perancangan he di sebangan gas plant
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Perancangan HE diSebangan Gas PlantKing Bima Sakti
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Content
• Gas Production System (2’)
• Ada apa dengan Sebanga? (2’)
• Data Gas (2’)
• STHE calculation (5’)
• Air-cooler exchanger calculation (5’)
• Kesimpulan (1’)
• Saran (1’)
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Gas Production System
• Gas Well
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Gas Production System
(cont’d) • Gas Plant
Compressor
Separator
Cooler
VRU
Dehydration Plant
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Gas Production System
(cont’d) • Standard gas
• Untuk pipa transmisi gas yang di pasang di daerah daerah seperti
southerm U.S Southeast Asia, Southherm Europe dan West Africa
kandungan uap air maksimumnya adalah 7 lb/MMscf.
•Untuk daerah di Northerm U.S.A Northerm Europe, Canada, danNorthem Asia kandungan uap air maksimum nya adalah 2 – 4
lb/MMscf.
• Untuk gas alam yang akan di cairkan menjadi LNG, kandungan
uap air maksimumnya adalah 1 ppm (0,05 lb/MMscf).
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Ada apa dengan Sebanga?
• Flow gas menurun hingga tak sesuai dengan desaign awal
• Engine merespon dengan menurunkan RPM
• Ingin mempertahankan putaran mesin untuk
mempertahankan reliabilitas mesin
• Modifikasi kompresor dengan menambahkan stage agar
tekanan suction bisa diturunkan
• Harapannya flow gas bisa meningkat
• Temperatur keluar kompresor jadi lebih tinggi
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Quest
• Dibutuhkan penukar kalor untuk mengakomodir peningkatan
temperatur gas sebelum masuk glycol contactor
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Data Gas
• 3rd discharge gas properties
Fraksi Mol Tempe rature (F)P re s s ur e
(ps ia )
De ns i ty
(mol/m3) x.rho
Volume
(m3/mol) x.v
Cp
(J/mol*K)x.Cp
Vis c os i ty
(P a*s ) x.miu
The rm.
Cond.
(W/m*K)
x.k P h a s e
H2S 0.0000 2 37 .68 34 9.7 8 17 .2 2 0 0.0012237 0 40 .618 0 1.7 5E- 0 5 0.00E+00 0.025974 0 vapor
Nitrogen 0.0602 237 .68 34 9.7 7 43 .6 4 44.767128 0.0013447 8.1E-05 29 .8 12 1. 79 46 82 4 2 .2 0E- 0 5 1.32E-06 0.032121 0.001934 vapor
Oksigen 0.0001 237 .68 34 9.7 7 49 .2 9 0.074929 0.0013346 1.33E-07 30 .6 46 0 .0 03 06 46 2 .5 5E- 05 2.55E-09 0.034135 3.41E-06 vapor
Metana 0.5666 237 .68 34 9.7 7 58 .0 3 429.499798 0.0013192 0.000747 4 1. 09 8 2 3 .2 8 612 6 8 1. 42 E- 0 5 8.03E-06 0.049174 0.027862 vapor
CO2 0.2028 237 .68 34 9.7 7 87 .5 2 159.709056 0.0012698 0.000258 4 4. 20 3 8 .9 64 36 84 1.9 3E- 0 5 3.92E-06 0.025016 0.005073 vapor
Etana 0.0714 2 37 .68 34 9.7 8 13 .4 8 58.082472 0.0012293 8.78E-05 6 8. 76 4 4 .9 09 74 96 1.2 5E- 0 5 8.93E-07 0.035523 0.002536 vapor
Propana 0.0494 237 .68 34 9.7 9 22 .6 7 45.579898 0.0010838 5.35E-05 10 6.6 8 5 .2 69 99 2 1. 13 E- 0 5 5.58E-07 0.032198 0.001591 vapor
i-Buthane 0.0087 2 37 .68 34 9.7 120 0.6 10.44522 0.0008329 7.25E-06 18 9.5 4 1. 64 89 98 1. 16 E- 0 5 1.01E-07 0.032996 0.000287 vapor
n-Buthane 0.0157 2 37 .68 34 9.7 7 618.9 119.61673 0.0001313 2.06E-06 19 2.5 6 3 .0 23 19 2 6 .7 4E- 05 1.06E-06 0.074796 0.001174 liquid
i -Pentane 0.0061 237 .68 34 9.7 7 26 6.6 44.32626 0.0001376 8.39E-07 2 03 .4 3 1. 24 09 23 0 .0 00 110 9 6.77E-07 0.083031 0.000506 liquid
n-Pentane 0.0059 237 .68 34 9.7 7 26 6.6 42.87294 0.0001376 8.12E-07 2 03 .4 3 1. 20 02 37 0 .0 00 110 9 6.54E-07 0.083031 0.00049 liquid
n-Hexane 0.0070 2 37 .68 34 9.7 66 16 46.312 0.0001512 1.06E-06 2 30 .5 2 1.6 13 64 0 .0 00 14 18 9.93E-07 0.10 119 0.000708 liquid
n-Heptane 0.0046 237 .68 34 9.7 6 02 0.9 27.69614 0.0001661 7.64E-07 2 62 .6 8 1. 20 83 28 0 .0 00 17 82 8.20E-07 0.11077 0.00051 liquid
n-Octane 0.0011 237 .68 34 9.7 5 48 7.4 6.03614 0.0001822 2E-07 2 9 5.3 6 0 .3 24 89 6 0 .0 00 22 72 2.50E-07 0.10136 0.000111 liquid
n-Nonane 0.0001 237 .68 34 9.7 5 02 8.6 0.50286 0.0001989 1.99E-08 3 28 .6 9 0 .0 32 86 9 0 .0 00 28 33 2.83E-08 0.1064 1.06E-05 liquid
n-Decane 0.0000 237 .68 34 9.7 4 63 2.4 0 0.0002159 0 36 2.3 6 0 0.0 00 33 11 0.00E+00 0.10896 0 liquid
H2O 0.0002 2 37 .68 34 9.7 52 6 64 10.5328 1.90E-05 3.8E-09 7 6. 18 6 0 .0 15 23 72 0 .0 00 24 52 4.90E-08 0.68376 0.000137 liquid
1046.05437 0.00124 54.536304 1.94E-05 0.04293
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Data Gas (cont’d)
• Desired gas properties
Fraksi Mol Tempe rature (F)P re s s ur e
(ps ia )
De ns i ty
(mol/m3) x.rho
Volume
(m3/mol) x.v
Cp
(J/mol*K)x.Cp
Vis c os i ty
(P a*s ) x.miu
The rm.
Cond.
(W/m*K)
x.k P h a s e
H2S 0.0000 90 34 9.7 22 20 4 0 4.50E-05 0.00E+00 78.825 0 0.0001267 0 0.13873 0 liquid
Nitrogen 0.0602 90 34 9.7 95 1.6 2 57.28752 0.0010508 6.33E-05 30.176 1.816595 1.85E-05 1.11484E-06 0.027109 0.001632 vapor
Oksigen 0.0001 90 34 9.7 96 2 .0 9 0.096209 0.0010394 1.04E-07 30.588 0.003059 2.14E-05 2.1369E-09 0.027739 2.77E-06 vapor
Metana 0.5666 90 34 9.7 98 6 .4 6 558.9282 0.0010137 5.74E-04 38.26 21.67812 1.18E- 05 6.66945E-06 0.0369 0.020908 vapor
CO2 0.2028 90 34 9.7 10 7 9.4 218.9023 0.0009264 1.88E-04 46.563 9.442976 1.56E-05 3.16976E-06 0.018664 0.003785 vapor
Etana 0.0714 90 34 9.7 117 7.8 84.09492 0.0008491 6.06E-05 68.295 4.876263 1.04E-05 7.44916E-07 0.025126 0.001794 vapor
Propana 0.0494 90 34 9.7 110 04 543.5976 9.09E-05 4.49E-06 121.85 6.01939 9.27E-05 4.5816E-06 0.091904 0.00454 liquid
i-Buthane 0.0087 90 34 9.7 93 9 3.4 81.72258 0.000 1065 9.26E-07 142.55 1.240185 0.0001453 1.26402E-06 0.088279 0.000768 liquid
n-Buthane 0.0157 90 34 9.7 97 7 6.5 153.4911 0.000 1023 1.61E-06 143.16 2.247612 0.0001526 2.39535E-06 0.10344 0.001624 liquid
i-Pentane 0.0061 90 34 9.7 85 4 8.4 52.14524 0.000117 7.14E-07 168.72 1.029192 0.0002115 1.29039E-06 0.11001 0.000671 liquid
n-Pentane 0.0059 90 34 9.7 85 4 8.4 50.43556 0.000117 6.90E-07 168.72 0.995448 0.0002115 1.24809E-06 0.11001 0.000649 liquid
n-Hexane 0.0070 90 34 9.7 75 5 2.9 52.8703 0.000 1324 9.27E-07 196.15 1.37305 0.0002849 1.99458E-06 0.1252 0.000876 liquid
n-Heptane 0.0046 90 34 9.7 67 4 4.8 31.02608 0.000 1483 6.82E-07 226.82 1.043372 0.0003697 1.70076E-06 0.13038 0.0006 liquid
n-Octane 0.0011 90 34 9.7 60 81.5 6.68965 0.000 1644 1.81E-07 256.94 0.282634 0.0004802 5.28264E-07 0.12335 0.000136 liquid
n-Nonane 0.0001 90 34 9.7 55 39 .1 0.55391 0.000 1805 1.81E-08 286.2 0.02862 0.000613 6.1302E-08 0.12568 1.26E-05 liquid
n-Decane 0.0000 90 34 9.7 50 8 0.4 0 0.000 1968 0.00E+00 315.48 0 0.0007874 0 0.12854 0 liquid
H2O 0.0002 90 34 9.7 55 28 5 11.057 1.81E-0 5 3.62E-09 75.185 0.015037 0.000761 1.5219E-07 0.62008 0.000124 liquid
1902.9 8.96E-04 52.0915 2.69177E-05 0.03812
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Data Gas (cont’d)
• Gas properties
Kondisi 3rd Stage Discharge Desired Cond. 1 MMSCFD
Vapour/Phase Fraction 1 1 13.8345881
Temperature [F] 237.6838168 90 - 100
Pressure [psig] 335 335
Molar Flow [MMSCFD] 4.07185249 4.07185249 56.3324021 mol/s
sifat 3rd discharge desired
ρ 1046.054371 1902.898179 mol/m3
v 0.001240375 8.96E-04 m3/mol
Cp 54.536304 52.0915494 J/mol*K
μ 1.94E-05 2.69177E-05 Pa*s
k 0.042933749 0.038121961 W/m*K
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Shell and Tube
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Menentukan Flow Air
• Qgas = ṅ . Cp . ΔT
• Qgas = 56.33 mol/s . 54.536 J/mol K . (114.27 – 32.22)K
• Qgas = 252058.66 W
• Qair = Qgas = ṁ . Cp . ΔT
• 252058.66 W = ṁ . 4179 J/KgK . (40 – 25) K
• ṁ = 4.021 Kg/s
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Perhitungan LMTD berserta faktor
koreksi
• ΔTlm =; ;(;)
(−)
(−)
=.; ;(.;)
(.−
.−)
= 28.76 oC
• ΔTm = Ft . ΔTlm
• R =;
; =
.;.
; = 5.47
• S =;
; =
;
.; = 0.168
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Perhitungan LMTD berserta faktor
koreksi (cont’d)
• Ft = 0.85
•ΔTm = 0.85 x 28.76 = 24.446 oC
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Luas permukaan perpindahan
panas yang dibutuhkan• Q = U.A. ΔTm
• 252058.66 W = 200 W/m2 oC . A . 24.446 Oc
• A = 51.55 m2
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Penentuan Dimensi
• Outer Diameter (OD) = 32 mm
• Inner Diameter (ID) = 30.3 mm
• Thickness (t) = 1.7 mm
• Panjang tube (L) = 3.66 m
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Penentuan Dimensi (cont’d)
• Area 1 tube (At) = π . OD . L = π . 32.103 m . 3.66 m = 0.367 m2
• Needed tube (n) =
=
.
. = 140.17 tubes ≈ 141 tubes
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Konfigurasi tube
• Db = 32
.
.
= 565.65 mm
• Dshell = Db + Clearance = 565.65 mm + 60 mm = 625.65 mm
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Purchasing Cost
•
Ce = a + bS
n
• Ce = 32000 + 70 x 51.551.2 = $ 39939.12
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Perhitungan pompa
• ṁ = 4.021 Kg/s = 4.04 x 10-3 m3/s = 53.45 GPM
• HP yang dibutuhkan untuk menghasilkan flow sebanyak 53.45
GPM adalah 0.4584 HP atau setara dengan 0.3418 kW
• Pump = $ 3554
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Total Purchasing Cost 2014
• = 1 +
• = $ 43,493.12 1 + 0.068
• = $ 56,585.55
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Air-cooler Exchanger
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Forced Draft
Kelebihan
• Udara inlet dingin
• Mudah dirawat
• Lebih murah
Kekurangan
• Distribusi udara
• Kemungkinan terjadi
resirkulasi• Natural draft rendah
• Sangat dipengaruhi
lingkungan
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Panas Yang Dipertukarkan
• Q = ṁ . Cp . ΔT
• Qgas = ṅ . Cp . ΔT = 56.33 mol/s . 54.536 J/mol K . (114.27 –
32.22)K
• Qgas = 252058.66 W = 860059.847 Btu/h
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Udara Yang Dibutuhkan
• Qudara = Qgas = ṁ . Cp . ΔT
• 252058.66 W = ṁ . 1.005 J/Kg K . (40 – 23) K
• ṁ = Wa= 14.75 Kg/s = 117065.46 lb/h
• ACFM =
. ..= 22712
= 13.078
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Perhitungan LMTD berserta faktor
koreksi
• Δta =:
:
1 =.:
:.
80.6
• Δta = 34.128 oF
•
t2 = 114.72
o
F
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Perhitungan LMTD berserta
faktor koreksi (cont’d)
• ΔTlm =; ;(;)
(−)
(−)
=;. ;(.;.)
(−.)
(.−.)
= 44.16 oF
• CMTD = Ft . ΔTlm
• Ft = 1.00 (Asumsi untuk 3 passes tube)
• ΔTm = 1.00 x 44.16 oF = 44.16 oF
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Dimensi
• Menggunakan air-cooler exchanger bertipe forced draft 1 fan
• Fin tube = 1 in outer diameter ½ in high fin
• Tube pithch = 2 ½ in triangular
• Bundle layout = 3 tube passes, 4 rows tubes, 30 ft long tubes
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Luas Permukaan kontak
• Q = U.A. ΔTm
• 860059.847 Btu/h = 3.1 Btu/h.ft2.oF x A x 44.16 oF
• A = 6282.58 ft2 = 583.67 m2 (permukaan extended )
• 860059.847 Btu/h = 45 Btu/h.ft2.oF x A x 44.16 oF
• A = 432.8 ft2 (bare tube area)
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Dimensi ACHE
• Fa =.
.= 77.75 ft2 (4 row) = 7.223 m2
• Width =.
= 2.6
• Jumlah tube =.
. = 55.11 ≈ 56 tubes
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Validasi asumsi Ux
• Bagian dalam
ht =. ./
.= 22,712.32
..
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Validasi asumsi Ux (cont’d)
•
=
.= 22.99
•
=
.22.99 + 0.001 22.99 +
.
• Ux = 5.54 6.4 Btu/h.ft2.oF
• Ux validasi > Ux asumsi. Accepted!
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Dimensi Kipas
• Fan Area per Fan =.
=
. .
= 108.85
• Fan Diameter =
.=
.
.
• = 11.72 ≈ 12
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Pressure Drop (cont’d)
• As = n . At
• As = 56 . 0.5945 sq in. = 0.0213 sq in.
• Volum jenis gas yang mengalir adalah = 0.00124 m3/mol
• Maka debit gas yang mengalir adalah = 0.00124 m3/mol x
56.33 mol
• Q = 0.00699 m3/s
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Pressure Drop (cont’d)
• Kecepatan aliran gas =
=
. /
. = 3.285 /
• = (0.79 ln 18922.5 1.64);= 0.026
• ΔP = 0.026 .
kg
m .
. 9.144 = 24983.78
•
ΔP = 3.623
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Kecepatan UdaraStaggered tube bank
• Vmax =
;
• V =
=
= . /
. = 1.81 /
• Vmax =
;.1.81 = 24.13 /
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Daya Kipas
• = 3 1 .
. .
.
0.4 = 393.72
• ≈ 0.057
• =
ƞ
• Ƞ = efisiensi pompa = 70%
• =
.
.= 9.85
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PurchasingCost
• A = 432.8 ft2 (bare tube area)
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Purchasing Cost at 2014
• 2014 = $ 35,000
.
• $ 51,496.8
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Kesimpulan
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Saran
• Pilih tipe air-cooler exchanger
• Dalam pembuatannya ada baiknya diberikan safety factor
pada luas permukaan kontak
• Menyediakan mekanisme drainase untuk menguras kondensat
pada alat penukar kalor• Saya menyarankan menggunakan air-cooler dengan susunan
forced draft
• Memodifikasi air-cooler exchanger yang sudah ada
•
STHE tanpa water HE karena air keluar sesuai denganperaturan KLH No.04/2007
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