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Neraca Panas Basis waktu
: 1 jam
Satuan panas
: Kilo jule (Kj)
Temperatur referensi
: 25 C
Kapasitas Produksi
298.15 K
82070.7071 kg/jam
Data Cp gas untuk komponen gas Komponen
A
B
C
D
E
NH3
33.573
-1.26E-02
8.89E-05
-7.18E-08
1.86E-11
H2SO4
9.486
3.38E-01
-3.81E-04
2.13E-07
-4.69E-11
H2O
33.933
-8.42E-03
2.99E-05
-1.78E-08
3.93E-12
N2
29.414
-4.60E-03
1.30E-05
-5.48E-09
2.92E-13
Data-data kontatnta kapasitas panas dalam bentuk cairan Komponen
A
B
C
D
NH3
-182
3.36E+00
-1.44E-02
2.04E-05
H2SO4
26.004
7.03E-01
-1.39E-03
1.03E-06
H2O
92.053
-4.00E-02
-2.11E-04
5.35E-07
(Sumber Perry, 1999 dan Yaws ) 1. Tangki penyimpanan H₂SO₄
T= 30 ⁰C 303.15 P= 1 atm 14.7 T ref= 25 ⁰C 298.15 T out = 107 ⁰C 380.15 Laju alir massa H₂SO₄ = Kadar bahan baku x Total Produk Laju lir molar H₂SO₄ =laju alir massa H₂SO₄ : BM H₂SO₄ Laju alir massa H₂O = Kadar bahan baku x Total produk
K psia K K 80429.29286 kg/jam 820.1965395 Kmol/jam 1641.41414 kg/jam
Laju alir mola H₂O= Laju alir massa H₂O : BM H₂O 91.114757866 Kmol/jam Panas Input Komponen Massa (Kg) N (Kmol) ʃCp dT Q (kj/jam) H₂SO₄ 80429.29286 820.196539501 698.54229633 572941.97415 H₂O 1641.41414 91.1147578658 377.47141324 34393.216419 TOTAL 82070.707 911.311297367 1076.0137096 607335.19057 Panas input = 607335.190565 kj/jam Panas Output Komponen Massa (Kg) N (Kmol) ʃCp dT Q (kj/jam) H₂SO₄ 91.114757866 820.196539501 11851.744696 9720759.9867 H₂O 34393.216419 91.1147578658 6172.4935286 562405.25328 TOTAL 34484.331177 911.311297367 18024.238225 10283165.24 10283165.24 Kj/jam Panas output = Menghitungan Kebutuhan steam Q in + Q steam = Qout Q steam = 9675830.0494 kj/jam
Oleh karena membutuhkan fluida panas yang berfungsi sebagai pemanas, yaitu saturated steam pada steam tabel dengan kondisi : P = 14.7 psia HL = 180.07 Kj/kg HV = 1150.4 Kj/kg 970.33 Kj/kg λ steam =Hv - HL Menghitung massa steam (m) m steam = Qsteam / λ steam m steam= 9971.6900945 kg panas steam masuk = m steam x Hv 11471432.285 Kj/jam panas steam keluar= m steam x HL 1795602.2353 kj/jam
Neraca panas total Panas input Q in 607335.19057 Q steam in 11471432.285 TOTAL
Panas output Q out 10283165.24 Q steam out 1795602.2353
12078767.475
12078767.475
2. Vaporizer Berfungsi : Untuk mengubah fasa amonia cair menjadi fase gas sebanyak 80% gas dan 20% cair T= -35
⁰C
238
K
P= 1
atm
14.7
psia
⁰C
298
K
T ref= 25
Laju alir massa NH₃ = Kadar bahan baku x Total Produk
81660.3535645 Kg/jam 4801.5730913447 Kmol/jam
Laju lir molar NH₃ =laju alir massa NH₃ : BM NH₃
410.3535355 Kg/jam
Laju alir massa H₂O = Kadar bahan baku x Total produk
22.7786894942 Kmol/jam
Laju alir mola H₂O= Laju alir massa H₂O : BM H₂O Anotoine Komponen
A
B
C
NH3
16.9481
2132.5
-32.98
CO2
22.5898
3103.39
22.5898
H2O
18.3036
3816.44
-46.13
Tdew komponen nh3 h2O
312.436575874 K 39.4365758735 °C zi ln P° P° K xi 0.9952783938 9.3172185533 11127.98686526 0.9960604068 0.0047216062 13.3266785759 613342.3708427 54.8999615864 1
Enthalpy vaporization = A (1-T/Tc)^n Komponen h20 nh3
A
Tc 52.053 31.523
n 647.13 405.65
0.321 0.364
1.00 0.00 1.00
Panas masuk Komponen
massa (kg/jam)
mi(Kmol/jam)
ʃCp.dt
Q(kj/jam)
NH₃
81660.3535645
4801.5730913447
-4640.043168
-22279506.4181468
H₂O
410.3535355
22.7786894942
-4592.5201872
-104611.591340045
Total
82070.7071
4824.3517808389
-22384118.0094869
Q keluar (sensibel) T=
312.4365758735 °K
komponen
massa
39.4365758735 C
kmol/jam
102.9858365724
ʃCpdT
zi
Q(sensibel) (kj/jam)
NH3
81660.3535645
4801.5730913447
0.9952783938
1184.056550324
5685334.07066593
H2O
410.3535355
22.7786894942
0.0047216062
1088.5856768057
24796.5551197833
Total
82070.7071
4824.3517808389
1
5710130.62578572
Q keluar ( latent) komponen
massa
kmol/jam
L(J / mol)
NH3
81660.3535645
4801.5730913447
H2O
410.3535355
22.7786894942
Total
82070.7071
4824.3517808389
Beban vaporizer total = (Q sensible + Q latent) - Q masuk = Neraca panas total Arus Qmasuk
input (kj/jam)
output (Kj/jam)
-22384118.01
Q(latent)
89580.01
Q(sensibel)
5710130.62578572
Qsteam
28183828.65
jumlah
5799710.63640273
5799710.63640273
Q (latent)
18.4565516859 88620.4819341117 42.1239634153
959.5286829012 89580.0106170129
28183828.65 Kj/jam
F
3. Centrifuge Separator Berfungsi : T=
60 C
P=
333.15 K
1.5 atm
Tref =
22.05 psia
25 C
298.15 K
Data-data kontatnta kapasitas panas dalam bentuk cairan Komponen
A
B
C
D
NH3
-182
3.36E+00
-1.44E-02
2.04E-05
H2SO4
26.004
7.03E-01
-1.39E-03
1.03E-06
H2O
92.053
-4.00E-02
-2.11E-04
5.35E-07
(NH₄)₂SO₄
51.6
Panas masuk centrifuge Komponen
Massa (Kg)
N(Kmol)
ʃCp dT
Q (kj/jam)
H₂SO₄
49.04
0.5000968785
4961.7517573498
2481.3565656116
(NH₄)₂SO₄
26558.8186
201.1102339071
1806
1519648.38722102
H₂O
393.2509
21.8472722222
2634.0941342613
57547.7716101656
TOTAL
1579677.5153968
Panas keluar centrifuge ke MLT Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 35.7606 0.3646770888 4961.7517573498 1809.4371859749 (NH₂)₂SO₂ (l) 13279.4093 201.1102339071 903 759824.19361051 H₂O 52.4037 2.9113166667 2634.0941342613 7668.6821546439 TOTAL 769302.31295113 Panas keluar Centrifuge ke Rotary Dryer Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 13.2794 0.1354197897 4961.7517573498 671.9193796367 (NH₂)₂SO₂ (k) 13279.4093 201.1102339071 903 759824.19361051 H₂O 340.8473 18.9359611111 2634.0941342613 49879.104089378 TOTAL 810375.21707952 Neraca panas total centrifuge Komponen Input Output Q in 1579677.5153968 Q dari MLT 769302.31295113 Q dari Dryer 810375.21707952 Total 1579678 1579678
4. Neraca panas Rotary Dryer Kondisi operasi dalam Rotary dryer T in = P= T ref =
90 C 1 atm 25 C
363.15 K 14.7 K 298.15 K
Neraca panas masuk : Q in rotary dryer = Q out centrifuge
810375.2171 Kj/jam
Neraca panas keluar : Neraca panas keuar Produk Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 13.1809 0.1344153129 9333.1972618401 1254.5246304707 (NH₂)₂SO₂ (k) 13147.93 99.5595217362 3354 1397130.7661862 H₂O 19.7713 1.0984055556 4888.7266588325 5369.8045216542 TOTAL 13180.8822 1403755.0953384 Neraca panas keluar ke cyclone T in = 48.94 C 322.09 K P= 1 atm 14.7 psia T ref = 25 C 298.15 K Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 0.0985 0.0010044768 3376.3942305137 3.3915096899 (NH₂)₂SO₂ (l) 131.4793 0.9955952174 1235.304 5145.7400834613 H₂O 321.0759 17.83755 1803.2995203263 32166.445358796 TOTAL 452.6537 37315.576951947
-630695.455 Kj/jam
Q Loss = Q in - Q out =
Neraca panas total Rotary Dryer Komponen Q input (Kj) Q output (Kj) Q masuk 810375.21707952 Q keluar 1441070.6722903 Q loss -630695.45521078 Total 810375.21707952 810375.21707952
5. Neraca Panas Reaktor Berfungsi: Tempat bereaksinya NH3 dan H2S04 untuk menghasilkan (NH4)2SO4 Kondisi Operasi: T=
107 C
P=
380.15 K
1 atm
14.7 psia
Tref = 25 C Panas masuk reaktor: panas masuk dari tangki asam sulfat (H₂SO₄) Panas masuk dari Vaporizer
298.15 K 12078767.4753 kj/jam 5799710.6364 kj/jam
Neraca panas Mother Liquor Tin =
60 C
P=
1.5 atm
T op =
333.15 22.05 psia
25 C
Komponen (NH₄)₂SO₄ (l)
Massa (Kg/jam) 13410.8886
298.15 K
N (mol/jam) 1771.0553594046
ʃCp.dt
Q (kj/jam) 903 1599262.98954235
H₂SO₄
35.8591
3.5163792051
4961.7517573498 17447.4007004133
H₂O
227.4066
4.0933188
2634.0941342613 10782.1870407416
TOTAL
1627492.57728351
Q mother liquor =
1627492.57728351 kj/jam
Panas aliran keluar dari rekator = T=
107 C
P=
380.15 K
1 atm
Tref =
14.7 psia
25 C
298.15 K
Menghitung entalpi pada tekanan standar (∆H⁰R 298.15 K) Komponen
∆Hf (kj/mol)
(NH₄)₂SO₄
-1169.498844
H₂SO₄
-813.9963013
NH₃
-45.887328
∆Hf 298.15 = ∆Hf produk - ∆Hf reaktan ∆Hf 298.15 = ∆Hf (NH₄)₂SO₄ - (∆Hf H₂SO₄ + ∆Hf NH₃)
=
-263.7278867 5.6217696308 -1482.6174243
Panas reaksi, (298.15 K) bernilai negatif maka reaksi adalah ekotermis. Panas reaksi utama standar =
_� (380.15 �)= 〖�� ° 〗 _(�(298.15�))+(∫_298.15^380.15▒���) �_� = 〖∆ ° 〗 _�+(∫_�1^�2▒∆� 〖��� ��〗 ) ∆ Neraca panas Produk Komponen
massa (kg/jam)
(NH₄)₂SO₄ (k)
ʃCp.dt
Q (kj/jam)
26558.8186
3507.3841431346
4231.2 14840443.7864311
49.04
4.80891144
11851.7446959737 56993.9906524271
393.2509
7.0785162
6172.493528577 43692.0954364275
H₂SO₄ H₂O
N (mol/jam)
TOTAL
14941129.87252
Neraca panas Kondensor Tin =
-35 C
P=
238.15 K
1 atm
14.7 psia
T reff =
25 C
298.15 K
T out =
107 C
386.15 K
Panas masuk Condensor Komponen
massa (Kg/jam)
mi(kmol/jam)
ʃCp.dt
Q (kj/jam)
NH3
17.03
289.62921
-4640.546173491
-1344037.72219673
H2O
17.03
306.54
-4592.1844503273 -1407688.22140334
Total
-2751725.94360007
Panas keluar Condensor Komponen
massa (Kg/jam)
mi(kmol/jam)
ʃCp.dt
Q (kj/jam)
NH3
2.7078
46.0515546
9067.2103000908
417559.130204314
H2O
2.7078
48.7404
6627.5648664234
323030.162615421
Total Q kondensor =
740589.292819735 3492315.23642 kj/jam
panas masuk = panas keluar+ Qc
Q masuk = 19505970.6889747
Qc = 1072525.58003496 Kj/jam
Q keluar = 18433445.1089398
Neraca panas Total Komponen
Input
Umpan Gas(NH3)
5799710.63640273
Umpan cair(H2SO4)
12078767.4752885
Output
Produk
14941129.87252
Mother liquor
1627492.57728351
Kondensat
3492315.2364198
Panas reaksi
-1482.6174242569
Panas hilang
-1482.6174242569
-1074008
1072525.58003496
TOTAL
19504488.0715505 19504488.0715505
Q yang dibutuhkan =
39008976.143101 kj/jam
Media pendingin yang digunakan adalah air : T in = 30
C
303.15
K
T out = 50
C
323.15
K
T ref = 25
C
298.15
K
H(323.15 K)-(H303.15 K) =[H(323.15 K)-H(29.15 K)]-[(H(303.15K)-(298.15 K)]
∫1_298.15^323.15▒ 〖〖��〗 _((�2 �)) �� −∫1_298.15^303.15▒ 〖〖� �〗 _((�2�)) �� = 〗〗
1882.9602088601 =
-
377.471413241
1505.4887956187 J/mol
= 83638.2664232609 J/kg =
83.6382664233 Kj/kg
Air pendingin yang dibutuhkan : m= Q/(H (323.15 K) -H (303.15 K))
= 466401.060319587 Kj/kg
kj/mol mol/jam kj/jam
x 1000 mol/kmol : 18 kg/kmol
3. Centrifuge Separator Berfungsi : T=
60 C
P=
333.15 K
1.5 atm
Tref =
22.05 psia
25 C
298.15 K
Data-data kontatnta kapasitas panas dalam bentuk cairan Komponen
A
B
C
D
NH3
-182
3.36E+00
-1.44E-02
2.04E-05
H2SO4
26.004
7.03E-01
-1.39E-03
1.03E-06
H2O
92.053
-4.00E-02
-2.11E-04
5.35E-07
(NH₄)₂SO₄
51.6
N(Kmol)
ʃCp dT
Q (kj/jam)
Panas masuk centrifuge Komponen Massa (Kg) H₂SO₄ (NH₄)₂SO₄ H₂O
305.3474
3.1138515822 4961.75175735 15450.15856
165368.3712 1252.21201717 2448.5752
34.825
182456.856724
136.031955556 2634.09413426 358320.976201
TOTAL
556227.991485
Panas keluar centrifuge ke MLT Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 45.8021 0.4670776353 4961.7517573 2317.523278 (NH₂)₂SO₂ ( 82684.1856 1252.2120172 22.75 119192.92148 H₂O 367.2863 20.404794444 2634.0941343 53748.149357 TOTAL 175258.59411 Panas keluar Centrifuge ke Rotary Dryer Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 259.5452 2.6467729271 4961.7517573 13132.630222 (NH₂)₂SO₂ ( 82684.1856 1252.2120172 12.075 63263.935246 H₂O 2081.289 115.62716667 2634.0941343 304572.84148 TOTAL 380969.40695 Neraca panas total centrifuge Komponen Input Output Q in 556227.99148 Q dari MLT 175258.59411 Q dari Dryer 380969.40695 Total 556228 556228
0.0
4. Neraca panas Rotary Dryer Kondisi operasi dalam Rotary dryer T in = P= T ref =
90 C 1 atm 25 C
363.15 K 14.7 K 298.15 K
0.0
Neraca panas masuk : Q in rotary dryer = Q out centrifuge
380969.4 Kj/jam
Neraca panas keluar : Neraca panas keuar Produk Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 259.5452 2.6467729271 9333.1972618 24702.853836 (NH₂)₂SO₂ ( 81865.5303 619.90693922 22.425 58163.448248 H₂O 123.1061 6.8392277778 4888.7266588 33435.115163 TOTAL 82248.1816 116301.41725 Neraca panas keluar ke cyclone T in = 48.94 C 322.09 K P= 1 atm 14.7 psia T ref = 25 C 298.15 K Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 177.4745 1.8098377541 3376.3942305 6110.7257509 (NH₂)₂SO₂ ( 818.6553 6.1990693695 15.561 403.60375245 H₂O 1958.1829 108.78793889 1803.2995203 196177.23802 TOTAL 2954.3127 202691.56752 Q Loss = Q in - Q out =
61976.42 Kj/jam
Neraca panas total Rotary Dryer Komponen Q input (Kj) Q output (Kj) Q masuk 380969.40695 Q keluar 318992.98477 Q loss 61976.42218 Total 380969.40695 380969.40695
5.
Neraca panas Cyclone Separator
Kondisi Operasi : T in = P= T ref =
48.94 C 1 atm 25 C
Neraca panas masuk : Q in cyclone searator = Q out Rotary dryer Komponen H₂O TOTAL
322.09 K 14.7 K 298.15 K
#REF! Kj/jam
Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) 1048.6602 58.2589 #REF! #REF! 1048.6602 #REF!
Neraca panas keluar : Neraca panas keluar ke Mother Liquor dan Udara Komponen Massa (Kg) N(Kmol) ʃCp dT Q (kj/jam) H₂SO₂ 177.4745 1.8098377541 #REF! #REF! (NH₂)₂SO₂ ( 818.6553 12.398138739 15.561 807.2075049 H₂O 1048.6602 58.2589 #REF! #REF! TOTAL
#REF!
