Hitung.xls
34
Flowrate HC 31190 m3/hari densitas HC 13.62 kg/m3 P 37 bar Tfeed HC = 187 1321.2 Tsteam 350 3102 rasio steam/HC 3.5 massa HC 17706.141 kg/jam massa steam 61971.494 kg steam/jam Total Qin 215628928.167 kJ/jam Tmix 311 oC DH HC 1681.620 kj/kg HC DH Steam 2999.023 kJ/kg Steam Total 215628928.167 0 1. Reformer Tmix 470 oC DH HC 2146.48 kJ/kg HC DH steam 3403 kJ/kg steam total massa 79677.635 kg/jam Total, Qin 248894942.863978 kJ/jam T reaksi 800 oC Reaksi : CH4 + H2O === CO + 3 H2 DHR1 206160 CO + H2O === CO2 + H2 DHR2 -41150 u/ 1 kmol CH4 e1 0.63 kmol e2 0.533 kmol Qr = e1 (-DHR1) + e2 (-DHR2) = -107947.850 kJ/kmol CH4 -6746.741 kJ/kg CH4 = -119458741.817 kJ/jam Produk pada T 800 oC Cp produk 9.573 kJ/kg oC Massa produk 79677.635 kg/jam Qout 591134351.226 kJ/jam Kebutuhan panas, QA = Qin + Qr - Qout 342246155.102 Pemanas menggunakan pembakaran fuel gas (asumsi CH4) LHV = 50032.26 kJ/kg fuel Qc = 50032.26 kJ/kg fuel udara pembakaran dengan 100% excess o C DH HC o C DH Steam
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Transcript of Hitung.xls
Flowrate HC 31190 m3/haridensitas HC 13.62 kg/m3
P 37 bar
Tfeed HC = 187 1321.2 kj/kg HC
Tsteam 350 3102 kJ/kg Steamrasio steam/HC 3.5massa HC 17706.141 kg/jammassa steam 61971.494 kg steam/jamTotal Qin 215628928.167 kJ/jam 20
40Tmix 311 oC 37DH HC 1681.619 kj/kg HCDH Steam 2999.023 kJ/kg Steam 20Total 215628928.167 0 40
371. ReformerTmix 470 oC 450DH HC 2146.48 kJ/kg HC 500DH steam 3403 kJ/kg steam 311total massa 79677.635 kg/jamTotal, Qin 248894942.863978 kJ/jam
T reaksi 800 oCReaksi :CH4 + H2O === CO + 3 H2 DHR1 206160 kJ/kmol CH4CO + H2O === CO2 + H2 DHR2 -41150 kJ/kmol CO
u/ 1 kmol CH4e1 0.63 kmole2 0.533 kmol
Qr = e1 (-DHR1) + e2 (-DHR2) = -107947.850 kJ/kmol CH4-6746.741 kJ/kg CH4
= -119458741.817 kJ/jam
Produk pada T 800 oCCp produk 9.573 kJ/kg oCMassa produk 79677.635 kg/jam
Qout 591134351.226 kJ/jam
Kebutuhan panas, QA = Qin + Qr - Qout 342246155.102 kJ/jam
Pemanas menggunakan pembakaran fuel gas (asumsi CH4)LHV = 50032.26 kJ/kg fuelQc = 50032.26 kJ/kg fuel
udara pembakaran dengan 100% excess
oC DH HCoC DH Steam
udara teoritis = 0.595 kmol udara/kg Fuel17.238 kg udara / kg fuel
untuk udara excess = 34.476 kg udara/kg fuel
udara masuk kompresor pada kondisi ambientT 303 KP 1.013 bar
rasio kompresi 10Pout kompresor 10.1325 bar
untuk udara , k = 1.387Tout = Tin (rc)^(k-1/k)
576 K303 oC
efisiensi kompres 85%Tout actual 624 oC 351Cp udara 1.029 kJ/kg KQudara 21258.5772531742 kJ/kg fuel
T fuel in 303 KCp 7.27 kJ/kg KQfuel 36.35 kJ/kg fuel
Total Qin 21294.9272531742 kJ/kg fuel
T flue gas 700 oCCp flue gas 1.075 kJ/kg Km flue gas = 35.476 kg flue gas/kg fuelQ flue 25742.411 kJ/kg fuelasumsi Qloss = 5 2279.239 kJ/kg fuelQA = Qin + Qc - Qout - Qloss
43305.538 kJ/kg fuel
kebutuhan fuel 7903.058 kg/jam 13921.518 m3/jamkebutuhan udara 272467.316 kg/jam 0.446massa flue gas 280370.374 kg/jamQflue gas 203443752.359 kJ/jam
2. Combustion chamberT udara bypass 624 oCCp 1.029 kJ/kg Kperbandingan udara bypass/udara ke furnace reformer 1.4massa udara by pass = 381454.243 kg/jamQ udara bypass 235210862.101 kJ/jam
Q total mix udara masuk combustion chamber
438654614.460 kJ/jamCp mix 1.065 kJ/kg Kmassa mix 661824.616 kg/jamTmix 647 oC
Total udara dalam mix 517687.901 kg/jam
teoritis udara/fuel 17.238 kg udara/kg fuel
untuk udara dengan 300% excess 51.714 kg udara/kg fuel
massa fuel in 0.019 kg fuel/kg udara10010.540 kg/jam
T fuel in 303 KCp 7.270 kJ/kg KQfuel 36.350 kJ/jam
Q total in CC 438654650.810 kJ/jam
LHV = 50032.260 kJ/kg fuelQc = 500849915.731 kJ/jam
Qout = 939504566.540 kJ/jam
m flue gas 671835.156 kg/jamCp flue gas 1.104 kJ/kg KT flue gas 1292 oC
1565 K
Turbin
Pout turbin 2 barPout/Pin 0.197
1.293Tout Turbin = Tin (Pout/Pin)^(k-1/k)
1083 K810 oC
Cp flue gas 1.082 kJ/kg KQout turbin 570839418.148 kJ/jam
Wt 349943137.103 kJ/jam
kompresormassa udara 653921.559 kg/jamCp udara 1.029 kJ/kg KTin 303 KTout 576 K
Wc 183733035.056 kJ/jam
Wnet 166210102.05 kJ/jam46169.47 kJ/s
46.17 MW 17913.597HE-01 4.9759991738829 kg/sQA = 33266014.697 kJ/kg HC
Qout flue gas 537573403.451005 kJ/kg HCmassa 671835.156 kg/jam
Cp 1.204 kJ/kg KTout 690 oC
963 K
HRSGBeda temperatur pada titik pinch 90 oCP steam 37 barT saturated 246 oCHl 1065.15 kJ/kg
Steam yang dihasilkan pada T 350 oCHv 3102 kJ/kg
Temperatur fluegas diatas T saturated = 336 oC
Qs' 286008760.414 kJ/jamSteam yang dihasilkan, ms = Qs'/(Hv-Hl)
140417.193 kg/jam 61971.4940291552.27
Temperatur air feed boiler = 42oCHl (42oC) 185.75 kJ/kg
Qs = ms (Hv - Hl(42oC))409491640.307 kJ/jam
Temperatur flue gas keluar HRSGTf = Tin - Qs/(mg Cp)Tin 690 oCCp 1.104 kJ/kg Kmg 671835.156 kg/jamTf = 137 oC
sisa steam 78445.699 kg/jam
Steam Turbineh3 3102 kJ/kg 536.78756476684 662s3 6.6201
T keluar kondens 50 oC 122 1024.1 1.58110625907h1 209.127 kJ/kg 2382.0566 6.62009190672
s1 0.7030 kJ/kg K
h5 2382.057 kJ/kgs5 8.075 kJ/kg K
h4s = 1953.313 kJ/kgefisiensi turbine 82%
941.923 kJ/kg
Wt 73889823.169 kJ/jam20.525 MW
Q total campuran fresh feed dengan dari kon 24194930.57565 kJ/jamHl 172.31 kJ/kgT 42 oC
eff reformer 86.56%eff gas turbine 33.19%eff steam turbine 32.30%Total daya yang dihasilkan 66.694 MW 240099925.216Total bahan bakar yang digunakan 17913.597 kg/jamLHV 50032.260 kJ/kgeff daya 26.79%Panas yang dapat diambil 375512169.799 kJ/jam 409491640.307eff panas 41.90% 33266014.697Jumlah daya dan panas yang dihasilkan 615612095.015 kJ/jam 342246155.102eff total 68.69%
DH =
3358 300 1650.733331 450 2088.16
3335.05 311 1682.808
34673445
3448.3
3448.33335.05
3763.135
r 20.75953 kg/m3V 45554 m3/h
12.65389 m3/sm 262.6888 kg/s
945.6797
8.6065
36 1057.638 1072.737 1065.15
530 1.6057540 1.6009
536.7876 1.602442
530 1.5514540 1.5759
536.7876 1.56803
700 1.56803600 1.602442662 1.581106
kJ/jam
Flowrate HC 31190 m3/haridensitas HC 13.62 kg/m3
P 37 bar
Tfeed HC = 187 1321.2 kj/kg HC
Tsteam 350 3102 kJ/kg Steamrasio steam/HC 3.5massa HC 17706.141 kg/jammassa steam 61971.494 kg steam/jamTotal Qin 215628928.167 kJ/jam 20
40Tmix 311 oC 37DH HC 1681.619 kj/kg HCDH Steam 2999.023 kJ/kg Steam 20Total 215628928.167 0 40
371. ReformerTmix 470 oC 450DH HC 2146.48 kJ/kg HC 500DH steam 3403 kJ/kg steam 311total massa 79677.635 kg/jamTotal, Qin 248894942.863978 kJ/jam
T reaksi 800 oCReaksi :CH4 + H2O === CO + 3 H2 DHR1 206160 kJ/kmol CH4CO + H2O === CO2 + H2 DHR2 -41150 kJ/kmol CO
u/ 1 kmol CH4e1 0.63 kmole2 0.533 kmol
Qr = e1 (-DHR1) + e2 (-DHR2) = -107947.850 kJ/kmol CH4-6746.741 kJ/kg CH4
= -119458741.817 kJ/jam
Produk pada T 800 oCCp produk 9.573 kJ/kg oCMassa produk 79677.635 kg/jam
Qout 591134351.226 kJ/jam
Kebutuhan panas, QA = Qin + Qr - Qout 342246155.102 kJ/jam
Pemanas menggunakan pembakaran fuel gas (asumsi CH4)LHV = 50032.26 kJ/kg fuelQc = 50032.26 kJ/kg fuel
udara pembakaran dengan 100% excessudara teoritis = 0.595 kmol udara/kg Fuel
17.238 kg udara / kg fuel
untuk udara excess = 34.476 kg udara/kg fuel
oC DH HCoC DH Steam
udara masuk kompresor pada kondisi ambientT 303 KP 1.013 bar
rasio kompresi 10Pout kompresor 10.1325 bar
untuk udara , k = 1.387Tout = Tin (rc)^(k-1/k)
576 K303 oC
efisiensi kompres 85%Tout actual 624 K 351 oCCp udara 1.029 kJ/kg KQudara 21258.5772531742 kJ/kg fuel
T fuel in 303 KCp 7.27 kJ/kg KQfuel 36.35 kJ/kg fuel
Total Qin 21294.9272531742 kJ/kg fuel
T flue gas 600 oCCp flue gas 1.075 kJ/kg Km flue gas = 35.476 kg flue gas/kg fuelQ flue 21928.720 kJ/kg fuelasumsi Qloss = 5 2469.923 kJ/kg fuelQA = Qin + Qc - Qout - Qloss
46928.544 kJ/kg fuel
kebutuhan fuel 7292.921 kg/jam 12846.741 m3/jamkebutuhan udara 251432.129 kg/jam 0.412massa flue gas 258725.050 kg/jamQflue gas 159924421.296 kJ/jam
2. Combustion chamberT udara bypass 351 oCCp 1.029 kJ/kg Kperbandingan udara bypass/udara ke furnace reformer 0.6567619908936massa udara by pass = 165131.065 kg/jamQ udara bypass 55434365.091 kJ/jam
Q total mix udara masuk combustion chamber215358786.387 kJ/jam
Cp mix 1.065 kJ/kg Kmassa mix 423856.115 kg/jamTmix 502 oC
Total udara dalam mix 290847.130 kg/jam
teoritis udara/fuel 17.238 kg udara/kg fuel
untuk udara dengan 300% excess 51.714 kg udara/kg fuel
massa fuel in 0.019 kg fuel/kg udara5624.116 kg/jam
T fuel in 303 KCp 7.270 kJ/kg KQfuel 36.350 kJ/jam
Q total in CC 215358822.737 kJ/jam
LHV = 50032.260 kJ/kg fuelQc = 281387222.491 kJ/jam
Qout = 496746045.228 kJ/jam
m flue gas 429480.231 kg/jamCp flue gas 1.104 kJ/kg KT flue gas 1073 oC
1346 K
Turbin
Pout turbin 2 barPout/Pin 0.197
1.293Tout Turbin = Tin (Pout/Pin)^(k-1/k)
932 K659 oC
Cp flue gas 1.082 kJ/kg KQout turbin 294454237.973 kJ/jam
Wt 192392882.441 kJ/jam
kompresormassa udara 416563.194 kg/jamCp udara 1.029 kJ/kg KTin 303 KTout 576 K
Wc 117042203.231 kJ/jam
Wnet 75350679.21 kJ/jam20930.74 kJ/s
20.93 MW 12917.037HE-01 3.5880657311402 kg/sQA = 33266014.697 kJ/kg HC
Qout flue gas 261188223.27599 kJ/kg HCmassa 429480.231 kg/jam
Cp 1.204 kJ/kg KTout 530 oC
803 K
HRSGBeda temperatur pada titik pinch 40 oC 97.73%P steam 37 bar 20.93T saturated 246 oCHl 1065.15 kJ/kg
Steam yang dihasilkan pada T 350 oCHv 3102 kJ/kg
Temperatur fluegas diatas T saturated = 286 oC
Qs' 126226637.613 kJ/jamSteam yang dihasilkan, ms = Qs'/(Hv-Hl)
61971.494 kg/jam 61971.4940291551.00
Temperatur air feed boiler = 42oCHl (42oC) 185.75 kJ/kg
Qs = ms (Hv - Hl(42oC))180724369.463 kJ/jam
Temperatur flue gas keluar HRSGTf = Tin - Qs/(mg Cp)Tin 530 oCCp 1.104 kJ/kg Kmg 429480.231 kg/jamTf = 149 oC
sisa steam 0.000 kg/jam
Steam Turbineh3 3102 kJ/kg 536.78756476684 662s3 6.6201
T keluar kondens 50 oC 122 1024.1 1.58110625907h1 209.127 kJ/kg 2382.0566 6.62009190672s1 0.7030 kJ/kg K
h5 2382.057 kJ/kgs5 8.075 kJ/kg K
h4s = 1953.313 kJ/kgefisiensi turbine 82%
941.923 kJ/kgDH =
Wt 0.000 kJ/jam0.000 MW
Q total campuran fresh feed dengan dari kon 7789816.799465 kJ/jamHl 125.70 kJ/kgT 42 oC
eff reformer 93.80%eff gas turbine 26.78%eff steam turbine #DIV/0!
Total bahan bakar yang digunakan 12917.037 kg/jamLHV 50032.260 kJ/kgTotal Panas masuk, Qin 646268535.207 kJ/jam
Panas diambil di Reformer 342246155.102 kJ/jamPanas diambil di HE 33266014.697 kJ/jamPanas diambil di HRSG 180724369.463 kJ/jam
180724369.463 kJ/jamTotal Panas yang di ambil 556236539.261 kJ/jam
Daya yang dihasilkan di Turbin gas 75350679.211 kJ/jamDaya yang dihasilkan di Turbin uap 0.000 kJ/jamTotal Daya yang dihasilkan 75350679.211 kJ/jam 20.93
Total Panas dan Daya yang dihasilkan 631587218.472
eff panas 86.07%
eff daya 11.66%
Eff total 97.73%
3358 300 1650.733331 450 2088.16
3335.05 311 1682.808
34673445
3448.3
3448.33335.05
3763.135 263003137.7-47374209.536
r 20.75953 kg/m3V 45554 m3/h
12.65389 m3/sm 262.6888 kg/s
945.6797
8.6065
36 1057.638 1072.737 1065.15
530 1.6057540 1.6009
536.7876 1.6024419689
530 1.5514540 1.5759
536.7876 1.5680295337
700 1.5680295337600 1.6024419689662 1.5811062591
MW
Flowrate HC 31190 m3/haridensitas HC 13.62 kg/m3
P 37 bar
Tfeed HC = 187 1321.2 kj/kg HC
Tsteam 350 3102 kJ/kg Steamrasio steam/HC 3.5massa HC 17706.141 kg/jammassa steam 61971.494 kg steam/jamTotal Qin 215628928.167 kJ/jam 20
192235574.478 40Tmix 311 oC 37DH HC 1681.619 kj/kg HCDH Steam 2999.023 kJ/kg Steam 20Total 215628928.167 0 40
371. ReformerTmix 550 oC 500DH HC 2379.78 kJ/kg HC 450DH steam 3561.55 kJ/kg steam 550total massa 79677.635 kg/jamTotal, Qin 262851295.148 kJ/jam
T reaksi 800 oCReaksi :CH4 + H2O === CO + 3 H2 DHR1 206160 kJ/kmol CH4CO + H2O === CO2 + H2 DHR2 -41150 kJ/kmol CO
u/ 1 kmol CH4e1 0.63 kmole2 0.533 kmol
Qr = e1 (-DHR1) + e2 (-DHR2) = -107947.850 kJ/kmol CH4 -129880.8-6746.741 kJ/kg CH4
= -119,458,741.817 kJ/jam
Produk pada T 800 oCCp produk 9.573 kJ/kg oCMassa produk 79677.635 kg/jam
Qout 591,134,351.226 kJ/jam
Kebutuhan panas, QA = Qin + Qr - Qout 328,289,802.818 kJ/jam328289802.818
Pemanas menggunakan pembakaran fuel gas (asumsi CH4)LHV = 50032.26 kJ/kg fuelQc = 50032.26 kJ/kg fuel
udara pembakaran dengan 100% excessudara teoritis = 0.595 kmol udara/kg Fuel
17.238 kg udara / kg fuel
untuk udara excess = 34.476 kg udara/kg fuel
oC DH HCoC DH Steam
udara masuk kompresor pada kondisi ambientT 303 KP 1.013 barStage 2rasio kompresi 20
4.472Pout kompresor 20.265 bar
untuk udara , k = 1.387Tout = Tin (rc)^(k-1/k)
368 K95 oC
efisiensi kompres 85%Tout actual 379 K 106 oCCp udara 1.029 kJ/kg KQudara 2875.68829485113 kJ/kg fuel 83.410848331317 2876
T fuel in 303 KCp 7.27 kJ/kg KQfuel 36.35 kJ/kg fuel
Total Qin 2912.03829485113 kJ/kg fuel
T flue gas 700 oCCp flue gas 1.075 kJ/kg Km flue gas = 35.476 kg flue gas/kg fuelQ flue 25742.411 kJ/kg fuelasumsi Qloss = 5 1360.094 kJ/kg fuelQA = Qin + Qc - Qout - Qloss
25841.793 kJ/kg fuel
kebutuhan fuel 12703.832 kg/jam 22378.254 m3/jamkebutuhan udara 437979.736 kg/jam 0.717massa flue gas 450683.568 kg/jamQflue gas 327027264.383 kJ/jam
2. Combustion chamberT udara bypass 106 oCCp 1.029 kJ/kg Kperbandingan udara bypass/udara ke furnace reformer 0.1massa udara by pass = 43797.974 kg/jamQ udara bypass 3653226.136 kJ/jam
Q total mix udara masuk combustion chamber 12917.037330680490.519 kJ/jam 1.01678269187
Cp mix 1.065 kJ/kg Kmassa mix 494481.542 kg/jamTmix 653 oC
Total udara dalam mix 262787.842 kg/jam10204.928
51024.63961229.567
4.01616.066 kg O2/kg fuel
0.0623811.150
teoritis udara/fuel 17.238 kg udara/kg fuel
untuk udara dengan 300% excess 68.952 kg udara/kg fuel
massa fuel in 0.015 kg fuel/kg udara3811.150 kg/jam 16514.982
-3597.945T fuel in 303 KCp 7.270 kJ/kg KQfuel 138535.289 kJ/jam
Q total in CC 330819025.809 kJ/jam
LHV = 50032.260 kJ/kg fuelQc = 190680429.665 kJ/jam
Qout = 521499455.473 kJ/jam
m flue gas 498292.692 kg/jamCp flue gas 1.104 kJ/kg KT flue gas 972.982387 oC
1246 K
Turbin
Pout turbin 5.34664823679099 barPout/Pin 0.264
1.293Tout Turbin = Tin (Pout/Pin)^(k-1/k)
921 K648 oC
Cp flue gas 1.082 kJ/kg KQout turbin 336033937.233 kJ/jam
Wt 185465518.240 kJ/jam 51.518199511249
kompresormassa udara 481777.710 kg/jamCp udara 1.029 kJ/kg KTin 303 KTout 379 K
Wc 75413482.359 kJ/jam 20.948189544166
Wnet 110052035.88 kJ/jam30570.01 kJ/s
30.57 MW 16514.982HE-01 4.5874949364958 kg/sQA = 47222366.981 kJ/kg HC
Qout flue gas 288811570.252022 kJ/kg HCmassa 498292.692 kg/jam
Cp 1.204 kJ/kg KTout 506 oC
779 K
HRSG
Beda temperatur pada titik pinch 50 81.09%P steam 37 bar 30.57T saturated 246 oCHl 1065.15 kJ/kg
Steam yang dihasilkan pada T 350Hv 3102 kJ/kg
Temperatur fluegas diatas T saturated = 296
Qs' 126226637.613 kJ/jamSteam yang dihasilkan, ms = Qs'/(Hv-Hl)
61971.494 kg/jam 61971.4940291551.00
Temperatur air feed boiler = 30oCHl (30oC) 125.7 kJ/kg
Qs = ms (Hv - Hl(42oC))184445757.679 kJ/jam
Temperatur flue gas keluar HRSGTf = Tin - Qs/(mg Cp)Tin 506 oCCp 1.104 kJ/kg Kmg 498292.692 kg/jamTf = 171 oC
sisa steam 0.000 kg/jam
Steam Turbineh3 3102 kJ/kg 536.78756476684 662s3 6.6201
T keluar kondens 50 oC 122 1024.1 1.58110625907h1 209.127 kJ/kg 2382.0566 6.62009190672s1 0.7030 kJ/kg K
oC
oC
oC
h5 2382.057 kJ/kgs5 8.075 kJ/kg K
h4s = 1953.313 kJ/kgefisiensi turbine 82%
941.923 kJ/kg
Wt 0.000 kJ/jam0.000 MW
Q total campuran fresh feed dengan dari kon 7789816.7994667 kJ/jamHl 125.70 kJ/kgT 42 oC
eff reformer 51.65%eff gas turbine 57.72%eff steam turbine 31.65%
Total bahan bakar yang digunakan 16514.982 kg/jamLHV 50032.260 kJ/kgTotal Panas masuk, Qin 826281861.881 kJ/jam
Panas diambil di Reformer 328289802.818 kJ/jamPanas diambil di HE 47222366.981 kJ/jamPanas diambil di HRSG 184445757.679 kJ/jam
184445757.679 kJ/jamTotal Panas yang di ambil 559957927.478 kJ/jam
Daya yang dihasilkan di Turbin gas 110052035.882 kJ/jamDaya yang dihasilkan di Turbin uap 0.000 kJ/jamTotal Daya yang dihasilkan 110052035.882 kJ/jam 30.57
Total Panas dan Daya yang dihasilkan 670009963.359
eff panas 67.77%
eff daya 13.32%
Eff total 81.09%
DH =
697.17942
3358 300 1650.733331 450 2088.16
3335.05 550 2379.78
34673445
3448.3
3448.33335.053561.55 262851295.15
-47222366.981
-119459617.65
328,289,802.818342,246,155.102
102049.27951024.6393
218988.656
229193.586
r 20.75953237751 kg/m3V 45554 m3/h
12.65388888889 m3/sm 262.6888160903 kg/s
945.6797379249
8.6065
36 1057.638 1072.737 1065.15
530 1.6057540 1.6009
536.7875647668 1.6024419689
530 1.5514540 1.5759
536.7875647668 1.5680295337
700 1.5680295337600 1.6024419689
662 1.5811062591
MW
