Ammonia - Heat & Mat. Balance

8/6/2019 Ammonia - Heat & Mat. Balance

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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******

Stream Number

Description

Phase

201 202/703 203 204 205 206 207

Process

Naphtha to

1432

Recycle

hydrogen from

3102

Proc. Naphtha +

rec. H2 at 1432

outlet

Proc. Naphtha +

rec H2 at 1104

outlet

Process Steam

from 1537

Primary reformer

1400 outlet

Process Air from

1433 to 1105

LIQUID VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR

Pressure Kg/cm2 a 43.0 42.0 39.4 39.4 43.5 29.9 32.0

Temperature oC 40 40 375 375 471 787 490

Dry gas rate Kg/hr 0 790 27608 27608 0 67164 59941

Steam rate Kg/hr 0 3 3 3 1111552 72003 282

Liquid rate Kg/hr 26818 0 0 0 0 0 0

Total rate Kg/hr 26818 793 27611 27611 1111552 139167 60223

Dry Gas flow rate Nm3/hr 0 2043 8032 8032 0 114864 46391

Steam to dry gas mole ratio n.a 0.00 0.00 0.00 n.a 0.78 0

Dry gas composition

N2 Mole % n.a 24.72 6.29 6.29 n.a 0.44 78.11

AR Mole % n.a 0.32 0.08 0.08 n.a 0.01 0.94O2 Mole % n.a 0.00 0.00 0.00 n.a 0.00 20.95

CH4 Mole % n.a 0.76 0.19 0.19 n.a 9.98 0.00

CO2 Mole % n.a 0.00 0.00 0.00 n.a 15.65 0.00

CO Mole % n.a 0.00 0.00 0.00 n.a 11.55 0.00

H2 Mole % n.a 74.20 18.87 18.87 n.a 62.37 0.00

NH3 Mole % n.a 0.00 0.00 0.00 n.a 0.00 0.00

Naphtha Mole % n.a 0.00 74.57 74.57 n.a 0.00 0.00

Sulphur Ppm wt 5.0 0 0.5 0.5 n.a 0 0

Component flow rate

N2 Kgmol/hr 0.0 22.5 22.5 22.5 0.0 22.5 1616.8

AR Kgmol/hr 0.0 0.3 0.3 0.3 0.0 0.3 19.5

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 433.5

CH4 Kgmol/hr 0.0 0.7 0.7 0.7 0.0 511.5 0.0CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 801.8 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 592.0 0.0

H2 Kgmol/hr 0.0 67.6 67.6 67.6 0.0 3196.5 0.0

H20 Kgmol/hr 0.0 0.2 0.2 0.2 6192.2 3996.8 15.6

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 267.2 0.0 267.2 267.2 0.0 0.0 0.0

Sulphur Kgmol/hr 5.0 0 5.0 5.0 0 0 0

Total flow rate Kgmol/hr 267.2 91.3 358.5 358.5 6192.2 9121.6 2085.4

MW 100.36 8.69 77.01 77.01 18.02 15.26 28.88

Enthalpy GCal/hr 0.13 -0.09 7.31 7.31 89.94 102.33 4.95


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Stream Number

Description

Phase

208 209/301 210/804 211 212 213 214

Secondary

Reformer 1105outlet

HT Shift Guard

Vessel inlet

Tail gas fuel from

PGHRU

Naphtha fuel to

1400

Preheated

combustion air

Flue gas at

reformer fire boxexit

Flue gas

After 1510

VAPOR VAPOR VAPOR LIQUID VAPOR VAPOR VAPOR

Pressure Kg/cm2 a 29.5 29.1 2.3 9.0 140 mmwc (g) -12 mmwc (g) -20.0 mmwc (g)

Temperature oC 972.5 380 40 40 277 940 871

Dry gas rate Kg/hr 120071 120071 2940 0 179183 177404 177404

Steam rate Kg/hr 79318 79318 0 0 4435 21906 21906


Total rate Kg/hr 199389 199389 2940 9836 183619 199310 199310


Steam to dry gas mole ratio 0.60 0.60 0.00 n.a 0.04 0.21 0.21

Dry gas composition

N2 Mole % 22.29 22.29 44.45 n.a 78.11 83.46 83.46

AR Mole % 0.27 0.27 12.66 n.a 0.94 1.29 1.29

O2 Mole % 0.00 0.00 0.00 n.a 20.95 2.72 2.72

CH4 Mole % 0.27 28.71 n.a 0.00 0.00 0.00

CO2 Mole % 10.70 10.70 0.00 n.a 0.00 12.53 12.53

CO Mole % 14.94 14.94 0.00 n.a 0.00 0.00 0.00

H2 Mole % 51.53 51.53 13.96 n.a 0.00 0.00 0.00

NH3 Mole % 0.00 0.00 0.21 n.a 0.00 0.00 0.00

Naphtha Mole % 0.00 0.00 0.00 n.a 0.00 0.00 0.00

Sulphur Ppm wt 0 0 0 n.a 0 0 0

Component flow rate

N2 Kgmol/hr 1639.3 1639.3 58.3 0.0 4832.8 4889.8 4889.8

AR Kgmol/hr 19.7 19.7 16.6 0.0 58.2 75.8 75.8

O2 Kgmol/hr 0.0 0.0 0.0 0.0 1296.2 159.2 159.2CH4 Kgmol/hr 20.1 20.1 37.6 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 787.0 787.0 0.0 0.0 0.0 734.0 734.0

CO Kgmol/hr 1098.2 1098.2 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 3789.0 3789.0 18.3 0.0 0.0 0.0 0.0

H20 Kgmol/hr 4402.9 4402.9 0.0 0.0 246.2 1216.0 1216.0

NH3 Kgmol/hr 0.0 0.0 0.3 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 98.0 0.0 0.0 0.0

Sulphur Kgmol/hr 0 0 0 800 0 0 0


MW 16.96 16.96 22.43 100.36 28.54 28.17 28.17

Enthalpy GCal/hr 136.15 75.42 -0.08 0.04 7,43 62.49 58.12


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Stream Number

Description

Phase

222 223/323 224/636 226 281

Atomizing

Steam to

1400 burners

BFW

From 1539

To 1106

Flash steam

From 1130 to 2.1

Kg/cm2 a header

Vaporized

naphtha + process

steam to reformer

CW to 1535

VAPOR LIQUID VAPOR VAPOR LIQUID

Pressure Kg/cm2 a 4.0 126.0 2.5 34.4 5.0

Temperature oC 160 238 127 445 32

Dry gas rate Kg/hr 0 0 0 27608 0

Steam rate Kg/hr 2962 0 3108 111555 31120

Liquid rate Kg/hr 0 161000 0 0 31120

Total rate Kg/hr 2962 161000 3108 139163 2962

Dry Gas flow rate Nm3/hr 0 0 0 8032 0

Steam to dry gas mole ratio n.a n.a n.a 17.28 n.a

Dry gas composition

N2 Mole % n.a n.a n.a 6.29 n.a

AR Mole % n.a n.a n.a 0.08 n.aO2 Mole % n.a n.a n.a 0.00 n.a

CH4 Mole % n.a n.a n.a 0.19 n.a

CO2 Mole % n.a n.a n.a 0.00 n.a

CO Mole % n.a n.a n.a 0.00 n.a

H2 Mole % n.a n.a n.a 18.87 n.a

NH3 Mole % n.a n.a n.a 0.00 n.a

Naphtha Mole % n.a n.a n.a 74.57 n.a

Sulphur Ppm wt n.a n.a n.a 0.5 n.a

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 22.5 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.3 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.7 0.0CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 67.6 0.0

H20 Kgmol/hr 164.4 8937.0 172.5 6192.3 1727.1

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 267.2 0.0

Sulphur Kgmol/hr 0 0 0 0 0

Total flow rate Kgmol/hr 164.4 8937.0 172.5 6550.7 1727.1

MW 18.02 18.02 18.02 21.24 18.02

Enthalpy GCal/hr 1.97 39.55 2.02 97.25 1.00


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Stream Number

Description

Phase

301/209 302 303 304 305 306 307

HT Shift

Guard Vessel

Inlet

HT Shift 1st

Bed outlet to

1539

HT Shift 2nd

Bed inlet

From 1539

HT Shift 2nd

Bed outlet

To 1514

Process Gas

Outlet from

1514

Quench Water

To 1111

LT Shift

Inlet gas

VAPOR VAPOR VAPOR VAPOR VAPOR LIQUID VAPOR

Pressure Kg/cm2 a 29.1 28.7 28.5 28.2 27.9 34.0 27.8

Temperature oC 380 449.2 350 363 302.5 126 205

Dry gas rate Kg/hr 120071 133869 133869 136622 136622 0 136622

Steam rate Kg/hr 79318 65521 65521 62768 62768 0 80210


Total rate Kg/hr 199389 199390 199390 199390 199390 17440 216832


Steam to dry gas mole ratio 0.60 0.45 0.45 0.42 0.42 n.a 0.54

Dry gas composition

N2 Mole % 22.29 20.19 20.19 19.82 19.82 n.a 19.82

AR Mole % 0.27 0.24 0.24 0.24 0.24 n.a 0.24O2 Mole % 0.00 0.00 0.00 0.00 0.00 n.a 0.00

CH4 Mole % 0.27 0.25 0.25 0.24 0.24 n.a 0.24

CO2 Mole % 10.70 19.13 19.13 20.62 20.62 n.a 20.62

CO Mole % 14.94 4.09 4.09 2.17 2.17 n.a 2.17

H2 Mole % 51.53 56.10 56.10 56.91 56.91 n.a 56.91

NH3 Mole % 0.00 0.00 0.00 0.00 0.00 n.a 0.00

Naphtha Mole % 0.00 0.00 0.00 0.00 0.00 n.a 0.00

Sulphur Ppm wt 0 0 0 0 0 n.a 0

Component flow rate

N2 Kgmol/hr 1639.3 1639.3 1639.3 1639.3 1639.3 0.0 1639.3

AR Kgmol/hr 19.7 19.7 19.7 19.7 19.7 0.0 19.7

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 20.1 20.1 20.1 20.1 20.1 0.0 20.1CO2 Kgmol/hr 787.0 1552.9 1552.9 1705.7 1705.7 0.0 1705.7

CO Kgmol/hr 1098.2 332.4 332.4 179.6 179.6 0.0 179.6

H2 Kgmol/hr 3789.0 4554.8 4554.8 4707.7 4707.7 0.0 4707.7

H20 Kgmol/hr 4402.9 3637.0 3637.0 3484.2 3484.2 968.1 4452.4

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 16.96 16.96 16.96 16.96 16.96 18.02 17.04

Enthalpy GCal/hr 75.42 76.78 66.97 67.14 61.20 2.16 63.36


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Stream Number

Description

Phase

308 309 310/401 311 320/432 321/731 322/732

LT Shift

Outlet gas

To 1550

Process gas

From 1550

To 1114

Process gas

From 1114

To 1517 a/B

Process

Condensate

From 1114

LP BFW

From 1513

To 1703

Deaerated

BFW to 1523

HP BFW from

1523 to 1553

and 1539

VAPOR MIXED VAPOR LIQUID LIQUID LIQUID LIQUID

Pressure Kg/cm2 a 27.5 27.1 26.9 26.9 3.7 127.0 126.5

Temperature oC 217.1 173 173 173 94 109 181

Dry gas rate Kg/hr 139454 139454 139454 0 0 0 0

Steam rate Kg/hr 77383 71942 71942 0 0 0 0

Liquid rate Kg/hr 0 5441 0 5441 293945 300400 300400

Total rate Kg/hr 216837 216837 211396 5441 293945 300400 300400


Steam to dry gas mole ratio 0.51 0.47 0.47 n.a n.a n.a n.a

Dry gas composition

N2 Mole % 19.45 19.45 19.45 n.a n.a n.a n.a

AR Mole % 0.23 0.23 0.23 n.a n.a n.a n.a

O2 Mole % 0.00 0.00 0.00 n.a n.a n.a n.aCH4 Mole % 0.24 0.24 0.24 n.a n.a n.a n.a

CO2 Mole % 22.10 22.10 22.10 n.a n.a n.a n.a

CO Mole % 0.27 0.27 0.27 n.a n.a n.a n.a

H2 Mole % 57.71 57.71 57.71 n.a n.a n.a n.a

NH3 Mole % 0.00 0.00 0.00 n.a n.a n.a n.a

Naphtha Mole % 0.00 0.00 0.00 n.a n.a n.a n.a

Sulphur Ppm wt 0 0 0 n.a n.a n.a n.a

Component flow rate

N2 Kgmol/hr 1639.3 1639.3 1639.3 0.0 0.0 0.0 0.0

AR Kgmol/hr 19.7 19.7 19.7 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 20.1 20.1 20.1 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 1862.6 1862.6 1862.6 0.0 0.0 0.0 0.0CO Kgmol/hr 22.6 22.6 22.6 0.0 0.0 0.0 0.0

H2 Kgmol/hr 4864.6 4864.6 4864.6 0.0 0.0 0.0 0.0

H20 Kgmol/hr 4295.5 4295.5 3993.5 302.0 16316.7 16674.0 16674.0

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 17,04 17,04 17,02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 63.56 56.52 55.57 0.95 27.63 32.88 55.49



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Stream Number

Description

Phase

323/223 324/644 325/433 327/627 328 329

BFW

From 1539

To 1106

BFW from

1553 to

aux. Boiler

LP steam from

1550 to 4

Kg/cm2a header

& 1117A

LP steam from

2.1 Kg/cm2a

header to 1703

Deaerated

BFW from

Deaerator

LP steam

Boiler 1550

Blowdown

LIQUID LIQUID VAPOR VAPOR LIQUID LIQUID

Pressure Kg/cm2 a 126.0 126.0 5.0 2.1 1.4 5.0

Temperature oC 238 218 151 243 109 151

Dry gas rate Kg/hr 0 0 0 0 0 0

Steam rate Kg/hr 0 0 12810 10763 0 0

Liquid rate Kg/hr 161000 139400 0 0 301947 200

Total rate Kg/hr 161000 139400 12810 10763 301947 200

Dry Gas flow rate Nm3/hr 0 0 0 0 0 0

Steam to dry gas mole ratio n.a n.a n.a n.a n.a n.a

Dry gas composition

N2 Mole % n.a n.a n.a n.a n.a n.a

AR Mole % n.a n.a n.a n.a n.a n.aO2 Mole % n.a n.a n.a n.a n.a n.a

CH4 Mole % n.a n.a n.a n.a n.a n.a

CO2 Mole % n.a n.a n.a n.a n.a n.a

CO Mole % n.a n.a n.a n.a n.a n.a

H2 Mole % n.a n.a n.a n.a n.a n.a

NH3 Mole % n.a n.a n.a n.a n.a n.a

Naphtha Mole % n.a n.a n.a n.a n.a n.a

Sulphur Ppm wt n.a n.a n.a n.a n.a n.a

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 8937.0 7737.6 711.1 597.5 16760.9 11.1

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

Sulphur Kgmol/hr 0 0 0 0 0 0

Total flow rate Kgmol/hr 8937.0 7737.6 711.1 597.5 16760.9 11.1

MW 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 39.55 31.14 8.44 7.60 32.96 0.03



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Stream Number

Description

Phase

330 340/403 341 343 344 345

Condensate

From 1534

To 1703

Converted

Gas from 1131

To 1554

Converted

Gas from

1554 to 1514

Conv. Gas from

1514 to

Methanator

Syn. Gas from

Methanator

To 1553

Syn. Gas

From 1553

To 1554

MIXED VAPOR VAPOR VAPOR VAPOR VAPOR

Pressure Kg/cm2 a 1.4 26.1 25.8 25.4 25.0 24.7

Temperature oC 109 70 179 305 335 220

Dry gas rate Kg/hr 0 57704 57704 57704 57055 57055

Steam rate Kg/hr 388 1452 1452 1452 2101 2101

Liquid rate Kg/hr 927 0 0 0 0 0

Total rate Kg/hr 1315 59156 59156 59156 59156 59156


Steam to dry gas mole ratio n.a 0.01 0.01 0.01 0.02 0.02

Dry gas composition

N2 Mole % n.a 24.96 24.96 24.96 25.32 25.32

AR Mole % n.a 0.30 0.30 0.30 0.31 0.31

O2 Mole % n.a 0.00 0.00 0.00 0.00 0.00CH4 Mole % n.a 0.31 0.31 0.31 0.76 0.76

CO2 Mole % n.a 0.10 0.10 0.10 0.3 ppmv 0.3 ppmv

CO Mole % n.a 0.34 0.34 0.34 0.6 ppmv 0.6 ppmv

H2 Mole % n.a 73.99 73.99 73.99 73.61 73.61

NH3 Mole % n.a 0.00 0.00 0.00 0.00 0.00

Naphtha Mole % n.a 0.00 0.00 0.00 0.00 0.00

Sulphur Ppm wt n.a 0 0 0 0 0

Component flow rate

N2 Kgmol/hr 0.0 1637.5 1637.5 1637.5 1637.5 1637.5

AR Kgmol/hr 0.0 19.7 19.7 19.7 19.7 19.7

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 20.1 20.1 20.1 49.4 49.4

CO2 Kgmol/hr 0.0 6.7 6.7 6.7 0.0 0.0CO Kgmol/hr 0.0 22.6 22.6 22.6 0.0 0.0

H2 Kgmol/hr 0.0 4854.6 4854.6 4854.6 4759.7 4759.7

H20 Kgmol/hr 73.0 80.6 80.6 80.6 116.6 116.6

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 8.91 8.91 8.91 8.99 8.99

Enthalpy GCal/hr 0.35 -4.52 0.60 6.53 8.38 2.98



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Stream Number

Description

Phase

401/310 402 403/340 404 405 406 407

Converted

Gas from 1114

To 1517 A/B

Converted

Gas from 1115

To 1116

Converted

Gas from 1131

To 1554

Semi lean

Soln. From

1117 A to B

Lean Soln.

From 1117 A

To 1117B

Semi lean

From 1117B

To 1520

Lean Solution

From 117B

To 1521

VAPOR VAPOR VAPOR LIQUID LIQUID LIQUID LIQUID

*** HEAT & MATERIAL BALANCE OF SECTIONS 400 & 500 BY GIAMMARCO VETROCOKE ***

Pressure Kg/cm2 a 26.9 26.3 26.1 3.6 3.3 4.0 2.0

Temperature oC 173 126 70 124 128 108 111111

Dry gas rate Kg/hr 139454 139454 57704 0 0 0 0

Steam rate Kg/hr 71942 15502 1452 0 0 0 0

Liquid rate Kg/hr 0 0 0 949072 347656 1631520 339773

Total rate Kg/hr 211396 154956 59156 949072 347656 1631520 339773


Steam to dry gas mole ratio 0.47 0.10 0.01 n.a n.a n.a n.a

Dry gas composition

N2 Mole % 19.45 19.45 24.96 n.a n.a n.a n.a

AR Mole % 0.23 0.23 0.30 n.a n.a n.a n.a

O2 Mole % 0.00 0.00 0.00 n.a n.a n.a n.aCH4 Mole % 0.24 0.24 0.31 n.a n.a n.a n.a

CO2 Mole % 22.10 22.10 0.10 n.a n.a n.a n.a

CO Mole % 0.27 0.27 0.34 n.a n.a n.a n.a

H2 Mole % 57.71 57.71 73.99 n.a n.a n.a n.a

NH3 Mole % 0.00 0.00 0.00 n.a n.a n.a n.a

Component flow rate

N2 Kgmol/hr 1639.3 1639.3 1637.7 n.a n.a n.a n.a

AR Kgmol/hr 19.7 19.7 19.7 n.a n.a n.a n.a

O2 Kgmol/hr 0.0 0.0 0.0 n.a n.a n.a n.a

CH4 Kgmol/hr 20.1 20.1 20.1 n.a n.a n.a n.a

CO2 Kgmol/hr 1862.6 1862.6 6.7 n.a n.a n.a n.a

CO Kgmol/hr 22.6 22.6 22.6 n.a n.a n.a n.a

H2 Kgmol/hr 4864.6 4864.6 4854.6 n.a n.a n.a n.a

H20 Kgmol/hr 3993.5 860.5 80.6 n.a n.a n.a n.a NH3 Kgmol/hr 0.0 0.0 0.0 n.a n.a n.a n.a

Total Flow Rate Kgmol/hr 12422.5 9289.5 6642.1 n.a n.a n.a n.a

MW 17.02 16.68 8.91 n.a n.a n.a n.a

Enthalpy GCal/hr 58.62 17.99 4.08 n.a n.a n.a n.a

GV Solution

Carbonate Wt% 19.7 28.6 20.5 29.3

Bicarbonate Wt% 12.7 6.8 12.6 6.9

Fractional conversion % 0.31 0.14 0.3 0.14

Density Kg/m3 1218 1262 1233 1278



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Stream Number

Description

Phase

408 409 410 411 412 413 414

1117A

overhead

vapor to X-100

1117B overhead

vapor to

1551

X-100 outlet

To 1519

1118 overhead

to 1119

Wash water

From 1119

To 3210

CO2 from 1120

To Urea

Plant

Overhead cond.

From 1150

To 3221 A/B

VAPOR VAPOR VAPOR VAPOR LIQUID VAPOR LIQUID


Pressure Kg/cm2 a 2.1 1.3 1.4 1.4 1.6 1.3 1.3

Temperature oC 107 99 98 80 45 40 77

Dry gas rate Kg/hr 53885 27860 81745 81745 864 80881 0

Steam rate Kg/hr 25915 25362 32112 18397 0 2081 0

Liquid rate Kg/hr 0 0 0 0 872851 0 19165

Total rate Kg/hr 79800 53222 113857 100142 873715 82962 19165


Steam to dry gas mole ratio 1.17 2.21 0.95 0.55 n.a 0.06 n.a

Dry gas composition

N2 Mole % 0.08 0.09 0.09 0.09 n.a 0.09 n.a

AR Mole % 0.00 0.00 0.00 0.00 n.a 0.00 n.a

O2 Mole % 0.00 0.00 0.00 0.00 n.a 0.00 n.aCH4 Mole % 0.00 0.00 0.00 0.00 n.a 0.00 n.a

CO2 Mole % 99.40 99.38 99.39 99.39 n.a 99.39 n.a

CO Mole % 0.00 0.00 0.00 0.00 n.a 0.00 n.a

H2 Mole % 0.51 0.53 0.52 0.52 n.a 0.53 n.a

NH3 Mole % 0.00 0.00 0.00 0.00 n.a 0.00 n.a

Component flow rate

N2 Kgmol/hr 1.0 0.6 1.6 1.6 0.0 1.6 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 1223.4 632.5 1855.9 1855.9 19.6 1836.3 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 6.3 3.4 9.7 9.7 0.0 9.7 0.0

H20 Kgmol/hr 1438.5 1407.8 1782.5 1021.2 48451.4 115.5 1063.8

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Total Flow Rate Kgmol/hr 2669.3 2044.3 3649.8 2888.5 48471.0 1963.2 1063.8

MW 29.90 26.03 31.20 34.67 18.03 42.26 18.02

Enthalpy GCal/hr 17.84 16.78 22.19 12.97 39.32 1.94 1.47

GV Solution

Carbonate Wt%

Bicarbonate Wt%

Fractional convers ion %

Density Kg/m3


13/30


Stream Number

Description

Phase

415 416 417 418 419 420 42

Excess

overhead

Condensate to

Drain header

Condensate

From 3221 A/B

To 3206 A/B

Process

Condensate

From 1115

Condensate

From 1115 to

3603-001

Condensate

From 1115 to

3215-001/002

Overhead cond.

From 1118 to

3216-001/002

Semi lean

Solution from

3207 A/B to 1116

LIQUID LIQUID LIQUID LIQUID LIQUID LIQUID LIQUID


Pressure Kg/cm2 a 1.3 2.0 26.3 26.3 26.3 1.5 30.1

Temperature oC 77 77 126 126 126 80 102.5

Dry gas rate Kg/hr 0 0 0 0 0 0 0

Steam rate Kg/hr 0 0 0 0 0 0 0

Liquid rate Kg/hr 4353 14812 56440 39000 17440 13715 1631520

Total rate Kg/hr 4353 14812 56440 39000 17440 13715 1631520


Steam to dry gas mole ratio n.a n.a n.a n.a n.a n.a n.a

Dry gas composition

N2 Mole % n.a n.a n.a n.a n.a n.a n.aAR Mole % n.a n.a n.a n.a n.a n.a n.a

O2 Mole % n.a n.a n.a n.a n.a n.a n.a

CH4 Mole % n.a n.a n.a n.a n.a n.a n.a

CO2 Mole % n.a n.a n.a n.a n.a n.a n.a

CO Mole % n.a n.a n.a n.a n.a n.a n.a

H2 Mole % n.a n.a n.a n.a n.a n.a n.a

NH3 Mole % n.a n.a n.a n.a n.a n.a n.a

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

H20 Kgmol/hr 241.6 822.2 3132.9 2164.9 968.1 761.3 n.a

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 n.a

Total Flow Rate Kgmol/hr 241.6 822.2 3132.9 2164.9 968.1 761.3 n.a

MW 18.02 18.02 18.02 18.02 18.02 18.02 n.a

Enthalpy GCal/hr 0.33 1.14 7.15 4.94 2.20 1.10 n.a

GV Solution

Carbonate Wt% 20.5

Bicarbonate Wt% 12.6

Fractional conversion % 0.3

Density Kg/m3 1236


14/30


15/30


Stream Number

Description

Phase

481 483 484

Cooling

Water to

1519

Cooling

Water to

1520

Cooling

Water to

1521

LIQUID LIQUID LIQUID


Pressure Kg/cm2 a 5.0 5.0 5.0

Temperature oC 33 32 32

Dry gas rate Kg/hr 0 0 0

Steam rate Kg/hr 0 0 0

Liquid rate Kg/hr 677345 840840 762300

Total rate Kg/hr 677345 840840 762300

Dry Gas flow rate Nm3/hr 0 0 0

Steam to dry gas mole ratio n.a n.a n.a

Dry gas composition

N2 Mole % n.a n.a n.a

AR Mole % n.a n.a n.aO2 Mole % n.a n.a n.a

CH4 Mole % n.a n.a n.a

CO2 Mole % n.a n.a n.a

CO Mole % n.a n.a n.a

H2 Mole % n.a n.a n.a

NH3 Mole % n.a n.a n.a

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0

H20 Kgmol/hr 37598.9 46674.4 42314.7

NH3 Kgmol/hr 0.0 0.0 0.0

Total Flow Rate Kgmol/hr 37598.9 46674.4 42314.7

MW 18.02 18.02 18.02

Enthalpy GCal/hr 22.33 26.88 24.39

GV Solution

Carbonate Wt%

Bicarbonate Wt%

Fractional convers ion %

Density Kg/m3


16/30


Stream Number

Description

Phase

501 502 503 504 505 581

Lean solution

To 3608

Lean solution

From 3608

To 3650

Lean solution

to 1552

Air to 1206 Lean solution

To 3206 A/B

Cooling

Water

To 1552

LIQUID LIQUID LIQUID VAPOR LIQUID LIQUID


Pressure Kg/cm2 a 5.7 5.7 1.9 8.0 1.8 5.0

Temperature oC 70 70 70 40 70 32

Dry gas rate Kg/hr 0 0 0 39 0 0

Steam rate Kg/hr 0 0 0 0 0 0

Liquid rate Kg/hr 76200 40640 19200 0 339773 52550

Total rate Kg/hr 76200 40640 19200 39 339773 52550


Steam to dry gas mole ratio n.a n.a n.a 0.00 n.a n.a

Dry gas composition

N2 Mole % n.a n.a n.a 78.09 n.a n.a

AR Mole % n.a n.a n.a 0.93 n.a n.aO2 Mole % n.a n.a n.a 20.95 n.a n.a

CH4 Mole % n.a n.a n.a 0.00 n.a n.a

CO2 Mole % n.a n.a n.a 0.03 n.a n.a

CO Mole % n.a n.a n.a 0.00 n.a n.a

H2 Mole % n.a n.a n.a 0.00 n.a n.a

NH3 Mole % n.a n.a n.a 0.00 n.a n.a

Component flow rate

N2 Kgmol/hr n.a n.a n.a 1.0 n.a 0.0

AR Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

O2 Kgmol/hr n.a n.a n.a 0.3 n.a 0.0

CH4 Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

CO2 Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

CO Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

H2 Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

H20 Kgmol/hr n.a n.a n.a 0.0 n.a 2917.0

NH3 Kgmol/hr n.a n.a n.a 0.0 n.a 0.0

Total Flow Rate Kgmol/hr n.a n.a n.a 1.3 n.a 2917.0

MW n.a n.a n.a 28.94 n.a 18.02

Enthalpy GCal/hr n.a n.a n.a n.a 1.68

GV Solution

Carbonate Wt% 27 27 27 29.3

Bicarbonate Wt% 6.4 6.4 6.4 6.9

Fractional conversion % 0.14 0.14 0.14 0.14

Density Kg/m3 1270 1270 1270 1303


17/30



18/30


19/30

Stream Number

Description

Phase

608 609 610 611 612 613 614

Steam to 3707-

001 Comb. Air

fan turbine

Steam to

Semilean pump

turbine 3709-

001/002

Let down to

12 Kg/cm2a

header

Steam to BFW

pump turbine

3704-001/002

Steam to lean

pump turbine

3705-001/002

Steam to Aux.

Boiler fan drives

Steam to OGT-

101A CW pump

turbine

VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR

Pressure Kg/cm2 a 45.0 45.0 45.0 45.0 45.0 45.0 45.0

Temperature oC 365 365 365 365 365 365 365


Vapour rate Kg/hr 1360 33200 0 34250 12200 14700 10500

Total rate Kg/hr 1360 33200 0 34250 12200 14700 10500


Steam to dry gas mole ratio - - - - - - -

Dry gas composition

N2 Mole % - - - - - - -

AR Mole % - - - - - - -

O2 Mole % - - - - - - -CH4 Mole % - - - - - - -

CO2 Mole % - - - - - - -

CO Mole % - - - - - - -

H2 Mole % - - - - - - -

NH3 Mole % - - - - - - -

Naphtha Mole % - - - - - - -

Sulphur Ppm wt - - - - - - -

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 75.5 1842.9 0.0 1901.2 677.2 816.0 582.8

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 1.01 24.77 0.00 25.55 9.10 10.97 7.83



20/30

Stream Number

Description

Phase

615 616 617 618 619 620 621

Steam to

OGT-101B

CW pump

turbine

Steam to process

air compressor

turbine 3702

Steam for

miscellaneous

uses

Steam to fuel oil

pump turbine

3711

Steam to process

naphtha pump

turbine 3712

Steam to fuel

naphtha pump

turbine 3713

Import steam to

45 Kg/cm2 a

header


Pressure Kg/cm2 a 45.0 12.0 23.0 12.0 12.0 12.0 12.0

Temperature oC 365 278 278 278 278 278 365


Vapour rate Kg/hr 21500 56300 14100 1750 3650 1100 17400

Total rate Kg/hr 21500 56300 14100 1750 3650 1100 17400



Dry gas composition

N2 Mole % - - - - - - -

AR Mole % - - - - - - -

O2 Mole % - - - - - - -CH4 Mole % - - - - - - -

CO2 Mole % - - - - - - -

CO Mole % - - - - - - -

H2 Mole % - - - - - - -

NH3 Mole % - - - - - - -

Naphtha Mole % - - - - - - -


Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 75.5 1842.9 0.0 1901.2 677.2 816.0 582.8

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 1.01 24.77 0.00 25.55 9.10 10.97 7.83



21/30

Stream Number

Description

Phase

622 623 624 625 626 627/327 628/435

Desuperheated

let down steam to

12 Kg/cm2a

header

Let down from

12 Kg /Cm2a to

2.1 Kg /cm2a

Letdown from

12Kg/cm2a

header

to 3605-001

Atomizing &

service steam

from 3605-001

Steam from

OGT-101B to 2.1

Kg/cm2 a header

Steam to 1703 LP Steam from

1550 to 4 ata

header


Pressure Kg/cm2 a 12.0 12.0 12.0 12.0 4.0 2.1 4.0

Temperature oC 278 278 278 187 200 243 151


Vapor rate Kg/hr 0 0 8320 9100 0 10763 4110

Total rate Kg/hr 0 0 8320 9100 0 10763 4110



Dry gas composition

N2 Mole % - - - - - - -

AR Mole % - - - - - - -

O2 Mole % - - - - - - -CH4 Mole % - - - - - - -

CO2 Mole % - - - - - - -

CO Mole % - - - - - - -

H2 Mole % - - - - - - -

NH3 Mole % - - - - - - -

Naphtha Mole % - - - - - - -


Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 0.0 0.0 461.8 505.1 0.0 597.4 228.1

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 0.00 0.00 5.96 6.05 0.00 7.60 2.70



22/30

Stream Number

Description

Phase

629 630 631 632 633 634 635

Export steam

from 4 ata

header

Vent from

12 Kg/Cm2 a

header

Steam to 3706-

002 Flue Gas fan

turbine

Steam to 3707-002

Comb. Air fan

turbine

Leak steam from

BP turbines to 2.1

Kg/cm2 a header

Vent from 2.1

Kg/cm2 a header

Bypass of 3701

turbine


Pressure Kg/cm2 a 4.0 12.0 45.0 45.0 2.1 2.1 106.0

Temperature oC 193 278 365 365 243 243 482


Vapor rate Kg/hr 25610 6130 2360 1360 3000 1845 10000

Total rate Kg/hr 25610 6130 2360 1360 3000 1845 10000



Dry gas composition

N2 Mole % - - - - - - -

AR Mole % - - - - - - -

O2 Mole % - - - - - - -

CH4 Mole % - - - - - - -CO2 Mole % - - - - - - -

CO Mole % - - - - - - -

H2 Mole % - - - - - - -

NH3 Mole % - - - - - - -

Naphtha Mole % - - - - - - -


Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 1421.8 340.3 131.0 75.50 166.5 102.4 555.1

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 17.37 4.39 1.76 1.01 2.12 1.30 7.94



23/30

Stream Number

Description

Phase

636/224 640 641 642 643 644/324 645

Flash steam

from 1130

Water to

desuperheater

3605-003

Water to

desuperheater

3605-002

Water to

desuperheater

3605-001

Steam condensate

to polishing unit

HP BFW from

1553 (New BFW

preheater)

Blowdown from

1702

VAPOR LIQUID LIQUID LIQUID LIQUID LIQUID LIQUID

Pressure Kg/cm2 a 2.5 55.0 55.0 55.0 5.0 126.0 106.0

Temperature oC 127 109 109 109 57 218 314

Liquid rate Kg/hr 0 767 0 780 152850 139400 5000

Vapor rate Kg/hr 3108 0 0 0 0 0 0

Total rate Kg/hr 3108 767 0 780 152850 139400 5000



Dry gas composition

N2 Mole % - - - - - - -

AR Mole % - - - - - - -

O2 Mole % - - - - - - -

CH4 Mole % - - - - - - -CO2 Mole % - - - - - - -

CO Mole % - - - - - - -

H2 Mole % - - - - - - -

NH3 Mole % - - - - - - -

Naphtha Mole % - - - - - - -


Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 172.5 42.6 0.0 43.3 8484.6 7737.6 277.5

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 2.02 0.09 0.00 0.09 8.72 31.14 1.70



24/30

Stream Number

Description

Phase

681 682 683 684 685 686

CW to

Condenser of

3701

CW to

Condenser of

3702

CW to

Condenser of

3703

CW to

Condenser of

3706/3707-001

CW to

Condenser of

3706/3707-002

CW to

Condenser of

OGT-101A

LIQUID LIQUID LIQUID LIQUID LIQUID LIQUID

Pressure Kg/cm2 a 5.0 5.0 5.0 5.0 5.0 5.0

Temperature oC 32 32 32 32 32 32

Liquid rate Kg/hr 3700000 3219000 1230000 212700 212700 600000

Vapor rate Kg/hr 0 0 0 0 0 0

Total rate Kg/hr 3700000 3219000 123000 212700 212700 600000


Steam to dry gas mole ratio - - - - - -

Dry gas composition

N2 Mole % - - - - - -

AR Mole % - - - - - -

O2 Mole % - - - - - -

CH4 Mole % - - - - - -CO2 Mole % - - - - - -

CO Mole % - - - - - -

H2 Mole % - - - - - -

NH3 Mole % - - - - - -

Naphtha Mole % - - - - - -

Sulphur Ppm wt - - - - - -

Component flow rate

N2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

AR Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

H20 Kgmol/hr 205384.4 178684.4 68276.4 11806.8 11806.8 33305.6

NH3 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0

Naphtha Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0



MW 18.02 18.02 18.02 18.02 18.02 18.02

Enthalpy GCal/hr 118.40 103.01 39.36 6.81 6.81 19.20



25/30

Stream Number

Description

Phase

701/348 702/802 703/202 704 705 706 707

Make-up Syn.

Gas from 1143

Recovered H2

from PGIHRU to

3102

Recycle H2 to

naphtha

vaporizer

SGC Losses Make-up Syn.

Gas to loop

Syn . Gas to 1526 Syn. Gas from

1526 to 1527

VAPOR VAPOR VAPOR VAPOR VAPOR MIXED MIXED

*** HEAT & MATERIAL BALANCE OF SECTIONS 700 & 800 ARE BY AMMONIA CASALE S.A ***

Pressure Kg/cm2 a 24.2 48.5 42.0 - 202.2 202.2 200.8

Temperature oC 40 40 40 - 40 16.4 7.5

Dry gas rate Kg/hr 56931 697 790 199 66458 273955 266693

Steam rate Kg/hr 359 0 3 0 50 0 0

Liquid rate Kg/hr 0 0 0 0 0 38377 45638

Total rate Kg/hr 57289 697 793 199 66507 312331 312331


Steam to dry gas mole ratio 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Composition (Dry basis)

N2 Mole % 25.32 4.82 24.72 24.27 24.27 18.67 18.67AR Mole % 0.30 0.59 0.32 0.76 0.74 3.37 3.37

O2 Mole % 0.00 0.00 0.00 0.00 0.00 0.00 0.00

CH4 Mole % 0.76 0.39 0.76 1.66 1.68 7.33 7.33

CO2 Mole % 0,3 ppmv 0.00 0.00 0.3 ppmv 0.3 ppmv 0.00 0.00

CO Mole % 0.6 ppmv 0.00 0.00 0.6 ppmv 0.6 ppmv 0.00 0.00

H2 Mole % 73,61 94.20 74.20 72.81 72.86 56.01 56.01

NH3 Mole % 0.00 0.00 0.00 0.49 0.45 14.62 14.62

Sulphur Ppm wt 0 0.00 0.00 0 0 0 0

Component flow rate

N2 Kgmol/hr 1634.1 9.5 22.5 5.4 1810.1 5127.1 5127.1

AR Kgmol/hr 19.7 1.2 0.3 0.2 55.4 924.5 924.5

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 49.3 0.8 0.7 0.4 125.1 2013.5 2013.5

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 4749.8 185.1 67.6 16.2 5434.4 15385.2 15385.2

H20 Kgmol/hr 19.9 0.0 0.2 0.0 2.8 2.8 2.8

NH3 Kgmol/hr 0.0 0.0 0.0 0.1 33.8 4016.6 4016.6



MW 8.85 3.55 8.69 8.93 8.91 11.37 11.37

Enthalpy GCal/hr 0.67 0.02 0.01 - 0.91 -14.51 -18.36



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Stream Number

Description

Phase

708 709 710 711 712 713 714

Recirc. Gas

from 1122 to

1525

Feed to

circulator 3103

Circulator

discharge to 1121

Syn. Gas from

1121 to 1523

Syn. Gas from

1523 to 1524

Syn. Gas from

1524 to 1525

Syn. Gas from

1525 to 1526

VAPOR VAPOR VAPOR VAPOR VAPOR MIXED MIXED


Pressure Kg/cm2 a 199.2 197.8 208.7 206.0 204.7 203.4 202.2

Temperature oC -2.5 30 40 257.3 123.4 35.5 20.3

Dry gas rate Kg/hr 259815 259815 249950 249952 249952 219655 201478


Liquid rate Kg/hr 0 0 0 0 0 30297 44346

Total rate Kg/hr 259815 259815 249950 249952 249952 249952 245824


Steam to dry gas mole ratio 0.00 0.00 0.00 0.00 0.00 0.00 0.00

Composition (Dry Basis)

N2 Mole % 21.01 21.01 21.01 16.62 16.62 16.62 16.58AR Mole % 3.78 3.78 3.78 4.35 4.35 4.35 4.34

O2 Mole % 0.00 0.00 0.00 0.00 0.00 0.00 0.00

CH4 Mole % 8.22 8.22 8.22 9.46 9.46 9.46 9.44

CO2 Mole % 0.00 0.00 0.00 0.00 0.00 0.00 0.00

CO Mole % 0.00 0.00 0.00 0.00 0.00 0.00 0.00

H2 Mole % 63.03 63.03 63.03 49.86 49.86 49.86 49.73

NH3 Mole % 3.96 3.96 3.96 19.70 19.70 19.70 19.91

Sulphur Ppm wt 0 0 0 0 0 0 0

Component flow rate

N2 Kgmol/hr 5120.4 5120.4 4926.0 3384.8 3384.8 3384.8 3317.0

AR Kgmol/hr 921.8 921.8 886.8 886.8 886.8 886.8 869.1

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 2002.9 2002.9 1926.8 1926.8 1926.8 1926.8 1888.4

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 15361.2 15361.2 14777.9 10154.3 10154.3 10154.3 9950.9

H20 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

NH3 Kgmol/hr 966.1 966.1 929.4 4011.8 4011.8 4011.8 3982.7



MW 10.66 10.66 10.66 12.27 12.27 12.27 12.29

Enthalpy GCal/hr -6.03 -0.06 1.74 35.42 12.60 -8.89 -14.82



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Stream Number

Description

Phase

715/801 716/803 717 718 719 731/321 732/322

Purge gas to

PGHRU

Liquid NH3 from

PGHRU to 1123

Liquid NH3 from

1122 to 1123

Liquid NH3

product from

1123

Vapor from 1123

to NH3 absorber

Deaerated BFW

from HP BFW

pump to 1523

BFW from 1523

to 1515 + 1539

VAPOR LIQUID LIQUID LIQUID LIQUID LIQUID LIQUID

*** HEAT & MATERIAL BALANCE OF SECTION 700 & 800 ARE BY AMMONIA CASALE S.A ***

Pressure Kg/cm2 a 202.2 21.1 199.2 21.1 21.1 127.0 126.5

Temperature oC 20.3 -3.3 -2.5 -3.3 -3.3 109 181

Dry gas rate Kg/hr 4128 0 -0 0 616 0 0


Liquid rate Kg/hr 0 491 52516 52390 0 300400 300400

Total rate Kg/hr 4128 491 52516 52390 616 300400 300400

Dry Gas flow rate Nm3/hr 7987 0 -0 0 1129 0 0

Steam to dry gas mole ratio 0.00 n.a n.a n.a 0.00 n.a n.a


N2 Mole % 19.01 0.03 0.22 0.02 12.13 n.a n.aAR Mole % 4.98 0.00 0.09 0.01 4.62 n.a n.a

O2 Mole % 0.00 0.00 0.00 0.00 0.00 n.a n.a

CH4 Mole % 10.78 0.03 0.34 0.01 20.23 n.a n.a

CO2 Mole % 0.00 0.00 0.00 0.00 0.00 n.a n.a

CO Mole % 0.00 0.00 0.00 0.00 0.00 n.a n.a

H2 Mole % 57.08 0.03 0.78 0.02 46.53 n.a n.a

NH3 Mole % 8.15 99.90 98.58 99.93 16.49 n.a n.a

Sulphur Ppm wt 0 0 0 0.00 0 n.a n.a

Component flow rate

N2 Kgmol/hr 67.8 0.0 6.7 0.6 6.1 0.0 0.0

AR Kgmol/hr 17.7 0.0 2.6 0.3 2.3 0.0 0.0

O2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CH4 Kgmol/hr 38.4 0.0 10.6 0.5 10.2 0.0 0.0

CO2 Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0 0.0 0.0 0.0

H2 Kgmol/hr 203.4 0.0 24.0 0.6 23.4 0.0 0.0

H20 Kgmol/hr 0.0 0.0 2.8 2.8 0.0 16674.1 16674.1

NH3 Kgmol/hr 29.1 28.8 3050.5 3071.0 8.3 0.0 0.0



MW 11.58 17.03 16.96 17.03 12.24 18.02 18.02

Enthalpy GCal/hr 0.05 -0.02 -16.16 -16.22 -0.01 32.66 55.49


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Stream Number

Description

Phase

781

Cooling Water

to 1524

LIQUID


Pressure Kg/cm2 a 5.0

Temperature oC 32

Dry gas rate Kg/hr 0

Steam rate Kg/hr 0

Liquid rate Kg/hr 1791200

Total rate Kg/hr 1791200

Dry Gas flow rate Nm3/hr 0

Steam to dry gas mole ratio n.a


N2 Mole % n.a

AR Mole % n.a

O2 Mole % n.a

CH4 Mole % n.a

CO2 Mole % n.a

CO Mole % n.a

H2 Mole % n.a

NH3 Mole % n.a

Sulphur Ppm wt n.a

Component flow rate

N2 Kgmol/hr 0.0

AR Kgmol/hr 0.0

O2 Kgmol/hr 0.0

CH4 Kgmol/hr 0.0CO2 Kgmol/hr 0.0

CO Kgmol/hr 0.0

H2 Kgmol/hr 99422.7

H20 Kgmol/hr 0.0

NH3 Kgmol/hr 0.0

Sulphur Kgmol/hr 0

Total flow rate Kgmol/hr 99422.7

MW 18.02

Enthalpy GCal/hr 57.3


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Stream Number

Description

Phase

801/715 802/702 803/716 804/210

Purge gas

from Syn.

Loop

Recovered H2

from PGHRU to

3102

Liquid NH3 from

PGHRU to 1123

Tail gas to

Primary reformer

fuel system

VAPOR VAPOR LIQUID VAPOR


Pressure Kg/cm2 a 202.2 48.5 21.1 2.3

Temperature oC 20.3 40 -3.3 40

Dry gas rate Kg/hr 4128 697 0 2940

Steam rate Kg/hr 0 0 0 0

Liquid rate Kg/hr 0 0 491 0

Total rate Kg/hr 4128 697 491 2940

Dry Gas flow rate Nm3/hr 7987 4404 0 2938

Steam to dry gas mole ratio 0.0 0.0 0.0 0.0


N2 Mole % 19.01 4.82 0.03 44.45

AR Mole % 4.98 0.59 0.00 12.66

O2 Mole % 0.00 0.00 0.00 0.00

CH4 Mole % 10.78 0.39 0.03 28.71

CO2 Mole % 0.00 0.00 0.00 0.00

CO Mole % 0.00 0.00 0.00 0.00

H2 Mole % 57.08 94.20 0.03 13.96

NH3 Mole % 8.15 0.00 99.90 0.21

Sulphur Ppm wt 0 0 0 0

Component flow rate

N2 Kgmol/hr 67.8 9.5 0.0 58.3

AR Kgmol/hr 17.7 1.2 0.0 16.6

O2 Kgmol/hr 0.0 0.0 0.0 0.0CH4 Kgmol/hr 38.4 0.8 0.0 37.6

CO2 Kgmol/hr 0.0 0.0 0.0 0.0

CO Kgmol/hr 0.0 0.0 0.0 0.0

H2 Kgmol/hr 203.4 185.1 0.0 18.3

H20 Kgmol/hr 0.0 0.0 0.0 0.0

NH3 Kgmol/hr 29.1 0.0 28.8 0.3

Sulphur Kgmol/hr 0 0 0 0

Total flow rate Kgmol/hr 356.4 196.5 28.8 131.1

MW 11.58 3.55 17.03 22.43

Enthalpy GCal/hr 0.05 0.02 -0.02 0.01


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Documents

Ammonia - Heat & Mat. Balance