© 2002, 2003 Foster Wheeler Energy Limited.

All rights reserved.

Version: 3.03 Feb-2020
Standard
Formatting
Reviewing
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LineSizeMenu
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 GENERAL INPUT.

CALCULATION No. ?
CUSTOMER : ?
LOCATION : ?
CONTRACT No. : ?
UNIT No. : ?
LINE No. : ?
DESCRIPTION : ?

LIQUID LINE SIZING CALCULATION. VAPOUR LINE SIZING

FLUID : Water Molecular Weight:

FLOWRATE : 129306 kg/h PRESSURE barg
SPECIFIC GRAVIT 1.01 (at flowing conditions) TEMP. degC
VISCOSITY : 1.01 cP cP = cSt X SG COMPRESSIBILITY
PIPE ROUGHNESS 0.046 mm
VOLUME FLOW 128.03 m3/h Calculated Dens
563.74 USGal/min

LINE SIZE : in. nom. 6 8 10

PIPE SCHEDULE : STD STD STD
Calculated PIPE IDin. 6.065 7.981 10.02 0
USER PIPE ID : in. 0 0 0
VELOCITY : m/s 1.91 1.10 0.70
REYNOLDS NO : 2.94E+05 2.23E+05 1.78E+05
FLOW REGIME : TURBUL TURBUL TURBUL FLOW AREA :
FRICTION FACTOR : 0.017 0.017 0.017 REL ROUGH :
PRESSURE DROP bar/100m 0.203 0.051 0.017
psi/100ft 0.896 0.228 0.074
Friction factors: Calcu
kg/cm2/100m 0.207 0.053 0.017

K METHOD CALCULATION.
LINE SIZE : in. nom. 6 8 10
No No x K No x K No x K K
90 DEG BEND : 0 0.0 0.0 0.0
90 DEG LR BEND : 0 0.0 0.0 0.0
45 DEG BEND : 0 0.0 0.0 0.0
GATE VALVE : 0 0.0 0.0 0.0
GLOBE VALVE : 0 0.0 0.0 0.0
BUTTERFLY VALVE: 0 0.0 0.0 0.0
CHECK VALVE: 0 0.0 0.0 0.0
THRU TEE : 0 0.0 0.0 0.0
 BRANCH TEE : 0 0.0 0.0 0.0

REDUCERS : 0.0 0 0.0

K 0 0 0
K x No. 0 0.0 0.0 0.0

EXPANDERS : 0.0 0.0 0.0

K 0 0 0
K x No 0 0.0 0.0 0.0

PIPE ENTRY : 0 0.0 0.0 0.0 0.5

PIPE EXIT : 0 0.0 0.0 0.0 1
OTHERS : 0 0.0 0.0 0.0 0
OTHERS : 0 0.0 0.0 0.0 0
TOT K FITTINGS : 0.0 0.0 0.0
STRAIGHT PIPE m : 55000 55000 55000 55000
STRAIGHT PIPE K : 6069.015 4620.826 3729.418
TOTAL K : 6069.01511 4620.826 3729.418 OPTION NOT USED
DEFAULT FITTINGS FACTOR : 1.4 1.6 1.6
USER FITTINGS FACTOR : ? ? ?
TOTAL Le : m 77000.0 88000.0 88000.0 FITTINGS FACTOR CALC.
USER TOTAL Le : #VALUE! #VALUE! #VALUE!
UPSTREAM PRESSURE ? #VALUE! #VALUE! #VALUE! #VALUE!
PRESSURE DROPbar 111.404 28.287 9.189
(Based on K Value psi 1615.797 410.282 133.279
kg/cm2 113.598 28.845 9.370

PRESSURE DROPbar #VALUE! #VALUE! #VALUE!

(USER FITTINGFACTO psi #VALUE! #VALUE! #VALUE!
kg/cm2 #VALUE! #VALUE! #VALUE!

SUMMARY OF RESULTS
------------------

NE SIZE SELECTED: in. nom. 8

Plus 10%
PRESSURE DROP : bar/100m Err:520 2
psi/100ft Err:520
kg/cm2/100m Err:520
1
PRESSURE DROP : bar Err:520 2
psi Err:520 3
kg/cm2 Err:520

TURBUL
PIPELINE SURGE PRESSURE CALCULATION
-----------------------------------
DENSITY : 1010 kg/m3
BULK MODULUS, 2413000000 N/m2 349974 psi
YOUNGS MODULU2.0685E+11 N/m2 3.000E+07 psi
MAX. PRESSURE 38 barg (eg. Pump shut-in)

LINE SIZE : in. nom. 6 8 10

--- --- ---
PIPE LENGTH : m 55000 55000 55000
PIPE THICKNESS in 0.280 0.322 0.365
PIPE OD. : in 6.625 8.625 10.750
ACOUSTIC VEL. m/s 1368.86 1349.71 1334.00
PIPELINE PERIODs 80.36 81.50 82.46
JOUKOWSKI HEAD bar 26.379 15.021 9.418
VALVE CLOSE TIMs 30 30 30
PRESSURE RISE bar 26.379 15.021 9.418
MAX SURGE PRESbarg 64.379 53.021 47.418

--END--
VAPOUR LINE SIZING CALCULATION
Minor corrections made to constants used
Molecular Weight: ? in formulae for Density, (Cell range
PRESSURE barg ? "CalcDensity"), and Cell Range
"Normal_Vol_Flow".
TEMP. degC ? BJH
COMPRESSIBILITY ? April 2002

Calculated Dens #VALUE! VOL FLOW#VALUE!

VOL FLOW#VALUE!

The line schedules are driven by the combo b

Pipe diameters: Line size and schedule selected - if no user ID IN_OUT sheet, the macro "Drop_Down18_Ch
has been entered then the pipe ID is looked up in a table on link cells T27, T28 and T29 on the IN_OUT sh
Look-ups sheet. If Range("PipeIDIndicator")=0 then use
system pipe Ids, but if range = 1 then use User Ids.

FLOW AREA : M2 0.01864 0.03228 0.05087

REL ROUGH : 0.00030 0.00023 0.00018

Friction factors: Calculated from formulas in process standards, and dependent on flow regime.

Schedule 40 K Values K Values for actual pipe ID

Line Size 1Line Size Line Size3 Line Size 1Line Size 2Line Size3

0.3 0.28 0.28 0.30 0.28 0.28

0.21 0.2 0.2 0.21 0.20 0.20
0.15 0.14 0.14 0.15 0.14 0.14
0.12 0.11 0.11 0.12 0.11 0.11
5.1 4.8 4.8 5.10 4.80 4.80
0.68 0.63 0.63 0.68 0.63 0.63
0.75 0.7 0.7 0.75 0.70 0.70
0.3 0.28 0.28 0.30 0.28 0.28
 0.9 0.84 0.84 0.90 0.84 0.84

Valves and tees: Looks up K value for fitting for Schedule 40

pipe. Then adjusts the K value depending on the actual pipe
selected.

Reducers/Expanders: Size selected on drop down menu on

IN_OUT, and written to a cell on that sheet. Cell linked to this
sheet, where the K value is looked up for that size. No
adjustment for different pipe sizes as effect negligible.

Fittings Factor: If no fittings have been selected

tees, reducers etc.) so the calculation is only for
then an equivalent length is calculated by multip
straight pipe length by a fittings factor. This fac
OPTION NOT USED on both the pipe size and the length of the pipe,
up on tables on the look-up sheet. There is an o
user to overwrite this value.
FITTINGS FACTOR CALC. Calculation Type: 0 The total pressure drop is then calculated by mu
total equivalent length by the pressure drop per
User=> #VALUE! #VALUE! #VALUE! #VALUE! at the end of the 'liquid line sizing calculation' s
PRESS DROP bar 156.130 45.308 14.718 dividing by 100).
(Based on Default psi 2263.891 656.966 213.414
Fitting Factors) kg/cm3 159.206 46.201 15.008

Pressure Drop Calculation: If K factor is being used (see box above) then the
pressure drop is calculated using: (p.2.0-10 Process Standards)

DP = 1.122x10-3 K Q2 SG x conversion factor imperial to metric

d2
OK

6
8
10
6
8
10
edules are driven by the combo boxes on the
et, the macro "Drop_Down18_Change", and the
7, T28 and T29 on the IN_OUT sheet.

egime.

Line Size3
 Equivalent Lengths
corresponding to the calculated
overall K values.
f no fittings have been selected (bends, valves,
c.) so the calculation is only for straight pipe, New feature added.
nt length is calculated by multiplying the BJH March 2002
gth by a fittings factor. This factor is dependent USED
size and the length of the pipe, and is looked
he look-up sheet. There is an option for the 55002.68 55002.68 55002.68
this value.
55000 55000 55000
e drop is then calculated by multiplying the Check
ength by the pressure drop per 100m calculated Values
'liquid line sizing calculation' sheet (and

ve) then the

#N/A
Range Names Range Locations
AcousticVelocity1 =Calculation!$D$119
AcousticVelocity2 =Calculation!$E$119
AcousticVelocity3 =Calculation!$F$119
Actual_Vol_Flow =Calculation!$L$28
AtmosPBar_in =IN_OUT!$D$175
AtmosPKg_in =IN_OUT!$F$175
BarPer100m1 =Calculation!$D$39
BarPer100m2 =Calculation!$E$39
BarPer100m3 =Calculation!$F$39
BulkModulus =IN_OUT!$C$106
BulkModulusPsi =Calculation!$E$110
Calc_K_1 =IN_OUT!$D$70
Calc_K_2 =IN_OUT!$E$70
Calc_K_3 =IN_OUT!$F$70
Calc_Type_Link =IN_OUT!$Q$70
CalcDensity =Calculation!$I$28
CalcFF1 =IN_OUT!$D$71
CalcFF2 =IN_OUT!$E$71
CalcFF3 =IN_OUT!$F$71
Calculation_Type =IN_OUT!$R$70
CalculationNumber =IN_OUT!$C$5
ComboBoxScheduleNumbers ='Look-ups'!$J$274:$K$292
Company_Name_1 =PRINT!$D$25
Company_Name_2 =PRINT!$D$121
Company_Name_3 =PRINT!$D$211
CompFlowWarn =IN_OUT!$Q$76
Compressibility =IN_OUT!$D$173
ContractNumber =IN_OUT!$C$8
Customer =IN_OUT!$C$6
D1PipeID =IN_OUT!$B$30
Data_File_1 =PRINT!$E$119
Data_File_2 =PRINT!$E$203
Data_File_3 =PRINT!$E$305
DeltaPBar1 =IN_OUT!$D$75
DeltaPBar2 =IN_OUT!$E$75
DeltaPBar3 =IN_OUT!$F$75
DeltaPKg1 =IN_OUT!$D$77
DeltaPKg2 =IN_OUT!$E$77
DeltaPKg3 =IN_OUT!$F$77
DeltaPPsi1 =IN_OUT!$D$76
DeltaPPsi2 =IN_OUT!$E$76
DeltaPPsi3 =IN_OUT!$F$76
Dens_Vap_Print =PRINT!$E$231
Density =Calculation!$C$109
Description =IN_OUT!$C$11
DescriptionOthers1 =IN_OUT!$B$65
DescriptionOthers2 =IN_OUT!$B$66
DesignPressure =Calculation!$C$11
DPipeID =Calculation!$B$33
Dsize =IN_OUT!$C$30
Expander1 =Calculation!$D$61
Expander2 =Calculation!$E$61
Expander3 =Calculation!$F$61
ExpanderK1 =Calculation!$D$62
ExpanderK2 =Calculation!$E$62
ExpanderK3 =Calculation!$F$62
ExpanderKValueLookupTable ='Look-ups'!$H$27:$J$167
ExpanderSelectionLookupTabl ='Look-ups'!$G$181:$K$220
ExpiryDate =Formula!$D$14
ExpiryDateList =Formula!$J$3:$J$22
ExpLink ='Look-ups'!$H$26
ExpSel1 =IN_OUT!$T$60
ExpSel2 =IN_OUT!$T$59
ExpSel3 =IN_OUT!$T$61
f_FullTurb_1 ='Look-ups'!$H$333
f_FullTurb_2 ='Look-ups'!$H$341
f_FullTurb_3 ='Look-ups'!$H$349
FF_1 =Calculation!$D$38
FF_2 =Calculation!$E$38
FF_3 =Calculation!$F$38
FF_Warn1 =IN_OUT!$G$71
FF_Warn2 =IN_OUT!$H$72
FFIndicator =Calculation!$G$76
FittingFactor1 =Calculation!$D$75
FittingFactor2 =Calculation!$E$75
FittingFactor3 =Calculation!$F$75
FittingFactorIndicator =IN_OUT!$B$71
FittingFactorLookUpTable ='Look-ups'!$A$363:$D$366
FittingFactorOffsetLookupTabl ='Look-ups'!$G$363:$H$365
Flag_Laminar =Calculation!$E$101
FlowArea1 =Calculation!$J$37
FlowArea2 =Calculation!$K$37
FlowArea3 =Calculation!$L$37
Flowrate =IN_OUT!$C$138
FlowRegime1 =Calculation!$D$37
FlowRegime2 =Calculation!$E$37
FlowRegime3 =Calculation!$F$37
Fluid_Vap_in =IN_OUT!$D$165
FluidName =IN_OUT!$C$137
FrictionFactor1 ='Look-ups'!$F$333
FrictionFactor2 ='Look-ups'!$F$341
FrictionFactor3 ='Look-ups'!$F$349
FrictionFactorCalculation ='Look-ups'!$A$327:$G$349
ID_Option_Link =IN_OUT!$W$28
IndicateFF =Calculation!$B$75
IndicateUFF =Calculation!$B$76
Indicator =IN_OUT!$G$72
InletTempDegF =Calculation!$C$8
JoukowskiHead1 =Calculation!$D$121
JoukowskiHead2 =Calculation!$E$121
JoukowskiHead3 =Calculation!$F$121
K =Calculation!$D$74
kgPercm2Per100m1 =Calculation!$D$41
KgPercm2Per100m2 =Calculation!$E$41
KgPercm2Per100m3 =Calculation!$F$41
KValueLookupTable ='Look-ups'!$A$421:$J$459
KValuePipeIDs ='Look-ups'!$A$468:$C$508
KxNo45DegBends1 =Calculation!$D$48
KxNo45DegBends2 =Calculation!$E$48
KxNo45DegBends3 =Calculation!$F$48
KxNo90DegBends1 =Calculation!$D$46
KxNo90DegBends2 =Calculation!$E$46
KxNo90DegBends3 =Calculation!$F$46
KxNo90DegLRBends1 =Calculation!$D$47
KxNo90DegLRBends2 =Calculation!$E$47
KxNo90DegLRBends3 =Calculation!$F$47
KxNoBflyValves1 =Calculation!$D$51
KxNoBflyValves2 =Calculation!$E$51
KxNoBflyValves3 =Calculation!$F$51
kxNoBranchTee1 =Calculation!$D$54
KxNoBranchTee2 =Calculation!$E$54
KxNoBranchTee3 =Calculation!$F$54
KxNoCheckValves1 =Calculation!$D$52
KxNoCheckValves2 =Calculation!$E$52
KxNoCheckValves3 =Calculation!$F$52
KxNoExp1 =Calculation!$D$63
KxNoExp2 =Calculation!$E$63
KxNoExp3 =Calculation!$F$63
KxNoGateValves1 =Calculation!$D$49
KxNoGateValves2 =Calculation!$E$49
KxNoGateValves3 =Calculation!$F$49
KxNoGlobeValves1 =Calculation!$D$50
KxNoGlobeValves2 =Calculation!$E$50
KxNoGlobeValves3 =Calculation!$F$50
KxNoOthers1 =Calculation!$D$69
kxNoOthers2 =Calculation!$E$69
KxNoOthers21 =Calculation!$D$70
KxNoOthers22 =Calculation!$E$70
KxNoOthers23 =Calculation!$F$70
KxNoOthers3 =Calculation!$F$69
kxNoPipeEntry1 =Calculation!$D$67
KxNoPipeEntry2 =Calculation!$E$67
KxNoPipeEntry3 =Calculation!$F$67
KxNoPipeExit1 =Calculation!$D$68
KxNoPipeExit2 =Calculation!$E$68
KxNoPipeExit3 =Calculation!$F$68
KxNoRed1 =Calculation!$D$58
KxNoRed2 =Calculation!$E$58
KxNoRed3 =Calculation!$F$58
KxNoThruTee1 =Calculation!$D$53
KxNoThruTee2 =Calculation!$E$53
KxNoThruTee3 =Calculation!$F$53
LengthOfStraightPipe =IN_OUT!$C$68
LengthOfStraightPipe1 =IN_OUT!$D$68
LengthOfStraightPipe2 =IN_OUT!$E$68
LengthOfStraightPipe3 =IN_OUT!$F$68
LineNumber =IN_OUT!$C$10
LineODLookupTable ='Look-ups'!$A$374:$B$414
LineSize1 =Calculation!$D$31
LineSize2 =IN_OUT!$E$28
LineSize3 =Calculation!$F$31
LineSizeNow =IN_OUT!$V$31
LineSizeSelected =IN_OUT!$E$84
LineSizeThen =IN_OUT!$V$32
LineWarning1 =IN_OUT!$H$24
LineWarning2 =IN_OUT!$H$25
LineWarning3 =IN_OUT!$H$26
LiqorVap =IN_OUT!$R$137
Location =IN_OUT!$C$7
MaxPressure =IN_OUT!$C$108
MaxSurgePressure1 =Calculation!$D$124
MaxSurgePressure2 =Calculation!$E$124
MaxSurgePressure3 =Calculation!$F$124
MolecularWeight =IN_OUT!$D$170
NewExpiryDate =Formula!$K$6
Normal_Vol_Flow =Calculation!$L$29
Number90DegBends =IN_OUT!$C$44
NumberOf45DegBends =IN_OUT!$C$46
NumberOf90DegLRBends =IN_OUT!$C$45
NumberOfBranchTees =IN_OUT!$C$52
NumberOfButterflyValves =IN_OUT!$C$49
NumberOfCheckValves =IN_OUT!$C$50
NumberOfExpander =IN_OUT!$C$59
NumberOfGateValves =IN_OUT!$C$47
NumberOfGlobeValves =IN_OUT!$C$48
NumberOfOthers1 =IN_OUT!$C$65
NumberOfOthers2 =IN_OUT!$C$66
NumberOfPipeEntry =IN_OUT!$C$63
NumberOfPipeExit =IN_OUT!$C$64
NumberOfReducer =IN_OUT!$C$55
NumberOfThruTees =IN_OUT!$C$51
OneBiggerOneSmaller ='Look-ups'!$A$278:$C$318
other1K =IN_OUT!$G$65
other2K =IN_OUT!$G$66
PipeID =Calculation!$B$34
PipeID1 =Calculation!$D$33
PipeID2 =Calculation!$E$33
PipeID3 =Calculation!$F$33
PipeIDIndicator =Calculation!$G$33
PipeIDSave1 =Calculation!$I$33
PipeIDSave2 =Calculation!$J$33
PipeIDSave3 =Calculation!$K$33
PipeIDText1 =IN_OUT!$H$30
PipeIDText2 =IN_OUT!$H$31
PipeLinePeriod1 =Calculation!$D$120
PipeLinePeriod2 =Calculation!$E$120
PipeLinePeriod3 =Calculation!$F$120
PipeOD1 =Calculation!$D$118
PipeOD2 =Calculation!$E$118
PipeOD3 =Calculation!$F$118
PipeRoughness =IN_OUT!$C$140
PipeThickness1 =Calculation!$D$117
PipeThickness2 =Calculation!$E$117
PipeThickness3 =Calculation!$F$117
Pressure =IN_OUT!$D$171
Pressure1Bar =Calculation!$D$80
Pressure1kgPercm2 =Calculation!$D$82
Pressure1Psi =Calculation!$D$81
Pressure2Bar =Calculation!$E$80
Pressure2kgPercm2 =Calculation!$E$82
Pressure2Psi =Calculation!$E$81
Pressure3Bar =Calculation!$F$80
Pressure3kgPercm2 =Calculation!$F$82
GENERAL INPUT for LIQUID or for VAPOUR

CALCULATION No.: ****

CUSTOMER : DPR-Co.
LOCATION : Dehloran
CONTRACT No. : ****
UNIT No. : 890
LINE No. : ***
DESCRIPTION : ***

Data File:

Go to the next page, (Fluid Properties), to

select Vapour or Liquid Linesizing.

LINE SIZING CALCULATION LIQUID

VOLUME FLOW : 128.03 m3/h

LINE SIZE : in. nom. 6 8 10

PIPE SCHEDULE : STD
STD 8
STD STD
STD Group Box 312
Calculated PIPE ID : in. 6.065 7.981 10.020 Use Calculated IDs
USER PIPE ID : in. Use Input IDs
VELOCITY : m/s 1.91 1.10 0.70
REYNOLDS NO : 2.94E+05 2.23E+05 1.78E+05
FLOW REGIME : TURBUL TURBUL TURBUL
FRICTION FACTOR : 0.017 0.017 0.017

PRESSURE DROP : bar/100m 0.203 0.051 0.017

psi/100ft 0.896 0.228 0.074
kg/cm /100m
2
0.207 0.053 0.017
 Go to next page for preliminary line sizing
K METHOD CALCULATION using Fittings Factors.

LINE SIZE : in. nom. 6 8 10 K for

No No x K No x K No x K 8" Line
90 DEG SR BEND : 0 0.00 0.00 0.00 0.28
90 DEG BEND: 0 0.00 0.00 0.00 0.20
45 DEG BEND : 0 0.00 0.00 0.00 0.14
GATE VALVE : 0 0.00 0.00 0.00 0.11
GLOBE VALVE : 0 0.00 0.00 0.00 4.80
BUTTERFLY VALVE: 0 0.00 0.00 0.00 0.63
SWING CHECK VALVE : 0 0.00 0.00 0.00 0.70
THRU TEE : 0 0.00 0.00 0.00 0.28
BRANCH TEE : 0 0.00 0.00 0.00 0.84

REDUCERS :
NUMBER : 0

EXPANDERS :
NUMBER : 0 There is more
on the next
page...

K METHOD CALCULATION (CONT.) K

PIPE ENTRY : 0 0.00 0.00 0.00 0.5
PIPE EXIT : 0 0.00 0.00 0.00 1
OTHERS: 0 0.00 0.00 0.00 0
OTHERS: 0 0.00 0.00 0.00 0
TOTAL K FITTINGS : 0.00 0.00 0.00
STRAIGHT PIPE m : 55000 55000 55000 55000
STRAIGHT PIPE K : 6069.02 4620.83 3729.42
TOTAL K : 6069.02 4620.83 3729.42 K VALUE CALCULATION
1.4 1.6 1.6
USER FITTINGS FACTOR: ? ? ?
Equivalent Total Le (m): 55002.7 55002.7 55002.7 EQUIV. LGTH. NOT USED

PRESSURE DROP
PRESSURE DROP : bar 111.404 28.287 9.189
Using
Using psi 1615.797 410.282 133.279
K Values
kg/cm2 113.598 28.845 9.370
PRESSURE DROP
Using
K Values

SUMMARY OF RESULTS Liquid Line Sizing

(Using K Values).

LINE SIZE SELECTED: in. nom. 8 2

With 10% contingency
PRESSURE DROP : bar/100m
psi/100ft
kg/cm2/100m

PRESSURE DROP : bar

psi
kg/cm2

PIPELINE SURGE PRESSURE CALCULATION

DENSITY : 1010.000 kg/m3
BULK MODULUS, K: 2.413E+09 N/m2 349974 psi
YOUNGS MODULUS,E: 2.069E+11 N/m2
3.00E+07 psi
MAX. PRESSURE : 38 barg (eg. Pump shut-in)

LINE SIZE : in. nom. 6 8 10

--- --- ---
PIPE LENGTH : m 55000 55000 55000
PIPE THICKNESS : in 0.2800 0.3220 0.3650
PIPE OD. : in 6.625 8.625 10.75
ACOUSTIC VEL. : m/s 1368.86 1349.71 1334.00
PIPELINE PERIOD : s 80.36 81.50 82.46
JOUKOWSKI HEAD : bar 26.379 15.021 9.418
VALVE CLOSE TIME: s 30 30 30
PRESSURE RISE : bar 26.379 15.021 9.418
MAX SURGE PRESS.: barg 64.379 53.021 47.418

---- END of LIQUID LINESIZING ----

LIQUID FLOW and PROPERTIES

LIQUID Water
OPERATING FLOW : 129306 kg/h
VISCOSITY : 1.01 cP
PIPE ROUGHNESS : 0.046 mm

SPECIFIC GRAVITY : 1.010 (At flowing conditions)

VAPOUR FLOW and PROPERTIES

GAS / VAPOUR : ?
FLOWRATE : ? Kg/h
VISCOSITY : ? Cp
PIPE ROUGHNESS : 0.046 mm

MOLECULAR WEIGHT : ?
PRESSURE : ? bar g
TEMPERATURE : ? deg C Click here to reset
Atmos. Pressure
COMPRESSIBILITY : ?

Local Atmos. Pres. : 1.013 Bar a 0 Altitude, m

VOLUME FLOW : 128.03 Am /h
3
#VALUE! Nm3/h

CALC. DENSITY : kg/m3

USER
INPUT DENSITY : kg/m3 (Optional)
Please input a value for PRESSURE
 Rev: 3.03

Properties), to
Linesizing.

Group Box 312

Use Calculated IDs

Use Input IDs

inary line sizing

L/D
L/D equiv.to the
fitting K value.
Equivalent
16
12
8
6
282
37
41
16
49

There is more
on the next
page...

Select -
K Value
Calculation

Default Fitting
Factors

User Input Fitting

Factors

K VALUE CALCULATION

EQUIV. LGTH. NOT USED

With 10% contingency
ick here to reset
mos. Pressure

Altitude, m
 ZOOM FACTOR 161

Put the Window Zoom Factor in

here, so the program can
remember it.

PIPE SCHEDULES:-
Schedule Selected= 11 Link Cell for Pipe ID Option Buttons
Schedule Selected = 11 4
Schedule Selected = 11

When the schedule is changed 8 Remember the current Line Size

for the central line size, the
schedules for the other two lines 8 Remember the previous Line Size
are set to the same, using macro
'DropDown18_Change'
 reducer2=
reducer1=
reducer3=

expand2=

expand1=

expand3=

Line sizes for

0.5 drop-down list.
Calculation Type 0.75
0 = Detailed, using K 1
1 = Default FF
2 = User FF 1.25
1.5
1 0 2
2.5
3
Equivalent length formula revised. 3.5
BJH March 2002 4
5
Vapour High dP Warning. 6
8
10

12

14

16
18
20
22
24
26
28
30
32
34
36
38
40
42
44
46

48
52

56

60
64
68
72
76
80
 Range
Liquid "LiqorVap"
0 User Input Density Flag
=1 if User input
=0 if Calculated density
Option Buttons

ous Line Size

 Detailed Calc.
Probably no longer required
Default F F

User F F
BJH
March 2002
Detailed K Calculation

Default Fitting Factors

Users Fitting Factors

 Probably no longer required.

BJH
March 2002

Factors
FOSTER WHEELER ENERGY LTD By: Date: 8-Apr-25
Checked: Date:
VAPOUR LINE SIZING CALCULATION Appr.: Date:
SHEET 1 Rev. By: Date:
WORKSHEET APPROVED FOR PROCESS DESIGN
Sheet: of
Calculation No.: ****

Customer: DPR-Co. Contract No.: ****

Location: Dehloran Unit: 890

LINE NO.: *** Atmospheric Pressure: 1.013 Bar a

DESCRIPTION: *** Altitude: 0 m

VAPOUR LINE SIZING CALCULATION

MOLECULAR WEIGHT: ?
FLUID : Water PRESSURE barg : ?
FLOWRATE : 129306 kg/h TEMPERATURE o
C: ?
DENSITY (Calculated) : 1010.000 (at flowing conditions) COMPRESSIBILTY : ?
VISCOSITY : 1.01 cP
PIPE ROUGHNESS : 0.046 mm
VOLUME FLOW : 128.03 Am3/h
Nm3/h
LINE SIZE (in nominal): 6 8 10
PIPE SCHEDULE : STD STD STD
PIPE I.D (in) : 6.065 7.981 10.020
FLOW AREA (m2) : 0.0186 0.0323 0.0509
VELOCITY (m/s) : 1.91 1.10 0.70
REYNOLDS NO : 2.94E+05 2.23E+05 1.78E+05
FLOW REGIME : TURBUL TURBUL TURBUL
RELATIVE ROUGHNESS : 0.00030 0.00023 0.00018
FRICTION FACTOR : 0.017 0.017 0.017

PRESSURE DROP : bar/100m 0.203 0.051 0.017

psi/100ft 0.896 0.228 0.074
kg/cm2/100m 0.207 0.053 0.017

K METHOD CALCULATION

LINE SIZE (in nominal): 6" 8" 10" K for Line Size
No No x K No x K No x K K 8"
90 DEG BEND : 0 0.00 0.00 0.00 0.28
90 DEG LR BEND : 0 0.00 0.00 0.00 0.20
45 DEG BEND : 0 0.00 0.00 0.00 0.14
GATE VALVE : 0 0.00 0.00 0.00 0.11
GLOBE VALVE : 0 0.00 0.00 0.00 4.80
BUTTERFLY VALVE : 0 0.00 0.00 0.00 0.63
SWING CHECK VALVE : 0 0.00 0.00 0.00 K dependent on 0.70
THRU TEE : 0 0.00 0.00 0.00 line size. 0.28
BRANCH TEE : 0 0.00 0.00 0.00 0.84

REDUCERS : Size :
NUMBER : 0

EXPANDERS : Size :
NUMBER : 0

PIPE ENTRY : 0 0 0 0 0
PIPE EXIT : 0 0 0 0 0
OTHERS: 0 0 0 0 0
OTHERS: 0 0 0 0 0
------- ------- -------
TOTAL K FITTINGS : 0.00 0.00 0.00

STRAIGHT PIPE (m) : 55000 55000 55000 55000

STRAIGHT PIPE K : 6069.02 4620.83 3729.42
TOTAL K : 6069.02 4620.83 3729.42

Equivalent Total Le (m) 55002.7 55002.7 55002.7 OPTION NOT USED

Upstream Pressure Bar g : ?
PRESSURE DROP : bar 111.404 28.287 9.189
(Using psi 1615.797 410.282 133.279
K Values) kg/cm2 113.598 28.845 9.370

SUMMARY OF RESULTS (Using K Values).

LINE SIZE SELECTED (in nominal): 8

W. 10% contingency
PRESSURE DROP : bar/100m
psi/100ft
kg/cm2/100m

PRESSURE DROP : bar

psi
kg/cm2

LINESIZE / Rev 3.03 Data File:

NOMINAL SCH 40 SCH 40
PIPE PIPE ID PIPE ID
SIZE (mm) (in)
0.125 6.8326 0.269
0.25 9.2456 0.364
0.375 12.5222 0.493
0.5 15.7988 0.622
0.75 20.9296 0.824
1 26.6446 1.049
1.25 35.052 1.38
1.5 40.894 1.61
2 52.5018 2.067
2.5 62.7126 2.469
3 77.9272 3.068
3.5 90.1192 3.548
4 102.2604 4.026
5 128.1938 5.047
6 154.051 6.065
8 202.7174 7.981
10 254.508 10.02
12 303.2252 11.938
14 333.3496 13.124
16 381 15
18 428.6504 16.876
20 477.8248 18.812
22 526 20.70866
24 574.6496 22.624
26 622 24.48819
28 669 26.33858
30 731 28.77953
32 777.8496 30.624
34 828.6496 32.624
36 876.3 34.5
38 925 36.41732
40 973 38.30709
42 1022 40.23622
44 1071 42.16535
46 1119 44.05512
48 1168 45.98425
52 1265 49.80315
56 1363 53.66142
60 1460 57.48031
64 1557 61.29921
68 1655 65.15748
72 1752 68.97638
76 1849 72.79528
80 1946 76.61417