orifice DP Sizing with Beta
Current Flange Spec Sheet_MonelITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE12120FO-0572800.0842506057a17.00100300Pilot gas to
acid relief header.23456789101. The actual flow of 20FO-057 is
about 110 SCFH for a bore diameter of 0.084.
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Flange-type Restrictive OrificesALL ITEMS SHALL COMPLY WITH
GENERAL SPECIFICATION SHEETSMATERIAL: MonelInstallation notes:1.
Orifice dia. As specified to suit required conditions.2. Gaskets
furnished by vendor.
Current Union Spec SheetITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE11120FO-1841-1/2800.2856057a0.5861003000Acid pump vent
header purge.23456789101. Item 1 is made of monel.
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Union Restrictive OrificesALL ITEMS SHALL COMPLY WITH GENERAL
SPECIFICATION SHEETSMATERIAL: 316SSInstallation notes:1. Unless
otherwise specified, the only markings on the orifice tab shall be
the orfice diameter indicated by a decimal fraction as shown on the
drawing with 1/16-in. figure stamping hand dies.2. Where lines are
to be insulated, the insulated material covering the union shall be
applied in such a manner that the markings on the tab will be fully
exposed.3. No asbestos-bearing material is acceptable; vendor to
provide TFE gaskets.
Current Flange Spec Sh_SSITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE11120FO-1752800.1356055a17.00100150Pilot gas to
20F-527.2345678910
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Flange-type Restrictive OrificesALL ITEMS SHALL COMPLY WITH
GENERAL SPECIFICATION SHEETSMATERIAL: 316SSInstallation notes:1.
Orifice dia. As specified to suit required conditions.2. Gaskets
furnished by vendor.
New Union Spec SheetITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE111280a1002345678910
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Union Restrictive OrificesALL ITEMS SHALL COMPLY WITH GENERAL
SPECIFICATION SHEETSMATERIAL: 316SSInstallation notes:1. Unless
otherwise specified, the only markings on the orifice tab shall be
the orfice diameter indicated by a decimal fraction as shown on the
drawing with 1/16-in. figure stamping hand dies.2. Where lines are
to be insulated, the insulated material covering the union shall be
applied in such a manner that the markings on the tab will be fully
exposed.3. No asbestos-bearing material is acceptable; vendor to
provide TFE gaskets.
InstructionsYellow is an input cell:Green is a
calculation:P1:60psigW =11.12PPHUnderline is value actually
used:Green in grey is a look-up value:0.603tp =2.500.607White in
black is a final answer:D2 =0.106in.Important reference information
about a cell is in violet:From Fluor tableCell for iteration with
goal seek:Target (To) cell for goal seek:Changing cell for goal
seek:[1st Cell][2nd Cell][3rd Cell]4.874.930.084
Sheet3No.DATEREVISIONSHEET NO.REV.NOMINAL LINE SIZE
IN.SPNOMONELANSI 150LBANSI 300LBANSI 600LBISSUE
DATE:1/2102321.5485454DIMENSIONS IN
MMMANUFACTURER:3/8102321.55767671102321.5677373P.O. No.:1
1/2102322.08695952102322.5105111111ISSUED:CHECK:3102323.01371491494102323.01751811946121323.02222512678121326.027930832110140456.034036240012140456.041042245714
OD140459.045148649216 OD152459.051454056518 OD1525112.054959761320
OD1525112.060365167924
OD1525116.07147717871/241-1/41/161-7/82-1/82-1/8DIMENSIONS IN
INCHES3/441-1/41/162-1/42-5/82-5/8141-1/41/162-5/82-7/82-7/81
1/241-1/45/643-3/83-3/43-3/4241-1/43/324-1/84-3/84-3/8341-1/21/85-3/85-7/85-7/8441-1/21/86-7/87-1/87-5/864-3/81-1/21/88-3/49-7/810-1/284-3/41-1/21/41112-1/812-5/8105-1/21-3/41/413-3/814-1/415-3/4125-1/21-3/41/416-1/816-5/81814
OD5-1/21-3/43/817-3/419-1/819-3/816 OD61-3/43/820-1/421-1/422-1/418
OD621/221-5/823-1/224-1/820 OD621/223-7/825-3/426-7/824
OD625/828-1/430-1/231-1/8NOMINAL LINE SIZE IN.SPNO316SSANSI
150LBANSI 300LBANSI 600LB1/2102321.5485454DIMENSIONS IN
MM3/8102321.55767671102321.56773731
1/2102322.08695952102322.51051111113102323.01371491494102323.01751811946121323.02222512678121326.027930832110140456.034036240012140456.041042245714
OD140459.045148649216 OD152459.051454056518 OD1525112.054959761320
OD1525112.060365167924
OD1525116.07147717871/241-1/41/161-7/82-1/82-1/8DIMENSIONS IN
INCHES3/441-1/41/162-1/42-5/82-5/8141-1/41/162-5/82-7/82-7/81
1/241-1/45/643-3/83-3/43-3/4241-1/43/324-1/84-3/84-3/8341-1/21/85-3/85-7/85-7/8441-1/21/86-7/87-1/87-5/864-3/81-1/21/88-3/49-7/810-1/284-3/41-1/21/41112-1/812-5/8105-1/21-3/41/413-3/814-1/415-3/4125-1/21-3/41/416-1/816-5/81814
OD5-1/21-3/43/817-3/419-1/819-3/816 OD61-3/43/820-1/421-1/422-1/418
OD621/221-5/823-1/224-1/820 OD621/223-3/425-5/826-3/424
OD625/828-1/430-3/831
New Flange Spec Sheet_SSITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE111280a1002345678910
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Flange-type Restrictive OrificesALL ITEMS SHALL COMPLY WITH
GENERAL SPECIFICATION SHEETSMATERIAL: 316SSInstallation notes:1.
Orifice dia. As specified to suit required conditions.2. Gaskets
furnished by vendor.
New Flange Spec Sheet_MonelITEMREV.QTY.TAG. NO.PIPE SIZE
(IN.)SCH.ORIFICE (IN.)FLOW QUANTITY (SCFH)UPSTREAM PRESSURE
(PSIG)DP (PSI)MWSGTEMP. (F)FLANGE
RATINGSERVICE111280a1002345678910
&L&"Arial Narrow,Regular"&10&P of
&N&R&9&F/&AINSTRUMENT SPECIFICATIONCitgo
Petroleum Corporation135th Street & New AvenueLemont, IL
60439Flange-type Restrictive OrificesALL ITEMS SHALL COMPLY WITH
GENERAL SPECIFICATION SHEETSMATERIAL: MonelInstallation notes:1.
Orifice dia. As specified to suit required conditions.2. Gaskets
furnished by vendor.
PropertiesCaution: this sheet calculates properties based on
yellow-highlighted cells. The viscosities will change and are a
function of pressure and temperature, however, the NIST values for
pure components will change so if T or P change update with
NIST.Gas PropertiesProperties using coresponding statesyTc, KPc,
atmVc, cm3/mol-1ZcwCpo, cal/gmol-KMm,
cPHydrogen033.2012.8065.000.31-0.226.912.020.00919Methane0.94190.6045.4099.000.290.018.6616.040.01167Ethane0.05305.4048.17148.000.290.1012.9830.070.00988Propane0.01369.8041.95203.000.280.1518.3044.100.00855Propylene0365.0045.60181.000.280.1515.7842.080.00904ButaneAverage,
Mixture:1.0000198.1345.65102.490.290.018.9817.02k =1.28R,
atm-cm^3/(K-gmole):8.21E+01Temperature, F:100311Pressure,
psig.:90Use initial (1) properties.Viscosity, cP:0.01151From VISC
Sheet - manual entry-- use NIST website for individual m, then use
Wilke's method in spreadsheet to calculate mixture m.m, cP @ 78
psigm, cP @ 90
psig100120100120Methane0.0116610.0120080.0116590.012006Ethane0.00985950.0101790.00988240.010201Propane0.00852980.00883560.00854690.0088525Propylene0.00901250.00934650.00903940.0093723Butane0.0092540.012779
Citgo Employee:k = Cp/(Cp-R) only for ideal gases, i.e.,
adiabatic flow of an ideal gas. For real gases, Cp and Cv must be
derived individually.
RO1RESTRICTIVE ORIFICE ---- Method 1Thin plate orifice
Low-Moderate DPNOT VERY ACCURATE!Rough method provided originally
in an article in Chemical Engineering magazinetb/bore diameter
=0.93P2/P1 =0.05Thin plate, no choked flow.Calculation not
applicable: refer to Kirk-Cunningham method.D, inches; Qg, gas flow
in SCFH (60 F, 1 atm); DP, P1, P2, psia; Sg = Mg/MairLine
Sizetp,mmT1, R; tp, plate thickness.0.51.5Using table from Fluor
specification: "Flange Type Restrictive Orifice"0.751.5Qg:250SCFH @
60 F, 1 atmComplete Property Sheet11.5DP =57.00Tr =2.51from
sheet1.52P1:60psigPr =0.1122.5P2:3psiUsing initial properties @ P1,
T133Mw:1743Sg =0.59manual allowed63T:100deg. Fk =1.2886Plate
Rate300300, 600# ANSI106tp =2.50mmFrom Fluor
table126Z:1.000.98Calculated using virial equations149D1,
nom:2.00in.Sch.:801691812Sat. Curve Test:0.749Test:OKAbbott
Equations are acceptable2012Hot Gas Test:0.433Saturated Area2416B1
=0.135Pr/Tr =0.044Z =1.00B0 =-0.014Pcf =40.98psigChoked Flow - for
thick plateD2 =0.106in.Beta =0.0551716.043CH4M =35.183X2
=0.050.957Selected diameter1.94IDNominal pipe dia. -
inches1.01.52.03.04.06.08.010.012.014.016.018.020.0Pipe dia. -
inches for schedule 40
pipe1.051.612.073.074.036.077.9810.0211.9413.1215.0016.8818.81Pipe
dia. - inches for schedule 80
pipe0.961.501.942.903.835.767.639.5611.3712.5014.3116.1217.94Pipe
dia. - inches for schedule 160
pipe0.821.341.692.623.445.196.818.5010.1311.1912.8114.4416.062.0671.9391.687
&L&G&L&P of &N&C&G Lemont,
Illinois&R&9&F/&AP1:P2:D1:D2:D=Qg/SQRT( DP(P1
+P2)/(2SgT1)78X5440(tp/0.125)X1/5Method assumes, implicitly, that
gas is ideal gas mixture or perfect gas.Flow through a thin plate
is never choked flow. For this to apply, the ratio of tb/bore
diameter must be < 6. (Reference: pg. 13.22, Richard Miller's
"Flow Measurement Engineering Handbook," 3rd ed., McGraw Hill,
1996. Page 13-22 refers to the work of Cunningham (1951) and
Ward-Smith (1979).Kirk-Cunningham applies when P20.995 taken as
Zf=1.00027.71327.711Corrected h-maxFdREAL GAS60.195NOMINALBASEGAS
DPDENSITYCInf.CInf.Cinf for Rosemount 1195 Integral
OrificesCInf.nb(IWC)(lbs./cf)N.D.I.D.bb[D>2.3][2 4000, it is
acceptable to use values from Richard Miller's "Flow Measurement
Engineering Handbook, " Table 9.1:C = C + b/ReDnn = 0.75b =
91.706b2.5b =0.144D =2.00ReD =4,8740.726D 2.3 inches:C = 0.5959 +
0.0312(b)2.1 - 0.184(b)8 + 0.09[b4/(D(1-b4)] - 0.0337[(b)3/D]0.596C
=0.5982 D 2.3 inches:C = 0.5959 + 0.0312(b)2.1 - 0.184(b)8 +
0.039[b4/((1-b4)] - 0.0337[(b)3/D]0.596
&L&G&R&"Century Gothic,Italic"&10This method
is more general.&L&P of &N&C&GLemont,
Illinois&R&"Arial
Narrow,Regular"&9&F/&AP1:P2:D1:Do:W=DPrEquation 2-24,
Crane TP 410, adapted on 3.24 of text.1891 Y C d20Flow through a
thin plate is never choked flow. For this to apply, the ratio of
tb/bore diameter must be < 6. (Reference: pg. 13.22, Richard
Miller's "Flow Measurement Engineering Handbook," 3rd ed., McGraw
Hill, 1996. Page 13-22 refers to the work of Cunningham (1951) and
Ward-Smith (1979). In 2005, Kirk explored the limits of
Cunningham's work. He found that ASME formulas worked fine with
adjustment of Y; C could be defined using ASME and other
methods.Kirk-Cunningham applies when P2 6), then the flow is choked
and a larger orifice will be required to flow the same
mass.DW:Based on ideal gas at inlet flow temperature. Slight error
can be expected for saturated conditions near critical point. K
affects Y so a significant deviation will be a problem. Ideal gas k
should not be used if residuals are large.DW:Cunningham showed that
a thin plate orifice is not restricted by choked flow. Until 2005,
it was assumed that Y and C would be different than for unchoked
flow. Kirk presented a new Y equation for conditions below
Pcritcal, whn P2/P1 are below 0.63. Without these new equations, an
error of up to 40%, or more, can be expected by using standard ASME
equations for Y and C.DW:Calculate Do with goal seek by selecting
Wcalc for set, typing in the value for Wd, and using the value of
Do for the change cell.DW:Not all of the pressure drop across the
orifice is lost. As the Beta is decreased, the permanent loss
approaches the tap measurement, which is always the larger of the
two.DW:This is the value used in Wcalc.DW:Target flow rate.DW:Re is
measured for the pipe not the bore.DW:Wd is the mass flow rate
based on Qg and SC density.DW:Wcalc is the mass flow rate based on
Crane equation 2-24.DW:This viscosity is the mixture viscosity from
the "Properties" sheet --- from "VISC." VISC calculates mixture
viscosity using the Wilke equation.DW:Manual input is allowed for
Z. (Although program will calculate Z, calculated Z will be ignored
if yellow cell has value.) In some circumstances Z will not be
calculated: if the Abbott equations do not apply. In this unlikely
event, read the Zo, Z1 values from the appropriate curves,
calculate Z by hand and enter here.Citgo Employee:Temperature
upstream of orifice, i.e., for D1. Final temperature will decrease
as a result of throttling. Usually, adiabatic expansion yields the
lowest pressure drop and temperature drop but isothermal expansion
has been assumed. Isothermal really only applies for long runs of
small pipe.DW:Real gas density at upstream conditions.DW:For the
Abbott equations to apply, an error curve was prepared relating
Tr(y) to Pr(x): Figure 3.16, Smith & Van Ness, "Introduction to
Chemical Engineering Thermodynamics," 4th edition. Above the curve,
the Abbott equations apply, below the curve, the charts for Zo, Z1
must be used. The curve has a break but can be approximated by two
straight line sections: "sat curve" and "hot gas curve."DW:M.M.
Abbott developed equations for Z in terms of a truncated virial
coefficient equation.DW:"Sch." affects the diameter, i.e.,
D1.DW:Below the calculated pressure, Pcf, a vena contracta will
form, beyond it, the gas passes through a sonic barrier. As the
pressure is reduced further, the vena contracta will approach the
bore.
R04RESTRICTIVE ORIFICE ---- Method 4Thin plate orifice All flow
conditionsCrane TP 410, "Flow of Fluids Through Valves, Fittings,
and Pipe," 23rd printing.tb/bore diameter =1.82P2/P1
=0.0333333333Thin plate, no choked flow.ASME calculation not
practical --- P2/P1 too low ---Kirk-Cunningham method.THIS IS BEST
METHOD!Complete Property SheetW: lbs./hr; Y: dimensionless; C:
1/ft; do: inches; DP: psi; r: #mass/cfEstimated Compressibility
Factor (Z) for Base and Inlet ConditionsStandard Conditions:P, psia
=14.696T, F =60For (b):Trb =1.46Sat. Curve Test:0.714Test:Choose
Cunningham (1),Miller (2), or Fluor (3) for Y1:OKPrb =0.04Hot Gas
Test:0.400OKFlange taps1CunninghamPr/Tr =0.030Saturated
AreaQg:250SCFHY1 =0.66Cunningham recommendedZb =0.980B1 =0.104Y0.77
=0.93Y0.63 =0.880.66Cunningham0.72Fluor: Miller eq. 9.580.71Miller,
Miller eq. 9.56rb, #/cf =0.05k =1.28manual0.980B0 =-0.148DP
=87.0Abbott Equations are acceptableP1:90psigC, ft-1 =0.595ASME,
Crane 410Zf =0.980P2:3psi0.607CunninghamMw:17manual allowedFor
(1):Tr1 =1.57Sat. Curve Test=0.772Test:r1, #/cf =0.02manual
allowedPr1 =0.16Hot Gas Test=0.455OKT:100deg. FPr/Tr
=0.100Saturated AreaPlate Rate300300, 600# ANSIB1 =0.113tp
=2.50mmFrom Fluor tableB0 =-0.122Z1:0.991manual allowedAbbott
Equations are acceptableD1, nom:2.00in.Sch.:80Zf =0.991mg,
cP=0.01151manual allowedRe1 =3,233DPp =86psigWd =11.43PPHWcalc
=11.31PPHProblem solved with goal seekMatch Qg:PPHQcalc =247SCFHPcf
=57.43psigChoked Flow - for thick plateDo =0.054in.Beta
=0.0280.0663in.Coefficients for AGA equation:K =0.607Ftb =1.000Ftf1
=0.964Fpv1Gr =0.994FGr =1.297Fpb =1.002hw, IWC =2,411Greal
=0.594Selected diameter1.94IDNominal pipe dia. -
inches1/23/41.01.52.03.04.06.08.010.012.014.016.018.020.0Pipe dia.
- inches for schedule 40
pipe0.620.821.051.612.073.074.036.077.9810.0211.9413.1215.0016.8818.81Pipe
dia. - inches for schedule 80
pipe0.550.740.961.501.942.903.835.767.639.5611.3712.5014.3116.1217.94Pipe
dia. - inches for schedule 160
pipe0.460.610.821.341.692.623.445.196.818.5010.1311.1912.8114.4416.062.0671.9391.687Line
Sizetp,mmTo estimate composition of natural gas based on M
alone:0.51.5Using table from Fluor specification: "Flange Type
Restrictive Orifice"0.751.51716.043CH411.5M =35.1831.52X2
=0.05other than CH422.50.95733436386106126149169181220122416Flow
Coefficient, C, 1/ft, Table from Crane 410:BetaSlopeRe00.2BetaRe1
=3,2330.616261081220000.6000.6000.6000.595Beta
=0.02790.139720782640000.5920.5920.592BetaRe00.20.30.40.50.60.70.8Values
read from "Flow Coefficient C for Square-Edged
Orifices30.530.530.4740.430.3880.3550.3020.27540.560.560.510.4680.4180.40.3620.33860.6050.6050.5650.5280.4960.460.4350.42580.6450.6450.60.5680.5280.5080.4920.486100.650.650.620.5950.5650.540.5350.535200.680.680.670.6550.6650.6550.650.692400.6950.6950.6950.6920.7080.7390.7780.872600.6920.6920.7020.7060.7280.770.8320.968800.6880.6880.6990.7080.7380.7850.871.031000.6840.6840.6980.7160.7450.7980.8881.0652000.6480.6480.6820.7010.7470.810.9291.1554000.6240.6240.6480.6680.7350.8040.9491.2186000.6140.6140.6340.6480.7230.7990.9521.238000.6080.6080.6250.6380.7140.7870.9451.23510000.6050.6050.6150.6280.7050.7770.9351.23420000.60.60.6060.6170.6830.740.8651.21540000.5920.5920.60.6080.660.70.7850.932If
the Re is > 4000, it is acceptable to use values from Richard
Miller's "Flow Measurement Engineering Handbook, " Table 9.1:C = C
+ b/ReDnn = 0.75b = 91.706b2.5b =0.028D =2.00ReD =3,2330.012D 2.3
inches:C = 0.5959 + 0.0312(b)2.1 - 0.184(b)8 + 0.09[b4/(D(1-b4)] -
0.0337[(b)3/D]0.596C =0.5962 D 2.3 inches:C = 0.5959 + 0.0312(b)2.1
- 0.184(b)8 + 0.039[b4/((1-b4)] - 0.0337[(b)3/D]0.596
&L&G&R&"Century Gothic,Italic"&10This method
is more general.&L&P of &N&C&GLemont,
Illinois&R&"Arial
Narrow,Regular"&9&F/&AP1:P2:D1:Do:W=DhPf1Adapted from
equation 9.68, "The AGA equation," in Richard Miller's Flow
Measurement Engineering Handbook, 3rd ed., McGraw Hill , CR 1996
(This equation was adapted originally from equation 2-24, Crane TP
410.)Flow through a thin plate is never choked flow. For this to
apply, the ratio of tb/bore diameter must be < 6. (Reference:
pg. 13.22, Richard Miller's "Flow Measurement Engineering
Handbook," 3rd ed., McGraw Hill, 1996. Page 13-22 refers to the
work of Cunningham (1951) and Ward-Smith (1979). In 2005, Kirk
explored the limits of Cunningham's work. He found that ASME
formulas worked fine with adjustment of Y; C could be defined using
ASME and other methods.Kirk-Cunningham applies when P2 6), then the
flow is choked and a larger orifice will be required to flow the
same mass.DW:Based on ideal gas at inlet flow temperature. Slight
error can be expected for saturated conditions near critical point.
K affects Y so a significant deviation will be a problem. Ideal gas
k should not be used if residuals are large.DW:Cunningham showed
that a thin plate orifice is not restricted by choked flow. Until
2005, it was assumed that Y and C would be different than for
unchoked flow. Kirk presented a new Y equation for conditions below
Pcritcal, whn P2/P1 are below 0.63. Without these new equations, an
error of up to 40%, or more, can be expected by using standard ASME
equations for Y and C.DW:Calculate Do with goal seek by selecting
Wcalc for set, typing in the value for Wd, and using the value of
Do for the change cell.DW:Not all of the pressure drop across the
orifice is lost. As the Beta is decreased, the permanent loss
approaches the tap measurement, which is always the larger of the
two.DW:This is the value used in Wcalc.DW:Target flow rate.DW:Re is
measured for the pipe not the bore.DW:Wd is the mass flow rate
based on Qg and SC density.DW:Wcalc is the mass flow rate based on
Crane equation 2-24.DW:This viscosity is the mixture viscosity from
the "Properties" sheet --- from "VISC." VISC calculates mixture
viscosity using the Wilke equation.DW:Manual input is allowed for
Z. (Although program will calculate Z, calculated Z will be ignored
if yellow cell has value.) In some circumstances Z will not be
calculated: if the Abbott equations do not apply. In this unlikely
event, read the Zo, Z1 values from the appropriate curves,
calculate Z by hand and enter here.Citgo Employee:Temperature
upstream of orifice, i.e., for D1. Final temperature will decrease
as a result of throttling. Usually, adiabatic expansion yields the
lowest pressure drop and temperature drop but isothermal expansion
has been assumed. Isothermal really only applies for long runs of
small pipe.DW:Real gas density at upstream conditions.DW:For the
Abbott equations to apply, an error curve was prepared relating
Tr(y) to Pr(x): Figure 3.16, Smith & Van Ness, "Introduction to
Chemical Engineering Thermodynamics," 4th edition. Above the curve,
the Abbott equations apply, below the curve, the charts for Zo, Z1
must be used. The curve has a break but can be approximated by two
straight line sections: "sat curve" and "hot gas curve."DW:M.M.
Abbott developed equations for Z in terms of a truncated virial
coefficient equation.DW:"Sch." affects the diameter, i.e., D1.DW:Qg
@ Wcalc.Citgo Employee:Add 1 to oversize the orifice, since ideal
gases always occupy more space than real gases.Type the calculated
value in the yellow cell to avoid a circular logic error when using
goal seek to calculate the required bore diameter.DW:For the Abbott
equations to apply, an error curve was prepared relating Tr(y) to
Pr(x): Figure 3.16, Smith & Van Ness, "Introduction to Chemical
Engineering Thermodynamics," 4th edition. Above the curve, the
Abbott equations apply, below the curve, the charts for Zo, Z1 must
be used. The curve has a break but can be approximated by two
straight line sections: "sat curve" and "hot gas curve."DW:M.M.
Abbott developed equations for Z in terms of a truncated virial
coefficient equation.Citgo Employee:Calculate Z for the gas at
standard (b) conditions. A lazy man would let the program calculate
Zf then calculate Zb if necessary, i.e., Zf < 0.99.DW:Includes
Zb --- pb is not an ideal gas density it is a real gas
density.DW:The permanent pressure loss is the goal of sizing the RO
not Do! The premanent pressure loss will never quite match the
desired drop but you can adjust P2 to get it close.DW:Below the
calculated pressure, Pcf, a vena contracta will form, beyond it,
the gas passes through a sonic barrier. As the pressure is reduced
further, the vena contracta will approach the bore.DW:Use Twater =
60 F.DW:Y1: the upstream gas expansion factor. Y2 is the downstream
gas expansion factor.DW:Cunningham will produce the largest
diameter, followed by Miller (eq. 9.56, for restrictive orifices).
Fluor will produce the largest Y and therefore the smallest orifice
bore.D W:To calculate the required flow through a fixed Do use the
following procedure. (2007 Excel is different than 2004):1. Click
on B28, the value for Wd. This will be the "Set Cell" for Goal
Seek.2. Go to Tools (in 2004) and select Goal Seek. (In 2007, you
will need to add in the analysis tool pak. Go to the office button,
select options, then add-ins and look for the analysis tool pac.
Once you've loaded the add-in, Goal Seek will be in the Data
pull-down menu under the Data Tools section. For 2007 users: click
Goal Seek.)3.Type in the value for Wd calculated for Do (fixed) in
the "To value" entry.4. For the "Change Cell" entry, click on B11,
for Qg. This will be the value adjusted.5. When done, click the
start button at the bottom of the Goal Seek menu.6. Goal Seek
should calculate a value after 50 or so iterations. Check the value
and accept or reject. If you reject, review the sheet for other
errors.
VISCG A S M I X T U R E V I S C O S I T YThis sheet talks with
the Properties Sheet.Enter values in "Yellow."Manual input values
are in "Green."Temperature38C100FCalculated values in "Light
Green".Program assumes that gases are perfect and form an ideal
vapor solution. Program will deviate slightly for high pressure
(>150 psig & presence of wet gas.Wilke method shows some
deviations where molecular weights are significantly different,
i.e., Mi>>Mj.Wilke Gas Mixture Viscosity Calculation for
Ideal Gases or Real Gases @ Low-Moderate
PressuresComponentyiManManual
hihiMFi1Fi2Fi3Fi4Fi5Fi6Fi7Fi8Fi9Fi10Sum FijSum
yihiNHydrogen0.00Yes0.0091890.02.020.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0001Methane0.94Yes0.0116720.011716.040.0001.0001.4731.8990.0000.0000.0000.0000.0000.0001.0330.0112Ethane0.05Yes0.0098820.009930.070.0000.6651.0001.3000.0000.0000.0000.0000.0000.0000.6890.0013Propane0.01Yes0.0085470.008544.100.5060.5060.7661.0000.0000.0000.0000.0000.0000.0000.5240.0004Propylene0.00Yes0.0090390.042.080.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0005Gas
61.00Yes0.0000000.00.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0006Gas
70.00Yes0.0000000.00.000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0007Gas
80.00Yes0.0000000.00.000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0008Gas
90.00Yes0.0000000.00.000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0009Gas
100.00Yes0.0000000.00.000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.0000.00010Total2.00mm
=0.0115m = a + b(T) + c(T)2 +d(T)3Cp = a + b(T) + c(T)2 + d(T)3 +
e(T)4 +
f(T)5GasabcMwt.abcdefAlCl297.899.040158.68E-03-5.89E-061.72E-09-1.82E-130AlCl3-0.000602550.0000136455-7.11E-10133.3412.257402.40E-02-4.39E-054.81E-08-2.66E-115.57E-15Carbon
Dioxide0.001872.39E-05-1.27E-0944.0096.214155.12E-03-6.03E-08000Carbon
Monoxide0.006282.16E-05-1.70E-0928.016.420438.88E-04-6.03E-08000Chlorine0.002150.00002013552.33E-0970.96.021276.56E-03-6.41E-063.01E-09-0.000000Hydrogen
Sulfide-7.57E-052.40E-05-3.40E-1033.0686.661502.85E-03-2.64E-07000Nitrogen0.003444.28E-057.15E-0928.0136.895007.62E-04-7.01E-08000Oxygen0.006242.59E-05-2.71E-0931.9986.442841.25E-03-1.89E-07000HCl0.001772.26E-053.95E-0936.4616.51457-6.00E-040000Sulfur
Dioxide1.23E-032.12E-05-1.44E-0964.0587.115955.93E-031.08E-06000TiCl40.00710.0000730.0000000116189.6913.313612.92E-02-2.81E-051.32E-08-2.99E-122.62E-16Water-0.000961.97E-05-3.84E-0918.0157.089761.55E-030000Information
Alligned for MBAL & VISC for auto entries.Cp = a + b(T) + c(T)2
+ d(T)3 + e(T)4 + f(T)5MAT-MATRIXa(m)b (m)c
(m)Mwtabcdef0000000000.00E+0000000000000.00E+000.00E+000000000.00E+000.00E+000.00E+000.00E+000.00E+0000000000000000000000.00E+000.00E+000.00E+000000000000.00E+000.00E+000000000000.00E+000.00E+000000000000.00E+000.00E+000000000000.00E+000.00E+000000000000.00E+000.00E+00
&A&L&"Times New Roman,Italic"&8D. Willard
&D&C&"Courier (W1),Regular"&8Plant
I&R&"Times New Roman,Regular"&8RELSIZE.XLS(VISC)
Assembed Union
Beta
Chart0.01438221820.01256761350.00722065380.03216798460.0280769930.01626122540.0454862560.03970676670.0230050870.06432699590.05614765030.0325032760.07878697060.06876860070.03982076150.09097362330.07940826860.04596658640.11141499770.09725118260.0562971075
T1 = 100oF, DP = 87 psig, P1 = 90 psig, Using Cunningham
calculation for Y1, as yielding the highest Q. The pressure drop is
not "hw;" the drop is the permanent pressure loss.W = Q(PM/RT) =
QM/408.67PPH: pounds per hourQ = W(408.66/M)k = 1.2; M = 30k=1.3; M
= 17k = 1.4; M = 2Q, SCFH (60 F, 14.7 psia)b, (bore dia./pipe ID)b
.v.s. Q for sq.-edged orifice plates
Sheet1T1 = 100oF, DP = 87 psig, P1 = 90 psig, Using
CunninghamkoQ, SCFHb, 2"b,
1"M1.2500.01440.0144301.22500.03220.03221.25000.04550.04551.21,0000.06430.06431.21,5000.07880.07881.22,0000.09100.09101.23,0000.11140.11141.24,0000.12980.12981.25,0000.14510.14511.3500.01260.0126171.32500.02810.02810.02791.35000.03970.03971.31,0000.05610.05611.31,5000.06880.06881.32,0000.07940.07941.33,0000.09730.09731.34,0000.13170.13171.35,0000.14720.14721.4500.00720.007221.42500.01630.01631.45000.02300.02301.41,0000.03250.03251.41,5000.03980.03981.42,0000.04600.04601.43,0000.05630.05631.44,0000.06600.06601.45,0000.07370.0737
D W:
