Heat Duty 3993x

REFORMER HEAT DUTY

H2 N2 CH4 C2H6 C3H8 C4H10 Enthalpy of gases Kcal/Kg.Mole CO Values of constants A -2.11E+03 -1.98E+03 -1.96E+04 -2.21E+04 -3.37E+04 -3.37E+04 -2.84E+04 B 7.21E+00 6.46E+00 3.36E+00 -1.04E-01 -5.74E-01 -5.74E-01 6.27E+00 C -5.56E-04 5.18E-04 8.50E-03 2.41E-02 4.67E-02 4.67E-02 8.99E-04 D 4.85E-07 2.03E-07 -7.11E-07 -7.78E-06 -1.60E-05 -1.60E-05 5.09E-09 E -8.19E-11 -7.65E-11 -2.55E-10 1.14E-09 2.39E-09 2.39E-09 -4.14E-11 Enthalpy of gases at I/L Kcal/Kg.mole Enthalpy of gases at O/L Kcal/Kg.mole Enthalpy of cond. Kcal/KgMole

H-201 INLET TEMP. OC O

H-201 OUTLET TEMP. C

Dry Gas composition at Reformer. I/L Dry Gas composition at Reformer. O/L M.W OF REFORMER O/L GAS M.W OF REFORMER O/L DRY GAS M.W OF REFORMER I/L DRY GAS M.W OF REFORMER I/L GAS

4034 6090 -67698

-10836 -5920

-8395 -31

-7915 7577

-7915 7577

-22228 -19976

-87688 -83986

H2

N2

CH4

C2H6

C3H8

C4H10

CO

CO2

8.9 66.83 14.00 10.90 15.89 17.28

3.84 0.89

84.93 6.37

0.0300 0.0000

0.0000 0.0000

0.0000 0.0000

0.0000 19.4700

2.2800 6.4400

600 884

100.0

KG MOLES/Hr

1,651.96 3,210.35 6,051.13 4,680.39 .

H2O

-9.63E+04 -6.01E+04 5.85E+00 7.42E+00 6.34E-03 6.31E-04 -2.29E-06 5.89E-07 3.40E-10 -1.52E-10

4149 6369

NM3/HR NG FLOW AT reformer I/LNM /Hr 37,029 STEAM FLOW AT reformer I/LNM3/Hr 71,960 3 reformer O/L DRY GAS FLOW NM /Hr 135636 REFORMER O/L STEAM FLOW NM3/Hr 104911 Reformer Heat Duty M Kcal/Hr -80.41 3

CO2

-52814 -50005

H2 NATURAL GAS I/L PR PR EXIT GAS RECYCLE GAS

NATURAL GAS I/L PR RECYCLE GAS FLOW STEAM FLOW P/R IN PRESS Pdi P/R EXIT PRESS. TOTAL C IN PR TOTAL O IN PR P/R EXIT GAS FLOW TOTAL O OUT PR STEAM OUT PR Pe Kwg Twg Kms Tms APPROACH

N2

0 65.39 3907.9072 72.17

CH4

CO

0.1 85.9 0.36 13.39 8.09 21.514706 800.227528 483.48325 26.06 1.18

FLOW PRESS TEMP MW 44400 39.8 29.12 1170 34 3.05 30.95 2046.89 7144.78 5976.31 2009.83 5134.95 30.903382 1.2012966 760 0.0184098 754 6.0000

DELTA P CALCULATION FEED

CO2

DESIGN REC. H2

STEAM

5.35 12.77 763.17442

C3H8

C4H10

AR

7.69

0.82

0.05

0

0

0 0.57

Z 18.86

C2H6

CF CFLOW KG/MOLE 0.918 0.9451892 41966.4 1872.33 1170 52.20 125000 6944.44

CH4 C2 C3 C4 CO CO2 H2 N2 O2 Ar Mw

98.39 1.4 0.1

0.01 0.1 16.28 41021 29794.057 1830.1018 140779.22

0.9

FEED REC H2 STEAM

35301.925 478.59798 125000 160780.52

Pdi

2.3383531

74.08 24.72 0.3 8.71 18.016 2018 FLOW,NM3/HR 784.16657 110201 KG/HR 90.030605 6116.84059 KGMOLES/HR TOTAL MASS FLOW

CNO. Mw 1.0929 18.85454 0.3425 11.44975 0.0118

9.168628

H2 NATURAL GAS I/L PR PR EXIT GAS

CH4

0 0.1 65.39 0.36 3907.91 21.5147 72.17 26.06

RECYCLE GAS

NATURAL GAS I/L PR RECYCLE GAS FLOW STEAM FLOW P/R IN PRESS Pdi P/R EXIT PRESS. TOTAL C IN PR TOTAL O IN PR P/R EXIT GAS FLOW TOTAL O OUT PR STEAM OUT PR Pe Kwg Twg

N2

CO

CO2

C2H6 C3H8 85.9 5.35 7.69 0.82 13.39 8.09 12.77 800.228 483.483 763.174 0 0 1.18

FLOW PRESS TEMP MW Z CF CFLOW 44400 39.8 29.12 18.86 0.918 0.94519 41966.4 1170 1170 125000 34 3.05 30.95 2046.89 7144.78 5976.31 2009.83 5134.95 30.9034 1.2013 760

Kms Tms APPROACH

0.01841 754 6.0000

DELTA P CALCULATION DESIGN FEED REC. H2 STEAM 98.39 0.9 1.4 0.1

0.01 0.1

74.08 24.72

0.3 16.28 8.71 41021 2018 29794.1 784.167

CH4 FEED C2 REC H2 C3 STEAM C4 CO CO2 Pdi H2 N2 O2 Ar 18.016 Mw FLOW,NM3/HR 110201 KG/HR

35301.9 478.598 125000 160781 2.33835

1830.1 90.0306 6116.84 KGMOLES/HR 140779 TOTAL MASS FLOW

C4H10 AR 0.05

CNO. Mw 1.0929 18.8545 0.3425 11.4497

0 0.57

KG/MOLE 1872.33 52.20 6944.44

0.0118 9.16863