orf1
DESCRIPTION
Orifice plate calculatorTRANSCRIPT
1 of 25 document.xls/Current Flange Spec Sheet_Monel
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 2 1 20FO-057 2 80 0.084 250 60 57 a 17.00 100 300 Pilot gas to acid relief header.
2
3
4
5
6
7
8
9
10
1. The actual flow of 20FO-057 is about 110 SCFH for a bore diameter of 0.084.
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Flange-type Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: Monel
Installation notes:1. Orifice dia. As specified to suit required conditions.2. Gaskets furnished by vendor.
2 of 25 document.xls/Current Union Spec Sheet
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 1 1 20FO-184 1-1/2 80 0.285 60 57 a 0.586 100 3000 Acid pump vent header purge.
2
3
4
5
6
7
8
9
10
1. Item 1 is made of monel.
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Union Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: 316SS
Installation 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.
3 of 25 document.xls/Current Flange Spec Sh_SS
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 1 1 20FO-175 2 80 0.135 60 55 a 17.00 100 150 Pilot gas to 20F-527.
2
3
4
5
6
7
8
9
10
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Flange-type Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: 316SS
Installation notes:1. Orifice dia. As specified to suit required conditions.2. Gaskets furnished by vendor.
4 of 25 document.xls/New Union Spec Sheet
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 1 1 2 80 a 100
2
3
4
5
6
7
8
9
10
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Union Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: 316SS
Installation 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.
Yellow is an input cell: Green is a calculation:P1: 60 psig W = 11.12 PPH
Underline is value actually used: Green in grey is a look-up value:0.603 tp = 2.500.607
White in black is a final answer:
D2 = 0.106 in.
Important reference information about a cell is in violet:From Fluor table
Cell for iteration with goal seek: Target (To) cell for goal seek: Changing cell for goal seek:[1st Cell] [2nd Cell] [3rd Cell]
4.87 4.93 0.084
Changing cell for goal seek:
7 of 25 document.xls/New Flange Spec Sheet_SS
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 1 1 2 80 a 100
2
3
4
5
6
7
8
9
10
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Flange-type Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: 316SS
Installation notes:1. Orifice dia. As specified to suit required conditions.2. Gaskets furnished by vendor.
8 of 25 document.xls/New Flange Spec Sheet_Monel
ITEM REV. QTY. TAG. NO. SCH. SERVICE
1 1 1 2 80 a 100
2
3
4
5
6
7
8
9
10
PIPE SIZE (IN.)
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE
(PSIG)DP
(PSI)MW
SG
TEMP. (F)
FLANGE RATING
INSTRUMENT SPECIFICATION
Citgo Petroleum Corporation135th Street & New AvenueLemont, IL 60439
Flange-type Restrictive Orifices
No. DATE REVISION SHEET NO. REV.
ISSUED: CHECK:
P.O. No.:
ISSUE DATE:
MANUFACTURER:
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: Monel
Installation notes:1. Orifice dia. As specified to suit required conditions.2. Gaskets furnished by vendor.
Gas Properties
y Tc, K Pc, atm Zc wHydrogen 0 33.20 12.80 65.00 0.31 -0.22Methane 0.94 190.60 45.40 99.00 0.29 0.01Ethane 0.05 305.40 48.17 148.00 0.29 0.10Propane 0.01 369.80 41.95 203.00 0.28 0.15Propylene 0 365.00 45.60 181.00 0.28 0.15Butane
Average, Mixture: 1.0000 198.13 45.65 102.49 0.29 0.01k =
R, atm-cm^3/(K-gmole): 8.21E+01Temperature, F: 100 311Pressure, psig.: 90 Use initial (1) properties.Viscosity, cP: 0.01151
100 120 100 120Methane 0.011661 0.012008 0.011659 0.012006Ethane 0.00986 0.010179 0.009882 0.010201Propane 0.00853 0.008836 0.008547 0.008853Propylene 0.009013 0.009347 0.009039 0.009372Butane 0.009254 0.012779
Caution: 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.
Properties using coresponding states
Vc, cm3/mol-
1
From VISC Sheet - manual entry-- use NIST website for individual m, then use Wilke's method in spreadsheet to calculate mixture m.
m, cP @ 78 psig m, cP @ 90 psig
M6.91 2.02 0.009198.66 16.04 0.01167
12.98 30.07 0.0098818.30 44.10 0.0085515.78 42.08 0.00904
8.98 17.021.28
Caution: 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
Cpo, cal/gmol-
K m, cP
From VISC Sheet - manual entry-- use NIST website for , then use Wilke's method in spreadsheet to calculate
11 of 25
Lemont, Illinoisdocument.xls/RO1
RESTRICTIVE ORIFICE ---- Method 1Rough method provided originally in an article in Chemical Engineering magazine tb/bore diameter = 0.93P2/P1 = 0.05 Thin 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/Mair Line Size tp,mm
T1, R; tp, plate thickness. 0.5 1.5
0.75 1.5Qg: 250 SCFH @ 60 F, 1 atm Complete Property Sheet 1 1.5
57.00 Tr = 2.51 from sheet 1.5 2P1: 60 psig Pr = 0.11 2 2.5P2: 3 psi 3 3Mw: 17 4 3Sg = 0.59 manual allowed 6 3T: 100 deg. F k = 1.28 8 6Plate Rate 300 300, 600# ANSI 10 6tp = 2.50 mm From Fluor table 12 6Z: 1.00 0.98 Calculated using virial equations 14 9D1, nom: 2.00 in. Sch.: 80 16 9
18 12Sat. Curve Test: 0.749 Test: OK Abbott Equations are acceptable 20 12
Hot Gas Test: 0.433 Saturated Area 24 16B1 = 0.135 Pr/Tr = 0.044 Z = 1.00B0 = -0.014
Thin plate orifice Low-Moderate DP
Using table from Fluor specification: "Flange Type Restrictive Orifice"
DP =
Using initial properties @ P1, T1
P1:D =
Qg/SQRT( DP(P1 +P2)/(2SgT1)7 8
X 5440
(tp/0.125) X 1/5
Method 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 P2<0.63P1. Cunningham showed that choked flow (critical, i.e., M =1 @ throat) does not occur for thin orifice plates.
12 of 25
Lemont, Illinoisdocument.xls/RO1
Pcf = 40.98 psig Choked Flow - for thick plate D2 = 0.106 in. Beta = 0.055
13 of 25Lemont, Illinois
document.xls/RO2
RESTRICTIVE ORIFICE ---- Method 2tb/db = 7.41 Thick plate method applies: choked flow. Min. Pressure is: 40.98 psig
A: throat cross-sectional area, sq. ft; W: #/s; Co = 0.72; P1: inlet pressure, psf; gc = 32.174T1: inlet temperature, F; R = 1545.3 ft-#f/#mole-R.
Qg: 250 SCFH @ 60 F, 1 atm St. T = 60 FW = 11.22 PPH 14.696 psia
0.04 lbs./cf Co: 0.72D1: 1.939 in.P1: 60 psig k = 1.28 Property Sheet
exp. = 8.03Mw: 17.02 Property Sheet
Pcf = 40.98 psig Choked FlowT: 100 deg. F
A = 0.004 sq. in. Complete Property SheetTr = 2.51 Using initial properties @ P1, T1
D = 0.067 in. Pr = 0.11Beta = 0.0348 Sat. Curve Test: 0.749 Below: use chartstp = 0.50 in. Hot Gas Test: 0.433 Saturated Area
Test: OK Abbott Equations are acceptableB1 = 0.135B0 = -0.014
Pr/Tr = 0.044
Thick plate orifice or flow nozzle, Choked Flow
Choked Flow: eq. 4-40, pg. 100, Daniel Crowl, Joseph Louvar, "Chemical Process Safety Fundamentals with Applications, Prentice-Hall, 1990.
r = Crowl/Louvar recommends 1.0 for Co with sharp-edged orifices with Re1 >30,000; seldom does this occur.
P1: A = W
Co P1 k gc M RT1
X 2k + 1
(k+1)/(k-1)
4-40Crowl & Louvar assume a thick orifice plate, or flow nozzle, not a thin plate.
Also found in Perry's 6th edition of "Chemical Engineering Handbook," pg. 5-14, equation 5.27. Assumes Beta < 0.2. (Ideal gas also assumed and implicite in solution using isentropic expansion).
This sheet is most useful in estimating flow from nozzles and holes in vessels or pipe.
14 of 25Lemont, Illinois
document.xls/RO2
Z = 1.00
04/08/2023 Calculation for North American Mfg. Co. Combustion Air FE
D. Willard International Steel Services, Inc. document.xls
ORIFICE DATA SHEET
Type of Orifice Plate: Standard
Drain Hole (for Condensate): None
MAXIMUM (URV-Ranged) DIFFERENTIAL PRESSURE = 40 IWC Pipe Diameter?
MAXIMUM FLOW RATE REQUIRED = 10,000 PPH
131,510 SCFH
DP (Required ) AT REQUIRED MAX. FLOW RATE = 29.78 IWC Y-Equation?
CALCULATED MAXIMUM FLOW RATE (At URV) = 11,589 PPH hw-O.K. Turndown O.K 0.895
152,400 SCFH Y-O.K.
PERMANENT PRESSURE LOSS AT MAX. RATE (At URV) = 1.35 PSIG
37.53 IWC
ORIFICE INLET MAX. CALC. REYNOLDS NUMBER = 1,050,626
Orifice Re?
NOMINAL DIFFERENTIAL PRESSURE = 7.45 IWC Re--tubulent--O.K.
NOMINAL FLOW RATE = 5,000 PPH Safe Min. Rate?
65,750 SCFH Min.---O.K.
MINIMUM DIFFERENTIAL PRESSURE = 0.30 IWC
MINIMUM (Practical) FLOW RATE = 1,000 PPH Mach No. OK?
13,150 SCFH Gas Orifice velocity is O.K.
MINIMUM ORIFICE INLET REYNOLDS NUMBER = 10,000
Change in Physical Properties?
FLUID: Change in properties --O.K
INITIAL GAS TEMPERATURE = 70 F
INITIAL GAS PRESSURE = 30 psig
GAS COMPRESSIBILITY COEFFICIENT, Z, = 1.000
GAS SPECIFIC HEAT RATIO, k, = 1.39817842048393
GAS VISCOSITY @ FLOW CONDITIONS = 0.01634555005 cP
BASE TEMPERATURE = 60 F
BASE PRESSURE = 14.696 psig
BASE COMPRESSIBILITY FACTOR, Z, = 1.000
NOMINAL PIPE DIAMETER, INCHES = 24" CS Pipe
PIPE INTERNAL DIAMETER, INCHES = 23.5 Inches
FLANGE ORIFICE DIAMETER, do, INCHES , = 4.26222527388441 Inches
ORIFICE BETA = 0.1814
PLATE MATERIAL = SS
PLATE BASE THERMAL EXPANSION = 0.0000097 1/F
PLATE THERMAL EXPANSION = 0.0000089 1/F
CHANGE IN GAS DENSITY OVER PLATE = -0.94%
CHANGE IN GAS TEMPERATURE = -4.9 F
DISCHARGE MACH NO., M=1 IS CRITICAL, = 0.126
For Maximum Flow CalculationC' (PPH) = 274.091 K = 0.5972 Y1 = 0.9905
Ftb = 1.003 C' (SCFH) = 3604.474 Fpv = 1.0000
Fm = 1.000 FG = 0.99857 FPb = 1.0000
Fa = 1.000 FTf = 0.9896 Fl = 0.9998
Flowing conditions were used to calculate the discharge rate of the orifice.
04/08/2023 Calculation for FE-344'A' Reactor Toluene Atomizing Nitrogen
D. Willard
ORIFICE DATA SHEET
Type of Orifice Plate: Integral
Drain Hole (for Condensate): None
MAXIMUM (URV-Ranged) DIFFERENTIAL PRESSURE = 60.2 IWC Pipe Diameter?
MAXIMUM FLOW RATE REQUIRED = 172 PPH
2,320 SCFH
DP (Required ) AT REQUIRED MAX. FLOW RATE = 60.20 IWC Y-Equation?
CALCULATED MAXIMUM FLOW RATE (At URV) = 171 PPH hw-O.K. Turndown O.K 0.416
2,320 SCFH Y-O.K.
PERMANENT PRESSURE LOSS AT MAX. RATE (At URV) = 1.56 PSIG
43.30 IWC
ORIFICE INLET MAX. CALC. REYNOLDS NUMBER = 176,990
Orifice Re?
NOMINAL DIFFERENTIAL PRESSURE = 15.03 IWC Re--tubulent--O.K.
NOMINAL FLOW RATE = 86 PPH Safe Min. Rate?
1,160 SCFH Min.---O.K.
MINIMUM DIFFERENTIAL PRESSURE = 0.60 IWC
MINIMUM (Practical) FLOW RATE = 17 PPH Mach No. OK?
230 SCFH Gas Orifice velocity is O.K.
MINIMUM ORIFICE INLET REYNOLDS NUMBER = 10,000
Change in Physical Properties?
FLUID: Change in properties --O.K
INITIAL GAS TEMPERATURE = 70 F
INITIAL GAS PRESSURE = 130 psig
GAS COMPRESSIBILITY COEFFICIENT, Z, = 1.000
GAS SPECIFIC HEAT RATIO, k, = 1.3
GAS VISCOSITY @ FLOW CONDITIONS = 0.018 cP
BASE TEMPERATURE = 60 F
BASE PRESSURE = 14.696 psig
BASE COMPRESSIBILITY FACTOR, Z, = 1.000
NOMINAL PIPE DIAMETER, INCHES = 1/2" Sch-40 CS
PIPE INTERNAL DIAMETER, INCHES = 0.664 Inches
FLANGE ORIFICE DIAMETER, do, INCHES , = 0.34 Inches
ORIFICE BETA = 0.5120
PLATE MATERIAL = SS
PLATE BASE THERMAL EXPANSION = 0.0000097 1/F
PLATE THERMAL EXPANSION = 0.0000089 1/F
CHANGE IN GAS DENSITY OVER PLATE = -0.35%
CHANGE IN GAS TEMPERATURE = -1.8 F
DISCHARGE MACH NO., M=1 IS CRITICAL, = 0.096
This method is more general.
17 of 25Lemont, Illinois
document.xls/RO3
RESTRICTIVE ORIFICE ---- Method 3Crane TP 410, "Flow of Fluids Through Valves, Fittings, and Pipe," 23rd printing. tb/bore diameter = 0.67P2/P1 = 0.016667 Thin plate, no choked flow.
Standard Conditions: P, psia = 14.696 T, F = 60
Complete Property Sheet
Flange taps Tr = 1.43 from sheetQg: 86 SCFH Y = 0.72 Kirk-Cunningham Pr = 0.11
0.06 k = 1.2859.00
P1: 60 psig 0.607 ASME, Crane 410 Sat. Curve Test: 0.749 Test:P2: 1 psi 0.607 Cunningham Hot Gas Test: 0.433 OKMw: 24 0.607 manual allowed Pr/Tr = 0.078
0.01 manual allowed B1 = 0.100T: 120 deg. F B0 = -0.156Plate Rate 300 300, 600# ANSI Abbott Equations are acceptabletp = 1.50 mm From Fluor table Z = 0.99Z: 0.99 manual allowedD1, nom: 0.75 in. Sch.: 160
0.01151 manual allowed 4,874
56 psig
Wd = 5.44 PPH Wcalc = 5.47 PPH Problem solved with goal seekMatch Qg: 4.93 PPH
Pcf = 40.98 psig Choked Flow - for thick plate Do = 0.088 in. Beta = 0.144
Thin plate orifice All flow conditions
ASME calculation not practical --- P2/P1 too low ---Kirk-Cunningham method.
W: lbs./hr; Y: dimensionless; C: 1/ft; do: inches; DP: psi; r: #mass/cf
@ 14.696 psia & 1 atm.r, #/cf = Using initial properties @
P1, T1DP =
C, ft-1 =
Saturated Arear, #/cf =
mg, cP= Re1 =
DPp =
P1:W =
DP r
Equation 2-24, Crane TP 410, adapted on 3.24 of text.
1891 Y C d 2 0
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<0.63P1. Cunningham showed that choked flow (critical, i.e., M =1 @ throat) does not occur for thin orifice plates.
This method is more general.
18 of 25Lemont, Illinois
document.xls/R04
RESTRICTIVE ORIFICE ---- Method 4Crane TP 410, "Flow of Fluids Through Valves, Fittings, and Pipe," 23rd printing. tb/bore diameter = 1.82P2/P1 = 0.033333 Thin plate, no choked flow.
Complete Property Sheet
Estimated Compressibility Factor (Z) for Base and Inlet Conditions
Standard Conditions: P, psia = 14.696 T, F = 60 For (b): 1.46 Sat. Curve Test: 0.714 Test:
OK
0.04 Hot Gas Test: 0.400 OK
Flange taps 1 Cunningham Pr/Tr = 0.030 Saturated Area
Qg: 250 SCFH 0.66 Cunningham recommended Zb = 0.980 B1 = 0.1040.05 k = 1.28 manual 0.980 B0 = -0.14887.0 Abbott Equations are acceptable
P1: 90 psig 0.595 ASME, Crane 410 Zf = 0.980P2: 3 psi 0.607 Cunningham
Mw: 17 manual allowed For (1): 1.57 Sat. Curve Test= 0.772 Test:
0.02 manual allowed 0.16 Hot Gas Test= 0.455 OK
T: 100 deg. F Pr/Tr = 0.100Saturated Area
Plate Rate 300 300, 600# ANSI B1 = 0.113tp = 2.50 mm From Fluor table B0 = -0.122Z1: 0.991 manual allowed Abbott Equations are acceptableD1, nom: 2.00 in. Sch.: 80 Zf = 0.991
0.01151 manual allowed 3,233
86 psig
Wd = 11.43 PPH Wcalc = 11.31 PPH Problem solved with goal seekMatch Qg: PPH Qcalc = 247 SCFH
Pcf = 57.43 psig Choked Flow - for thick plate Do = 0.054 in. Beta = 0.028
Thin plate orifice All flow conditions
ASME calculation not practical --- P2/P1 too low ---Kirk-Cunningham method.
W: lbs./hr; Y: dimensionless; C: 1/ft; do: inches; DP: psi; r: #mass/cf
Trb =
Choose Cunningham (1),Miller (2), or Fluor (3) for Y1: Prb =
Y1 =rb, #/cf =DP =
C, ft-1 =
Tr1 =
r1, #/cf = Pr1 =
mg, cP= Re1 =
DPp =
P1: W = DhPf1
Adapted 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<0.63P1. Cunningham showed that choked flow (critical, i.e., M =1 @ throat) does not occur for thin orifice plates.
P2: 338.178 rb K d2 Y1 FPb FTb FTf1 FPvGr FGr
VISC
D. Willard 04/08/2023 Plant I RELSIZE.XLS(VISC)
G A S M I X T U R E V I S C O S I T Y
This sheet talks with the Properties Sheet.
Manual input values are in "Green."
Temperature 38 C 100 F
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 Pressures
Component Man M N
Hydrogen 0.00 Yes 0.009189 - 2.02 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 1
Methane 0.94 Yes 0.011672 0.0117 16.04 0.000 1.000 1.473 1.899 0.000 0.000 0.000 0.000 0.000 0.000 1.033 0.011 2
Ethane 0.05 Yes 0.009882 0.0099 30.07 0.000 0.665 1.000 1.300 0.000 0.000 0.000 0.000 0.000 0.000 0.689 0.001 3
Propane 0.01 Yes 0.008547 0.0085 44.10 0.506 0.506 0.766 1.000 0.000 0.000 0.000 0.000 0.000 0.000 0.524 0.000 4
Propylene 0.00 Yes 0.009039 - 42.08 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 5
Gas 6 1.00 Yes 0.000000 - 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 6
Gas 7 0.00 Yes 0.000000 - 0.00 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 7
Gas 8 0.00 Yes 0.000000 - 0.00 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 8
Gas 9 0.00 Yes 0.000000 - 0.00 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 9
Gas 10 0.00 Yes 0.000000 - 0.00 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 0.000 10
Total 2.00 0.0115
Gas a b c Mwt. a b c d e fAlCl2 97.89 9.04015 8.68E-03 ### 1.72E-09 ### 0AlCl3 -0.0006 1.365E-05 -7.11E-10 133.34 ### 2.40E-02 ### 4.81E-08 ### 5.57E-15Carbon Dioxide 0.00187 2.39E-05 -1.27E-09 44.009 6.21415 5.12E-03 ### 0 0 0Carbon Monoxide 0.00628 2.16E-05 -1.70E-09 28.01 6.42043 8.88E-04 ### 0 0 0Chlorine 0.00215 2.014E-05 2.33E-09 70.9 6.02127 6.56E-03 ### 3.01E-09 0.00000 0Hydrogen Sulfide ### 2.40E-05 -3.40E-10 33.068 6.66150 2.85E-03 ### 0 0 0Nitrogen 0.00344 4.28E-05 7.15E-09 28.013 6.89500 7.62E-04 ### 0 0 0Oxygen 0.00624 2.59E-05 -2.71E-09 31.998 6.44284 1.25E-03 ### 0 0 0HCl 0.00177 2.26E-05 3.95E-09 36.461 6.51457 ### 0 0 0 0Sulfur Dioxide ### 2.12E-05 -1.44E-09 64.058 7.11595 5.93E-03 1.08E-06 0 0 0TiCl4 0.0071 0.000073 1.157E-08 189.69 ### 2.92E-02 ### 1.32E-08 ### 2.62E-16Water -0.00096 1.97E-05 -3.84E-09 18.015 7.08976 1.55E-03 0 0 0 0
Information Alligned for MBAL & VISC for auto entries.MAT-MATRIX Mwt a b c d e f
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Enter values in "Yellow." Calculated values in "Light Green".
y i Manual h i h i F i1 F i2 F i3 F i4 F i5 F i6 F i7 F i8 F i9 F i10 Sum F ij Sum y ih i
mm =
m = a + b(T) + c(T)2 +d(T)3 Cp = a + b(T) + c(T)2 + d(T)3 + e(T)4 + f(T)5
Cp = a + b(T) + c(T)2 + d(T)3 + e(T)4 + f(T)5
a(m) b (m) c (m)
0 500 1,000 1,500 2,000 2,500 3,000 3,5000.000
0.010
0.020
0.030
0.040
0.050
0.060
0.070
0.080
0.090
0.100
0.110
0.120
. . . .- b v s Q for sq edged orifice plates
k = 1.2; M = 30
k=1.3; M = 17
k = 1.4; M = 2
Q, SCFH (60 F, 14.7 psia)
, (
./
)
bbore
dia
pip
eID
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)
Q, SCFH M1.2 50 0.0144 0.0144 301.2 250 0.0322 0.03221.2 500 0.0455 0.04551.2 1,000 0.0643 0.06431.2 1,500 0.0788 0.07881.2 2,000 0.0910 0.09101.2 3,000 0.1114 0.11141.2 4,000 0.1298 0.12981.2 5,000 0.1451 0.14511.3 50 0.0126 0.0126 171.3 250 0.0281 0.0281 0.02791.3 500 0.0397 0.03971.3 1,000 0.0561 0.05611.3 1,500 0.0688 0.06881.3 2,000 0.0794 0.07941.3 3,000 0.0973 0.09731.3 4,000 0.1317 0.13171.3 5,000 0.1472 0.14721.4 50 0.0072 0.0072 21.4 250 0.0163 0.01631.4 500 0.0230 0.02301.4 1,000 0.0325 0.03251.4 1,500 0.0398 0.03981.4 2,000 0.0460 0.04601.4 3,000 0.0563 0.05631.4 4,000 0.0660 0.06601.4 5,000 0.0737 0.0737
T1 = 100oF, DP = 87 psig, P1 = 90 psig, Using Cunningham
ko b, 2" b, 1"