists when the Reynolds number value exceeds 4000. Leak Rate: That amount of flow that passes through a fully closed valve at rated pressure conditions. See the Leakage section of this manual for further discussion. Low Recovery Rate: A valve design that dissipates a considerable amount of flow stream energy due to turbulence created by the contours of the flow path. Consequently, pressure downstream of the valve vena contracta recovers to a lesser percentage of its inlet value than is the case with a valve having a more streamlined flow path. Although individual designs vary, conventional globe style valves generally have a low-pressure recovery capability.

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Manipulated Variable: That which is changed so as to effect correction in a control system. For example, if flow rate is the controlled variable, the valve position is the manipulated variable. Manual Valve: A valve utilizing a manually operated device such as a handle or gear unit to effect changes in the valve position. Manual Reset: A manual change in the set point of the controller, such as to eliminate droop. Modulus: The ratio of stress to strain (the amount by which a dimension of a body changes when subjected to a load), within the proportional limit of a material in tension or compression. This term applies to elastomers as well as metals and is of significance in choosing proper elastomers for valve usage. On/Off Control (Two Position): A control action by a controller providing output only to fully open or fully close a valve. Of course, a controller need not be present to have on/off actuation of a valve. Proportional Band: The range of measured values of a monitored variable over which a controller produces full output span. Proportional Control: The basic control concept utilized by controllers whereby an output signal is generated in direct proportion to the value of a monitored system variable. Rangeability: The ratio of maximum to minimum values of valve capacity within the valves inherent characteristic range. i.e., Max Cv Min Cv at the ends of the inherent characteristic span. Refer to Valve Sizing section of manual for further discussion. Recovery Coefficient: An experimentally determined value used to calculate the pressure differential across a valve above which, for a given inlet pressure, no additional liquid flow will be obtained. Remote Set Point Adjustment: Denotes the ability to change the set point of a controller from a remote location via modification of an input signal to the controller. An example could be a change in an instrument air signal. This option of a controller avoids the need to enter the controller for manual set point adjustment. Seat Leak Test: Unlike disc hydrostatic testing, which confirms the structural integrity of the valve body, seat leak testing confirms the ability of the valve disc and seat to retain rated pressure without exceeding a specified leak rate. Several industrial standards exist which provide seat leak test procedures. Seat leak testing should be performed by the manufacturer on all tight shutoff valves to assure proper operation when installed by the user. Set Point: A term used to describe the value at which a controller will attempt to maintain a controlled variable. For example, if a controller is to maintain a system pressure of 50 psig, this value is the set point. Stability: The ability of a system to respond to changes in a manner such that repetitive over-correction is avoided. When a system change occurs, such as a change in flow rate, a valve may be directed by a controller to change its position to maintain constant system pressure. Normally some over-correction in the form of excess valve movement will occur, thereby necessitating a reversal of valve movement. In a stable system, such reversals occur only a few times, with the valve reaching a new position compatible with the current flow rate.

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In an unstable system, valve reversal and resultant pressure fluctuations recur continually, or for an excess period of time. Excessive system gain could result in this action. Our example of a one-time change in flow rate is, of course, simplistic. In many systems, the flow rate may change frequently such that the valve seldom rests at any one position. Valve response must still, however, be compatible to the needs of the system. Step Response: Step response is a measurement of the ability of a valve and actuator to respond to a rapid change in control signal. In at least one case it is defined as the time required for a valve to travel 63.2% of that amount of travel caused by an instantaneous change in input signal when the change in input signal equals 10% of the full input signal span. Step response can relate to variables other than valve position, such as process variable, controller output, etc. Tight Shut Off: Many valve manufacturers use this term to indicate that no visually detectable leakage will occur past the valve seat during test or after installation. This varies with some manufacturers however, and may in a few cases indicate only that the leak rate is small compared to the maximum valve capacity. A leak rate standard had been developed, ANSI B16.104-1976, which provides leakage classifications. Torques: Rotary motion valves such as butterfly valves require the application of torque to cause, or in some cases to prevent valve motion. This required torque is an important consideration when selecting an actuator for the valve. The required torque is also an important factor in valve design and material selection, as all components must accept the resultant stresses without permanent deformation or failure. Turbulent Flow: A state of flow in which all laminar flow has disappeared and full turbulence exists in the fluid. Turbulent flow normally exists in applications where the Reynolds number value exceeds 4000 and seldom exists where the Reynolds number value is less than 2000. Two Phase Flow: The combined simultaneous flow of gas and liquid. Special sizing techniques are required. Vena Contracta: When the fluid in the pipeline passes through a restriction such as a valve, there is a converging of the flow as it enters the restriction. The cross section of the flowing stream continues to diminish for a short distance downstream of the restriction. The area of smallest cross section is the Vena Contracta. It is not uncommon for the term Vena Contracta to be used in a slightly broader sense to refer to the length of flow stream, downstream of the restriction, which is less in cross section, greater in velocity and lower in pressure than that which exists further downstream in the piping. Viscosity: Viscosity is a measure of the internal fluid friction or the resistance of a fluid to flow. Viscosity absolute:

The ratio of the shearing stress to the shear rate of fluid. Usually expressed in centipoises.

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Viscosity Kinematic:

The absolute viscosity divided by the density of the fluid. Usually expressed in centistokes.

Viscosity SUS:

Saybolt Universal Seconds (SUS). Based upon the time in seconds for 50 ml of oil to flow through a standard orifice at a given temperature (ASTM D88-56).

Viscosity Index:

A measure of the viscosity temperature characteristics of a fluid as referred to that of two arbitrary reference fluids (ASTM DS67-53).

Water Hammer, Causes: Because certain types of valves can be closed quickly with todays actuators and accessories, their use on water lines could cause a pressure surge in the line known as water hammer. This condition is familiar to anyone who has closed his or her household faucet quickly and heard the resulting noise in the adjacent piping. When this occurs in a large pipeline where the amount and velocity of the liquid (yes, it is not only with water) are both high, and in conjunction with the speed of closure along with the length of line, the pressure waves rebounding in the pipe reinforce each other which results in significant damage to pipe, fittings and valves.

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VALVE SIZING & SELECTION

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VALVE SIZING In sizing valves it is important to understand that the control valve is sized for process requirements that will actually occur not by the pipe size that it will be installed in. In doing this, the process flow requirements of minimum, normal and maximum required are the key elements. If the valve is not sized to the actual or theoretical flow requirements, then one of the problems that will arise is valve over sizing. Over sizing of valves generally occurs when attempting to optimize process performance through a reduction of process variability. This usually results from using line-size valves, especially with high-capacity rotary valves as well as the conservative addition of multiple safety factors at different stages in the design. Over sizing the valve impairs process variability in two ways. First, the over sized valve puts too much gain the system leaving less flexibility in adjustments to the controller. Best performance results when loop gain comes from the controller. The second impairment is that the over sized valve is likely to operate more frequently at lower valve openings where seal and friction can be greater, particularly in rotary valves. Because an over sized valve produces a disproportionately large flow change for a given increment of travel, this can greatly exaggerate the process variable. Regardless of its actual inherent valve characteristic, a severely over sized valve tends to act more along the lines of a quick opening valve which results in high installed process gain in the lower rotation of the valve. In addition, the valve tends to reach system capacity at relatively low travel. Consequently, there is little hope of achieving acceptable process variability in this occurrence. When selecting a valve, it is important to consider the valve style, inherent characteristic and valve size that will provide the broadest possible control range for the application. **There are numerous techniques and equations available with which to determine proper valve sizes for each application. What we will outline for reference purposes in this manual is a Method A sizing equation for liquid, gas and steam. These equations reflect a simple approach and do not inherently consider the effects of cavitation, swaged pipe or laminar flow. Under most conditions though this method will provide suitable results. The Tyco E-size valve sizing program will have all the updated equations as per ISA (Instrument Society of America) that will provide consideration of all system characteristics based off of your input into the program. This program should be used for all of your sizing purposes. The above Method A equations are provided for that rare instance where you might have to manually calculate a flow condition for a customer. In any case, you should always check your results with the Tyco program.

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Method A

(1) Liquid Sizing Equation:

A. To solve for valve size, determine Cv required. Select valve size from Cv table.

Cv = )(.).()PGSQ

(

B. To solve for flow volume.

Q = ).()()GSPCv (

Cv = Valve capacity coefficientQ = Flow U.S.G.P.M. P = Differential pressure

across valve - PSI S.G. = Specific gravity of liquid (water = 1)

C. To solve for pressure differential

P = .).()()(

2

2

GSCvQ

Equations (B) and (C) are transformations of equation (A). (2) Gas Sizing Equation:

(A) To solve for valve size, determine Cv required. Select valve size from Cv table.

Cv =))((

.).()(2 PPGSQ

P2 = Pipeline pressure downstream

of the valve absolute (PSIA) P = Pressure differential PSI P

may not exceed of the inlet pressure absolute (PSIA). If this should occur, refer to sizing method ISA.

Q = Flow SCFM Cv = Valve capacity coefficient

(same value as for liquids) S.G. = Specific gravity of gas (air = 1)

(B) To solve for volume of flow (SCFM).

Q = .).(

))(() 2

GSPP

Cv

(

(C) To solve for pressure differential.

))((.).)((

22

2

PCvGSQP =

Equations (B) and (C) are transformation of equation (A).

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(3). Steam Sizing Equation:

(A) To solve for valve size, determine Cv required. Select valve size from Cv table.

W = Flow lbs per hour P = Pressure differential PSI.

P may not exceed of the inlet pressure absolute (PSIA). If this should occur, refer to sizing method ISA.

2P = Downstream pressure PSIA. Cv = Valve flow coefficient (same as

liquid value) S.G. = Specific gravity (air = 1) Q = SCFH MW = Molecular Wt = Density in #/ft3 at standard

conditions.

))(()3( 2 PPWCv

=

(B) To solve for of flow.

))((3 2 PPCvW =

(C) To solve for pressure differential.

))()(9()(

22

2

PCvWP =

Equations (B) and (C) are transformation of equation (A). To convert from pounds per hour to SCFH:

GS

WQ.

)1.13)((=

To convert from SCFH to pounds per hour:

1.13

.).)(( GSQW =

Also:

)379()(

)(MWWQ =

wQ =

S.G. = (0.0331)(MW)

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VALVE SELECTION

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CONTROL VALVE CHARACTERISTICS AND SYSTEM REQUIREMENTS Description: There are several control characteristics. A few are described below. It must be noted that a valve having a stated inherent characteristic may provide a different installed characteristic due to interaction with the system. Linear Characteristic: Flow rate is proportional to valve travel. Equal Percentage: Equal increments of valve travel produce equal percentage changes in flow rate as related to the flow rate which existed at the previous travel position.

Example: If a valve travel change from 20% open to 30% open produced a 70% change in flow rate, then a valve travel change from 30% open to 40% open would produce another 70% change in flow rate. If flow rate at 20% open was 100 GPM, then flow rate at 30% open would be 170 GPM and the flow rate at 40% open would be 70% greater than at 30% travel or 289 GPM, etc. for each additional incremental travel position.

Quick Opening: Flow rate through the valve increases very rapidly for incremental changes in valve travel when valve position is near closed. As valve position becomes more open, flow rate changes diminish with incremental changes in valve travel approaching zero change as the valve position nears full open.

ROTARY VALVES Butterfly Valves

Bodies require minimum space for installation. Provide high capacity with low pressure loss through the valve. Are economic, particularly in larger sizes and in terms of flow capacity per investment

dollar. Conventional disc provides throttling control from 30-60 degree rotation. Bodies mate with standard raised-faced pipeline flanges. Standard liners can provide good shutoff and corrosion protection. Standard butterfly valves are available within Tyco in sizes through 102 for

miscellaneous applications. Butterfly valves exhibit an approximately equal percentage flow characteristic. They can be used for throttling or for on-off control.

V-Port Ball Control Valves

Construction is similar to standard ball valve but controlling member is a partial sphere with a segmented v-port (notch). The V-notch produces an equal percentage flow characteristic. These valves have good rangeability, control and shutoff capabilities. The paper industry, chemical plants, power industry, petroleum refining and sewage treatment facilities use such valves.

Straight through flow design exhibits little pressure drop.

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V-notch valves typically are used to control erosive or viscous fluids, paper stock or other slurries containing entrained solids or fibers.

The ball or sphere remains in contact with the seat during rotation, which produces a shearing effect as the ball closes and minimizes clogging.

Control ranges from 100:1 to 250:1 Bodies are available in flanges or flangeless configuration. Both styles mate with Class

150 and 300 flanges. Added Note: Butterfly valves are high recovery valves. This means that compared to some types of valves, such as globe styles, butterfly valves exhibit lower FL values. Based upon the previous P max formula, it would be fair to expect that cavitation occurs in butterfly valves more easily than in globe valves. This is true when comparing valves placed in systems requiring specific pressure drops. In these cases, globe valves can be used on higher Ps than can butterfly valves. In flow control applications however, butterfly valves can flow considerably more for a given valve size, than can a globe valve before cavitation occurs. An example can be used for demonstration. Butterfly Valve Globe Valve Size 6" 6" FL (at full travel position) 0.55 0.866 Fluid Water Water Specific Gravity 1.0 1.0 Temperature 100F 100F P1 100 psia 101 psia PV .95 psia .95 psia FF 0.96 0.96 P max = FL2 (P1 FF PV 30 PSI 74.3 PSI Cv 2790 770

Q = GSP.

Cv 15281 GPM at cavitation

6637 GPM at cavitation

The purpose of this section is to demonstrate that it is not appropriate to conclude that either butterfly or globe style valves, or any other styles, are superior for control applications simply on the basis of their recovery characteristics.

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Velocity vs Component Deformation: (Butterfly Valves) Butterfly valve seats are subjected to the forces generated by fluids passing through the valves. As the flowing velocity increases, the forces increase in magnitude and effect. Generally the maximum velocities are dictated by the type and geometry of the seat. Guidelines are as follows: Seat Max Liquid Velocity Max Gas Velocity

None * *

Full elastomer seat w/o internal support or with non-metallic internal support

20 ft/sec

200 ft/sec

Full elastomers seat with internal steel support

25 ft/sec 300 ft/sec

Small section elastomers or polymer seat fully supported on 3 surfaces by valve structure

25 ft/sec

350 ft/sec

Metal seats, retained on 3 surfaces by valve structure * *

* Note: There is no practical limit imposed by the seat geometry. Velocity limitations for the valve would be as discussed previously in this section.

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CAVITATION & FLASHING Causes: IEC liquid sizing standards calculate an allowable sizing pressure drop or dP max, which is defined by system conditions of P1 (inlet) and P2 (outlet), which equates to actual pressure drop across the valve. If the actual pressure drop (P1-P2) is greater than the dP max then either cavitation or flashing may occur. This occurrence may cause structural damage to the valve and or adjacent piping. Cavitation and flashing are physical phenomenas that occur because they represent actual changes in the form of the fluid. This is represented by the fluid changing from liquid state to the vapor state which results from the increase in fluid velocity which is at or near downstream of the greatest flow restriction, usually the valve port. As the fluid passes through this restriction it narrows or necks down which is usually referred to as the vena contracta. To maintain a constant flow of liquid through the valve the velocity must be the greatest at the vena contracta. This increase in velocity is accompanied by a substantial decrease in pressure. Further downstream as the fluid expands into a larger area, velocity decreases and pressure increases but never recovers to the pressure that exists upstream of the valve. Irrespective of the recovery characteristic of the valve, the pressure differential of concern regarding cavitation and or flashing is the differential between the valve inlet pressure and the vena contracta. If the pressure at the vena contracta drops below the vapor pressure of the liquid, bubbles will form in the flow stream. Formation of bubbles will increase rapidly as the vena contracta pressure drops further below the vapor pressure of the fluid. If the pressure at the valve outlet remains below the vapor pressure of the liquid, then bubbles will remain in the downstream system and the process is considered to have flashed. Flashing can cause serious erosion damage to the valve internals and the typical appearance is a smooth, polished to the eroded surface. Furthermore, if the downstream pressure recovers and increases the outlet pressure above the vapor pressure of the liquid, the bubbles will implode which creates tiny microscopic jets of liquid or cavitation. The collapsing or implosion of the bubbles releases energy and produces a noise that sounds like gravel flowing through the valve. Cavitation damage is recognized by a rough surface usually described as a Swiss cheese appearance. Generally high recovery valves tend to be more conducive to cavitation because the downstream pressure recovers faster back above the liquids vapor pressure. Flashing: To clarify this condition, the variables that create flashing are not directly controlled by the valve. What this means is that there is no way for any control valve to prevent this condition. The best solution to this problem is to select a valve with a proper geometry to minimize the effects. Making the affected surfaces as hard as possible or lowering the velocity of the flow are also effective options. Cavitation: This condition can be addressed as follows:

Eliminate the condition by managing the pressure drop. If this can be controlled where the pressure never drops below the vapor pressure, then the formation of bubbles is unlikely.

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Hardening of the effected surfaces to minimize the effects, this method does not eliminate but merely lengthens the life of the valve.

Change the system to prevent the occurrence. Elevation of P2 or downstream pressure so that the vena contracta does not fall below vapor pressure. Applying an orifice plate or similar backpressure devices can also raise P2 at the valve.

If using Butterfly valves, select a larger valve that has the desired Cv at a lower travel position. The recovery factor is greater for lower travel positions; there is a practical limit due to the control that is obtainable.

Placing valves in series where simultaneous and duplicate actuation will cause equal sharing of the pressure drop.

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VALVE TORQUE DATA

CRITERIA FOR DETERMINING SEATING AND UNSEATING TORQUE BY APPLICATION CATEGORY RESILIENT SEATED VALVES

The seating-unseating torque anticipated in resilient seated valves varies widely with service conditions. Factors affecting torque values listed generally in order of significance follow: (1) Operating Frequency: The first opening after sustained period of closure is the tough one. (2) Media Lubricating Characteristics: Water is probably the best all-around lubricant for metal elastomers contact. Is the service completely dry? Seat compounds contain some lubricant. Is it extracted in service? LUBRICATING NON-LUBRICATING Water Air Dry Gas Aqueous Process Streams Dry Powder, Pellets Lubricating Oil Aromatic Hydrocarbons, i.e. diesel oil/JP fuels Industrial Solvents, i.e. acetone/ethyl acetate (3) Condition of Disc Edge: It is an iron disc in corrosive service? Iron discs in uninhibited water systems corrode. The edge roughens and corrosion deposits build up. Is there anticipated a deposit on seating surfaces calcium in a hard water system various salts in seawater. (4) Temperature: High or low Operating temperature approaching upper limits of seat material tend to increase hardness over a sustained period. Temperature approaching the lower limits of elastomers raise hardness immediately. Both conditions increase operating torque. (5) Chemical Attack on Elastomer Causing Swell: Increased interference and torque results. In the accompanying data Anticipated Seating and Unseating Torque is provided by category. Following is a general definition of categories I, II and III. Category I Note: Category I values should be used only for proportioning service where full 90 closure is not required. Ideal Conditions

- operating frequency at least once per day - lubricating media aqueous liquid - disc totally resistant to corrosion by line media; no solids deposition - temperature well within elastomers limits - no chemical effect on elastomers

Page 23 of 25

Torque values provided in this category approximate results of short term shop tests on new equipment under ideal conditions. No allowance is made for torque increase under service conditions. Selection of proportioning type actuators where shutoff requirements are not critical or where travel stops prevent 90 closure may be made under Category I. Category II Normal Conditions

- operating frequency at least once per month - lubricating media aqueous liquid - disc corrosion - mild/minor deposition - temperature within material limits - chemical effects on elastomers minor

Torque values provided in this category incorporate a factor of two over shop tests in establishing frictional resistance of media-exposed elements. Experience has indicated that selection of actuators based on Category II values provides totally satisfactory results except in the most severe applications. Category III Severe Torque Conditions

- operating frequency indefinitely long - non-lubricating media air, dry gas - disc corrosion severe - temperature outside recommended limits - chemical effects on elastomers unknown

Torque values provided in this category incorporate a factor of three over shop test in establishing frictional resistance of media-exposed elements. Pneumatic conveying is a typical Category III application. In selecting actuators under Category III, it is also necessary to compare Anticipated Seating-Unseating Torque with Allowable Operating Torque on valve. This is especially important in power actuators not equipped with speed controls where impact loading may occur.

Page 24 of 25

NOTES:(1) ALL ACTUATOR SELECTION VALVE

TABLES CONTAINED IN THE SIZE 0 50 100 150 175KEYSTONE PRODUCT MANUAL 2" 110 114 119 123 125ARE BASED ON CATEGORY - II 2.5" 135 142 149 156 159TORQUE REQUIREMENTS. 3" 160 170 180 190 195CATEGORY - I SHOULD NOT 4" 240 260 279 299 309BE USED UNLESS ALL OF THE 5" 325 362 399 436 454CRITERIA FOR IT ARE MET. 6" 450 503 556 609 636

8" 750 860 970 1080 1135(2) THE CHARTED TORQUE VALUES 10" 1150 1371 1592 1813 1924

ABOVE ARE THE TOTAL OF ALL 12" 1550 1868 2187 2505 2664INTERNAL FRICTIONAL RESIST- 14" 2150 2997 3845 4692 --ANCES FOR OPENING OR 16" 2750 4058 5366 6674 --CLOSING AGAINST INDICATED 18" 3450 5360 7270 9180 --PRESSURE. 20" 4250 6922 9595 12267 --

(3) THE EFFECT OF DYNAMICTORSION IS NOT CONSIDERED VALVEIN THIS TABULATION. SIZE 0 50 100 150 175

2" 220 224 229 233 235(4) TORSIONAL CAPACITY OF 2.5" 270 277 284 291 294

VALVE STEM IS NOT 3" 320 330 340 350 355CONSIDERED IN THIS 4" 480 500 519 539 549TABULATION. 5" 650 687 724 761 779

6" 900 953 1006 1059 1086(5) IF PRESSURE DIFFERENTIAL 8" 1500 1610 1720 1830 1885

IS NOT KNOWN, USE FULL 10" 2300 2521 2742 2963 3074RATED PRESSURE CAPABILITY 12" 3100 3418 3737 4055 4214OF THE VALVE. 14" 4300 5147 5995 6842 --

16" 5500 6808 8116 9424 --18" 6900 8810 10720 12630 --20" 8500 11172 13845 16517 --

VALVESIZE 0 50 100 150 175

2" 330 334 339 343 3452.5" 405 412 419 426 4293" 480 490 500 510 5154" 720 740 759 779 7895" 975 1012 1049 1086 11046" 1350 1403 1456 1509 15368" 2250 2360 2470 2580 263510" 3450 36741 3892 4113 422412" 4650 4968 5287 5605 576414" 6450 7297 8145 8992 --16" 8250 9558 10866 12174 --18" 10350 12260 14170 16080 --20" 12750 15422 18095 20767 --

11/13/02

PRESSURE DIFFERENTIAL

CATEGORY III (SEVERE CONDITIONS)PRESSURE DIFFERENTIAL

AR1/AR2 VALVESSEATING AND UNSEATING TORQUES (INCH-LBS.)

STANDARD DISC DIAMETERSSIZES 2" - 20"

CATEGORY I (IDEAL CONDITIONS)PRESSURE DIFFERENTIAL

CATEGORY II (NORMAL CONDITIONS)


TABLES CONTAINED IN THE SIZE 0 50KEYSTONE PRODUCT MANUAL 4" 165 185ARE BASED ON CATEGORY - II 5" 220 257TORQUE REQUIREMENTS. 6" 305 358CATEGORY - I SHOULD NOT 8" 500 610BE USED UNLESS ALL OF THE 10" 750 971CRITERIA FOR IT ARE MET. 12" 1000 1318

14" 1450 2297(2) THE CHARTED TORQUE VALUES 16" 1850 3158

ABOVE ARE THE TOTAL OF ALL 18" 2350 4260INTERNAL FRICTIONAL RESIST- 20" 2850 5522ANCES FOR OPENING OR CLOSING AGAINST INDICATEDPRESSURE.

(3) THE EFFECT OF DYNAMICTORSION IS NOT CONSIDERED VALVEIN THIS TABULATION. SIZE 0 50

4" 330 350(4) TORSIONAL CAPACITY OF 5" 440 477

VALVE STEM IS NOT 6" 610 663CONSIDERED IN THIS 8" 1000 1110TABULATION. 10" 1500 1721

12" 2000 2318(5) IF PRESSURE DIFFERENTIAL 14" 2900 3747

IS NOT KNOWN, USE FULL 16" 3700 5008RATED PRESSURE CAPABILITY 18" 4700 6610OF THE VALVE. 20" 5700 8372

(6) SIZE 2", 2.5" AND 3" ARE NOTAVAILABLE WITH REDUCEDDISC DIAMETERS.

VALVESIZE 0 50

4" 495 5155" 660 6976" 915 9688" 1500 161010" 2250 247112" 3000 331814" 4350 519716" 5550 685818" 7050 896020" 8550 11222



AR1/AR2 VALVESSEATING AND UNSEATING TORQUES (INCH-LBS.)

REDUCED DISC DIAMETERS50 PSI MAXIMUM RATING

SIZES 4" - 20"






ABOVE ARE THE TOTAL OF ALL 12" 1550 2050 2550 3050 3550INTERNAL FRICTIONAL RESIST- 14" 2150 2950 3750 4550 5350ANCES FOR OPENING OR 16" 2750 3950 5150 6350 7550CLOSING AGAINST INDICATED 18" 3450 5250 7050 8850 10650PRESSURE. 20" 4250 6750 9250 11750 14250

(3) THE EFFECT OF DYNAMICTORSION IS NOT CONSIDERED VALVEIN THIS TABULATION. SIZE 0 50 100 150 200

2" 220 230 240 250 260(4) PRESSURE CAPACITY (RATING) 2.5" 270 280 290 300 310

OF VALVES IS NOT CONSIDERED 3" 320 340 360 380 400IN THIS TABULATION. 4" 480 510 540 570 600

5" 650 700 750 800 850(5) TORSIONAL CAPACITY OF 6" 900 1000 1100 1200 1300

VALVE STEM IS NOT 8" 1500 1700 1900 2100 2300CONSIDERED IN THIS 10" 2300 2600 2900 3200 3500TABULATION. 12" 3100 3600 4100 4600 5100

14" 4300 5100 5900 6700 7500(6) IF PRESSURE DIFFERENTIAL 16" 5500 6700 7900 9100 10300

IS NOT KNOWN, USE FULL 18" 6900 8700 10500 12300 14100RATED PRESSURE CAPABILITY 20" 8500 11000 13500 16000 18500OF THE VALVE.

(7) FOR 1" AND 1.5" VALVES, USE VALVETHE 2" VALVE TORQUE VALUES. SIZE 0 50 100 150 200

2" 330 340 350 360 3702.5" 405 410 420 430 4403" 480 500 520 540 5604" 720 750 780 810 8405" 975 1025 1075 1125 11756" 1350 1450 1550 1650 17508" 2250 2450 2650 2850 305010" 3450 3750 4050 4350 465012" 4650 5150 5650 6150 665014" 6450 7250 8050 8850 965016" 8250 9450 10650 11850 1305018" 10350 12150 13950 15750 1750020" 12750 15250 17750 20250 22750

11/13/02



FIGURE 99, 100, 129, 239, 990/992 AND 999 VALVESSEATING AND UNSEATING TORQUES (INCH-LBS.)




SIZE 50 PSI 100 PSI 150 PSI 200 PSI 250 PSI2" 85 108 126 144 162

2.5" 126 153 175 198 2213" 180 207 256 297 3394" 355 414 472 531 5905" 562 652 715 787 8696" 918 1035 1152 1269 13868" 1440 1692 1944 2205 247610" 2466 3010 3550 4095 466012" 3510 4140 5616 7686 1055614" 5200 6000 7500 8550 NA16" 6900 8000 9500 10750 NA18" 9000 10500 12000 13500 NA20" 11000 14000 15200 17600 NA24" 16000 21000 28000 33700 NA

Since torque greatly increases for dry and non-lubricating fluids and temperatur variations, please contact your Tyco Valves & Controls representative for accurate values for these applications.

LINE PRESSURE

FIGURE 601/602 VALVESSEATING AND UNSEATING TORQUES (INCH-LBS.)


Torque is the rotary effort required to operate a valve. This turning force in a butterfly valve is determined by three factors -- the friction of the disc and seat due to interference for sealing, bearing friction, and fluid dynamic torque.

NOTES:(1) CATEGORY - I SHOULD NOT VALVE

BE USED UNLESS ALL OF THE SIZE 0 50 100 150CRITERIA FOR IT ARE MET. 24" 4875 8497 12119 15741

30" 7500 14574 21648 28722(2) THE CHARTED TORQUE VALUES 36" 10500 22724 34948 47172

ABOVE ARE THE TOTAL OF ALL 42" 21750 49480 77210 104940INTERNAL FRICTIONAL RESIST- 48" 28125 68871 109617 150364ANCES FOR OPENING OR CLOSING AGAINST INDICATEDPRESSURE. VALVE

SIZE 0 50 100 150(3) THE EFFECT OF DYNAMIC 24" 9750 13372 16994 20616

TORSION IS NOT CONSIDERED 30" 15000 22074 29148 36222IN THIS TABULATION. 36" 21000 33224 45448 57672

42" 43500 71230 98960 126690(4) TORSIONAL CAPACITY OF 48" 56250 96996 137742 178489

VALVE STEM IS NOTCONSIDERED IN THISTABULATION. VALVE

SIZE 0 50 100 150(5) IF PRESSURE DIFFERENTIAL 24" 14625 18247 21869 25491

IS NOT KNOWN, USE FULL 30" 22500 29574 36648 43722RATED PRESSURE CAPABILITY 36" 31500 43724 55948 68172OF THE VALVE. 42" 65250 92980 120710 148440

48" 84375 125121 165867 206614



FIGURE 106, 601/602 VALVESSEATING AND UNSEATING TORQUES (INCH-LBS.)







ABOVE ARE THE TOTAL OF ALL 12" 2100 2577 3055 3532 4487INTERNAL FRICTIONAL RESIST-ANCES FOR OPENING OR CLOSING AGAINST INDICATED VALVEPRESSURE. SIZE 0 50 100 150 250

2" 115 122 128 135 1482.5" 150 160 171 181 202

(3) THE EFFECT OF DYNAMIC 3" 175 190 205 220 250TORSION IS NOT CONSIDERED 4" 270 299 329 358 417IN THIS TABULATION. 5" 445 500 556 611 721

6" 585 665 744 824 983(4) TORSIONAL CAPACITY OF 8" 1560 1725 1890 2055 2385

VALVE STEM IS NOT 10" 2640 2972 3303 3635 4298CONSIDERED IN THIS 12" 3000 3477 3955 4432 5387TABULATION.

(5) IF PRESSURE DIFFERENTIAL VALVEIS NOT KNOWN, USE FULL SIZE 0 50 100 150 250RATED PRESSURE CAPABILITY 2" 288 294 301 307 321OF THE VALVE. 2.5" 375 385 396 406 427

3" 438 452 467 482 5124" 675 704 734 763 8225" 1113 1168 1223 1278 13896" 1463 1542 1622 1701 18608" 3900 4065 4230 4395 472510" 6600 6932 7263 7595 825812" 7500 7977 8455 8932 9887

11/13/02



FIGURE 222 VALVESEATING AND UNSEATING TORQUES (INCH-LBS.)




SIZE(MM)

SIZE(IN)

TORQUE0 PSI

TORQUE50 PSI

TORQUE100 PSI

50 2" 44 51 5865 2.5" 58 68 7880 3" 67 82 97100 4" 104 133 163125 5" 171 227 282150 6" 225 305 384200 8" 764 929 1095250 10" 1294 1625 1957300 12" 1470 1947 2425

SIZE(MM)

SIZE(IN)

TORQUE0 PSI

TORQUE50 PSI

TORQUE100 PSI

50 2" 63 70 7765 2.5" 83 93 10380 3" 96 111 126100 4" 149 178 207125 5" 245 300 355150 6" 322 401 481200 8" 1092 1257 1422250 10" 1848 2180 2511300 12" 2100 2577 3055

SIZE(MM)

SIZE(IN)

TORQUE0 PSI

TORQUE50 PSI

TORQUE100 PSI

50 2" 158 165 17165 2.5" 206 217 22780 3" 241 256 270100 4" 371 401 430125 5" 612 667 722150 6" 804 884 964200 8" 2730 2895 3060250 10" 4620 4952 5283300 12" 5250 5727 6205

11/13/02

UNDERCUT FIGURE 222 TORQUE FIGURES

LUBRICIOUS SERVICE: OIL(.7 APPLICATION FACTOR)

WATER: NON CORROSIVE DISC EDGE(1.0 APPLICATION FACTOR)

DRY SERVICE: AIR(2.5 APPLICATION FACTOR)


TABLES CONTAINED IN THE SIZE 0 50 100 150 200 250 285KEYSTONE PRODUCT MANUAL 2" 69 78 86 95 103 112 118ARE BASED ON CATEGORY - II 2.5" 107 124 141 158 176 193 205TORQUE REQUIREMENTS. 3" 131 150 169 188 207 226 239CATEGORY - I SHOULD NOT 4" 195 230 265 301 336 371 396BE USED UNLESS ALL OF THE 5" 245 329 413 496 580 664 722CRITERIA FOR IT ARE MET. 6" 336 447 558 669 779 890 968

8" 375 624 873 1121 1370 1619 1793(2) THE CHARTED TORQUE VALUES 10" 509 933 1358 1782 2207 2632 2929

ABOVE ARE THE TOTAL OF ALL 12" 728 1338 1949 2559 3170 3781 4208INTERNAL FRICTIONAL RESIST-ANCES FOR OPENING OR CLOSING AGAINST INDICATED VALVEPRESSURE. SIZE 0 50 100 150 200 250 285

2" 92 101 109 118 126 135 141(3) THE EFFECT OF DYNAMIC 2.5" 122 138 155 171 188 204 216

TORSION IS NOT CONSIDERED 3" 133 153 173 193 213 232 246IN THIS TABULATION. 4" 260 296 333 369 406 442 468

5" 327 411 495 579 664 748 807(4) PRESSURE CAPACITY (RATING) 6" 448 563 677 792 906 1021 1101

OF VALVES IS NOT CONSIDERED 8" 386 646 905 1165 1425 1684 1866IN THIS TABULATION. 10" 678 1119 1560 2000 2441 2882 3191

12" 970 1604 2238 2873 3507 4141 4585(5) TORSIONAL CAPACITY OF

VALVE STEM IS NOTCONSIDERED IN THIS VALVETABULATION. SIZE 0 50 100 150 200 250 285

2" 175 183 192 200 209 217 223(6) IF PRESSURE DIFFERENTIAL 2.5" 270 287 304 322 339 356 368

IS NOT KNOWN, USE FULL 3" 333 351 370 389 408 427 440RATED PRESSURE CAPABILITY 4" 494 529 564 600 635 670 695OF THE VALVE. 5" 621 705 789 872 956 1040 1099

6" 851 962 1073 1184 1295 1406 1483(7) FOR 1" AND 1.5" VALVES, USE 8" 950 1199 1448 1696 1945 2194 2368

THE 2" VALVE TORQUE VALUES. 10" 1288 1713 2137 2562 2987 3411 370912" 1843 2454 3064 3675 4285 4896 5324

######


PRESSURE DIFFERENTIALCATEGORY II (NORMAL CONDITIONS)


FIGURE 310/312 VALVESBI-DIRECTIONAL SEATING AND UNSEATING TORQUES

SIZES 2" - 12"

VALVESIZE 0 150 200

ANSI 150285 400 500

ANSI 300740

2" 200 220 280 380 460 520 5802.5" 200 220 280 380 460 520 5803" 230 250 320 430 520 590 6504" 400 475 600 820 995 1120 12355" 810 925 1125 1350 1570 1750 19006" 980 1370 1600 1850 2150 2390 29008" 1720 2060 2330 3200 4020 4870 672010" 2700 3340 3650 4700 6250 7450 985012" 3750 4590 5250 6400 8160 9690 1294014" 5520 6750 7560 9150 11450 13300 1720016" 7100 9350 10450 12600 15000 17500 2220018" 8700 11900 13300 15800 19500 21900 2850020" 10000 15600 17500 21000 25200 28700 3614024" 12250 21700 25340 30600 36900 42100 5400030" 15000 29200 35000 43500 54500 62500 8000036" 35000 52500 58500 70000 85000 97500 125000

NOTES: (1)

(2)

(3)

ABOVE VALUES INCLUDE PACKING AND BEARING AS WELL AS ECCENTRIC DISC IMBALANCE TORQUES.

IF PRESSURE DIFFERENTIAL IS NOT KNOWN, USE FULL RATED PRESSURE CAPABILITY OF THE VALVE.


K-LOKFIGURE 360, 362, 370 AND 372 VALVES

BI-DIRECTIONAL SEATING AND UNSEATING TORQUES (INCH-LBS.)SIZES 2" - 36"

TFE AND RTFE SEATS

TORQUE VALUES REPRESENT TESTED BREAKAWAY TORQUES WITH ADEQUATE SAFETY MARGIN FOR CLEAN SERVICES WITH TEMPERATURES ABOVE -20 DEGREES F.

NOTES: VALVE PRESSURE DIFFERENTIALSIZE 285

(1) TORQUE VALUES REPRESENT TESTED 2" 760BREAKAWAY TORQUES WITH ADEQUATE 2.5" 760SAFETY MARGIN FOR CLEAN SERVICES 3" 860WITH TEMPERATURES ABOVE -20 4" 1640DEGREES F. 5" 2700

6" 3700(2) ABOVE VALUES INCLUDE PACKING AND 8" 6400

BEARING AS WELL AS ECCENTRIC DISC 10" 9400IMBALANCE TORQUES. 12" 12800

14" 1830016" 2540018" 3160020" 4200024" 6120030" NA36" NA

11/13/02



METAL AND FIRESAFE SEATS

VALVESIZE 0 150 200

ANSI 150285 400 500

ANSI 300740

2" 260 286 364 494 598 676 7542.5" 260 286 364 494 598 676 7543" 299 325 416 559 676 767 8454" 520 618 780 1066 1294 1456 16065" 1053 1203 1463 1755 2041 2275 24706" 1274 1781 2080 2405 2795 3107 37708" 2236 2678 3029 4160 5226 6331 873610" 3510 4342 4745 6110 8125 9685 1280512" 4875 5967 6825 8320 10608 12597 1682214" 7176 8775 9828 11895 14885 17290 2236016" 9230 12155 13585 16380 19500 22750 2886018" 11310 15470 17290 20540 25350 28470 3705020" 13000 20280 22750 27300 32760 37310 4698224" 15925 28210 32942 39780 47970 54730 7020030" 19500 37960 45500 56550 70850 81250 10400036" 45500 68250 76050 91000 110500 126750 162500

NOTES: (1)

(2)

(3)

(4)

11/13/02



ULTRA HIGH MOLECULAR WEIGHT POLYETHYLENE SEATS (UHMWPE)




FOR SOLIDS OR ABRASIVE SERVICE, USE 1.3 X THE ABOVE VALUES.


VALVESIZE 0 150 200

ANSI 150285 400 500

ANSI 300740

2" 280 308 392 532 644 728 8122.5" 280 308 392 532 644 728 8123" 322 350 448 602 728 826 9104" 560 665 840 1148 1393 1568 17295" 1134 1295 1575 1890 2198 2450 26606" 1372 1918 2240 2590 3010 3346 40608" 2408 2884 3262 4480 5628 6818 940810" 3780 4676 5110 6580 8750 10430 1379012" 5250 6426 7350 8960 11424 13566 1811614" 7728 9450 10584 12810 16030 18620 2408016" 9940 13090 14630 17640 21000 24500 3108018" 12180 16660 18620 22120 27300 30660 3990020" 14000 21840 24500 29400 35280 40180 5059624" 17150 30380 35476 42840 51660 58940 7560030" 21000 40880 49000 60900 76300 87500 11200036" 49000 73500 81900 98000 119000 136500 175000

NOTES: (1)

(2)

(3)

11/13/02





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t:;:-:~ -::=--:7------=-= ----

=::'_ "::

:::.:::L:

=~. ~~..-- :_. :' -_..:-- .....

--- ::::L_:' :'1--

---- --- ....- "----- --+-'" - - '

,e",

.:- -

:-r=

---'---' -_..

---==1'.

----, -- -

1---

.. .. !-- .:::: ---:-

1- -

..- -----

----I

' :'--

,_.. .._.m_.._--

-- -'- ---

.. uT:-

'::? - - --- -=-.:.--- -_::=- --.. ,_. _. . :-.

:F.

:-- :-.

:c-

~:'=-- ;:-

~L~: -::::r-=--

,-_ :_- -- --- .~~-

-- u

= -::~' :_- -- :'. ::.-- --=--:_-

-. n

-----. .-..--...- ..-.-----

100 150 200 350250 300 400 450 500 550 600 650DIFFERENTIAL PRESSURE PSI

, 0, Box 21 9007 Houston . Texas 77218 . (713) 492-8800 . Fax (713) 492-8905

6 "

5 .,4 "

2-1/2"

1-1/2"

1 "

- -..-

700

ENGINEERING DATA

Page 25 of 25

To Convert From ToDegreesCelcius

Degrees Fahrenheit

DegreesCelcius Kelvin

Degrees Fahrenheit Degrees Celcius

Degrees Fahrenheit Degrees Rankin

Note: Use Multiplier at Convergence of Row and Column

Cubic Decimeters

(Liters)

Cubic Inches

Cubic Feet

U.S.Quart

U.S.Gallon

Imperial Gallon

U.S. Barrel (Petroleum)

Cubic Decimeters(Liters) 1 61.0234 0.035311 1.05668 0.264178 0.220083 0.00629Cubic Inches 0.01639 1 5.787 x 10-4 0.01732 0.004329 0.003606 0.000103Cubic Feet 28.317 1728 1 29.9221 7.48055 6.22888 0.1781U.S. Quart 0.94636 57.75 0.03342 1 0.25 0.2082 0.00595U.S. Gallon 3.78543 231 0.13368 4 1 0.833 0.02381Imperial Gallon 277.274 277.274 0.16054 4.80128 1.20032 1 0.02877U.S. Barrel(Petroleum) 5.6146 9702 5.6146 168 42 34.973 1

Note: Use Multiplier at Convergence of Row and Column

LitersPer Minute

CubicMeters

Per Hour

Cubic FeetPer Hour

Liters PerHour

U.S. GallonPer Minute

U.S. BarrelPer Day

LitersPer Minute 1 0.06 2.1189 60 0.264178 9.057

Cubic Meters Per Hour 16.667 1 35.314 1000 4.403 151

Cubic FeetPer Hour 0.4719 0.028317 1 28.317 0.1247 4.2746

LitersPer Hour 0.016667 0.001 0.035314 1 0.004403 0.151

U.S. GallonPer Minute 3.785 0.2273 8.0208 227.3 1 34.28

U.S. Barrel Per Day 0.1104 0.006624 0.23394 6.624 0.02917 1

TEMPERATURE CONVERSION FORMULAS

VOLUME RATE EQUIVALENTS

VOLUME EQUIVALENTS

Substitute in Formula

(C x 9/5) + 32

(C = 273.16)

(F - 32) x 5/9

(F + 459.69)

Ammonia 1636

Temp (F) Saturation Pressure

(Lbs/In2 Absolute)

Weight(Lbs/ Gallon)

Specific Gravity 60/60F

Conversion Factor, (1) lbs/hr

to GPMArgon 705.6 32 0.0885 8.345 1.0013 0.00199Butane 550.4 40 0.1217 8.345 1.0013 0.00199Carbon Dioxide 1071.6 50 0.1781 8.34 1.0007 0.00199Carbon Monoxide 507.5 60 0.2653 8.334 1 0.00199Chlorine 118.7 70 0.3631 8.325 0.9989 0.002Dowtherm A 465 80 0.5069 8.314 0.9967 0.002Ethane 708 90 0.6982 8.303 0.9963 0.002Ethylene 735 100 0.9492 8.289 0.9946 0.00201Fluorine 808.5 110 1.2748 8.267 0.9919 0.00201Helium 33.2 120 1.6924 8.253 0.9901 0.00201Hydrogen 188.2 130 2.2225 8.227 0.9872 0.00202Hydrogen Chloride 1198 140 2.8886 8.207 0.9848 0.00203Isobutane 529.2 150 3.718 8.182 0.9818 0.00203Isobutylene 580 160 4.741 8.156 0.9786 0.00204Methane 673.3 170 5.992 8.127 0.9752 0.00205Nitrogen 492.4 180 7.51 8.098 0.9717 0.00205Nitrous Oxide 1047.6 190 9.339 8.068 0.9681 0.00206Oxygen 736.5 200 11.526 8.039 0.9646 0.00207Phosgene 823.2 210 14.123 8.005 0.9605 0.00208Propane 617.4 212 14.696 7.996 0.9594 0.00208Propylene 670.3 220 17.186 7.972 0.9566 0.00209Refrigerant 11 635 240 24.969 7.901 0.948 0.0021Refrigerant 12 596.9 260 35.429 7.822 0.9386 0.00211Refrigerant 22 716 280 49.203 7.746 0.9294 0.00215Water 3206.2 300 67.013 7.662 0.9194 0.00217

350 134.63 7.432 0.8918 0.00224400 247.31 7.172 0.8606 0.00232450 422.6 6.892 0.827 0.00241500 680.8 6.553 0.7863 0.00254550 1045.2 6.132 0.7358 0.00271600 1542.9 5.664 0.6796 0.00294700 3093.7 3.623 0.4347 0.0046

Multiply # of

Kilogram ForceMeterkgf m

Foot Pound ft lb

Inch Poundin lb

Nm 0.102 0.7376 8.851kgf m 1 7.233 86.8ft lb 0.1383 1 12in lb 0.01152 0.08333 1

11/13/02

9.8071.3560.113

TORQUE

Critical Pressureof Various Fluids, Psia* Properties of Water

Newton MeterNm

1

1. Multiply flow in pounds per hour by the factor to get equivalent flow in galls per minute. Weight per gallon is based on 7.48 gallons per cubic foot.

by To obtain

Leakage

Leakage Class

Designation

Maximum Leakage Allowable Test Medium Test Procedures

Testing Procedures Required for Establishing Rating

I -- -- -- No test required provided user and supplier so agree.

II 0.5% of rated capacityAir or water at 50 -

125F(10 - 52C)

45 - 60 psig or max operating differential,

whichever is lower(3 - 4 bar)

Pressure applied to valve inlet, withoutlet open to atmosphere or connected to a low head loss measuring device, full normal

closing thrust provided by actuator.

III 0.1% of rated capacity As above As above As above

IV 0.01% of rated capacity As above As above As above

V

0.0005 ml per minute per inche of port diameter per psi

differential

Water at50 - 125F(10 - 52C)

Max service pressure drop across valve plug,

not to exceed ANSI body rating (100 psi pressure

drop min) or lesser pressure by agreement

Pressure applied to valve inlet, after filling entire body cavity and connected piping with water and stroking valve plug closed. Use

net specified max actuator thrust, but no more, even if available

during test. Allow time for leakage flow to stabilize.

VINot to exceed amounts shown in table 2 based

on port diameter

Air to nitrogen at 50 - 125F (10 - 52C)

50 psig or max rated differential pres-across valve plug, whichever is

lower (3.5 bar)

Actuator should be adjusted to operating conditions specified with full normal closing thrust applied to

valve plug seat. Allow time for leakage flow to stabilize and use

suitable measuring device.

11/13/02

STANDARD LEAKAGE RATES

In the Terminology section of this manual "tight shut off" was indicated as having various meanings, dependent upon the type of valve and the manufacturer. Such inconsistencies were recognized by many in the valve industry who worked together to develop a uniform method of catagorizing various leakage rates. The result of these efforts is the ANSI standard B16.104 which establishes six leakage classifications as follows:

Millimeters Inches ML Per Minute Bubbles Per Minute*25 1 0.15 138 1-1/2 0.3 251 2 0.45 364 2-1/2 0.6 476 3 0.9 6102 4 1.7 11152 6 4 27203 8 6.75 45

Preferably the test will consist of having a small amount of air entrapped below the valve disc (pressure generated hydraulically with water) and a pool of water on top of the disc. The absence of air bubbles rising through the pool of water indicates tight shutoff and zero effective leakage.

Occasionally, high test pressures or the orientation of the test valve will prohibit the use of entrapped air or the pool of water. In these instances, water may be the test media, and a lack of visually detectable water leakage indicates tight shutoff and zero effective leakage.

NOMINAL PORT DIAMETER

*Bubbles per minute as tabulated are a suggested alternative to a calibrated measuring device, in this case a 1/4 inch (6.3 mm) O.D. x 0.032 inch (0.8 mm) wall tube submerged in water to a depth of from 1/8 to 1/4 inch (3 to 6 mm). The tube end shall be cute square and smooth with no chamfers or burrs and the tube axis shall be perpendicular to the surface of the water. Other apparatus may be constructed and the number of bubbles per minute may differ from those shown as long as they correctly indicate the flow in ml per minute.

Missing from the ANSI standard is any reference of zero leak rate valves. This is partially because nearly all valves leak, even those proven to shutoff tight by specified shutoff tests. The point here is not to indicate or to imply that valves cannot provide required shutoff and tight sealing because the leakage in many cases is infinitesimally small. Given the most critical of tests, some leakage may be determinable, yet for all practical purposes and for most applications, effective zero leakage exists.

Tight shutoff, for the purposes of this manual is considered to exist when 110% of the rated shutoff pressure can be applied to one side of the valve disc with no leakage visually detectable past the seat or any of the valve components.

Feet* Miles Meters F CInches

Hg Abs.MM

Hg Abs. PSIAKg/sq

? kPa A-5000 -- -1526 77 25 35.58 903.7 17.48 1.229 120.5-4500 -- -1373 75 24 35 889 17.19 1.209 118.5-4000 -- -1220 73 23 34.42 974.3 16.9 1.181 116.5-3500 -- -1068 71 22 33.84 859.5 16.62 1.169 114.6-3000 -- -915 70 21 33.27 845.1 16.34 1.149 112.7

-2500 -- -763 68 20 32.7 830.6 16.06 1.129 110.7-2000 -- -610 66 19 32.14 816.6 15.78 1.109 108.8-1500 -- -458 64 18 31.58 802.1 15.51 1.091 106.9-1000 -- -305 63 17 31.02 787.9 15.23 1.071 105-500 -- -153 61 16 30.47 773.9 14.96 1.052 103.1

0 -- 0 59 15 29.92 760 14.696 1.0333 101.33500 -- 153 57 14 29.38 746.3 14.43 1.015 88.481000 -- 305 55 13 28.86 733 14.16 0.956 97.831500 -- 458 54 12 28.33 719.6 13.91 0.978 85.912000 -- 610 52 11 27.02 706.6 13.46 0.98 34.19

2500 -- 763 50 10 27.32 693.9 13.41 0.943 92.453000 -- 915 48 9 26.82 681.2 13.17 0.926 90.813500 -- 1068 47 8 26.33 668.2 12.93 0.909 89.154000 -- 1220 45 7 25.84 656.3 12.69 0.892 87.484500 -- 1373 43 6 25.37 644.4 13.45 0.876 85.91

5000 0.95 1526 41 5 24.9 632.5 12.23 0.86 84.336000 1.1 1831 38 3 23.99 609.3 11.78 0.828 81.227000 1.3 2136 34 1 23.1 586.7 11.34 0.797 78.198000 1.5 2441 31 -1 22.23 564.6 10.91 0.767 75.229000 1.7 2746 27 -3 21.39 543.3 10.5 0.738 72.4

10000 1.9 3050 23 -5 20.58 522.7 10.1 0.71 69.6415000 2.8 4577 6 -14 16.89 429 8.29 0.583 57.1620000 3.8 6102 -12 -24 13.76 369.5 6.76 0.475 45.6125000 4.7 7628 -30 -34 11.12 282.4 5.46 0.384 37.0530000 5.7 9153 -48 -44 8.903 226.1 4.37 0.307 30.13

35000 63.6 10679 -66 -57 7.06 179.3 3.47 0.244 23.8340000 7.6 12204 -70 -57 5.558 141.2 2.73 0.192 18.8245000 8.5 13730 -70 -57 4.375 111.1 2.15 0.151 14.8250000 9.5 15253 -70 -57 3.444 89.5 1.69 0.119 11.5555000 10.4 16781 -70 -57 2.712 68.9 1.33 0.0935 9.17

60000 11.4 18306 -70 -57 2.135 54.2 1.05 0.0738 7.2470000 13.3 21357 -67 -55 1.325 33.7 0.651 0.0458 4.4980000 15.2 24408 -62 -52 8.273-1 21 0.406 0.0285 2.890000 17.1 27459 -57 -59 5.200-1 13.2 0.255 0.0179 1.76100000 18.9 30510 -51 -46 3.290-1 8.36 0.162 0.0114 1.12

Altitude Above Sea Level Temperature ** Barometer* Atmospheric Pressure

Temperature Class A Class A

NPS 1-12NPS1-12

NPS 14-24

NPS1-12

NPS 1-12

NPS14-24

F-20 to 150 175 200 150 400 500 300

200 165 190 135 370 460 280225 155 180 130 355 440 270250 150 175 125 340 4156 260275 145 170 120 325 395 250300 140 165 110 310 375 240325 130 155 105 295 355 230353 125 150 100 280 335 220375 ---- 145 -- 265 315 210406 ---- 140 -- 250 290 200425 ---- 130 -- -- 270 --450 ---- 125 -- -- 250 --C

-29 to 66 12 14 10 28 34 2193 11 13 9 26 32 19107 11 12 9 24 30 19121 10 12 9 23 29 18135 10 12 8 22 27 17149 10 11 8 21 26 17163 9 11 7 20 24 16178 9 10 7 19 23 15191 ---- 10 ---- 18 22 14207 ---- 10 ---- 17 20 14218 ---- 9 ---- -- 19 --232 ---- 9 ---- -- 17 --

Class B Class B

Psig

Bar

Cast Iron (ASTM A126) -- Cast iron is an inexpensive, non-ductile material used for valve bodies controlling steam, water, gas and non-corrosive fluids.

Pressure-Temperature Ratings for ASTM a216 Cast Iron Valves (in accordance with ASME/ANSI B16.1 - 1989)

Class 125ASTM A 127

Class 250ASTM A 126

150 300 600 900 1500F

200 235 620 1240 1860 3095300 215 560 1120 1680 2795400 195 515 1025 1540 2570500 170 480 955 1435 2390600 140 450 900 1355 2255650 125 445 890 1330 2220700 110 430 870 1305 2170750 95 425 855 1280 2135800 80 420 845 1265 2110850 65 420 835 1255 2090900 50 415 830 1245 2075950 35 385 775 1160 19301000 20(1) 350 700 1050 17501050 20(1) 345 685 1030 17201100 20(1) 305 610 915 15251150 20(1) 235 475 710 11851200 20(1) 185 370 555 9251250 20(1) 145 295 440 7351300 20(1) 115 235 350 5851350 20(1) 95 190 290 4801400 20(1) 75 150 225 3801450 20(1) 60 115 175 2901500 20(1) 40 85 125 205C

-29 to 38 19 50 99 149 24893 16 43 85 128 213149 15 39 77 116 193204 13 36 71 106 177260 12 33 66 99 165316 10 31 62 93 155343 9 31 61 92 153371 8 29 60 90 150399 7 29 59 88 147427 6 29 58 87 145454 4 29 58 87 144482 3 27 57 86 143510 2 24 533 80 133538 1 24 48 72 121565 1(1) 21 47 71 119593 1(1) 16 42 63 105621 1(1) 13 33 49 82649 1(1) 10 26 38 64676 1(1) 8 1620 30 51704 1(1) 6 16 24 40732 1(1) 4 13 20 33760 1(1) 3 10 16 26788 1(1) 2 8 12 20815 1(1) 2 6 9 14

11/13/02

Bar

1. For welding end valves only. Flanged end ratings terminate at 1000F.

Pressure-Temperature Ratings for Standard ClassASTM A351 Grade CF8M and ASTM A479 Grade UNS S31700 Valves (in

accordance with ASME B16.34-1996) (continued)WORKING PRESSURES BY CLASSTemperature

Psig

Use Multiplier at Convergence of Row & Column

Kg Per Sq Cm

Lb Per Sq In Atm Bar

In of Hg

Kilo-pascals

In of Water

Ft of Water

Kg Per Sq Cm 1 14.22 0.9678 0.98067 28.96 98.067 394.05 32.84Lb Per Sq In 0.07031 1 0.06804 0.06895 2.036 6.895 27.7 2.309

Atm 1.0332 14.696 1 1.01325 29.92 101.325 407.14 33.93Bar 1.01972 14.5038 0.98692 1 29.53 100 402.156 33.513

In of Hg 0.03453 0.4912 0.03342 0.033864 1 3.3864 13.61 11.134

Kilopascals0.010197

2 0.145038 0.00987 0.01 0.2953 1 4.02156 0.33513

In of Water 0.002538 0.0361 0.00246 0.00249 0.007349 0.249 1 0.0833Ft of Water 0.03045 0.4332 0.02947 0.029839 0.8819 2.9839 12 1

0 1 2 3 4 5 6 7 8 9

0 0 0.068948 0.1379 0.206843 0.27579 0.344738 0.413685 0.482633 0.551581 0.62052810 .689476 0.758423 0.82737 0.896318 0.965266 1.034214 1.103161 1.172109 1.241056 1.310004

20 1.378951 1.447899 1.51685 1.585794 1.654742 1.723689 1.792637 1.861584 1.930532 1.99948

30 2.068427 2.137375 2.20632 2.27527 2.344217 2.413165 2.482113 2.55106 2.620008 2.688955

40 2.757903 2.82685 2.8958 2.964746 3.033693 3.102641 3.171588 3.240536 3.309484 3.37843150 3.447379 3.616326 3.58527 3.654221 3.723169 3.792117 3.861064 3.930012 3.998959 4.06790760 4.136854 4.205802 4.27748 4.343697 4.412645 4.481592 4.55054 4.619487 4.688435 4.75738370 4.826330 4.895278 4.96423 5.033173 5.10212 5.171068 5.240016 5.308963 5.377911 5.44685880 5.515806 5.584753 5.6537 5.722649 5.791596 5.860544 5.929491 5.998439 6.067386 6.13633490 6.205282 6.274229 6.34318 6.412124 6.481072 6.550019 6.618967 6.687915 6.756862 6.82581

100 6.894757 6.963705 7.03265 7.1016 7.170548 7.239495 7.308443 7.37739 7.446338 7.515285

HorsepowerKgKg per Kilowatts

DegreesGalsGramsHorsepower

Note: To convert to kilopascals, move decimal point two positions to right; to convert to Megapascals, move decimal point one position to left. For example, 30 psi, = 2.068427 bar = 206.8427 kPa = 0.2068427 Mpa.Note: Round off decimal points to provide no more than the desired degree of accuracy.

To Convert FromCu Ft (Methane)Cu Ft of Water

Pressure Equivalents

Pounds Per Square Inch Bar

Pressure Conversion--Pounds per Square Inch to Bar*

LbsLbs of AirLbs per Cu FtLbs per Hr (Gas)Lbs per Hr (Water)Lbs per Sec (Gas)RadiansScfh AirScfh AirScfh AirScfh

ToB.T.U.Lbs of WaterRadiansLbs of WaterOuncesFt Lbs per MinWattsLbsLbs per Cu FtHorsepowerKgCu Ft of AirKg per Cu MeterStd Cu Ft per HrGals per MinStd Cu Ft per HrDegreesScfh PropaneScfh ButaneScfh 0.6 Natural GasCu Meters per Hr

Multiply By1000 (approx.)622.40.017458.3360.035233000

16.018413.1/Specific Gravity

7462.2050.062431.341

0.711.290.028317

Other Useful Conversions

0.00246160/Specific 57.30.81

0.453613.1

Critical Temp (F)

Critical Pressure

(psia)

Liquid,(3), (4)

60F/60FGas at 60F

(Air=1)(1)

1 Methane CH4 16.043 -258.69 (5000)(2) -296.46(5) -116.63 667.8 0.3(8) 0.5539

2 Ethane C2H6 30.07 -127.48 (800)(2) -297.89(5) 90.09 707.8 0.3564(7) 1.0382

3 Propane C3H8 44.097 -43.67 190 -305.84(5) 206.01 616.3 0.5077(7) 1.5225

4 n-Butane C4H10 58.124 31.10 51.6 -217.05 305.65 550.7 0.5844(7) 2.0068

5 Isobutane C4H10 58.124 10.90 72.2 -255.29 274.98 529.1 0.5631(7) 2.0068

6 n-Pentane C5H12 72.151 96.92 15.57 -201.51 385.7 488.6 0.631 2.49117 Isopentane C5H12 72.151 82.12 20.44 -255.83 369.1 490.4 0.6247 2.49118 Neopentane C5H12 72.151 49.10 35.9 2.17 321.13 464 0.5967

(7) 2.49119 n-Hexane C6H14 86.178 155.72 4.956 -139.58 453.7 436.9 0.664 2.975310 2-Methylpentane C6H14 86.178 140.47 6.767 -244.63 435.83 436.6 0.6579 2.975311 3-Methylpentane C6H14 86.178 145.89 6.098 --- 448.3 453.1 0.6689 2.975312 Neohexane C6H14 86.178 121.52 9.856 -147.72 420.13 446.8 0.654 2.975313 2,3-Dimethylbutane C6H14 86.178 136.36 7.404 -199.38 440.29 453.5 0.6664 2.975314 n-Heptane C7H16 100.205 209.17 1.62 -131.05 512.8 396.8 0.6882 3.459615 2-Methylhexane C7H16 100.205 194.09 2.271 -180.89 495 396.5 0.683 3.459616 3-Methylhexane C7H16 100.205 197.32 2.13 --- 503.78 408.1 0.6917 3.459617 3-Ethylpentane C7H16 100.205 200.25 2.012 -181.48 513.48 419.3 0.7028 3.459618 2,2-Dimethylpentane C7H16 100.205 174.54 3.492 -190.86 477.23 402.2 0.6782 3.459619 2,4-Dimethylpentane C7H16 100.205 176.89 3.292 -182.63 475.95 396.9 0.6773 3.459620 3,3-Dimethylpentane C7H16 100.205 186.91 2.773 -210.01 505.85 427.2 0.6976 3.459621 Triptane C7H16 100.205 177.58 3.374 -12.82 496.44 428.4 0.6946 3.459622 n-Octane C8H18 114.232 258.22 0.537 -70.18 564.22 360.6 0.7068 3.943923 Disobutyl C8H18 114.232 228.39 1.101 -132.07 530.44 360.6 0.6979 3.943924 Isooctane C8H18 114.232 210.63 1.708 -161.27 519.46 372.4 0.6962 3.943925 n-Nonane C9H20 128.259 303.47 0.179 -64.28 610.68 332 0.7217 4.428226 n-Decane C10H22 142.286 345.48 0.0597 -21.36 652.1 304 0.7342 4.912527 Cyclopentane C5H10 70.135 120.65 9.914 -136.91 461.5 653.8 0.7504 2.421528 Methylcyclopentane C6H12 84.162 161.25 4.503 -224.44 499.35 548.9 0.7536 2.905729 Cyclohexane C6H12 84.162 177.29 3.264 43.77 536.7 591 0.7834 2.905730 Methylcyclohexane C7H14 98.189 213.68 1.609 -195.87 570.27 503.5 0.774 3.3931 Ethylene C2H4 28.054 -154.62 --- -272.45

(5) 48.58 729.8 --- 0.968632 Propene C3H6 42.081 -53.90 226.4 -301.45

(5) 196.9 669 0.5220(7) 1.452933 1-Butene C4H8 56.108 20.75 63.05 -301.63

(5) 295.6 583 0.6013(7) 1.937234 Cis-2-Butene C4H8 56.108 38.69 45.54 -218.06 324.37 610 0.6271

(7) 1.937235 Trans-2-Butune C4H8 56.108 33.58 49.8 -157.96 311.86 595 0.6100

(7) 1.937236 Isobutene C4H8 56.108 19.59 63.4 -220.61 292.55 580 0.6004

(7) 1.937237 1-Pentane C5H10 70.135 85.93 19.115 -265.39 376.93 590 0.6457 2.421538 1,2-Butadiene C4H6 54.092 51.53 (20)

(2) -213.16 (339)(2) (653)(2) 0.6587 1.867639 1,3-Butadiene C4H6 54.092 24.06 (60)

(2) -164.02 306 628 0.6272(7) 1.867640 Isoprene C5H8 68.119 93.30 16.672 -230.74 (412)

(2) (558.4)(2) 0.6861 2.315941 Acetylene C2H2 26.038 -119

(6) --- -114(5) 95.31 890.4 0.615(9) 0.89942 Benzene C6H6 78.114 176.17 3.224 41.96 552.22 710.4 0.8844 2.696943 Toluene C7H8 92.141 231.13 1.032 -138.94 605.55 595.9 0.8718 3.181244 Ethylbenzene C8H10 106.168 277.16 0.371 -138.91 651.24 523.5 0.8718 3.665545 o-Xylene C8H10 106.168 291.97 0.264 -13.3 675 541.4 0.8848 3.665546 m-Xylene C8H10 106.168 282.41 0.326 -54.12 651.02 513.6 0.8687 3.665547 p-Xylene C8H10 106.168 281.05 0.342 55.86 649.6 509.2 0.8657 3.665548 Styrene C8H8 293.29 293.29 (0.24)

(2) -23.1 706 580 0.911 3.595949 Isopropylbenzene C9H12 306.34 306.34 0.188 -140.82 676.4 465.4 0.8663 4.1498

1 Calculated values.23456789

1.33

GasSpecific Heat Ratio (k)

1.40

1.40

1.21

1.15

Specific Heat Ratio (k)1.38

1.40

1.67

1.40

1.26

1.32

Specific GravityPhysical Constants of Hydrocarbons

Critical Constants

No.

( ) - Estimated values.Air saturated hydrocarbons.

Boiling Point at 14.696

PSIA (F)

Vapor Pressure at 100F (PSIA)

Freezing Point at

14.696 PSIA (F)

Compound Formula Molecular Weight

Apparent value for methane at 60F.Specific Gravity, 119F/60F (sublimation point).

Absolute values from weights in vacuum.At saturation pressure (triple point).Sublimation point.Saturation pressure and 60F.

GasAcetylene

Air

Argon

Butane

Carbon Monoxide

Carbon Dioxide

Ethane

1.17

1.40

1.29

1.25

1.66

Oxygen

Propane

Propylene

Steam (1)

Specific Heat Ratio (k)

1. Use property tables if available for greater accuracy.

Hydrogen

Methane

0.6 Natural Gas

Helium

Nitrogen

Lbs/Sq In P'

Inches of Hg

0.20 0.41 29.51 53.14 21.21 1063.8 1085.0 1526.00.25 0.51 29.41 59.30 27.36 1060.3 1087.7 1235.30.30 0.61 29.31 64.47 32.52 1057.4 1090.0 1039.50.35 0.71 29.21 68.93 36.97 1054.9 1091.9 898.50.40 0.81 29.11 72.86 40.89 1052.7 1093.6 791.90.45 0.92 29.00 76.38 44.41 1050.7 1095.1 708.5

0.50 1.02 28.90 79.58 47.60 1048.8 1096.4 641.40.60 1.22 28.70 85.21 53.21 1045.7 1098.9 540.00.70 1.43 28.49 90.08 58.07 1042.9 1101.0 466.90.80 1.63 28.29 94.38 62.36 1040.4 1102.8 411.70.90 1.83 28.09 98.24 66.21 1038.3 1104.5 368.4

1.00 2.04 27.88 101.74 69.70 1036.3 1106.0 333.61.20 2.44 27.48 107.92 75.87 1032.7 1108.6 280.91.40 2.85 27.07 113.26 81.20 1029.6 1110.8 243.01.60 3.26 26.66 117.99 85.91 1026.9 1112.8 214.31.80 3.66 26.26 122.23 90.14 1024.5 1114.6 191.8

2.00 4.07 25.85 126.08 93.99 1022.2 1116.2 173.732.20 4.48 25.44 129.62 97.52 1020.2 1117.7 158.852.40 4.89 25.03 132.89 100.79 1018.3 1119.1 146.382.60 5.29 24.63 135.94 103.83 1016.5 1120.3 135.782.80 5.70 24.22 138.79 106.68 1014.8 1121.5 126.65

3.00 6.11 23.81 141.48 109.37 1013.2 1122.6 118.713.50 7.13 22.79 147.58 115.46 1009.6 1125.1 102.724.00 8.14 21.78 152.97 120.86 1006.4 1127.3 90.634.50 9.16 20.76 157.83 125.71 1003.6 1129.3 81.165.00 10.18 19.74 162.24 130.13 1001.0 1131.1 73.52

5.50 11.20 1.72 166.30 134.19 998.5 1132.7 67.246.00 12.22 17.70 170.06 137.96 996.2 1134.2 61.986.50 13.23 16.69 173.56 141.47 994.1 1135.6 57.507.00 14.25 15.67 176.85 144.76 992.1 1136.9 53.647.50 15.27 14.65 179.94 147.86 990.2 1138.1 50.29

8.00 16.29 13.63 182.86 150.79 988.5 1139.3 47.348.50 17.31 12.61 185.64 153.57 986.8 1140.4 44.739.00 18.32 11.60 188.28 156.22 985.2 1141.4 42.409.50 19.34 10.58 190.80 158.75 983.6 1142.3 40.3110.00 20.36 9.56 193.21 161.17 982.1 1143.3 38.42

11.00 22.40 7.52 197.75 165.73 979.3 1145.0 5.1412.00 24.43 5.49 201.96 169.96 976.6 1146.6 32.4013.00 26.47 3.45 205.88 173.91 974.2 1148.1 30.0614.00 28.50 1.42 209.56 177.61 971.9 1149.5 28.04

Latent Heat of Evaporation

(BTU/LB)

Total Heat of Steam

Hg(BTU/LB)

Specific Volume

V(Cu Ft/Lb)

PROPERTIES OF SATURATED STEAMAbsolutePressure Vacuum

(Inches of Hg)

Temperaturet

(F)

Heat of the Liquid

(BTU/LB)

AbsoluteP'

GaugeP

14.696 0.0 212.00 180.07 970.3 1150.4 26.80015.0 0.0 213.03 181.11 969.7 1150.8 26.29016.0 1.3 213.32 184.42 967.6 1152.0 24.75017.0 2.3 219.44 187.56 965.5 1153.1 23.39018.0 3.3 222.41 190.56 963.6 1154.2 22.17019.0 4.3 225.24 193.42 961.9 1155.3 21.08020.0 5.3 227.96 196.16 960.1 1156.3 20.08921.0 6.3 230.57 198.79 958.4 1157.2 19.19222.0 7.3

Tyco Control Valve Manual

Documents

control loop

automated valve

cascade control system

common final control

process industry

process information

process variables

desired set point