SIST EN 60534-2-1:2011

SLOVENSKI STANDARD
01-julij-2011
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SIST EN 60534-2-1:2001
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Industrial-process control valves - Part 2-1: Flow capacity - Sizing equations for fluid flow
under installed conditions (IEC 60534-2-1:2011)
Stellventile für die Prozessregelung - Teil 2-1: Durchflusskapazität -
Bemessungsgleichungen für Fluide unter Betriebsbedingungen (IEC 60534-2-1:2011)
Vannes de régulation des processus industriels - Partie 2-1: Capacité d'écoulement -
Equations de dimensionnement pour l'écoulement des fluides dans les conditions
d'installation (CEI 60534-2-1:2011)
Ta slovenski standard je istoveten z: EN 60534-2-1:2011
ICS:
23.060.40 7ODþQLUHJXODWRUML Pressure regulators
25.040.40 Merjenje in krmiljenje Industrial process
industrijskih postopkov measurement and control
2003-01.Slovenski inštitut za standardizacijo. Razmnoževanje celote ali delov tega standarda ni dovoljeno.

EUROPEAN STANDARD
EN 60534-2-1
NORME EUROPÉENNE
May 2011
EUROPÄISCHE NORM
ICS 23.060.40; 25.040.40 Supersedes EN 60534-2-1:1998

English version
Industrial-process control valves -
Part 2-1: Flow capacity -
Sizing equations for fluid flow under installed conditions
(IEC 60534-2-1:2011)
Vannes de régulation des processus Stellventile für die Prozessregelung -
industriels - Teil 2-1: Durchflusskapazität -
Partie 2-1: Capacité d'écoulement - Bemessungsgleichungen für Fluide unter
Equations de dimensionnement pour Betriebsbedingungen
l'écoulement des fluides dans les (IEC 60534-2-1:2011)
conditions d'installation
(CEI 60534-2-1:2011)
This European Standard was approved by CENELEC on 2011-05-04. CENELEC members are bound to comply
with the CEN/CENELEC Internal Regulations which stipulate the conditions for giving this European Standard
the status of a national standard without any alteration.

Up-to-date lists and bibliographical references concerning such national standards may be obtained on
application to the Central Secretariat or to any CENELEC member.

This European Standard exists in three official versions (English, French, German). A version in any other
language made by translation under the responsibility of a CENELEC member into its own language and notified
to the Central Secretariat has the same status as the official versions.

CENELEC members are the national electrotechnical committees of Austria, Belgium, Bulgaria, Croatia, Cyprus,
the Czech Republic, Denmark, Estonia, Finland, France, Germany, Greece, Hungary, Iceland, Ireland, Italy,
Latvia, Lithuania, Luxembourg, Malta, the Netherlands, Norway, Poland, Portugal, Romania, Slovakia, Slovenia,
Spain, Sweden, Switzerland and the United Kingdom.

CENELEC
European Committee for Electrotechnical Standardization
Comité Européen de Normalisation Electrotechnique
Europäisches Komitee für Elektrotechnische Normung

Management Centre: Avenue Marnix 17, B - 1000 Brussels

© 2011 CENELEC - All rights of exploitation in any form and by any means reserved worldwide for CENELEC members.
Ref. No. EN 60534-2-1:2011 E
Foreword
The text of document 65B/783/FDIS, future edition 2 of IEC 60534-2-1, prepared by SC 65B, Devices &
process analysis, of IEC TC 65, Industrial-process measurement, control and automation, was submitted
to the IEC-CENELEC parallel vote and was approved by CENELEC as EN 60534-2-1 on 2011-05-04.
This European Standard supersedes EN 60534-2-1:1998.
EN 60534-2-1:1998:
— the same fundamental flow model, but changes the equation framework to simplify the use of the
standard by introducing the notion of ∆p ;
sizing
— changes to the non-turbulent flow corrections and means of computing results;
— multi-stage sizing as an Annex.
Attention is drawn to the possibility that some of the elements of this document may be the subject of
patent rights. CEN and CENELEC shall not be held responsible for identifying any or all such patent
rights.
The following dates were fixed:
– latest date by which the EN has to be implemented
at national level by publication of an identical
national standard or by endorsement (dop) 2012-02-04
– latest date by which the national standards conflicting
with the EN have to be withdrawn (dow) 2014-05-04
Annex ZA has been added by CENELEC.
__________
Endorsement notice
The text of the International Standard IEC 60534-2-1:2011 was approved by CENELEC as a European
Standard without any modification.
__________
- 3 - EN 60534-2-1:2011
Annex ZA
(normative)
Normative references to international publications
with their corresponding European publications

The following referenced documents are indispensable for the application of this document. For dated
references, only the edition cited applies. For undated references, the latest edition of the referenced
document (including any amendments) applies.

NOTE  When an international publication has been modified by common modifications, indicated by (mod), the relevant EN/HD
applies.
Publication Year Title EN/HD Year

IEC 60534-1 2005 Industrial-process control valves - EN 60534-1 2005
Part 1: Control valve terminology and general
considerations
IEC 60534-2-3 1997 Industrial-process control valves - EN 60534-2-3 1998
Part 2-3: Flow capacity - Test procedures

IEC 60534-2-1 ®
Edition 2.0 2011-03
INTERNATIONAL
STANDARD
NORME
INTERNATIONALE
Industrial-process control valves –
Part 2-1: Flow capacity – Sizing equations for fluid flow under installed
conditions
Vannes de régulation des processus industriels –
Partie 2-1: Capacité d'écoulement – Equations de dimensionnement pour
l'écoulement des fluides dans les conditions d'installation

INTERNATIONAL
ELECTROTECHNICAL
COMMISSION
COMMISSION
ELECTROTECHNIQUE
PRICE CODE
INTERNATIONALE
CODE PRIX XA
ICS 23.060.40; 25.040.40 ISBN 978-2-88912-399-5

– 2 – 60534-2-1  IEC:2011
CONTENTS
FOREWORD . 4
1 Scope . 6
2 Normative references . 6
3 Terms and definitions . 7
4 Symbols . 8
5 Installation . 9
6 Sizing equations for incompressible fluids . 10
6.1 Turbulent flow . 10
6.2 Pressure differentials . 11
6.2.1 Sizing pressure differential, ∆p . 11
sizing
6.2.2 Choked pressure differential, ∆p . 11
choked
6.2.3 Liquid critical pressure ratio factor, F . 11
F
6.3 Non-turbulent (laminar and transitional) flow . 11
7 Sizing equations for compressible fluids . 11
7.1 General . 11
7.2 Pressure differentials . 12
7.2.1 Sizing pressure drop ratio, x . 12
sizing
7.2.2 Choked pressure drop ratio, x . 12
choked
7.3 Specific heat ratio factor, F . 12
γ
7.4 Expansion factor, Y . 13
7.5 Compressibility factor, Z . 13
7.6 Non-turbulent (laminar and transitional) flow . 14
8 Correction factors common to both incompressible and compressible flow . 14
8.1 Piping geometry correction factors . 14
8.2 Estimated piping geometry factor, F . 14
P
8.3 Estimated combined liquid pressure recovery factor and piping geometry
factor with attached fittings, F . 15
LP
8.4 Estimated pressure differential ratio factor with attached fittings, x . 16
TP
9 Reynolds Number, Re . 16
V
Annex A (normative) Sizing equations for non-turbulent flow . 18
Annex B (normative) Sizing equations for fluid flow through multistage control valves. 21
Annex C (informative) Piping factor computational considerations . 28
Annex D (informative) Engineering Data . 34
Annex E (informative) Reference calculations . 41
Bibliography . 54

Figure 1 – Reference pipe section for sizing . 10
Figure B.1 – Multistage multipath trim . 23
Figure B.2 – Multistage single path trim . 24
Figure B.3 – Disk from a continuous resistance trim The complete trim consists of a
number of these disks stacked together. . 25
Figure B.4 – Sectional view of continuous resistance trim with multiple flow passages
having vertical undulations . 25
Figure C.1 – Determination of the upper limit of the flow coefficient by the iterative
method . 32

60534-2-1  IEC:2011 – 3 –
Figure C.2 – Determination of the final flow coefficient by the iterative method . 33
Figure D.1 – Piping geometry factors . 37
Figure D.2 – Pressure recovery factors . 39
Figure D.3 – Liquid critical pressure ratio factor F . 40
F
Table 1 – Numerical constants N . 17
Table B.1 – Values of the stage interaction factors, k, and the reheat factors, r for
multistage single and multipath control valve trim . 27
Table B.2 – Values of the stage interaction factors, k, and the reheat factors, r for
continuous resistance control valve trim . 27
Table C.1 – Incompressible flow . 31
Table C.2 – Compressible flow . 31
Table D.1 – Typical values of valve style modifier F , liquid pressure recovery factor F
d L
a)
and pressure differential ratio factor x at full rated travel . 35

T
– 4 – 60534-2-1  IEC:2011
INTERNATIONAL ELECTROTECHNICAL COMMISSION
____________
INDUSTRIAL-PROCESS CONTROL VALVES –

Part 2-1: Flow capacity –
Sizing equations for fluid flow under installed conditions

FOREWORD
1) The International Electrotechnical Commission (IEC) is a worldwide organization for standardization comprising
all national electrotechnical committees (IEC National Committees). The object of IEC is to promote
international co-operation on all questions concerning standardization in the electrical and electronic fields. To
this end and in addition to other activities, IEC publishes International Standards, Technical Specifications,
Technical Reports, Publicly Available Specifications (PAS) and Guides (hereafter referred to as “IEC
Publication(s)”). Their preparation is entrusted to technical committees; any IEC National Committee interested
in the subject dealt with may participate in this preparatory work. International, governmental and non-
governmental organizations liaising with the IEC also participate in this preparation. IEC collaborates closely
with the International Organization for Standardization (ISO) in accordance with conditions determined by
agreement between the two organizations.
2) The formal decisions or agreements of IEC on technical matters express, as nearly as possible, an international
consensus of opinion on the relevant subjects since each technical committee has representation from all
interested IEC National Committees.
3) IEC Publications have the form of recommendations for international use and are accepted by IEC National
Committees in that sense. While all reasonable efforts are made to ensure that the technical content of IEC
Publications is accurate, IEC cannot be held responsible for the way in which they are used or for any
misinterpretation by any end user.
4) In order to promote international uniformity, IEC National Committees undertake to apply IEC Publications
transparently to the maximum extent possible in their national and regional publications. Any divergence
between any IEC Publication and the corresponding national or regional publication shall be clearly indicated in
the latter.
5) IEC itself does not provide any attestation of conformity. Independent certification bodies provide conformity
assessment services and, in some areas, access to IEC marks of conformity. IEC is not responsible for any
services carried out by independent certification bodies.
6) All users should ensure that they have the latest edition of this publication.
7) No liability shall attach to IEC or its directors, employees, servants or agents including individual experts and
members of its technical committees and IEC National Committees for any personal injury, property damage or
other damage of any nature whatsoever, whether direct or indirect, or for costs (including legal fees) and
expenses arising out of the publication, use of, or reliance upon, this IEC Publication or any other IEC
Publications.
8) Attention is drawn to the Normative references cited in this publication. Use of the referenced publications is
indispensable for the correct application of this publication.
9) Attention is drawn to the possibility that some of the elements of this IEC Publication may be the subject of
patent rights. IEC shall not be held responsible for identifying any or all such patent rights.
International Standard IEC 60534-2-1 has been prepared by subcommittee 65B: Measurement
and control devices, of IEC technical committee 65: Industrial-process measurement, control
and automation.
This second edition cancels and replaces the first edition published in 1998. This edition
constitutes a technical revision.
This edition includes the following significant technical changes with respect to the previous
edition:
• the same fundamental flow model, but changes the equation framework to simplify the
use of the standard by introducing the notion of ∆p ;
sizing
• changes to the non-turbulent flow corrections and means of computing results;
• multi-stage sizing as an Annex.
The text of this standard is based on the following documents:

60534-2-1  IEC:2011 – 5 –
FDIS Report on voting
65B/783/FDIS 65B/786/RVD
Full information on the voting for the approval of this standard can be found in the report on
voting indicated in the above table.
This publication has been drafted in accordance with the ISO/IEC Directives, Part 2.
A list of all the parts of the IEC 60534 series, under the general title Industrial-process control
valves, can be found on the IEC website.
The committee has decided that the contents of this publication will remain unchanged until
the stability date indicated on the IEC web site under "http://webstore.iec.ch" in the data
related to the specific publication. At this date, the publication will be
• reconfirmed,
• withdrawn,
• replaced by a revised edition, or
• amended.
– 6 – 60534-2-1  IEC:2011
INDUSTRIAL-PROCESS CONTROL VALVES –

Part 2-1: Flow capacity –
Sizing equations for fluid flow under installed conditions

1 Scope
This part of IEC 60534 includes equations for predicting the flow of compressible and
incompressible fluids through control valves.
The equations for incompressible flow are based on standard hydrodynamic equations for
Newtonian incompressible fluids. They are not intended for use when non-Newtonian fluids,
fluid mixtures, slurries or liquid-solid conveyance systems are encountered. The equations for
incompressible flow may be used with caution for non-vaporizing multi-component liquid
mixtures. Refer to Clause 6 for additional information.
At very low ratios of pressure differential to absolute inlet pressure (∆p/p ), compressible
fluids behave similarly to incompressible fluids. Under such conditions, the sizing equations
for compressible flow can be traced to the standard hydrodynamic equations for Newtonian
incompressible fluids. However, increasing values of ∆p/p result in compressibility effects
which require that the basic equations be modified by appropriate correction factors. The
equations for compressible fluids are for use with ideal gas or vapor and are not intended for
use with multiphase streams such as gas-liquid, vapor-liquid or gas-solid mixtures.
Reasonable accuracy can only be maintained when the specific heat ratio, γ, is restricted to
the range 1,08 < γ < 1,65. Refer to Clause 7.2 for more information.
For compressible fluid applications, this standard is valid for valves with x ≤ 0,84 (see Table
T
D.2). For valves with x > 0,84 (e.g. some multistage valves), greater inaccuracy of flow
T
prediction can be expected.
Reasonable accuracy can only be maintained for control valves if:
C
< 0,047
N d
Note that while the equation structure utilized in this document departs radically from previous
versions of the standard, the basic technology is relatively unchanged. The revised equation
format was adopted to simplify presentation of the various equations and improve readability
of the document.
2 Normative references
The following referenced documents are indispensable for the application of this document.
For dated references, only the edition cited applies. For undated references, the latest edition
of the referenced document (including any amendments) applies.
IEC 60534-1:2005, Industrial-process control valves – Part 1: Control valve terminology and
general considerations
IEC 60534-2-3:1997, Industrial-process control valves – Part 2-3: Flow capacity – Test
procedures
60534-2-1  IEC:2011 – 7 –
3 Terms and definitions
For the purposes of this document, the terms and definitions given in IEC 60534-1, and the
following apply.
3.1
valve style modifier
the ratio of the hydraulic diameter of a single flow passage to the diameter of a circular
orifice, the area of which is equivalent to the sum of areas of all identical flow passages at a
given travel. It should be stated by the manufacturer as a function of travel (see Annex A).
3.2
standard volumetric flowrates
compressible fluid volumetric flow rates in cubic metres per hour, identified by the symbol Q ,
S
refer to either
a) Standard conditions, which is an absolute pressure of 1 013,25 mbar and a
temperature of 288,6 K, or
b) Normal conditions, which is an absolute pressure of 1 013,25 mbar and a temperature
of 273 K.
Numerical constants for the flow equations are provided for both conventions (see Table 1).

– 8 – 60534-2-1  IEC:2011
4 Symbols
Symbo Description Unit
l
C Flow coefficient (K , C ) Various (see IEC 60534-1)
v v
(see Note 4)
d Nominal valve size mm
D Internal diameter of the piping mm
D Internal diameter of upstream piping mm
D Internal diameter of downstream piping mm
D Orifice diameter mm
o
F Valve style modifier (see Annex A) Dimensionless
d
(see Note 4)
F Liquid critical pressure ratio factor Dimensionless
F
F Liquid pressure recovery factor of a control valve without attached fittings Dimensionless
L
(see Note 4)
F Combined liquid pressure recovery factor and piping geometry factor of a Dimensionless
LP
control valve with attached fittings
F Piping geometry factor Dimensionless
P
F Reynolds number factor Dimensionless
R
F Specific heat ratio factor Dimensionless
γ
M Molecular mass of flowing fluid kg/kmol
N Numerical constants (see Table 1) Various (see Note 1)
p Inlet absolute static pressure measured at point A (see Figure 1) kPa or bar (see Note 2)
p Outlet absolute static pressure measured at point B (see Figure 1) kPa or bar
p Absolute thermodynamic critical pressure kPa or bar
c
p Reduced pressure (p /p ) Dimensionless
r 1 c
p Absolute vapour pressure of the liquid at inlet temperature kPa or bar
v
∆p Differential pressure between upstream and downstream pressure taps kPa or bar
actual
(P – P )
1 2
Computed value of limiting pressure differential for incompressible flow kPa or bar
∆p
choked
∆p Value of pressure differential used in computing flow or required flow kPa or bar
sizing
coefficient for incompressible flows
Q Actual volumetric flow rate m /h

Q Standard volumetric flow rate (see definition 3.2) m /h
S
Re Valve Reynolds number Dimensionless
v
T Inlet absolute temperature K
T Absolute thermodynamic critical temperature K
c
T Reduced temperature (T /T ) Dimensionless
r 1 c
t Absolute reference temperature for standard cubic metre K
s
W Mass flow rate kg/h
x Dimensionless
Ratio of actual pressure differential to inlet absolute pressure (∆P/P )
x Choked pressure drop ratio for compressible flow Dimensionless
choked
x Value of pressure drop ratio used in computing flow or required flow Dimensionless
sizing
coefficient for compressible flows

60534-2-1  IEC:2011 – 9 –
Symbo Description Unit
l
x Pressure differential ratio factor of a control valve without attached fittings Dimensionless
T
at choked flow (see Note 4)
x Pressure differential ratio factor of a control valve with attached fittings at Dimensionless
TP
choked flow
Y Expansion factor Dimensionless
Z Compressibility factor at inlet conditions Dimensionless
ν Kinematic viscosity m /s (see Note 3)
Density of fluid at p and T kg/m
ρ
1 1
Dimensionless
ρ /ρ Relative density (ρ /ρ = 1,0 for water at 15 °C)
1 o 1 o
Specific heat ratio Dimensionless
γ
ζ Velocity head loss coefficient of a reducer, expander or other fitting Dimensionless
attached to a control valve or valve trim
Upstream velocity head loss coefficient of fitting Dimensionless
ζ
ζ Downstream velocity head loss coefficient of fitting Dimensionless
ζ Inlet Bernoulli coefficient Dimensionless
B1
Outlet Bernoulli coefficient Dimensionless
ζ
B2
NOTE 1 To determine the units for the numerical constants, dimensional analysis may be performed on the
appropriate equations using the units given in Table 1.
2 5
NOTE 2 1 bar = 10 kPa = 10 Pa
–6 2
NOTE 3 1 centistoke = 10 m /s
NOTE 4 These values are travel-related and should be stated by the manufacturer.

5 Installation
In many industrial applications, reducers or other fittings are attached to the control valves.
The effect of these types of fittings on the nominal flow coefficient of the control valve can be
significant. A correction factor is introduced to account for this effect. Additional factors are
introduced to take account of the fluid property characteristics that influence the flow capacity
of a control valve.
In sizing control valves, using the relationships presented herein, the flow coefficients calculated
are assumed to include all head losses between points A and B, as shown in Figure 1.

– 10 – 60534-2-1  IEC:2011
Flow
l l
1 2
Pressure tap Pressure tap
A B
Control valve with or without attached fittings
IEC  509/11
l = two nominal pipe diameters
l = six nominal pipe diameters
Figure 1 – Reference pipe section for sizing
6 Sizing equations for incompressible fluids
6.1 Turbulent flow
The fundamental flow model for incompressible fluids in the turbulent flow regime is given as:
∆p
sizing
Q = CN F (1)
1 P
ρ
ρ
o
NOTE 1 The numerical constant N depends on the units used in the general sizing equation and the type of flow
coefficient: K or C .
v v
NOTE 2 The piping geometry factor, F , reduces to unity when the valve size and adjoining pipe sizes are
P
identical. Refer to 8.1 for evaluation and additional information.
This model establishes the relationship between flow rate, flow coefficient, fluid properties,
related installation factors, and pertinent service conditions for control valves handling
incompressible fluids. Equation (1) may be used to compute the required flow coefficient, the
flow rate or applied pressure differential given any two of the three quantities.
This model rigorously applies only to single component, single phase fluids (i.e., no multi-
phase mixtures, no multi-component mixtures). However, this model may be used with caution
under certain conditions for multi-component mixtures in the liquid phase. The underlying
assumptions of the flow model would be satisfied for liquid-liquid fluid mixtures subject to the
following restrictions:
• the mixture is homogenous;
• the mixture is in chemical and thermodynamic equilibrium;
• the entire throttling process occurs well away from the multiphase region.
When these conditions are satisfied, the mixture density should be substituted for the fluid
density ρ in Equation (1).
60534-2-1  IEC:2011 – 11 –
6.2 Pressure differentials
6.2.1 Sizing pressure differential, ∆p
sizing
The value of the pressure differential used in Equation (1) to predict flow rate or compute a
required flow coefficient is the lesser of the actual pressure differential or the choked pressure
differential:
∆p if ∆p < ∆p

choked
∆p = (2)
sizing 
∆p if ∆p ≥ ∆p
 choked choked
6.2.2 Choked pressure differential, ∆p
choked
The condition where further increase in pressure differential at constant upstream pressure no
longer produces a corresponding increase in flow through the control valve is designated
“choked flow”. The pressure drop at which this occurs is known as the choked pressure
differential and is given by the following equation:
 
F
LP
 
∆p = (p − F p ) (3)
choked 1 F v
 
F
 P 
F
LP 2
NOTE The expression ( ) reduces to F when the valve size and adjoining pipe sizes are identical. Refer to
L
F
P
8.1 for more information.
6.2.3 Liquid critical pressure ratio factor, F
F
F is the liquid critical pressure ratio factor. This factor is the ratio of the apparent vena
F
contracta pressure at choked flow conditions to the vapour pressure of the liquid at inlet
temperature. At vapor pressures near zero, this factor is 0,96.
Values of F may be supplied by the user if known. For single component fluids it may be
F
determined from the curve in Figure D.3 or approximated from the following equation:
p
v
F = 0,96 − 0,28 (4)
F
p
c
Use of Equation (4) to describe the onset of choking of multi-component mixtures is subject to
the applicability of appropriate corresponding states parameters in the flashing model.
6.3 Non-turbulent (laminar and transitional) flow
The flow model embodied in Equation (1) is for fully developed, turbulent flow only. Non-
turbulent conditions may be encountered, especially when flow rates are quite low or fluid
viscosity is appreciable. To affirm the applicability of Equation (1), the value of the valve
Reynolds Number (see Equation (23)) should be computed. Equation (1) is applicable if
Re ≥ 10 000.
V
7 Sizing equations for compressible fluids
7.1 General
The fundamental flow model for compressible fluids in the turbulent flow regime is given as:
W = CN F Y x p ρ (5)
6 P sizing 1 1
– 12 – 60534-2-1  IEC:2011
This model establishes the relationship between flow rates, flow coefficients, fluid properties,
related installation factors and pertinent service conditions for control valves handling
compressible fluids.
Two equivalent forms of Equation (5) are presented to accommodate conventional available
data formats:
x M
sizing
W = CN F p Y (6)
8 P 1
T Z
1 1
x
sizing
Q = CN F p Y (7)
s 9 P 1
MT Z
1 1
NOTE See Annex D for values of M.
Equation (6) is derived by substituting the fluid density as computed from the ideal gas
equation-of-state into Equation (5). Equation (7) expresses the flow rate in standard
volumetric units. Equations (5) through (7) may be used to compute the required flow
coefficient, the flow rate or applied pressure differential given any two of the three quantities.
7.2 Pressure differentials
7.2.1 Sizing pressure drop ratio, x
sizing
The value of the pressure drop ratio used in Equations (5) through (7) to predict flow rate or
compute a required flow coefficient is the lesser of the actual pressure drop ratio or the
choked pressure drop ratio:
x if x < x

choked
x = (8)
sizing 
x if x ≥ x
 choked choked
where
∆p
x = (9)
p
7.2.2 Choked pressure drop ratio, x
choked
The pressure drop ratio at which flow no longer increases with increased value in pressure
drop ratio, is the choked pressure drop ratio, given by the following equation:
x = F x (10)
choked γ TP
NOTE The expression x reduces to x when the valve size and adjoining pipe sizes are identical. Refer to 8.1
TP T
for more information.
7.3 Specific heat ratio factor, F
γ
is based on air near atmospheric pressure as the flowing fluid with a specific
The factor x
T
heat ratio of 1,40. If the specific heat ratio for the flowing fluid is not 1,40, the factor F is used
γ
to adjust x . Use the following equation to calculate the specific heat ratio factor:
T
γ
F = (11)
γ
1,4
NOTE See Annex D for values of γ and F .
γ
60534-2-1  IEC:2011 – 13 –
Equation (11) evolved from assumption of perfect gas behaviour and extension of an orifice
plate model based on air and steam testing to control valves. Analysis of that model over a
range of 1,08 < γ < 1,65 leads to adoption of the current linear model embodied in Equation
(11). The difference between the original orifice model, other theoretical models and Equation
(11) is small within this range. However, the differences become significant outside of the
indicated range. For maximum accuracy, flow calculations based on this model should be
restricted to a specific heat ratio within this range and to ideal gas behaviour.
7.4 Expansion factor, Y
The expansion factor Y accounts for the change in density as the fluid passes from the valve
inlet to the vena contracta (the location just downstream of the orifice where the jet stream
area is a minimum). It also accounts for the change in the vena contracta area as the
pressure differential is varied.
Theoretically, Y is affected by all of the following:
a) ratio of port area to body inlet area;
b) shape of the flow path;
c) pressure differential ratio x;
d) Reynolds number;
e) specific heat ratio γ.
The influence of items a), b), c), and e) is accounted for by the pressure differential ratio
factor x , which may be established by air test and which is discussed in 8.4.
T
The Reynolds number is the ratio of inertial to viscous forces at the control valve orifice. In
the case of compressible flow, its value is beyond the range of influence since turbulent flow
almost always exists.
The pressure differential ratio x is influenced by the specific heat ratio of the fluid.
T
Y shall be calculated using Equation (12).
x
sizing
Y = 1− (12)
3x
choked
NOTE The expansion factor, Y, has a limiting value of under choked flow conditions.
7.5 Compressibility factor, Z
Several of the sizing equations do not contain a term for the actual density of the fluid at
upstream conditions. Instead, the density is inferred from the inlet pressure and temperature
based on the laws of ideal gases. Under some conditions, real gas behavior can deviate
markedly from the ideal. In these cases, the compressibility factor Z shall be introduced to
compensate for the discrepancy. Z is a function of both the reduced pressure and reduced
temperature. Reduced pressure p is defined as the ratio of the actual inlet absolute pressure
r
to the absolute thermodynamic critical pressure for the fluid in question. The reduced
temperature T is defined similarly. That is:
r
p
p =
r (13)
p
c
T
T =
r (14)
T
c
– 14 – 60534-2-1  IEC:2011
NOTE See Annex D for values of p and T .
c c
7.6 Non-turbulent (laminar and transitional) flow
The flow model embodied in Equations (5) through (7) is for fully developed, turbulent flow
only. Non-turbulent conditions may be encountered, especially when flow rates are quite low
or fluid viscosity is appreciable. To affirm the applicability of the flow model, the value of the
valve Reynolds Number (see Equation (23)) should be computed. The flow model is
applicable if Re ≥ 10 000.
V
8 Correction factors common to both incompressible and compressible flow
8.1 Piping geometry correction factors
The various piping geometry factors (F , F , x ) are necessary to account for fittings
P LP TP
attached upstream and/or downstream to a control valve body. The F factor is the ratio of the

P
flow rate through a control valve installed with attached fittings to the flow rate that would
result if the control valve was installed without attached fittings and tested under identical
conditions which will not produce choked flow in either installation (see Figure 1).
To meet the stated flow accuracy of ± 5 %, all piping geometry factors shall be determined by
test in accordance with IEC 60534-2-3.
When estimated values of the piping geometry factors are permissible, the following equations
should be used for concentric reducers and expanders directly coupled to the control valve.
These equations derive from an analytical accounting of the additional resistance and
interchange between the static and dynamic head introduced by the fittings.
The validity of this method is a function of the degree to which the control valve and attached
fittings remain hydraulically or aerodynamically independent of each other such that the
cumulative effects remain additive. This condition is likely to be satisfied for the majority of
practical applications. However, in certain styles of control valves, such as butterfly valves
and ball valves, pressure recovery is likely to occur principally in the downstream pipe as
rather than within the valve body. Replacement of the downstream pipe section with an
arbitrary pipe fitting may alter the recovery zone in some cases. Under this condition, it is
doubtful that the simple flow resistance method of correction will adequately account for these
effects.
8.2 Estimated piping geometry factor, F
P
The F factor is the ratio of the flow rate through a control valve installed with attached fittings
P
to the flow rate that would result if the control valve was installed without attached fittings and
tested under identical conditions which will not produce choked flow in either installation (see
Figure 1). When estimated values are permissible, the following equation shall be used:
F = (15)
P
Σζ  C 
1+  
 2 
N
d
2  
In this equation, the factor Σζ is the algebraic sum of all of the effective velocity head loss
coefficients of all fittings attached to the control valve. The velocity head loss coefficient of
the control valve itself is not included.
Σζ = ζ + ζ + ζ − ζ (16)
1 2 B1 B2
In cases where the piping diameters approaching and leaving the control valve are different,
the ζ coefficients are calculated as follows:
B
60534-2-1  IEC:2011 – 15 –
d
 
(17)
ζ = 1−  
B
D
 
If the inlet and outlet fittings are short-length, commercially available, concentric reducers, the
ζ and ζ coefficients may be approximated as follows:
1 2
Inlet reducer:
 
 
d
   
ζ = 0,5 1− (18)
 
D
 
 1 
 
Outlet reducer (expander):
 
 
d
ζ = 1,0 1−    (19)
 
D
 
 2 
 
Inlet and outlet reducers of equal size:
 
d
 
ζ + ζ = 1,5 1−    (20)
1 2
D
 
 
 
The F values calculated with the above ζ factors generally lead to the selection of valve
P
capacities slightly larger than required. See Annex C for methods of solution.
For graphical approximations of F , refer to Figures D.2a) and D.2b) in Annex D.
P
8.3 Estimated combined liquid pressure recovery factor and piping geometry factor
with attached fittings, F
LP
F is the liquid pressure recovery factor of the valve without attached fittings. This factor
L
accounts for the influence of the valve internal geometry on the valve capacity at choked flow.
It is defined as the ratio of the actual maximum flow rate under choked flow conditions to a
theoretical, non-choked flow rate which would be calculated if the pressure differential
used was the difference between the valve inlet pressure and the apparent vena contracta
pressure at choked flow conditions. The factor F may be determined from tests in
L
accordance with IEC 60534-2-3. Typical values of F versus percent of rated flow coefficient
L
are shown in Figure D.3.
F is the combined liquid pressure recovery factor and piping geometry factor for a control
LP
valve with attached fittings. It is obtained in the same manner as F .
L
To meet a deviation of ± 5 % for F , F shall be determined by testing. When estimated
LP LP
values are permissible, Equation (21) shall be used:
F
L
F = (21)
LP
F  C 
L
1+ (Σζ ) 
 2 
N
 d 
Here Σζ is the velocity head loss coefficient, ζ + ζ , of the fitting attached upstream of the
1 1 B1
valve as measured between the upstream pressure tap and the control valve body inlet.

– 16 – 60534-2-1  IEC:2011
8.4 Estimated pressure differential ratio factor with attached fittings, x
TP
x is the pressure differential ratio factor of a control valve installed without reducers or other
T
fittings. If the inlet pressure p is held constant and the outlet pressure p is progressively
1 2
lowered, the mass flow rate through a valve will increase to a maximum limit, a condition
referred to as choked flow. Further reductions in p will produce no further increase in flow
rate.
This limit is reached when the pressure differential x reaches a value of F x . The limiting
γ T
value of x is defined as the critical differential pressure ratio. The value of x used in any of the
sizing equations and in the relationship for Y (Equation (12)) shall be held to this limit even
though the actual pressure differential ratio is greater. Thus, the numerical value of Y may
range from 0,667, when x = F x , to 1,0 for very low differential pressures.
γ T
The values of x may be established by air test. The test procedure for this determination is
T
covered in IEC 60534-2-3.
NOTE 1 Representative values of x for several types of control valves with full size trim and at full rated
T
openings are given in Table D.1. Caution should be exercised in the use of this information. When precise values
are required, they should be obtained by test.
If a control valve is installed with attached fittings, the value of x will be affected.
T
x is the pressure differential ratio factor of a control valve with attached fittings at choked
TP
flow. To meet a deviation of ±5 % for x , the valve and attached fittings shall be tested as a
TP
unit. When estimated values are permissible, the Equation (22) shall be used:
x
T
F
P
x = (22)
TP
x ζ C
 
T i
1+  
N
d
 
NOTE 2 Values for N are given in Table 1 below.
In the above relationship, x is the pressure differential ratio factor for a control valve installed
T
without reducers or other fittings. ζ is the sum of the inlet velocity head loss coefficients
i
(ζ + ζ ) of the reducer or other fitting attached to the inlet face of the valve.
1 B1
If the inlet fitting is a short-length, commercially available reducer, the value of ζ may be
estimated using Equation (18).
9 Reynolds Number, Re
V
The incompressible and compressible flow models presented in the preceding clauses are for
fully developed turbulent flow. When non-turbulent flow conditions are established through a
control valve because of a low pressure differential, a high viscosity, a very small flow
coefficient, or a combination thereof, a different flow model is required.
The valve Reynolds Number, Re , is employed to determine whether the flow is fully
V
turbulent. Tests show that flow is fully turbulent when the valve Re ≥ 10 000. The valve
V
Reynolds Number is given by Equation (23):
1/ 4
 
N F Q F C
4 d
L
 
Re = +1 (23)
v
 
ν CF N d
L  2 
NOTE 1 The flow rate in Equation (23) is in actual volumetric flow rate units for both incompressible and
compressible flows.
60534-2-1  IEC:2011 – 17 –
NOTE 2 The kinematic viscosity, ν, should be evaluated at flow conditions.
When Re < 10 000, the equations presented in
...