Condensor Parsial [PDF]

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KONDENSOR PARSIAL - 01 Tugas Jenis Skema



: : :



Mengembunkan hasil keluaran reaktor menggunakan pendingin air Penukar kalor selongsong dan tabung



Data Fluida panas (gas masuk) Suhu masuk, T1 Tekanan masuk, P1



= =



Komposisi fluida panas masuk Kondensor parsial mol massa Komponen f. mol (kmol/jam) (kg/jam) n-C4H10 296.3738 17226.4326 0.3229 i-C4H10 0.507 29.4705 0.0006 n-C4H8 136.332 7634.5899 0.1485 C4H6 116.1346 6281.7224 0.1265 H2 368.6012 737.2025 0.4015 Total 917.9487 31909.4178 1 Tekanan uap komponen konsable (mmHg), T (K) A B C Komponen



n-C4H10 i-C4H10 n-C4H8 C4H6



27.0441 31.2541 27.3116 30.0572



-1.9E+03 -2.0E+03 -1.9E+03 -2.0E+03



f. massa 0.5399 0.0009 0.2393 0.1969 0.0231 1



D



E



-7.2E+00 -6.68E-11 4.22E-06 -8.8E+00 8.92E-11 5.75E-06 -7.2E+00 7.49E-12 3.68E-06 -8.3E+00 2.57E-10 5.13E-06



H2



3.4132 -3.1E+00 1.1E+00 -6.69E-10 1.46E-04



Persamaan yang digunakan : log (Puap,i) = A + B/T + Clog(T) + DT + ET2 Suhu beku (K), suhu didih (K), suhu kritis (K) Komponen Tf (K) Tb (K) Tc(K) 134.86 272.65 425.18 n-C4H10



i-C4H10 n-C4H8 C4H6 H2



113.54



261.43



408.14



87.8



266.9



419.59



164.25 13.95



268.74 20.39



425.37 33.18



Viskositas fase gas (kg/m.s), T (K)



Komponen n-C4H10 i-C4H10 n-C4H8 C4H6 H2



A -4.946 -4.731 -9.143 10.256 27.758



B 2.90E-01 2.91E-01 3.16E-01 2.68E-01 2.12E-01



C -7E-05 -8E-05 -8E-05 4E-05 -3E-05



Persamaan yang digunakan : µgas = A+BT+CT2 Viskositas rata-rata :



Sumber : Carl .L. Yaws,1999, “Chemical Properties Handbook”, Mc. Graw Hill,New York Kapasitas panas fase gas (J/mol.K), T (K) Komponen A B C n-C4H10 20.056 2.82E-01 -1E-05 i-C4H10 6.772 3.41E-01 -1E-04 n-C4H8



24.915 18.835



2.06E-01 2.05E-01



6E-05 6E-05



D



E



-9E-08 -4E-08 -1E-07 -2E-07



3E-11 2E-11 5E-11 6E-11



C4H6 H2 25.399 2.02E-02 -4E-05 3E-08 Persamaan yang digunakan: Cp = A + BT + CT2 + DT3 + ET4



-9E-12



Sumber : Carl .L. Yaws,1999, “Chemical Properties Handbook”, Mc. Graw Hill,New York Panas laten (kJ/mol,) T (K) A



Tc



n



33.02



425.18



0.377



31.954



408.14



0.392



33.39



419.59



0.393



35.17



425.37



0.448



0.659



33.18



0.38



Menentukan suhu Keluar Fluida Panas a. Buble point P total = Pcd = Trial T = Komponen xi n-C4H10 0.5363 i-C4H10 0.002 n-C4H8 0.247 C4H6 0.2147 Total 1



b. Dew point P total = Pcd = Trial T = Komponen n-C4H10 i-C4H10 n-C4H8 C4H6 Total



yi 0.5363 0.002 0.247 0.2147 1



9 atm = 5.4 atm = 53.54 C = P0 K=P0/Pcd yi=xi.K 5.4186 1.0039 0.5384 7.391 1.3693 0.0027 6.5802 1.2191 0.3011 3.9738 0.7362 0.1581 23.3636 4.3286 1.0003



9 atm = 5.4 atm = 54.67 C = P0 K=P0/Pcond xi=yi/K 4237.6808 1.0331 0.5192 5769.7337 1.4065 0.0014 5143.3833 1.2538 0.197 3116.2509 0.7597 0.2826 18267.0487 4.4531 1.0002



Suhu keluar kondensor parsial ditetapkan, T2 =



54.67 C



Selanjutnya kondensor parsial dibagi menjadi 2 zona : 1. Zona desuperheater dari suhu masuk hingga suhu embun 2. Zona kondensasi dari suhu embun Tinjauan pada zone kondensasi Pada zona kondensasi dalam perhitungan dibagi menjadi 4 subzone Persamaan yang digunakan : K = Po/P Ln = Vn - 1 / (1+(K.V/L))fase cair komponen pd inkremen n Vn = Vn-1 - Ln fase uap komponen pd inkr (pers 13.9, Kern 1950) ΔT



=



Tdew point - T bubble point 4



326.54



6840 4102.1 327.67



=



0.2825 C



=



Zona Desuperheater



Err:509 Err:509 Err:509



Err:509 Err:509 Err:509



Qds t2 tdew cek Qt



Err:509 Err:509 Err:509



Err:509 Err:509 Err:509



3847005.30 323.15 317.64 8519429.61 Err:509 Err:509



Qds/T



Zona Pengembunan



Fluida Panas Dingin Qcond Qcond/T



Suhu Atas (KSuhu Bawah (delT 327.82 326.54 10.18 317.64 303.15 23.39 46346327 15.9 2919245.5



Subzone 1 ΔT 0.282094699 R= danL = F (1-R) Tsubzone 1 327.3840151 sehingga didapat : Tekanan (a 5.397506417 V (kmol/ja 0 R trial 0 L (kmol/ja 543.01623 Komponen Fraksi mol P° (mmHg) P° (atm) Ki xi = n-C4H10 0.536326645 4191.6099094 5.5152762 1.0218193 0.5363266 i-C4H10 0.001990376 5710.9487247 7.51440622 1.3921996 0.0019904 n-C4H8 0.246990198 5088.4972891 6.69539117 1.2404601 0.2469902 C4H6 0.214692782 3079.155838 4.05152084 0.7506283 0.2146928 Total 1 18070.211761 23.7765944 4.4051072 1



Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



58.124 58.124 56 54.09 2



Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



58.124 58.124 56 54.09 2



Mol (kmol/jamMassa (kg/j Fraksi Cair 291.23407211 16927.6892 0.5363266 1.0808063242 62.8207868 0.0019904 134.11968581 7510.70241 0.2469902 116.58166476 6305.90225 0.2146928 0 0 0 543.01622901 30807.1146 1 Mol (kmol/jamMassa (kg/j Fraksi Uap 0.0291263198 1.69293821 8.036E-05 0.0001080914 0.00628271 2.982E-07 0.0134133099 0.75114536 3.701E-05 0.0116593324 0.63065329 3.217E-05 362.37462384 724.749248 0.9998502 362.4289309 727.830267 1 cek nm 31534.9449



Subzone 2 ΔT 0.282094699 R= danL = F (1-R) Tsubzone 2 327.1019204 sehingga didapat : Tekanan (a 5.397506417 V (kmol/ja 0.3261709 R trial 0.000600665 L (kmol/ja 542.69006 Komponen Fraksi mol P° (mmHg) P° (atm) Ki xi = n-C4H10 0.536326645 4161.7344061 5.47596632 1.0145363 0.536322 i-C4H10 0.001990376 5672.8099197 7.46422358 1.3829022 0.0019899 n-C4H8 0.246990198 5052.8955738 6.64854681 1.2317812 0.2469558 C4H6 0.214692782 3055.1222562 4.01989771 0.7447694 0.2147257 Total 1 17942.562156 23.6086344 4.3739891 0.9999934 Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



Mol (kmol/jamMassa (kg/j Fraksi Cair 58.124 291.05659661 16917.3736 0.5363255 58.124 1.0799087468 62.768616 0.0019899 56 134.02046608 7505.1461 0.2469574 54.09 116.52950314 6303.08082 0.2147271 2 0 0 0 542.68647458 30788.3692 1



Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



Mol (kmol/jamMassa (kg/j Fraksi Uap 58.124 0.206601821 12.0085242 0.0005695 58.124 0.0010056688 0.05845349 2.772E-06 56 0.1126330421 6.30745036 0.0003105 54.09 0.063820955 3.45207545 0.0001759 2 362.37462384 724.749248 0.9989413 362.75868533 746.575751 1



cek nm



31534.9449



Subzone 3 ΔT 0.282094699 R= danL = F (1-R) Tsubzone 3 326.8198257 sehingga didapat : Tekanan (a 5.397506417 V (kmol/jam) R trial -2.3125E-06 L (kmol/jam) Komponen Fraksi mol P° (mmHg) P° (atm) Ki n-C4H10 0.536326645 4132.0179137 5.43686568 1.0072921 i-C4H10 0.001990376 5634.8593478 7.41428862 1.3736507 n-C4H8 0.246990198 5017.4755558 6.60194152 1.2231466 C4H6 0.214692782 3031.2333828 3.98846498 0.7389459 Total 1 17815.5862 23.4415608 4.3430353 Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



Mol (kmol/jamMassa (kg/j Fraksi Cair 58.124 291.23475051 16927.7286 0.3414756 58.124 1.0808097575 62.8209863 0.0012673 56 134.12006518 7510.72365 0.1572571 54.09 426.43562545 23065.903 0.5 2 0 0 0 852.8712509 47567.1763 1



Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



Mol (kmol/jamMassa (kg/j Fraksi Uap 58.124 0.0284479213 1.65350698 0.0005411 58.124 0.0001046581 0.00608315 1.991E-06 56 0.0130339438 0.72990085 0.0002479 54.09 -309.8423014 -16759.37 -5.893461 2 362.37462384 724.749248 6.8926703 52.573909014 -16032.231 1 cek nm 31534.9449



Subzone 4 ΔT 0.282094699 R= danL = F (1-R) Tsubzone 4 326.537731 sehingga didapat : Tekanan (a 5.397506417 V (kmol/ja 4.344E-05 R trial 8E-08 L (kmol/ja 543.01619 Komponen Fraksi mol P° (mmHg) P° (atm) Ki xi = n-C4H10 0.536326645 4102.4598956 5.39797355 1.0000865 0.5363266 i-C4H10 0.001990376 5597.0964086 7.36460054 1.364445 0.0019904 n-C4H8 0.246990198 4982.2366954 6.5555746 1.2145561 0.2469902 C4H6 0.214692782 3007.488632 3.95722188 0.7331574 0.2146928 Total 1 17689.281632 23.2753706 4.3122451 1 Komposisi BM n-C4H10



Mol (kmol/jamMassa (kg/j Fraksi Cair 58.124 291.23404881 16927.6879 0.5363266



i-C4H10 n-C4H8 C4H6 H2 Total



58.124 1.0808062062 62.8207799 0.0019904 56 134.11967278 7510.70168 0.2469902 54.09 116.58165792 6305.90188 0.2146928 2 0 0 0 543.01618573 30807.1122 1



Komposisi BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total



Mol (kmol/jamMassa (kg/j Fraksi Uap 58.124 0.0291496206 1.69429255 8.043E-05 58.124 0.0001082094 0.00628956 2.986E-07 56 0.0134263416 0.75187513 3.705E-05 54.09 0.0116661702 0.63102315 3.219E-05 2 362.37462384 724.749248 0.99985 362.42897419 727.832728 1 cek nm 31534.9449



Beban panas Dihitung dengan persamaan Qsubzone1 = Qlaten + Qsg Qsubzone2 = Qlaten + Qsg + Qsl Qsubzone3 = Qlaten + Qsg + Qsl Qsubzone4 = Qlaten + Qsg + Qsl Dengan hubungan: Qsg = Beban panas untuk menurunkan suhu gas dari Tdew sampai T', [kJ/jam] Qsg = Σmi cpgi ( Tdew - T') Menghitung Beban Panas Desuperheater



Suhu Masuk T1 (K) = 690.651397 Suhu Embun Tdew (K) = 327.81611 Komponen mol (kmol/jamMassa (kg/jam)Qds n-C4H10 291.2631984 16929.382146 15712747 i-C4H10 1.080914416 62.827069494 58492.5229 n-C4H8 134.1330991 7511.4535509 6286946.89 C4H6 116.5933241 6306.5329003 5059804.52 H2 362.3746238 724.74924769 3847005.3 Total 905.4451599 31534.944914 30964996 Sehingga Beban Panasnya : Qt (kJ/jam) 30964996.02 Menghitung Beban Panas Subzone 1



Beban panas untuk menurunkan suhu gas



Suhu masuk Tdew (K) 327.81611 Suhu keluar T' (K) 327.384015 Komponen mol (kmol/jamMassa (kg/jam)Qsg n-C4H10 0.02912632 1.6929382146 1.35849923 i-C4H10 0.000108091 0.0062827069 0.0049767 n-C4H8 0.01341331 0.7511453551 0.54797742 C4H6 0.011659332 0.63065329 0.43972373 H2 362.3746238 724.74924769 4523.93615 Total 362.4289309 727.83026726 4526.28733 Beban panas untuk pengembunan



Suhu Masuk Zona 1 (K) 327.38401505 Komponen mol (kmol/jamMassa (kg/jam)λ (kJ/kmol) Qv (kJ/jam) n-C4H10 291.0565966 16917.373622 18973.8796 5522473 i-C4H10 1.079908747 62.768616 16931.6986 18284.689 n-C4H8 134.0204661 7505.1461005 18407.5706 2466991 C4H6 116.5295031 6303.0808248 18219.0728 2123060 Total 542.6864746 30788.369163 72532.2216 10130808 Qsubzone 1 10135334.47 Menghitung Beban Panas Subzone 2



Beban panas untuk menurunkan suhu gas



Suhu masuk T' (K) 327.38401505 Suhu keluar T'' (K) 327.10192035 Komponen mol (kmol/jamMassa (kg/jam)Qsg n-C4H10 0.206601821 12.008524246 6.28591444 i-C4H10 0.001005669 0.058453494 0.03020193 n-C4H8 0.112633042 6.3074503583 3.00171312 C4H6 0.063820955 3.4520754547 1.57011588 H2 362.3746238 724.74924769 10.8879454 Total 362.7586853 746.57575124 21.7758908 Beban panas untuk menurunkan suhu embunan



Suhu T'' (K) 327.10192035 Komponen mol (kmol/jamMassa (kg/jam)λ (kJ/kmol) Qv (kJ/jam) n-C4H10 291.0565966 16917.373622 18994.4945 5528473 i-C4H10 1.079908747 62.768616 16954.859 18309.701 n-C4H8 134.0204661 7505.1461005 18429.6823 2469955 C4H6 116.5295031 6303.0808248 18242.5524 2125796 H2 0 0 0 0 Total 542.6864746 30788.369163 72621.5882 10142533 Beban panas untuk pengembunan



Suhu masuk327.3840151 Suhu keluar327.1019204 Komponen mol (kmol/jamMassa (kg/jam)QsL n-C4H10 291.0565966 16917.373622 12410.0109 i-C4H10 1.079908747 62.768616 46.6323415 n-C4H8 134.0204661 7505.1461005 5329.99816 C4H6 116.5295031 6303.0808248 4311.34218 H2 0 0 0 Total 542.6864746 30788.369163 22097.9836 Qsubzone 2 10164652.55 Menghitung Beban Panas Subzone 3



Beban panas untuk menurunkan suhu gas



Suhu masuk327.1019204 Suhu keluar 326.8198257 Komponen mol (kmol/jamMassa (kg/jam)Qsg n-C4H10 0.028447921 1.6535069801 6.28184769 i-C4H10 0.000104658 0.0060831498 0.0301807 n-C4H8 0.013033944 0.7299008539 2.99985939 C4H6 -309.842301 -16759.37008 1.56910479 H2 362.3746238 724.74924769 2953.21042 Total 52.57390901 -16032.23134 2964.09141 Beban panas untuk pengembunan



Suhu T''' (K 327.1019204 Komponen mol (kmol/jamMassa (kg/jam)λ (kJ/mol) Qv (kJ/jam) n-C4H10 291.2347505 16927.728639 18994.4945 5531857 i-C4H10 1.080809757 62.820986344 16954.859 18324.977



n-C4H8 134.1200652 7510.72365 18429.6823 2471790 C4H6 426.4356254 23065.902981 18242.5524 7779274 H2 0 0 0 0 Total 852.8712509 47567.176256 72621.5882 15801246 Beban panas untuk menurunkan suhu cair



Suhu masuk327.1019204 Suhu keluar 326.8198257 Komponen mol (kmol/jamMassa (kg/jam)QsL n-C4H10 291.2347505 16927.728639 12408.2813 i-C4H10 1.080809757 62.820986344 46.6328325 n-C4H8 134.1200652 7510.72365 5329.74578 C4H6 426.4356254 23065.902981 15765.3257 H2 0 0 0 Total 852.8712509 47567.176256 33549.9857 Qsubzone 3 15837760.34



Menghitung Beban Panas Subzone 4



Beban panas untuk menurunkan suhu gas



Suhu masuk326.8198257 Suhu keluar 326.537731 Komponen mol (kmol/jamMassa (kg/jam)Qsg n-C4H10 0.029149621 1.6942925469 0.88573716 i-C4H10 0.000108209 0.0062895642 0.00324514 n-C4H8 0.013426342 0.7518751287 0.3573751 C4H6 0.01166617 0.6310231476 0.28664011 H2 362.3746238 724.74924769 2953.09584 Total 362.4289742 727.83272808 2954.62884 Beban panas untuk menurunkan suhu embunan



Suhu T'''' ( 326.537731 Komponen mol (kmol/jamMassa (kg/jam)λ (kJ/mol) Qv (kJ/jam) n-C4H10 291.2340488 16927.687853 19035.6138 5543819 i-C4H10 1.080806206 62.820779929 17001.0332 18374.822 n-C4H8 134.1196728 7510.7016757 18473.7832 2477698



C4H6 116.5816579 6305.9018772 18289.4002 2132209 H2 0 0 0 0 Total 543.0161857 30807.112186 72799.8304 10172100 Beban panas untuk pengembunan



Suhu masuk326.8198257 Suhu keluar 326.537731 Komponen mol (kmol/jamMassa (kg/jam)QsL n-C4H10 291.2340488 16927.687853 12398.979 i-C4H10 1.080806206 62.820779929 46.5945102 n-C4H8 134.1196728 7510.7016757 5325.54183 C4H6 116.5816579 6305.9018772 15753.4781 H2 0 0 0 Total 543.0161857 30807.112186 33524.5935 Qsubzone 4 10208579.26



Menghitung Jumlah Pendingin (AIR)



Cp (kJ/kmo



Err:509 Err:509



Err:509 Err:509



Suhu Masuk t1 (K) 303.15 Suhu Keluar t2 (K) 323.15 Cp air (kJ/kmolK) 1505.5337 Beban Panas Q(kJ/jam) 30964996.016 Massa Pendingin (kg/jam 370,214.18



Menghitung beda suhu rerata



Qt sigma Q/T



30964996 2957860 10.4687



Err:509 Err:509



Err:509 Err:509



Koefisien Perpindahan kalor Towler dan Sinnot "Chemical Engineering Design and Principles Practice and Economics of Plant and Process Design" halaman 797



Luas perpindahan kalor yang diperlukan



A



821.6278 m2



A



8,843.92 ft2



Luas perpindahan kalor lebih dari >10 m2, maka alat penukar kalor jenis shell and tube sesuai untuk digunakan. Ukuran tabung



Dari tabel 10 Kern halaman 843 dipilih pipa 0.5 18 0.402 0.127 0.3925



OD BWG ID at a"



0.0127 14.0000 0.0102 0.00008 0.1196



in in in2 ft2/ft



m m m2 m2/m



Pajang tabung standar 6, 8 , 10 ,12, 16, 24 ft Towler and Sinnot Halaman 805 Dipilih panjang pipa 18 ft 5.4864 m



Menentukan jumlah pipa



nt  nt



A a" L



=



1251.7945



Alat penukar kalor standar



Dari tabel 10-10 A , Ludwig , E.E., hal 49 in Ids np nt



m 0.8382 2 830



33 2 830



Susunan : ¾” pada 1-in triangular pitch pitch 1 in 0.025400051 de 0,73 in 0.018542 A Fig. 28 Kern



544.7788



m2



Koefisien perpindahan kalor standar (Terkoreksi)



Ud



5429.470 kJ/jam.m2.K 1.5082 kJ/s.m2.K



Route Fluida Fluida panas dialirkan dalam selongsong (shell) dan fluida dingin dialirkan dalam tabung (tube). Koefisien perpindahan kalor dalam tabung Luas aliran shell



Jarak antar baffle berkisar antara Ids/5 sampai Ids. Ids 0.8382 m B 0.16764 m C' 0.012700051 m Pitch 0.025400051 m As 0.070258065 m2 Flux massa



Gs



438528.9558 121.8135988



kg/jam.m2 kg/s.m2



Tav



508.59456



Komponen BM Kmol/jam yi kth (J/s.m. yi.kth.BM1yi.BM1/3 n-C4H10 58.124 291.26319843 0.32167956 0.0437875 0.0545622 1.2460686 i-C4H10 58.124 1.0809144156 0.00119379 0.0450458 0.0002083 0.0046243 n-C4H8 56 134.13309912 0.1481405 0.0387956 0.021988 0.5667652 C4H6 54.09 116.5933241 0.12876906 0.0446978 0.0217672 0.4869868 H2 2 362.37462384 0.40021709 0.2562503 0.1292122 0.5042419 Total 905.44515991 1 0.4285771 0.2277379 2.8086868 kth 0.081083417 J/s.m.K 0.291900301 kJ/jam.m.K



Komponen BM n-C4H10 i-C4H10 n-C4H8 C4H6 H2 Total μav cpav Bmcamp cpav



Kmol/jam Yi μ μ.yi.BM0,5yi.BM0,5 cp yi.cp 58.124 291.26319843 0.32167956 0.0448313 0.1099468 2.4524559 149.68446 48.15043 58.124 1.0809144156 0.00119379 0.0440917 0.0004013 0.0091014 150.39309 0.1795383 56 134.13309912 0.1481405 0.0466593 0.0517256 1.108582 129.95724 19.25193 54.09 116.5933241 0.12876906 0.0566535 0.0536534 0.9470437 120.63498 15.534053 2 362.37462384 0.40021709 0.0457545 0.0258967 0.5659924 29.298035 11.725574 905.44515991 1 0.2379902 0.2416237 5.0831754 579.96779 94.841525



0.04753401 kg/m.jam 94.84152499 kJ/kmolK 34.82811142 2.723131434 kJ/kgK



Bilangan reynold



Re



171060.7611



Bilangan Prandl



Pr



0.443443724



Koefisien perpindahan kalor



ho  0.36 ho



kthav 0.8  0.14 Re Pr1/ 3 ( ) De w



66401.867 18.44496305 kJ/m2.s.K



kJ/m2.jam.K



Tabung (tube) = fluida dingin



At



0.034003158 m2



Flux massa pada pendingin



Gt



10887641.14 kg/jam.m2 3024.34476 kg/s.m2



Tav kth



313.15 K 0.625267466 J/s.m.K 2.250962878 kJ/jam.m.K 0.000663454 kg/m.s 75.26697615 kJ/kmolK 1.391513702 kJ/kgK 1013.645317 kg/m3



μ Cp



Kecepatan liner



Vlin



10741.07575 m/jam 2.983632152 m/s



Bilangan Reynold Re = ID tube.Gt/miu



2.38843327 kg/m.jam



Re



46545.79539



Bilangan Prandl



Pr



1.47649597



Koefisien perpindahan kalor



hi



28591.89748 kJ/m2.jam.K 7.942193744 kJ/m2.s.K



hio



22987.88557 kJ/m2.jam.K 6.38552377 kJ/m2.s.K



Koefisien perpindahan kalor gabungan (Uc)



Uc



17076.21373 kJ/m2.jam.K 4.743392703 kJ/m2.s.K



Rd



0.000125619 m2.jam.K/kJ 0.452228549 m2.s.K/kJ



Rdmin



0.001 ft2.s.F/BTU 0.176366843 m2.s.K/kJ



Menghitung Pressure Drop Shell



kern halaman 840



Gs IDs N+1 De Re



438528.9558 121.8135988 kg/s.m2 0.8382 m L/B 32.72727273 0.018542 m 171060.7611



f  0.0035 



0.264 Re 0.42



f 0.005173712 rho fase cai 547.4991903 kg/m3 Ps



Ps max



103.7244703 kg/m.s2 0.001023678 atm 0.01504806 psi 5 psi



Tube



Gt rho air IDt pass L Re



10887641.14 kg/jam.m2 3024.34476 kg/s.m2 1013.645317 kg/m3 0.0102108 m 2 5.4864 m 46545.79539



ΔPr = v2 / 2g x ρ g x np Vlin g np Pr



10741.07575 m/jam 2.983632152 m/s 9.8 m/s2 2 9023.532265 kg/m.s2 9023.532265 Pa 0.089055315 atm



kg/jam.m2



1.309113136 psi



f  0.0014 



0.125 Re0.32



f



0.005410405



Pt



26232.16133 kg/m.s2 0.258890447 atm 3.805689565 psi



ΔPT = ΔPt + ΔPr PT PT max



5.1148027 psi 0.348040467 atm 10 psi