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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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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
Liquid rate Kg/hr 0 0 0 9836 0 0 0
Total rate Kg/hr 199389 199389 2940 9836 183619 199310 199310
Dry Gas flow rate Nm3/hr 164816 164816 2938 0 138678 131317 131317
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
Total flow rate Kgmol/hr 11756.3 11756.3 131.1 98.0 6433.4 7074.8 7074.8
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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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
Liquid rate Kg/hr 0 0 0 0 0 17440 0
Total rate Kg/hr 199389 199390 199390 199390 199390 17440 216832
Dry Gas flow rate Nm3/hr 164816 181982 181982 185408 185408 0 185408
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 11756.3 11756.3 11756.3 11756.3 11756.3 968.1 12724.5
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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Dry Gas flow rate Nm3/hr 188687 188687 188687 0 0 0 0
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 12724.5 12724.5 12422.5 302.0 16316.7 16674.0 16674.0
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Dry Gas flow rate Nm3/hr 0 147116 147116 147116 144937 144937
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
Sulphur Kgmol/hr 0 0 0 0 0 0
Total flow rate Kgmol/hr 73.0 6641.9 6641.9 6641.9 6583.1 6583.1
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Dry Gas flow rate Nm3/hr 188687 188687 147116 0 0 0 0
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
*** HEAT & MATERIAL BALANCE OF SECTIONS 400 & 500 BY GIAMMARCO VETROCOKE ***
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
Dry Gas flow rate Nm3/hr 27401 14170 41571 41571 0 41134 0
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
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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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
*** HEAT & MATERIAL BALANCE OF SECTIONS 400 & 500 BY GIAMMARCO VETROCOKE ***
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
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0 0
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
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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
Stream Number
Description
Phase
481 483 484
Cooling
Water to
1519
Cooling
Water to
1520
Cooling
Water to
1521
LIQUID LIQUID LIQUID
*** HEAT & MATERIAL BALANCE OF SECTIONS 400 & 500 BY GIAMMARCO VETROCOKE ***
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
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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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
*** HEAT & MATERIAL BALANCE OF SECTIONS 400 & 500 BY GIAMMARCO VETROCOKE ***
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
Dry Gas flow rate Nm3/hr 0 0 0 30 0 0
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
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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Liquid rate Kg/hr 0 0 0 0 0 0 0
Vapour rate Kg/hr 1360 33200 0 34250 12200 14700 10500
Total rate Kg/hr 1360 33200 0 34250 12200 14700 10500
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0 0
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 75.5 1842.9 0.0 1901.2 677.2 816.0 582.8
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
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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
VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR
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
Liquid rate Kg/hr 0 0 0 0 0 0 0
Vapour rate Kg/hr 21500 56300 14100 1750 3650 1100 17400
Total rate Kg/hr 21500 56300 14100 1750 3650 1100 17400
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0 0
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 75.5 1842.9 0.0 1901.2 677.2 816.0 582.8
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
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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
VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR
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
Liquid rate Kg/hr 0 0 0 0 0 0 0
Vapor rate Kg/hr 0 0 8320 9100 0 10763 4110
Total rate Kg/hr 0 0 8320 9100 0 10763 4110
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0 0
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 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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 0.0 0.0 461.8 505.1 0.0 597.4 228.1
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
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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
VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR VAPOR
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
Liquid rate Kg/hr 0 0 0 0 0 0 0
Vapor rate Kg/hr 25610 6130 2360 1360 3000 1845 10000
Total rate Kg/hr 25610 6130 2360 1360 3000 1845 10000
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0 0
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 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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 1421.6 340.3 131.0 75.5 166.5 102.4 555.1
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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 flow rate Nm3/hr 0 0 0 0 0 0 0
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 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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 172.5 42.6 0.0 43.3 8484.6 7737.6 277.5
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
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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
Dry Gas flow rate Nm3/hr 0 0 0 0 0 0
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
Sulphur Kgmol/hr 0 0 0 0 0 0
Total flow rate Kgmol/hr 205384.4 178684.4 68276.4 11806.8 11806.8 33305.6
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Dry Gas flow rate Nm3/hr 144635 4404 2043 500 167178 565033 555368
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 6472.9 196.5 91.3 22.3 7461.5 27469.7 27469.7
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
*** HEAT & MATERIAL BALANCE OF SECTIONS 700 & 800 ARE BY AMMONIA CASALE S.A ***
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
Steam rate Kg/hr 0 0 0 0 0 0 0
Liquid rate Kg/hr 0 0 0 0 0 30297 44346
Total rate Kg/hr 259815 259815 249950 249952 249952 249952 245824
Dry Gas flow rate Nm3/hr 546271 546271 525530 456441 456441 416372 389855
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 24372.3 24372.3 23446.9 20364.5 20364.5 20364.5 20008.1
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
Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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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
Steam rate Kg/hr 0 0 0 0 0 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
Composition (Dry basis)
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
Sulphur Kgmol/hr 0 0 0 0 0 0 0
Total flow rate Kgmol/hr 356.4 28.8 3097.3 3075.8 50.4 16674.1 16674.1
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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
Stream Number
Description
Phase
781
Cooling Water
to 1524
LIQUID
*** HEAT & MATERIAL BALANCE OF SECTIONS 700 & 800 ARE BY AMMONIA CASALE S.A ***
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
Composition (Dry basis)
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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Project: SPIC AMMONIA REVAMP ****** HEAT AND MATERIAL BALANCE ******
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
*** HEAT & MATERIAL BALANCE OF SECTIONS 700 & 800 ARE BY AMMONIA CASALE S.A ***
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
Composition (Dry basis)
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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