Line Sizing

Liquid Line sizing

mass flow density mass flow mas mass flo flow (m) area ( a) velocity ( v) m R

220000 1000 220 0.06 .061111 2 3.14 x R 2

kg/hr kg/m3 m3/hr m3/s m3/se ec m /s

axv 2 =

2 =

R R= R= Dia Dia =

(mass flow / velocity) / 3.14

0.009731 0.098646 m 98.64618 mm 197. 197.3 3 mm

Line Sizing with Steam at 2.2 bar a or 1.2 Bar G mass flow density mass flow mas mass flo flow (m) area ( a) velocity ( v) m R

600 1.23 487.8049 0.13 .135501 2 3.14 x R 25

kg kg/hr kg/m3 m3/hr m3/s m3/se ec m /s

axv 2 =

2 =

R R= R= Dia =


0.001726 0.041547 m 41.54674 mm 83.093 83.09349 49 mm

Line Sizing with Steam at 4.5 bar a or 3.5 Bar G mass flow density mass flow mas mass flo flow (m) area ( a) velocity ( v)

3000 2.16 1388.889 0.38 .385802 2 3.14 x R 40

kg k g/hr kg/m3 m3/hr m3/s m3/se ec m /s

m R

axv 2 =

2 =

R R= R= Dia =


0.003072 0.055423 m 55.4227 mm 110.8454 mm

Line Sizing with Steam at 9.5 bar a or 8.5 bar G mass flow density mass flow mass flow (m) area ( a) velocity ( v) m R

983 4.65 211.3978 0.058722 2 3.14 x R 25

kg/hr kg/m3 m3/hr m3/sec

from steam table at 9.5 bar a

m/s

axv 2 =

2 =

R R= R= Dia =


0.000748 0.02735 m 27.35043 mm 54.70087 mm

m R

10000 1030 9.708738 0.002697 2 3.14 x R 1.5

kg/hr kg/m3 m3/hr m3/sec m/s

axv 2 =

2 =

R R= R= Dia =

mass flow 3000 density 3.66 mass flow 819.6721 mass flow ( 0.227687 2 3.14 x R area ( a) velocity ( v) 35 m R

axv 2 =

(mass flow

2 =

0.002072 0.045517 45.51662 91.03324

R R= R= Dia =

Line sizing for Brine-10%

mass flow density mass flow mass flow (m) area ( a) velocity ( v)

Line Sizing with Stea


0.000573 0.023929 m 23.92873 mm 47.9 mm

Line Sizing with Steam at 23 bar a mass flow density mass flow mass flow (m) area ( a) velocity ( v) m R

12000 11.51 1042.572 0.289603 2 3.14 x R 25


from staem table software at 95 bar a

m/s

axv 2 =

2 =

R R= R= Dia =


0.003689 0.060739 m 60.73889 mm 121.4778 mm

150 mm

Line Sizing with Steam at 13 bar a mass flow density mass flow mass flow (m) area ( a) velocity ( v) m R

1600 6.61 242.0575 0.067238 2 3.14 x R 25


from staem table software at 95 bar a

m/s

axv 2 =

2 =

R R= R= Dia =


0.000857 0.029267 m 29.26666 mm 58.53332 mm

Line Sizing with gas at 2.2 bar a or 1.2 Bar G

mass flow density mass flow mass flow (m) area ( a) velocity ( v) m R

60 164 0.06 1.67E-05 2 3.14 x R 20

kg/hr kg/m3 m3/hr m3/sec m/s

axv 2 =

2 =

R R= R= Dia =


2.65E-07 0.000515 m 0.515163 mm 1.030326 mm

0.06 m3/hr

bio con HE 14300 kcal/hr

considering Cp of mass - 1 k cal /kg °c

3575 kg/hr 3.575 m3 /hr

cooling water req considering CW in 31°C and out 35°C delta T - 5°C

12000 kcal/hr

considering Cp of mass - 1 k cal /kg °c

2400 kg/hr 2.4 m3 /hr

cooling water req considering CW in 31°C and out 35°C delta T - 5°C

at 7 bar a or 6 Bar G kg/hr kg/m3 m3/hr m3/sec m/s

/ velocity) / 3.14

m mm mm

Density of Gas in Kg/M3 0.031 0.7 0.113 8.864

Gas O2 CO2 Air LPG N2 H2 H2 H2 IPA

Temp °C. 35 35 32 32 30 125 100 90 82

K Mkoles /Kg. M3 At NTP M3 At 35°C. & 6.0 Kg/cm2 (g) Density in Kg/M3 At 35°C. & 6.0 Kg/cm2 (g) Pressure Density Line Kg/cm2 Molecular of Gas in Size Velocity (g) wt of Gas Kg/M3 (NB) (M/s.) 6 32 8.620931 40 25 6 44 11.85378 40 25 6 29 7.889565 40 25 6 50.75 13.80674 6 25 150 28 164.6651 6 20 11 2 0.713403 25 25 10 2 0.697958 25 25 9 2 0.652182 25 25 6.6 60 15.22062 25 25

Flow Flow rate rate M3/Hr. Kg/Hr. 113.1 975 113.1 1341 113.1 892.3 2.5447 35.13 2.0358 335.2 44.179 31.52 44.179 30.83 44.179 28.81 44.179 672.4

Client:

Case D

Project: Unit: Job No.:

Line Sizes

INPUT DATA Line Number P&ID Number From To Service Nominal Bore or Internal diameter (NB / ID) Diameter Schedule (STD for Standard) Pipe roughness (X to default Commercial Steel) Phase (L, G, M or N) Liquid Flowrate Gas Flowrate Temperature Inlet Pressure Gas Molecular Weight Liquid Density Gas Density ( X to calculate) Gas Cp/Cv (X to default 1.4) Gas Compressibility Factor Z (X to default 1) Gas Viscosity (X to default 0.025) Liquid / Mixed Phase Viscosity Liquid Surface Tension (Reqd. if Phase = M) Actual Pipe Segment Length First Point Elevation of Pipe Segment Last Point Elevation of Pipe Segment No. of 45° Standard Elbows (L/D=16) No. of 90° Standard Elbows (L/D=30) No. of 45° Long Radius Elbows (L/D=10) No. of 90° Long Radius Elbows (L/D=16) No. of 180° Return Bends (L/D=50) No. of Tees: thru flow (L/D=20) No. of Tees: branch flow (L/D=60) No. of Valves - Gate (L/D=8) No. of Valves - Globe (L/D=340) No. of Valves - Butterfly (L/D=20) No. of Valves - Angle (L/D=145) No. of Valves - Ball (L/D=3) No. of Valves - Check (L/D=100)

PROGRAM

STEAM

[in] [in] [kg/h] [kg/h] [°C] [kg/cm2g] [kg/kgmole] [kg/m3] [kg/m3]

[cP] [cP] [dynes/cm] [m] [m] [m]

NB 2 STD X G 0 983.00 170 3.000 18 0 X X X 0.0135 0.00 0 100 0 0 0 2 0 0 0 0 0 0 2 0 0 0 0

NB 3 STD X G 0 983.00 170 3.000 18 0 X X X 0.0135 0.00 0 100 0 0 0 2 0 0 0 0 0 0 2 0 0 0 0

Sudden Enlarge. Nom. Diam. Sudden Contr. Nom. Diam. Pipe Sharp Edged Entrance (K=0.5) Pipe Exit (K=1) Sum of other Equiv. Lengths (L/D) Sum of other K's Sum of other Pressure Drops

[in] [in]

[kg/cm2]

PROCESS DATA INPUT CHECK

0 0 0 0 0 0 0

GAS DATA OK GAS DATA OK DIA. OK, SCHED. OK

DIA. OK, SCHED. OK

2.067 0.0018 Fully Turb. 4.901E+05 139 0.00 1.932 0.014 1.400 1.000 535.7 0.122 87.8 65.273

3.068 0.0018 Turbulent 3.302E+05 154 0.00 1.932 0.014 1.400 1.000 535.7 0.055 87.8 29.628

[kg/cm2]

1.519

0.206

[kg/cm2]

2.109

0.317

[kg/cm2]

0.000

0.000

[kg/cm2]

2.109

0.317

[kg/cm2g]

0.891

2.683

MECHANICAL DATA INPUT CHECK OUTPUT RESULTS Pipe Internal Diameter Pipe Roughness Factor Flow Characteristic Reynolds Number Total Equivalent Length Total K Mixed Phase Density Mixed Phase Flow Pattern Gas Density Gas Viscosity Gas k (=Cp/Cv) Gas Compressibility Factor Z Sonic Velocity Mach number Maximum Allowable Velocity Minimum Velocity (Mixed phase) Velocity Frictional Pressure Drop per 100m Total Frictional Pressure Drop Pressure Drop due to Static Head Total Pressure Drop (including Static Head) Outlet Pressure PROGRAM OUTPUT CHECK

0 0 0 0 0 0 0

[in]

[m] [kg/m3] [kg/m3] [cP]

[m/s] [m/s] [m/s] [m/s]

scription

By:

Rev.:

Checked:

Date:

29-Sep

VALIDATION / VERIFICATION sh.5 of 7

NB 4 STD X G 0 983.00 170 3.000 18 0 X X X 0.0135 0.00 0 100 0 0 0 2 0 0 0 0 0 0 2 0 0 0 0

0 0 0 0 0 0 0 GAS DATA OK DIA. OK, SCHED. OK

4.026 0.0018 Turbulent 2.516E+05 168 0.00 1.932 0.014 1.400 1.000 535.7 0.032 87.8 17.205 0.052 0.087 0.000 0.087 2.913

Case Description

Client: Project: Unit: Job No.: INPUT DATA Line Number P&ID Number From To Service Nominal Bore or Internal diameter (NB / ID) Diameter Schedule (STD for Standard) Pipe roughness (X to default Commercial Steel) Phase (L, G, M or N) Liquid Flowrate Gas Flowrate Temperature Inlet Pressure Gas Molecular Weight Liquid Density Gas Density ( X to calculate) Gas Cp/Cv (X to default 1.4) Gas Compressibility Factor Z (X to default 1) Gas Viscosity (X to default 0.025) Liquid / Mixed Phase Viscosity Liquid Surface Tension (Reqd. if Phase = M) Actual Pipe Segment Length First Point Elevation of Pipe Segment Last Point Elevation of Pipe Segment No. of 45° Standard Elbows (L/D=16) No. of 90° Standard Elbows (L/D=30) No. of 45° Long Radius Elbows (L/D=10) No. of 90° Long Radius Elbows (L/D=16) No. of 180° Return Bends (L/D=50) No. of Tees: thru flow (L/D=20) No. of Tees: branch flow (L/D=60) No. of Valves - Gate (L/D=8) No. of Valves - Globe (L/D=340) No. of Valves - Butterfly (L/D=20) No. of Valves - Angle (L/D=145) No. of Valves - Ball (L/D=3) No. of Valves - Check (L/D=100) Sudden Enlarge. Nom. Diam. Sudden Contr. Nom. Diam. Pipe Sharp Edged Entrance (K=0.5) Pipe Exit (K=1) Sum of other Equiv. Lengths (L/D) Sum of other K's Sum of other Pressure Drops

PROGRAM VALIDATION / VERI

PROCESS WATER NB

NB

2

2.5

3

40 X L 220000

40 X L 220000

40 X L 220000

30 4.000 0 1000 X X X X 1.00 0 100 0 4.5 0 0 0 0 0 0 0 0 0 0 0 2 0 0 0 0 0 0 0 0

30 4.000 0 1000 X X X X 1.00 0 100 0 4.5 0 0 0 0 0 0 0 0 0 0 0 2 0 0 0 0 0 0 0 0

30 4.000 0 1000 X X X X 1.00 0 100 0 4.5 0 0 0 0 0 0 0 0 0 0 0 2 0 0 0 0 0 0 0 0

PROCESS DATA INPUT CHECK

LIQUID DATA OK

LIQUID DATA OK

LIQUID DATA OK

MECHANICAL DATA INPUT CHECK

DIA. OK, SCHED. OK

DIA. OK, SCHED. OK

DIA. OK, SCHED. OK

2.067 0.0018 Fully Turb. 1.481E+06 100 0.00 28.228

2.469 0.0018 Fully Turb. 1.240E+06 100 0.00 19.784

3.068 0.0018 Fully Turb. 9.975E+05 100 0.00 12.813

[kg/cm2]

147.030

57.972

18.608

[kg/cm2] [kg/cm2]

147.494 0.450

58.190 0.450

18.695 0.450

OUTPUT RESULTS Pipe Internal Diameter Pipe Roughness Factor Flow Characteristic Reynolds Number Total Equivalent Length Total K Mixed Phase Density Mixed Phase Flow Pattern Gas Density Gas Viscosity Gas k (=Cp/Cv) Gas Compressibility Factor Z Sonic Velocity Mach number Maximum Allowable Velocity Minimum Velocity (Mixed phase) Velocity Frictional Pressure Drop per 100m Total Frictional Pressure Drop Pressure Drop due to Static Head Total Pressure Drop (including Static Head) Outlet Pressure PROGRAM OUTPUT CHECK

[in] [in] [kg/h] [kg/h] [°C] [kg/cm2g] [kg/kgmole] [kg/m3] [kg/m3]

[cP] [cP] [dynes/cm] [m] [m] [m]

[in] [in]

[kg/cm2]

[in]

[m] [kg/m3] [kg/m3] [cP]

[m/s] [m/s] [m/s] [m/s]

NB

[kg/cm2]

147.944

58.640

19.145

[kg/cm2g]

-143.944

-54.640

-15.145

Line Sizing

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