No.
DATE
REVIS IO ION SHEET NO.
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSU ISSUED ED::
CHEC CHECK: K:
INSTRUMENT SPECIFICATION Flange-type Restrictive Orifices ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS SHEETS
Installation notes: 1. Orifice dia. dia. As specified to suit required conditions. conditions. 2. Gaskets furnished by vendor.
MATERIAL: Monel M E T I
REV. QTY.
1
2
1
TAG. NO NO.
20FO-057
PIPE SIZE (IN.)
#
###
SCH.
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG)
DP (PSI)
80
0.084
250
60
57
M S W G
a
17.00
TEMP. (F)
FLANGE RATING
100
300
SERVICE
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.
1 of 24
204569257.xls.ms_office/Curr 204569257.xls.ms_office/Current ent Flange Spec Sheet_Monel
No.
DATE
REVISI ON ON SHEET NO .
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSU ISSUED ED::
INSTRUMENT SPECIFICATION
CHEC CHECK: K:
Union Restrictive Orifices
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
MATERIAL: 316SS M E T I
REV. QTY.
1
1
1
TAG. NO NO.
Installation notes: 1. Unless otherwise specified, the only markings on on the orifice tab tab shall be the orfice 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 the insulated material material covering the union shall be be applied in such a manner that the markings on the tab will be fully exposed. 3. No asbestos-bearing asbestos-bearing material is acceptable; vendor vendor to provide provide TFE gaskets.
PIPE SIZE (IN.)
20 20FO-184
1-1/
SCH.
ORIFICE (IN.)
80
0.285
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG)
DP (PSI)
60
57
M S W G
a
0.586
TEMP. (F)
FLANGE RATING
100
3000
SERVICE
Acid pump vent header purge.
2 3 4 5 6 7 8 9 10
1. Item 1 is made of monel.
2 of 24
204569257.xls.ms_office/Current Union Spec Sheet
No.
DATE
REVISION S HEET NO.
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSUED:
INSTRUMENT SPECIFICATION
CHECK:
Flange-type Restrictive Orifices
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
Installation notes: 1. Orifice dia. As specified to suit required conditions. 2. Gaskets furnished by vendor.
MATERIAL: 316SS M E T I
REV. QTY.
1
1
1
TAG. NO.
20FO-175
PIPE SIZE (IN.)
#
###
SCH.
ORIFICE (IN.)
80
0.135
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG) 60
DP (PSI)
M S W G
55
a
17.00
TEMP. (F)
FLANGE RATING
100
150
SERVICE
Pilot gas to 20F-527.
2 3 4 5 6 7 8 9 10
3 of 24
204569257.xls.ms_office/Current Flange Spec Sh_SS
No.
DATE
REVISION S HEET NO.
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSUED:
INSTRUMENT SPECIFICATION
CHECK:
Union Restrictive Orifices
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
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 full y exposed. 3. No asbestos-bearing material is acceptable; vendor to provide TFE gaskets.
MATERIAL: 316SS M E T I
REV. QTY.
1
1
1
TAG. NO.
PIPE SIZE (IN.)
#
###
SCH.
80
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG)
DP (PSI)
M S W G
a
TEMP. (F)
FLANGE RATING
SERVICE
100
2 3 4 5 6 7 8 9 10
4 of 24
204569257.xls.ms_office/New Union Spec Sheet
Yellow is an input cell: P1: 60 psig
Green is a calculation: W= 11.12 PPH
Underline is value actually used: Green in grey is a look-up value: tp = 2.50 0.603 0.607 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: [1st Cell] 4.87
Target (To) cell for goal seek: [2nd Cell] 4.93
Changing cell for goal [3rd Cell] 0.084
seek:
No.
DATE
REVISION S HEET NO.
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSUED:
INSTRUMENT SPECIFICATION
CHECK:
Flange-type Restrictive Orifices
ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
Installation notes: 1. Orifice dia. As specified to suit required conditions. 2. Gaskets furnished by vendor.
MATERIAL: 316SS M E T I
REV. QTY.
1
1
1
TAG. NO.
PIPE SIZE (IN.)
#
###
SCH.
80
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG)
DP (PSI)
M S W G
a
TEMP. (F)
FLANGE RATING
SERVICE
100
2 3 4 5 6 7 8 9 10
7 of 24
204569257.xls.ms_office/New Flange Spec Sheet_SS
No.
DATE
REVISION S HEET NO.
REV.
ISSUE DATE: Citgo Petroleum Corporation 135th Street & New Avenue Lemont, IL 60439
MANUFACTURER: P.O. No.: ISSUED:
CHECK:
INSTRUMENT SPECIFICATION Flange-type Restrictive Orifices ALL ITEMS SHALL COMPLY WITH GENERAL SPECIFICATION SHEETS
Installation notes: 1. Orifice dia. As specified to suit required conditions. 2. Gaskets furnished by vendor.
MATERIAL: Monel M E T I
REV. QTY.
1
1
1
TAG. NO.
PIPE SIZE (IN.)
#
###
SCH.
80
ORIFICE (IN.)
FLOW QUANTITY (SCFH)
UPSTREAM PRESSURE (PSIG)
DP (PSI)
M S W G
a
TEMP. (F)
FLANGE RATING
SERVICE
100
2 3 4 5 6 7 8 9 10
8 of 24
204569257.xls.ms_office/New Flange Spec Sheet_Monel
Caution: this sheet calculates properties based on yellow-highlighted cells. The viscosities pressure and temperature, however, the NIST values for pure components will change so if NIST. Gas Properties Vc, cm3/molProperties using coresponding states y Tc, K Pc, atm 1 Zc Hydrogen 0 33.20 12.80 65.00 0.31 -0.22 Methane 0.94 190.60 45.40 99.00 0.29 0.01 Ethane 0.05 305.40 48.17 148.00 0.29 0.10 Propane 0.01 369.80 41.95 203.00 0.28 0.15 Propylene 0 365.00 45.60 181.00 0.28 0.15 Butane Average, Mixture: 1.0000 198.13 45.65 102.49 0.29 0.01 k=
R, atm-cm^3/(K-gmole): Temperature, F: Pressure, psig.: Viscosity, cP:
Methane Ethane Propane Propylene Butane
8.21E+01 100 311 90 Use initial (1) properties. From VISC Sheet - manual entry-- use NIS 0.01151 individual m , then use Wilke's method in sp calculate mixture m . m, cP @ 78 psig m, cP @ 90 psig 100 120 100 120 0.011661 0.012008 0.011659 0.012006 0.00986 0.010179 0.009882 0.010201 0.00853 0.008836 0.008547 0.008853 0.009013 0.009347 0.009039 0.009372 0.009254 0.012779
ill change and are a function of T or P change update with Cp , cal/gmolK 6.91 8.66 12.98 18.30 15.78
8.98 1.28
website for eadsheet to
M 2.02 16.04 30.07 44.10 42.08
17.02
, cP 0.00919 0.01167 0.00988 0.00855 0.00904
Thin plate orifice Low-Moderate P
RESTRICTIVE ORIFICE ---- Method 1 Rough method provided originally in an article in Chemical Engineering magazine P2/P1 = 0.05
tb/bore diameter =
0.93
T h i n p l a t e, n o c h o k e d f l o w . C a l c u l at i o n n o t a p p l i c a b l e: r e f e r t o K i r k - Cu n n i n g h a m m e t h o d .
P1: D =
Qg/SQRT( DP(P1 +P2)/(2SgT1)
7 X 8
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.
1/5 X (tp/0.125)
5440
D, inches; Qg, gas flow in SCFH (60 F, 1 atm); DP, P1, P2, psia; Sg = Mg/Mair
Line Size
tp,mm
0.5
1.5
0.75 1 1.5 2 3 4 6 8 10 12 14 16 18 20 24
1.5 1.5 2 2.5 3 3 3 6 6 6 9 9 12 12 16
T1, R; tp, plate thickness. Qg: DP = P1: P2: Mw: Sg = T: Plate Rate tp = Z: D1, nom:
250 57.00 60 3 17 0.59 100 300 2.50 1.00 2.00
SCFH @ 60 F, 1 atm
Complete Property Sheet Tr = 2.51 from sheet Pr = 0.11
psig psi
Using initial properties @ P1, T1
manual allowed deg. F k = 1.28 300, 600# ANSI mm From Fluor table 0.98 Calculated using virial equations in. Sch.: 80
Sat. Curve Test: Hot Gas Test: B1 = B0 =
0.749 0.433 0.135 -0.014
Test: OK Saturated Area Pr/Tr = 0.044
Abbott Equations are acceptable
Pcf = 40.98
psig
Choked Flow - for thick plate
Using table from Fluor specification: "Flange Type Restrictive Orifice"
Z = 1.00
D2 =
11 of 24
0.106 in.
Lemont, Illinois
Beta =
0.055
204569257.xls.ms_office/RO1
Thick plate orifice or flow nozzle, Choked Flow
RESTRICTIVE ORIFICE ---- Method 2
tb/db = 7.41 Thick plate method applies: choked flow. Min. Pressure is: 40.98 Choked Flow: eq. 4-40, pg. 100, Daniel Crowl, Joseph Louvar, "Chemical Process Safety Fundamentals with Applications, Prentice-Hall, 1990. P1:
4-40 Crowl & Louvar assume a thick orifice plate, or flow nozzle, not a thin plate.
W
A = Co P1
k gc M RT1
X
psig
2 k+1
(k+1)/(k-1)
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).
A: throat cross-sectional area, sq. ft; W : #/s; Co = 0.72; P1: inlet pressure, psf; gc = 32.174 T1: inlet temperature, F; R = 1545.3 ft-#f/#mole-R. This sheet is most useful in estimating flow from nozzles and holes in vessels or Qg: W= = D1: P1:
250 11.22 0.04 1.939 60
SCFH @ 60 F, 1 atm PPH lbs./cf in. psig
Mw:
17.02
Property Sheet
St. T = Co:
60 14.696 0.72
k = 1.28 exp. = 8.03 Pcf = 40.98
T:
100
deg. F
F psia Crowl/Louvar recommends 1.0 for Co with sharp-edged orifices with Re 1 >30,000; seldom does this occur. Property Sheet
psig
Choked Flow
Thick plate orifice or flow nozzle, Choked Flow
RESTRICTIVE ORIFICE ---- Method 2
tb/db = 7.41 Thick plate method applies: choked flow. Min. Pressure is: 40.98 Choked Flow: eq. 4-40, pg. 100, Daniel Crowl, Joseph Louvar, "Chemical Process Safety Fundamentals with Applications, Prentice-Hall, 1990. P1:
4-40 Crowl & Louvar assume a thick orifice plate, or flow nozzle, not a thin plate.
W
A = Co P1
k gc M RT1
X
psig
2 k+1
(k+1)/(k-1)
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).
A: throat cross-sectional area, sq. ft; W : #/s; Co = 0.72; P1: inlet pressure, psf; gc = 32.174 T1: inlet temperature, F; R = 1545.3 ft-#f/#mole-R. This sheet is most useful in estimating flow from nozzles and holes in vessels or Qg: W= = D1: P1:
250 11.22 0.04 1.939 60
SCFH @ 60 F, 1 atm PPH lbs./cf in. psig
Mw:
17.02
Property Sheet
St. T = Co:
60 14.696 0.72
k = 1.28 exp. = 8.03 Pcf = 40.98
T:
100
deg. F
A =
0.004
sq. in.
D= Beta = tp =
12 of 24
0.067 0.0348 0.50
in. in.
F psia Crowl/Louvar recommends 1.0 for Co with sharp-edged orifices with Re 1 >30,000; seldom does this occur. Property Sheet
psig
Complete Property Sheet Tr = 2.51 Pr = 0.11 Sat. Curve Test: Hot Gas Test: Test: B1 = B0 = Pr/Tr =
Choked Flow
Using initial properties @ P1, T1 0.749 0.433 OK 0.135 -0.014 0.044
Lemont, Illinois
Z = 1.00
Below: use charts Saturated Area Abbott Equations are acceptable
204569257.xls.ms_office/RO2
Z = 1.00
13 of 24
Lemont, Illinois
1/16/2014
204569257.xls.ms_office/RO2
Calculation for North American Mfg. Co. Combustion Air FE
ORIFICE DATA SHEET Type of Orifice Plate:
Standard
Drain Hole (for Condensate):
None
MAXIMUM (URV-Ranged) DIFFERENTIAL PRESSURE MAXIMUM FLOW RATE REQUIRED
=
40 IW C
Pipe Diameter?
10,000 PPH
=
131,510 SCFH DP (Required ) AT REQUIRED MAX. FLOW RATE = CALCULATED MAXIMUM FLOW RATE (At URV) =
29.78 IWC 11,589 PPH 152,400 SCFH
PERMANENT PRESSURE LOSS AT MAX. RATE (At URV) =
Y-Equation? hw-O.K. Turndown O. Y-O.K.
1.35 PSIG 37.53 IW C
ORIFICE INLET MAX. CALC. REYNOLDS NUMBER =
1,050,626 Orifice Re?
NOMINAL DIFFERENTIA L PRESSURE NOMINAL FLOW RATE
=
7.45 IWC 5,000 PPH
=
65,750 SCFH MINIMUM DIFFERENTIAL PRESSURE
=
0.30 IWC
Re--tubulent--O.K. Safe Min. Rate? Min.---O.K.
0.895
1/16/2014
Calculation for North American Mfg. Co. Combustion Air FE
ORIFICE DATA SHEET Type of Orifice Plate:
Standard
Drain Hole (for Condensate):
None
MAXIMUM (URV-Ranged) DIFFERENTIAL PRESSURE MAXIMUM FLOW RATE REQUIRED
40 IW C
=
Pipe Diameter?
10,000 PPH
=
131,510 SCFH 29.78 IWC
DP (Required ) AT REQUIRED MAX. FLOW RATE =
11,589 PPH
CALCULATED MAXIMUM FLOW RATE (At URV) =
152,400 SCFH
Y-Equation? hw-O.K. Turndown O.
0.895
Y-O.K.
1.35 PSIG
PERMANENT PRESSURE LOSS AT MAX. RATE (At URV) =
37.53 IW C 1,050,626
ORIFICE INLET MAX. CALC. REYNOLDS NUMBER =
Orifice Re? NOMINAL DIFFERENTIA L PRESSURE NOMINAL FLOW RATE
7.45 IWC
=
5,000 PPH
=
65,750 SCFH MINIMUM DIFFERENTIAL PRESSURE MINIMUM (Practical) FLOW RATE
Re--tubulent--O.K. Safe Min. Rate? Min.---O.K.
0.30 IWC
=
1,000 PPH
=
13,150 SCFH MINIMUM ORIFICE INLET REYNOLDS NUMBER
Mach No. OK? Gas Orifice velocity is O.K.
10,000
=
Change in Physical Properties? Change in properties --O.K
FLUID: INITIAL GAS TEMPERATURE
70 F
=
INITIAL GAS PRESSURE
30 psig
=
1.000
GAS COMPRESSIBILITY COEFFICIENT, Z, = GAS SPECIFIC HEAT RATIO, k,
=
1.39817842
GAS VISCOSITY @ FLOW CONDITIONS
=
0.01634555 cP
BASE TEMPERATURE
=
BASE PRESSURE
=
BASE COMPRESSIBILITY FACTOR, Z,
=
60 F 14.696 psig 1.000 24" CS Pipe
NOMINAL PIPE DIAMETER, INCHES
=
PIPE INTERNAL DIAMETER, INCHES
=
23.5 Inches
FLANGE ORIFICE DIAMETER, do, INCHES , =
4.262225274 Inches
ORIFICE BETA
=
PLATE MATERIAL
=
0.1814 SS
PLATE BASE THERMAL EXPANSION
=
0.0000097 1/F
PLATE THERMAL EXPANSION
=
0.0000089 1/F
CHANGE IN GAS DENSITY OVER PLATE
=
-0.94%
=
-4.9
DISCHARGE MACH NO., M=1 IS CRITICAL, =
0.126
CHANGE IN GAS TEMPERATURE
F
F o r M a x i m u m F l o w C a l c u l a t io n C' (PPH)
= 274.091
K = 0.5972
Ftb
= 1.003
Fm
= 1.000
C' (SCFH) = 3604.474 FG = 0.99857
Fa
= 1.000
FTf = 0.9896
Y1 = 0.9905 Fpv = 1.0000 FPb = 1.0000 Fl = 0.9998
Flowing conditions were used to calculate the discharge rate of the orifice.
D. Willard
International Steel Services, Inc.
204569257.xls.ms_office
This method is more general.
Thin plate orifice All flow conditions
RESTRICTIVE ORIFICE ---- Method 3 Crane TP 410, "Flow of Fluids Through Valves, Fittings, and Pipe," 23rd printing. P2/P1 = 0.016667
tb/bore diameter =
0.67
T h i n p l a t e, n o c h o k e d f l o w .
ASME calculation not p ractical --- P2/P1 too low ---Kirk-Cunn ingh am method.
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 P 2<0.63P1. Cunningham showed that choked flow (critical, i.e., M =1 @ throat) does not occur for thin orifice plates.
P1: 2 DP r W = 1891 Y C d 0 Equation 2-24, Crane TP 410,
W: lbs./hr; Y: dimensionless; C: 1/ft; do: inches; DP: psi; r: #mass/cf Standard Conditions:
P, psia =
14.696
T, F =
60 Complete Property Sheet
Qg: 86 r, #/cf = 0.06 DP = 59.00 P1: 60 P2: 1 Mw: 24 r, #/cf = 0.01 T: 120 Plate Rate 300 tp = 1.50 Z: D1, nom: 0.75 mg, cP= 0.01151 DPp =
56
SCFH
Y= k=
@ 14.696 psia & 1 atm.
psig psi
Flange taps 0.72 Kirk-Cunningham 1.28 0.607 0.607 0.607
-1
C, ft =
manual allowed deg. F 300, 600# ANSI mm From Fluor table 0.99 manual allowed in.
Sch.: Re1 =
manual allowed
Tr = 1.43 Pr = 0.11
from sheet
Using initial properties @ P1, T1
ASME, Crane 410 Cunningham manual allowed
Sat. Curve Test: 0.749 Test: Hot Gas Test: 0.433 OK Pr/Tr = 0.078 Saturated B1 = 0.100 Area B0 = -0.156 Abbott Equations are acceptable Z = 0.99
160 4,874
psig
Wd = 5.44 Match Qg: 4.93 Pcf = 40.98
PPH PPH psig
Wcalc =
5.47
PPH
Choked Flow - for thick plate
Problem solved with goal seek
Do =
0.088
15 of 24
in.
Beta =
Lemont, Illinois
0.144
204569257.xls.ms_office/RO3
This method is more general.
Thin plate ori All flow conditi
RESTRICTIVE ORIFICE ---- Method 4 Crane TP 410, "Flow of Fluids Through Valves, Fittings, and Pipe," 23rd printing. P2/P1 = 0.033333
tb/bore diameter = T h in p l at e, n o c h o k e A SM E ca lc u la ti o n n ot p r ac ti c al -- - P 2/P 1 t o o lo w - -- Ki r k- Cu n n in method.
P1:
P2:
W =
338.178 rb K d2 Y1 FPb FTb FTf1 FPvGr FGr
Flow through a thin plate is never choked flow. For this to apply, the ratio of tb/bore diameter must be < 6 pg. 13.22, Richard Miller's "Flow Measurement Engineering Handbook," 3rd ed., McGraw Hill, 1996. Pag refers to the work of Cunningham (1951) and Ward-Smith (1979). In 2005, Kirk explored the li mits of Cun work. He found that ASME formulas worked fine with adjustment of Y; C could be defined using ASME a methods. Kirk-Cunningham applies when P2<0.63P1. Cunningham showed that choked flow (crit ical, i.e., M =1 @ t not occur for thin orifice plates.
Dh Pf1
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.)
Complete Property Sheet W: lbs./hr; Y: dimensionless; C: 1/ft; do: inches; DP: psi; r: #mass/cf Standard Conditions:
P, psia =
14.696
T, F =
60
For (b):
Prb = 0.04
Choose Cunningham ( 1 ),Miller ( 2 ), or Fluor ( 3 ) for
Qg:
250
rb, #/cf = DP =
0.05 87.0 90 3 17
P1: P2: Mw: r1, #/cf = T:
SCFH
k= psig psi
0.02 100
Flange taps Y1 = 0.66
-1
C, ft =
manual allowed deg F
1.28 0.595 0.607
1
Estimated Compressibility Factor (Z) for Base and Inlet Conditions Trb = 1.46 Sat. Curve Test: 0.714 Test:
Cunningham recommended
OK
manual ASME, Crane 410 Cunningham manual allowed
Hot Gas Test: 0.400 Pr/Tr = 0.030
Cunningham
Zb =
0.980 0.980
For (1):
OK Saturated
B1 = 0.104 B0 = -0.148 Abbott Equations are acceptable Zf = 0.980
Tr1 = 1.57
Sat. Curve Test= 0.772
Pr1 = 0.16
Hot Gas Test= 0.455 Pr/Tr = 0 100
Test: OK Saturated
This method is more general.
Thin plate ori All flow conditi
RESTRICTIVE ORIFICE ---- Method 4 Crane TP 410, "Flow of Fluids Through Valves, Fittings, and Pipe," 23rd printing. P2/P1 = 0.033333
tb/bore diameter = T h in p l at e, n o c h o k e A SM E ca lc u la ti o n n ot p r ac ti c al -- - P 2/P 1 t o o lo w - -- Ki r k- Cu n n in method.
P1:
P2:
W =
338.178 rb K d2 Y1 FPb FTb FTf1 FPvGr FGr
Flow through a thin plate is never choked flow. For this to apply, the ratio of tb/bore diameter must be < 6 pg. 13.22, Richard Miller's "Flow Measurement Engineering Handbook," 3rd ed., McGraw Hill, 1996. Pag refers to the work of Cunningham (1951) and Ward-Smith (1979). In 2005, Kirk explored the li mits of Cun work. He found that ASME formulas worked fine with adjustment of Y; C could be defined using ASME a methods. Kirk-Cunningham applies when P2<0.63P1. Cunningham showed that choked flow (crit ical, i.e., M =1 @ t not occur for thin orifice plates.
Dh Pf1
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.)
Complete Property Sheet W: lbs./hr; Y: dimensionless; C: 1/ft; do: inches; DP: psi; r: #mass/cf Standard Conditions:
P, psia =
14.696
T, F =
60
For (b):
Prb = 0.04
Choose Cunningham ( 1 ),Miller ( 2 ), or Fluor ( 3 ) for
Qg:
250
rb, #/cf = DP =
0.05 87.0 90 3 17
P1: P2: Mw: r1, #/cf =
Flange taps Y1 = 0.66
SCFH
k= psig psi
-1
C, ft =
0.02
deg. F 300, 600# ANSI mm From Fluor table manual allowed in.
DPp =
psig
11.43 Wd = Match Qg: Pcf = 57.43
Cunningham recommended
1.28 0.595 0.607
manual allowed
PPH PPH psig
Wcalc = Qcalc =
11.31 247
Choked Flow - for thick plate
Sch.: Re1 =
PPH SCFH Do =
16 of 24
Hot Gas Test: 0.400 Pr/Tr = 0.030
Cunningham
OK
Zb =
manual ASME, Crane 410 Cunningham manual allowed
0.980 0.980
For (1):
manual allowed
T: 100 Plate Rate 300 tp = 2.50 Z1: 0.991 D1, nom: 2.00 mg, cP= 0.01151 86
1
Estimated Compressibility Factor (Z) for Base and Inlet Conditions Trb = 1.46 Sat. Curve Test: 0.714 Test: OK Saturated
B1 = 0.104 B0 = -0.148 Abbott Equations are acceptable Zf = 0.980
Tr1 = 1.57
Sat. Curve Test= 0.772
Pr1 = 0.16
Hot Gas Test= 0.455
Test: OK
Pr/Tr = 0.100 Saturated B1 = 0.113 B0 = -0.122 Abbott Equations are acceptable Zf = 0.991
80 3,233
Problem solved with goal seek 0.054
in.
Lemont, Illinois
Beta =
0.028
204569257.xls.ms_office/R04
This method is more general.
ice ons 1.82
flow. gham
. (Reference: e 13-22 ningham's nd other hroat) does
rea
This method is more general.
ice ons 1.82
flow.
gham
. (Reference: e 13-22 ningham's nd other hroat) does
rea
rea
17 of 24
Lemont, Illinois
204569257.xls.ms_office/R04
VISC
GAS
MIXTURE
VISCOSITY
This sheet talks with the Properties Sheet. Enter values in "Yellow." 38 Temperature
Manual input values are in "Green."
C
Calculated values in "Light Green".
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
yi
Hydrogen Methane
0.00 0.94
Ethane
0.05
Propane
0.01
Propylene
0.00
Gas 6
1.00
Gas 7
0.00
Gas 8 Gas 9 Gas 10
0.00 0.00 0.00
Total
2.00
Man Manual
Yes Yes Yes Yes Yes Yes Yes Yes Yes Yes
i
2
AlCl2 AlCl3 Carbon Dioxide Carbon Monoxide Chlorine Hydrogen Sulfide Nitrogen Oxygen HCl
0.0117 0.0099 0.0085 -
M
i1
i2
i3
i4
i5
i6
i7
i8
i9
i10
Sum
3
c
-0.0006 0.00187 0.00628 0.00215 ####### 0.00344 0.00624 0 00177
1.365E-05 2.39E-05 2.16E-05 2.014E-05 2.40E-05 4.28E-05 2.59E-05 2 26E 05
-7.11E-10 -1.27E-09 -1.70E-09 2.33E-09 -3.40E-10 7.15E-09 -2.71E-09 3 95E 09
i
N
0.000 1.000
0.000 1.473
0.000 1.899
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 1.033
0.000 0.011
1 2
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
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
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
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
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
0.00 0.00 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
0.000 0.000 0.000
0.000 0.000 0.000
0.000 0.000 0.000
0.000 0.000 0.000
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 9 10
2
b
Sum yi
0.000 0.000
3
4
5
Cp = a + b(T) + c(T) + d(T) + e(T) + f(T)
a
ij
2.02 16.04
mm =
m = a + b(T) + c(T) +d(T) Gas
i
0.009189 0.011672 0.009882 0.008547 0.009039 0.000000 0.000000 0.000000 0.000000 0.000000
Mwt. a b c d e f 97.89 9.04015 8.68E-03 ####### 1.72E-09 ####### 0 133.34 12.25740 2.40E-02 ####### 4.81E-08 ####### 5.57E-15 44.009 6.21415 5.12E-03 ####### 0 0 0 28.01 6.42043 8.88E-04 ####### 0 0 0 70.9 6.02127 6.56E-03 ####### 3.01E-09 0.00000 0 33.068 6.66150 2.85E-03 ####### 0 0 0 28.013 6.89500 7.62E-04 ####### 0 0 0 31.998 6.44284 1.25E-03 ####### 0 0 0 36 461 6 51457 ####### 0 0 0 0
0.0115
VISC
GAS
MIXTURE
VISCOSITY
This sheet talks with the Properties Sheet. Enter values in "Yellow." 38 Temperature
Manual input values are in "Green."
C
Calculated values in "Light Green".
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
yi
Hydrogen Methane
0.00 0.94
Ethane
0.05
Propane
0.01
Propylene
0.00
Gas 6
1.00
Gas 7
0.00
Gas 8 Gas 9 Gas 10
0.00 0.00 0.00
Total
2.00
Man Manual
Yes Yes Yes Yes Yes Yes Yes Yes Yes Yes
i
2
AlCl2 AlCl3 Carbon Dioxide Carbon Monoxide Chlorine Hydrogen Sulfide Nitrogen Oxygen HCl Sulfur Dioxide TiCl4 Water
0.0117 0.0099 0.0085 -
i1
i2
i3
i4
i5
i6
i7
i8
i9
i10
Sum
ij
Sum yi
i
N
2.02 16.04
0.000 0.000
0.000 1.000
0.000 1.473
0.000 1.899
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 0.000
0.000 1.033
0.000 0.011
1 2
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
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
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
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
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
0.00 0.00 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
0.000 0.000 0.000
0.000 0.000 0.000
0.000 0.000 0.000
0.000 0.000 0.000
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 9 10
3
2
3
4
0.0115
5
Cp = a + b(T) + c(T) + d(T) + e(T) + f(T)
a
b
c
-0.0006 0.00187 0.00628 0.00215 ####### 0.00344 0.00624 0.00177 ####### 0.0071 -0.001
1.365E-05 2.39E-05 2.16E-05 2.014E-05 2.40E-05 4.28E-05 2.59E-05 2.26E-05 2.12E-05 0.000073 1.97E-05
-7.11E-10 -1.27E-09 -1.70E-09 2.33E-09 -3.40E-10 7.15E-09 -2.71E-09 3.95E-09 -1.44E-09 1.16E-08 -3.84E-09
Information Alligned for MBAL & VISC for auto entries. a(m) b (m) c (m) MAT-MATRIX #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A
D. Willard 1/16/2014
M
mm =
m = a + b(T) + c(T) +d(T) Gas
i
0.009189 0.011672 0.009882 0.008547 0.009039 0.000000 0.000000 0.000000 0.000000 0.000000
Mwt. a b c d e f 97.89 9.04015 8.68E-03 ####### 1.72E-09 ####### 0 133.34 12.25740 2.40E-02 ####### 4.81E-08 ####### 5.57E-15 44.009 6.21415 5.12E-03 ####### 0 0 0 28.01 6.42043 8.88E-04 ####### 0 0 0 70.9 6.02127 6.56E-03 ####### 3.01E-09 0.00000 0 33.068 6.66150 2.85E-03 ####### 0 0 0 28.013 6.89500 7.62E-04 ####### 0 0 0 31.998 6.44284 1.25E-03 ####### 0 0 0 36.461 6.51457 ####### 0 0 0 0 64.058 7.11595 5.93E-03 1.08E-06 0 0 0 189.69 13.31361 2.92E-02 ####### 1.32E-08 ####### 2.62E-16 18.015 7.08976 1.55E-03 0 0 0 0 2
Mwt #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A
3
4
5
Cp = a + b(T) + c(T) + d(T) + e(T) + f(T) a b c d e #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A
Plant I
f #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A #N/A
RELSIZE.XLS(VISC)
.v.s. Q for sq.-edged orifice plates 0.120 0.110 0.100 0.090 0.080 ) D I e0.070 p i p / . a0.060 i d e r o 0.050 b ( ,
0.040 0.030
T1 = 100 oF, DP = 87 psig, P 1 = 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.
.v.s. Q for sq.-edged orifice plates 0.120 T1 = 100 oF, DP = 87 psig, P 1 = 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.
0.110 0.100 0.090 0.080 ) D I e0.070 p i p / . a0.060 i d e r o 0.050 b ( ,
0.040 0.030 k = 1.2; M = 30
0.020
k=1.3; M = 17
W = Q(PM/RT) = QM/408.67 PPH: pounds per hour Q = W(408.66/M)
0.010
k = 1.4; M = 2
0.000 0
500
1,000
1,500
2,000
2,500
3,000
Q, SCFH (60 F, 14.7 psia)
o
T1 = 100 F, DP = 87 psig, P1 = 90 psig, Using Cunningham o
k 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.3 1.3 1.3 1.3
Q, SCFH 50 250 500 1,000 1,500 2,000 3,000 4,000 5,000 50 250 500 1,000
2" 0.0144 0.0322 0.0455 0.0643 0.0788 0.0910 0.1114 0.1298 0.1451 0.0126 0.0281 0.0397 0.0561
" 0.0144 0.0322 0.0455 0.0643 0.0788 0.0910 0.1114 0.1298 0.1451 0.0126 0.0281 0.0397 0.0561
M 30
17 0.0279
3,500
o
T1 = 100 F, DP = 87 psig, P1 = 90 psig, Using Cunningham o
k 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.2 1.3 1.3 1.3 1.3 1.3 1.3 1.3 1.3 1.3 1.4 1.4 1.4 1.4 1.4 1.4 1.4 1.4 1.4
Q, SCFH 50 250 500 1,000 1,500 2,000 3,000 4,000 5,000 50 250 500 1,000 1,500 2,000 3,000 4,000 5,000 50 250 500 1,000 1,500 2,000 3,000 4,000 5,000
2" 0.0144 0.0322 0.0455 0.0643 0.0788 0.0910 0.1114 0.1298 0.1451 0.0126 0.0281 0.0397 0.0561 0.0688 0.0794 0.0973 0.1317 0.1472 0.0072 0.0163 0.0230 0.0325 0.0398 0.0460 0.0563 0.0660 0.0737
" 0.0144 0.0322 0.0455 0.0643 0.0788 0.0910 0.1114 0.1298 0.1451 0.0126 0.0281 0.0397 0.0561 0.0688 0.0794 0.0973 0.1317 0.1472 0.0072 0.0163 0.0230 0.0325 0.0398 0.0460 0.0563 0.0660 0.0737
M 30
17 0.0279
2
