Neraca Massa 220219.xls
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density (ρ) T= ρ= KOMPONEN C8H4O3 C2H5OH C12H14O4 H2O H2SO4 Na2SO4 kapasitas panas (Cp) T= Cp = KOMPONEN C8H4O3 C2H5OH C12H14O4 H2O H2SO4
80 C A.B^-(1-T/Tc)^n A 0.35183 0.2657 0.34999 0.3471 0.42169 0.26141
= B 0.2322 0.26395 0.25154 0.274 0.19356 0.1
130 C = A+(B*T)+(C*T^2)+(D*T^3) A B -105.627 1.96E+00 59.342 3.64E-01 125.381 1.58E+00 92.503 -4.00E-02 26.00400 0.70337
0.2346 0.2367 0.3525 0.28571 0.28570 0.28571
353 K (ρ = gr/mL; T=K) Tc Tmin 791 404.26 516.25 195.05 757 296.15 647.13 273.16 925.00000 283.46 3700 1157
C -3.66E-03 -1.22E-03 -3.47E-03 -2.11E-04 -0.00139
403 K (Cp= Joule/mol K; T=K) D Tmin 2.85E-06 405 1.80E-06 160 3.33E-06 270 5.35E-07 273 0.00000 296
n
Viskositas (µ) Yaws, hal 487, table 22.1 viscosity of liquid log µ = A+(B/T)+(C*T)+(D*T^2) (µ = cP; T=K) T= 80 = 353 K Komponen A B C D C8H4O3 -25.1512 5.0387E+03 4.1950E-02 -2.4927E-05 C2H5OH -6.4406 1.1176E+03 1.3721E-02 -1.5465E-05 C12H14O4 -12.1587 2.5728E+03 1.8732E-02 -1.1566E-05 H2SO4 -18.7045 3.4962E+03 3.3080E-02 -1.7018E-05 H2O -10.2158 1.7925E+03 1.7730E-02 -1.2631E-05 Na2SO4 11.2905 -4.58E+03 -6.78E-03 9.24E-07 TOTAL -61.3803 9.4409E+03 0.1184282 -8.06826E-05
Tmax 791 516.25 757 647.13 363.49 2000
Tmax 712 465 681 615 879
Tmin 405 240 269 283 273 1180 2650
Tmax 791 516 757 367 643 1267 4341
Konduktifitas panas (k) Yaws, hal 535, table 24.1 thermal conductifity of liquid organic: log k = A+B(1-T/C)^(2/7) (k=W/m.K;T=K) inorganic: k= A+BT+CT^2 Komponen A B C Tmin C8H4O3 -1.6831 1.0293 791 404 C2H5OH -1.3172 0.6987 516.25 159 C12H14O4 -1.3265 0.5567 757 269 H2SO4 0.1553 1.07E-03 -1.29E-06 283 H2O -0.2758 4.61E-03 -5.54E-06 273 TOTAL -4.4473 2.2903819 2064.249993175 1388
T= k (25ᵒC) 0.1694 0.1432 0.36 0.607 1.2796
Tmax 751 490 719 833 633 3426
Vapor Pressure (P) Yaws, pers 7-1 hal. 159. Vapor Pressure Organic and Inorganic Compound log P= A+(B/T)+(C log T)+(D*T)+(E*T^2) (P=mmHg , T=K)
T=
Komponen C2H5OH C12H14O4 H2O
A 71.2535 23.8442 29.8605
B -5.50E+03 -2.86E+03 -3.15E+03
C -2.14E+01 -5.47E+00 -7.30E+04
D 3.81E-10 3.74E-11 2.42E-09
E 5.03E-06 2.74E-07 1.81E-06
log P 1.41E+00 1.47E+00 -1.84E+05
ρ (g/cm^3) 1.25419 0.73262 1.0578 0.9757 1.7647 2.4495
ρ (kg/m^3) fv (m3/jam) 1254.19 732.62 1057.8 975.7 1764.7 2449.5
Cp 25 (g/cm^3) 264.72 107.4 374.9 75.55 139.95
Cp (kg/m^3) fv (m3/jam) 2.77E+02 1.26E+02 4.15E+02 7.71E+01 1.52E+02
log µ
µ
0.8250 -0.3582 0.3009 0.7564 -0.4531 -3.9551 -2.8841605583
333
fraksi mol 6.6828 0.4384 1.9992 5.7068 0.3523 0.0001 15.1795426745
K
k 0.157550286 0.1594126978 0.1397125053 2.6693365175 3.1199624425 6.2459744491
fraksimol
333 K
P 2.56E+01 2.92E+01 0.00E+00
NERACA MASSA PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan ETYL ALKOHOL KAPASITAS 30.000 TON/TH Kapasitas produksi
= = =
kemurnian produk impuritis
30000.0000 30000.0000 3787.8788 0.9900 0.0100
ton/tahun ton/th x 1 th/330 hari x 1 hari/24 j x 1000 kg/ton kg/j 17.0625 C12H14O4 3750.0000 H20 37.8788 3787.8788
REAKTOR reaksi yang terjadi C8H4O3
+
DEP Terbentuk Etanol 20% berlebihan
=
komposisi bahan terbentuk / berx DEP Terbentuk H2O terbentuk PA brx EA brx
NETRALIZER Reaksi: M R S M R S Kebutuhan NaOH= H2O (Impurities NaOH)= Neraca Massa Netralizer Komponen
kg/jam 16.8919
= = = = = = =
kg/jam 3750 304.0540540541 2500 1554.0540540541 kg/jam
21.1149 0.1602399754 42.2297297297 50.6756756757 6.8160265529 0.637755102 0.070861678 kmol/jam
= = = = = =
3750.0000
16.8919 16.8919 16.8919 33.7837837838 kmol/jam
Komposisi Bahan Keluar PA MA EA H2O H2SO4 DEP
C12H14O4
kmol/jam = = = =
Komposisi Bahan Masuk Reaktor PA masuk reaktor MA masuk reaktor EA stci EA masuk reaktor H2O dalam EA H2SO4 MR H2O dalam H2SO4
2 C2H5OH kmol/jam
3125.00000 15.70352 1942.56757 2331.08108 122.68848 62.50000 1.27551 5623.433509
EA recycle= EA (FF)= H2O impurities EA FF=
H2O dari recycle (Asumsi 2% H2O
kg/jam
4.2230 0.1602 16.8918918919 21.8446 0.637755102 16.8919
625.0000 15.7035 777.0270 393.2030 62.5000 3750.0000 5623.4335085886
H2SO4 0.637755102 0.637755102 0 C6H4(CO)2O 4.2229730 4.2229730 0 10.0419361008 24.1750313538
+2NaOH 1.2755102041 1.2755102041 0 +2NaOH 8.4459459459 8.4459459459 0 kmol/jam kmol/jam
----->
= =
0 0.637755102 0.637755102 C8H4Na2O4 0 4.2229730 4.2229730 401.67744403 435.15056437
BM
Masuk
kg/j
Keluar
---->
Na2SO4
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 DECANTER Komponen MA DEP H2O EA Na2SO4 C8H4Na2O4 C4H2Na2O4
148.0000 98.0000 222.000 18.0000 98.0000 46.000 40.0000 142.0000 210.0000 160
4.2230 0.1602 16.8919 46.0196 0.637755102 16.8918918919 10.0419361008 0 0 0
98.0000 222.000 18.0000 46.000 142.0000 210.0000 160
Masuk Decanter 0.0000 16.8919 51.6783636159 16.8919 0.6378 4.2230 0.1602400
BM
625 0 15.7035175879 0.0000 3750 16.8919 828.3535283417 51.6784 62.5 0 777.027027027 16.891891892 401.6774440321 0 0 0.637755102 0 4.2229730 0 0.1602 6460.2615 kg/j Densitas 0 0.185 3750 1.0578 930.2105450857 0.9757 777.027027027 0.73262 90.5612244898 2.4495 886.8243243243 2.34 25.6383960619 2.2 6460.2615169888
Hasil Atas Decanter Asumsi H2O sebagai hasil atas decanter sebesar 2% H2O terbentuk di reaktor Komponen BM kmol/jam kg/j Densitas DEP 222.000 16.8919 3750 1.0578 EA 46.000 16.8919 777.027027027 0.73262 H2O 18.0000 2.4422 43.9598689599 0.9757 4570.9868959869 Hasil Bawah Decanter Komponen BM kmol/jam kg/j Densitas H2O 18.0000 49.2361 886.2506761258 0.9757 Na2SO4 142.0000 0.6378 90.5612244898 2.4495 C8H4Na2O4 210.0000 4.2230 886.8243243243 2.34 C4H2Na2O4 160 0.1602400 25.6383960619 2.4 1889.2746210019 KELUAR DECANTER 6460.2615169888 EVAPORATOR Bahan Masuk Evaporator 0.953358709 Komponen BM kmol/jam kg/j DEP 222.000 16.8919 3750 EA 46.000 16.8919 777.027027027 H2O 18.0000 2.4422 43.9598689599 4570.9868959869 Evaporator dijalankan pada suhu 85 C TD Bahan MA 202 C Berdasarkan titik didih bahan maka komponen yang menja DEP 295 C dan yang menjadi hasil bawah evaporator adalah DEP dan EA 78.29 C H2O 100 C Hasil Atas Evaporator Komponen BM kmol/jam kg/j EA 46.000 16.8919 777.027027027 H2O 18.0000 0.3378 6.0810810811 783.1081081081 Hasil Bawah Evaporator
Komponen DEP H2O
BM
kmol/jam 222.000 18.0000
kg/j 16.8919 2.1044
KELUAR EVAPORATOR MIXER Komponen Masuk Mixer Komponen PA MA EA H2O Komponen Keluar Mixer Komponen PA MA EA H2O
BM
kmol/jam 148.0000 98.0000 46.000 18.0000
BM
21.1149 0.1602399754 50.6757 4.8819
kmol/jam 148.0000 98.0000 46.0000 18.0000
21.1149 0.1602399754 50.6756756757 4.8818555398
3750 37.8787878788 3787.8787878788 4570.9868959869
kg/j 3125 15.7035175879 2331.0810810811 87.8733997155 5559.6579983845 kg/j 3125 15.7035175879 2331.0810810811 87.8733997155 5559.6579983845
AS 30.000 TON/TH KOMPONEN C8H4O3 C2H5OH C12H14O4 H2SO4 NaOH Na2SO4 H2O MA C8H4Na2O4
hari/24 j x 1000 kg/ton kg/jam kg/jam
+
16.8919 kmol/jam 2.1044 kmol/jam
H2O
x=
C8H4O3 + 21.1148649 16.8919 4.2230
0.8000 2 C2H5OH 50.6756757 33.7837838 16.8918919 EA keluar reaktor= EA masuk reaktor=
O impurities EA FF=
16.8918919 kmol/jam 33.7837838 kmol/jam 81.7923186 kg/jam
O dari recycle (Asumsi 2% H2O terbentuk )=
+2H2O 0 1.2755102041 1.2755102041 +H2O 0 4.2229730 4.222972973 kg/jam kg/jam kg/j
M R S
BM 148.0000 46.000 222.000 98.0000 40.0000 142.0000 18.0000 98.0000 210.0000
C12H14O4
+
0 16.8919 16.8919 16.8918918919 kmol/jam 50.6756756757 kmol/jam
2331.08108 777.027027 kg/jam 1554.05405 kg/jam 4.5440177 kmol/jam 0.33783784 kmol/jam
6.0810810811 kg/jam
C4H2O3 + 2NaOH ---> 0.1602 0.3204799508 0.1602 0.3204799508 0 0
C4H2Na2O4 0 0.1602 0.1602
0 0 3750 930.21054509 0 777.02702703 0 90.56122449 886.82432432 25.638396062 6460.261517 Data Kelarutan Bahan MA bereaksi menjadi maleic acid DEP 1g/100mL H2O tercampur dengan etanol EA tercampur dengan air Na2SO4 13,9g/100mL C8H4Na2O sedikit larut dalam air
volume 3545.0935905 1060.6139977 45.054698124 4650.7622863 densitas rata-rata= volume 908.32292316 36.971310263 378.98475398 10.682665026 densitas rata-rata= 1334.9616524
0.98284681
1.41522763
han maka komponen yang menjadi hasil atas evaporator adalah EA dan H2O wah evaporator adalah DEP dan MA
Tabel Neraca Massa Total Komponen FF PA MA EA H2O DEP H2SO4 NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL Neraca Massa Overall Komponen PA MA EA H2O H2SO4 NaOH DEP Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
MIXER Masuk (kg/jam) RC 3125.0000 15.7035 1554.0541 777.0270 81.7923 6.0811
5559.6580 Masuk (kg/jam) Katalis
FF 3125.0000 15.7035 1554.0541 81.7923
1.2755 62.5000
5677.1534
Kemurnian Bahan Baku PA EA H2SO4 NaOH
99.50% 95% 98% 48%
H2O x= 0.3378378378 16.8919 17.2297
0.8000
777.027027027 2331.0810810811
Tabel Neraca Massa Reaktor Komponen
MF
PA MA EA H2SO4 H2O DEP TOTAL
Masuk (kg/jam) Katalis 3125.00000 15.70352 2331.08108 87.87340 5623.4335
Keluar (kg/jam)
62.50000 1.27551
625.0000 15.7035 777.0270 62.5000 393.2030 3750.0000 5623.4335
+ H2O 0 0.1602 0.1602
Tabel Neraca Massa Netralizer Komponen
Masuk (kg/jam) Keluar Reaktor Penetral
Keluar (kg/jam)
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
625.0000 15.7035 0 3750.0000 3750 393.2030 435.1505643681 930.2105450857 62.5000 777.0270 777.027027027 401.6774440321 90.5612244898 886.8243243243 25.6383960619 6460.2615 6460.261516989
Tabel Neraca Massa Dekanter Komponen C4H2Na2O4 DEP H2O EA Na2SO4 C8H4Na2O4 TOTAL
Masuk (kg/jam) 25.6383960619 3750 930.2105450857 777.027027027 90.5612244898 886.8243243243 6460.2615169888
Keluar (kg/jam) Hasil Atas Hasil Bawah 0 25.6383960619 3750 43.9598689599 886.2506761258 777.027027027 90.5612244898 886.8243243243 6460.2615169888
Tabel Neraca Massa Evaporator Komponen DEP EA
Masuk (kg/jam) 3750 777.027027027
Keluar (kg/jam) Hasil Atas Hasil Bawah 3750 777.027027027
H2O TOTAL
43.9598689599 4570.9868959869
Tabel Neraca Massa Mixer Komponen
FF
PA MA EA H2O TOTAL
MIXER Keluar (kg/jam) 3125.0000 15.7035 2331.0811 87.8734
5559.6580
uk (kg/jam)
677.1534
6.0810810811 37.8787878788 4570.9868959869
MF
Masuk (kg/jam) Keluar (kg/jam) RC 3125 3125 15.7035175879 15.7035175879 1554.0540540541 777.027027027 2331.081081081 81.7923186344 6.0810810811 87.8733997155 5559.6579983845 5559.657998385
REAKTOR NETRALIZER Masuk (kg/jam) Masuk (kg/jam) Keluar (kg/jam) Katalis Keluar Reaktor Penetral 3125.0000 625.0000 625.0000 15.7035 15.7035 15.7035 2331.0811 777.0270 777.0270 87.8734 1.2755 393.2030 393.2030 435.1506 3750.0000 3750.0000 62.5000 62.5000 62.5000 401.6774
5623.4335
5623.4335
Keluar (kg/jam) Hasil Bawah Dekanter Produk
Penetral
435.1506
886.2507
37.8788
401.6774 3750.0000 90.5612 886.8243 25.6384 5677.1534
6460.2615
TRALIZER Keluar (kg/jam)
DECANTER Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
0.0000 777.0270 930.2105 3750.0000
0.0000 777.0270 930.2105 3750.0000
90.5612 886.8243 25.6384 6460.2615
90.5612 886.8243 25.6384 6460.2615
0.0000 777.0270 43.9599 3750.0000
886.2507
EVAPORATOR Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah 0.0000 777.0270 43.9599 3750.0000
0.0000 777.0270 6.0811
37.8788 3750.0000
90.5612 886.8243 25.6384 6460.2615
4570.9869
4570.9869
PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan ETYL ALKOHOL KAPASITAS PRODUKSI 30.000 TON/TH H2SO4
62.500
H2O
1.2755 63.7755
EA= H2O=
777.027027027 6.0810810811 783.1081081081
EA= 1554.05405405 H2O= 81.7923186344 1635.8464 PA=
3125
MA=
15.7035
Mixer 1 atm
3140.7035
PA=
3125
Reaktor 1 atm
MA= 15.703518
PA=
625.0000
EA= 2331.0811
MA=
15.7035
87.8734
EA=
777.0270
5559.658
H2SO4=
62.5000
H2O=
393.2030
DEP=
3750.0000
H2O=
NaOH= 401.677444032 H2O= 435.150564368
3750
H2O=
43.9598689599
EA=
777.027027027 4570.98690
Evaporator 1 atm
5623.4335
836.8280084 FF+RC Katalis+MF RP+Netral UPL+HADec HAEvap+P
DEP=
Netralizer 1 atm
5559.6580 5623.4335 6460.2615 6460.26152 4570.9869
Produk :
Decanter 1 atm
DEP=
DEP=
3750
H2O=
930.2105
H2O=
EA=
777.0270
Na2SO4=
90.5612
C8H4Na2O4=
886.8243
C4H2Na2O4=
25.6384
Na2SO4=
90.5612244898
6460.2615
C4H2Na2O4=
25.6383960619
C8H4Na2O4=
886.8243243243
ke UPL H20=
886.2506761258
1889.2746210019
Evaporator 1 atm
3750 37.8788 3787.8788
NERACA MASSA PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan 2-ETYL ALKOHOL KAPASITAS 25.000 TON/TH Kapasitas produksi
= = =
kemurnian produk impuritis
25000.0000 25000.0000 3156.5657 0.9900 0.0100
ton/tahun ton/th x 1 th/330 hari x 1 hari/24 j x 1000 kg/ton kg/j 14.2188 C12H14O4 3125.0000 H20 31.5657 3156.5657
REAKTOR reaksi yang terjadi C8H4O3
+
DEP Terbentuk Etanol 20% berlebihan
=
komposisi bahan terbentuk / berx DEP Terbentuk H2O terbentuk PA brx EA brx
NETRALIZER Reaksi: M R S M R S Kebutuhan NaOH= H2O (Impurities NaOH)= Neraca Massa Netralizer Komponen
kg/jam 14.0766
= = = = = = =
kg/jam 3125 253.3783783784 2083.3333333333 1295.0450450451 kg/jam
17.5957 0.1335333128 35.1914414414 42.2297297297 5.6800221274 0.531462585 0.0590513983 kmol/jam
= = = = = =
3125.0000
14.0766 14.0766 14.0766 28.1531531532 kmol/jam
Komposisi Bahan Keluar PA MA EA H2O H2SO4 DEP
C12H14O4
kmol/jam = = = =
Komposisi Bahan Masuk Reaktor PA masuk reaktor MA masuk reaktor EA stci EA masuk reaktor H2O dalam EA H2SO4 MR H2O dalam H2SO4
2 C2H5OH kmol/jam
2604.16667 13.08626 1618.80631 1942.56757 102.24040 52.08333 1.06293 4686.194590
EA recycle= EA (FF)= H2O impurities EA FF=
H2O dari recycle (Asumsi 2% H2O
kg/jam
3.5191 0.1335 14.0765765766 18.2038 0.531462585 14.0766
520.8333 13.0863 647.5225 327.6691 52.0833 3125.0000 4686.1945904905
H2SO4 0.531462585 0.531462585 0 C6H4(CO)2O 3.5191441 3.5191441 0 8.368280084 20.1458594615
+2NaOH 1.0629251701 1.0629251701 0 +2NaOH 7.0382882883 7.0382882883 0 kmol/jam kmol/jam
----->
= =
0 0.531462585 0.531462585 C8H4Na2O4 0 3.5191441 3.5191441 334.73120336 362.62547031
BM
Masuk
kg/j
Keluar
---->
Na2SO4
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 DECANTER Komponen MA DEP H2O EA Na2SO4 C8H4Na2O4 C4H2Na2O4
148.0000 98.0000 222.000 18.0000 98.0000 46.000 40.0000 142.0000 210.0000 160
3.5191 0.1335 14.0766 38.3497 0.531462585 14.0765765766 8.368280084 0 0 0
98.0000 222.000 18.0000 46.000 142.0000 210.0000 160
Masuk Decanter 0.0000 14.0766 43.0653030132 14.0766 0.5315 3.5191 0.1335333
BM
520.8333333333 0 13.0862646566 0.0000 3125 14.0766 690.2946069514 43.0653 52.0833333333 0 647.5225225225 14.076576577 334.7312033601 0 0 0.531462585 0 3.5191441 0 0.1335 5383.5513 kg/j Densitas 0 0.185 3125 1.0578 775.1754542381 0.9757 647.5225225225 0.73262 75.4676870748 2.4495 739.0202702703 2.34 21.3653300516 2.2 5383.5512641573
Hasil Atas Decanter Asumsi H2O sebagai hasil atas decanter sebesar 2% H2O terbentuk di reaktor Komponen BM kmol/jam kg/j Densitas DEP 222.000 14.0766 3125 1.0578 EA 46.000 14.0766 647.5225225225 0.73262 H2O 18.0000 2.0352 36.6332241332 0.9757 3809.1557466558 Hasil Bawah Decanter Komponen BM kmol/jam kg/j Densitas H2O 18.0000 41.0301 738.5422301048 0.9757 Na2SO4 142.0000 0.5315 75.4676870748 2.4495 C8H4Na2O4 210.0000 3.5191 739.0202702703 2.34 C4H2Na2O4 160 0.1335333 21.3653300516 1574.3955175016 KELUAR DECANTER 5383.5512641573 EVAPORATOR Bahan Masuk Evaporator Komponen BM kmol/jam kg/j DEP 222.000 14.0766 3125 EA 46.000 14.0766 647.5225225225 H2O 18.0000 2.0352 36.6332241332 3809.1557466558 Evaporator dijalankan pada suhu 120 C TD Bahan MA 202 C Berdasarkan titik didih bahan maka komponen yang menja DEP 295 C dan yang menjadi hasil bawah evaporator adalah DEP dan EA 78.29 C H2O 100 C Hasil Atas Evaporator Komponen BM kmol/jam kg/j EA 46.000 14.0766 647.5225225225 H2O 18.0000 0.2815 5.0675675676 652.5900900901 Hasil Bawah Evaporator
Komponen DEP H2O
BM
kmol/jam 222.000 18.0000
kg/j 14.0766 1.7536
KELUAR EVAPORATOR MIXER Komponen Masuk Mixer Komponen PA MA EA H2O Komponen Keluar Mixer Komponen PA MA EA H2O
BM
kmol/jam 148.0000 98.0000 46.000 18.0000
BM
17.5957 0.1335333128 42.2297 4.0682
kmol/jam 148.0000 98.0000 46.0000 18.0000
17.5957 0.1335333128 42.2297297297 4.0682129498
3125 31.5656565657 3156.5656565657 3809.1557466558
kg/j 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963 4633.0483319871 kg/j 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963 4633.0483319871
ITAS 25.000 TON/TH KOMPONEN C8H4O3 C2H5OH C12H14O4 H2SO4 NaOH Na2SO4 H2O MA C8H4Na2O4
hari/24 j x 1000 kg/ton kg/jam kg/jam
+
14.0766 kmol/jam 1.7536 kmol/jam
H2O
x=
C8H4O3 + 17.5957207 14.0766 3.5191
0.8000 2 C2H5OH 42.2297297 28.1531532 14.0765766 EA keluar reaktor= EA masuk reaktor=
O impurities EA FF=
14.0765766 kmol/jam 28.1531532 kmol/jam 68.1602655 kg/jam
O dari recycle (Asumsi 2% H2O terbentuk )=
+2H2O 0 1.0629251701 1.0629251701 +H2O 0 3.5191441 3.5191441441 kg/jam kg/jam kg/j
M R S
BM 148.0000 46.000 222.000 98.0000 40.0000 142.0000 18.0000 98.0000 210.0000
C12H14O4
+
0 14.0766 14.0766 14.0765765766 kmol/jam 42.2297297297 kmol/jam
1942.56757 647.522523 kg/jam 1295.04505 kg/jam 3.78668142 kmol/jam 0.28153153 kmol/jam
5.0675675676 kg/jam
C4H2O3 + 2NaOH ---> 0.1335 0.2670666256 0.1335 0.2670666256 0 0
C4H2Na2O4 0 0.1335 0.1335
0 0 3125 775.17545424 0 647.52252252 0 75.467687075 739.02027027 21.365330052 5383.5512642 Data Kelarutan Bahan MA bereaksi menjadi maleic acid DEP 1g/100mL H2O tercampur dengan etanol EA tercampur dengan air Na2SO4 13,9g/100mL C8H4Na2O sedikit larut dalam air
volume 2954.2446587 883.84499812 37.54558177 3875.6352386 densitas rata-rata=
0.98284681
volume 756.9357693 30.809425219 315.82062832 1103.5658228 densitas rata-rata=
1.42664396
han maka komponen yang menjadi hasil atas evaporator adalah EA dan H2O wah evaporator adalah DEP dan MA
Tabel Neraca Massa Total Komponen
MIXER Masuk (kg/jam) FF RC 2604.166666667 13.0862646566 1295.045045045 647.5225225225 68.1602655287 5.0675675676
PA MA EA H2O DEP H2SO4 NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL Neraca Massa Overall Komponen PA MA EA H2O H2SO4 NaOH DEP Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
4633.0483319871
Masuk (kg/jam) FF Katalis 2604.166666667 13.0862646566 1295.045045045 68.1602655287 1.06293 52.08333
4730.9611740672
Kemurnian Bahan Baku PA EA H2SO4 NaOH
99.50% 95% 98% 48%
H2O x= 0.2815315315 14.0766 14.3581
0.8000
647.5225225225 1942.5675675676
Tabel Neraca Massa Reaktor Komponen
Masuk (kg/jam) MF
PA MA EA H2SO4 H2O DEP TOTAL
Katalis 2604.16667 13.08626 1942.56757 73.22783
52.08333 1.06293
4686.1946
Keluar (kg/jam) 520.8333 13.0863 647.5225 52.0833 327.6691 3125.0000 4686.1946
+ H2O 0 0.1335 0.1335
Tabel Neraca Massa Netralizer Komponen
Masuk (kg/jam) Keluar Reaktor Penetral
Keluar (kg/jam)
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
520.8333 13.0863 0 3125.0000 3125 327.6691 362.62547 775.1754542381 52.0833 647.5225 647.5225225225 334.731203 75.4676870748 739.0202702703 21.3653300516 5383.5513 5383.551264157
Tabel Neraca Massa Dekanter Komponen C4H2Na2O4 DEP H2O EA Na2SO4 C8H4Na2O4 TOTAL
Masuk (kg/jam) 21.3653300516 3125 775.1754542381 647.5225225225 75.4676870748 739.0202702703 5383.5512641573
Keluar (kg/jam) Hasil Atas Hasil Bawah 0 21.3653300516 3125 36.6332241 738.5422301048 647.522523 75.4676870748 739.0202702703 5383.5512641573
Tabel Neraca Massa Evaporator Komponen DEP EA
Masuk (kg/jam)
Keluar (kg/jam) Hasil Atas Hasil Bawah
3125 647.5225225225 647.522523
3125
H2O TOTAL
36.6332241332 5.06756757 31.5656565657 3809.1557466558 3809.1557466558
Tabel Neraca Massa Mixer Komponen
Masuk (kg/jam)
PA MA EA H2O TOTAL
2604.1666666667 2604.166666667 13.0862646566 13.0862646566 1295.0450450451 647.522523 1942.567567568 68.1602655287 5.06756757 73.2278330963 4633.0483319871 4633.048331987
MIXER Keluar (kg/jam) 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963
4633.0483319871
uk (kg/jam)
9611740672
Penetral
362.6254703067
Keluar (kg/jam)
RC
FF
MF
REAKTOR NETRALIZER Masuk (kg/jam) Masuk (kg/jam) Keluar (kg/jam) Katalis Keluar Reaktor Penetral 2604.16667 520.8333 520.8333 13.08626 13.0863 13.0863 1942.56757 647.5225 647.5225 73.22783 1.06293 327.6691 327.6691 362.625470307 3125.0000 3125.0000 52.08333 52.0833 52.0833 334.73120336
4686.1946
4686.1946
Keluar (kg/jam) Hasil Bawah Dekanter Produk
738.5422301048 31.5656566
334.7312033601 3125 75.4676870748 739.0202702703 21.3653300516 4730.9611740672
5383.5513
TRALIZER Keluar (kg/jam) 0 647.5225225225 775.1754542381 3125
75.4676870748 739.0202702703 21.3653300516 5383.5513
DECANTER Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
EVAPORATOR Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
0 0 0 0 647.5225225225 647.52252 647.5225225225 647.52252 775.1754542381 36.633224 738.542230105 36.6332241332 5.0675676 31.565656566 3125 3125 3125 3125
75.4676870748 739.0202702703 21.3653300516 5383.5512641573
75.4676870748 739.02027027 21.3653300516 5383.5512641573 3809.155746656
3809.15575
80 C A.B^-(1-T/Tc)^n A 0.35183 0.2657 0.34999 0.3471 0.42169 0.26141
= B 0.2322 0.26395 0.25154 0.274 0.19356 0.1
130 C = A+(B*T)+(C*T^2)+(D*T^3) A B -105.627 1.96E+00 59.342 3.64E-01 125.381 1.58E+00 92.503 -4.00E-02 26.00400 0.70337
0.2346 0.2367 0.3525 0.28571 0.28570 0.28571
353 K (ρ = gr/mL; T=K) Tc Tmin 791 404.26 516.25 195.05 757 296.15 647.13 273.16 925.00000 283.46 3700 1157
C -3.66E-03 -1.22E-03 -3.47E-03 -2.11E-04 -0.00139
403 K (Cp= Joule/mol K; T=K) D Tmin 2.85E-06 405 1.80E-06 160 3.33E-06 270 5.35E-07 273 0.00000 296
n
Viskositas (µ) Yaws, hal 487, table 22.1 viscosity of liquid log µ = A+(B/T)+(C*T)+(D*T^2) (µ = cP; T=K) T= 80 = 353 K Komponen A B C D C8H4O3 -25.1512 5.0387E+03 4.1950E-02 -2.4927E-05 C2H5OH -6.4406 1.1176E+03 1.3721E-02 -1.5465E-05 C12H14O4 -12.1587 2.5728E+03 1.8732E-02 -1.1566E-05 H2SO4 -18.7045 3.4962E+03 3.3080E-02 -1.7018E-05 H2O -10.2158 1.7925E+03 1.7730E-02 -1.2631E-05 Na2SO4 11.2905 -4.58E+03 -6.78E-03 9.24E-07 TOTAL -61.3803 9.4409E+03 0.1184282 -8.06826E-05
Tmax 791 516.25 757 647.13 363.49 2000
Tmax 712 465 681 615 879
Tmin 405 240 269 283 273 1180 2650
Tmax 791 516 757 367 643 1267 4341
Konduktifitas panas (k) Yaws, hal 535, table 24.1 thermal conductifity of liquid organic: log k = A+B(1-T/C)^(2/7) (k=W/m.K;T=K) inorganic: k= A+BT+CT^2 Komponen A B C Tmin C8H4O3 -1.6831 1.0293 791 404 C2H5OH -1.3172 0.6987 516.25 159 C12H14O4 -1.3265 0.5567 757 269 H2SO4 0.1553 1.07E-03 -1.29E-06 283 H2O -0.2758 4.61E-03 -5.54E-06 273 TOTAL -4.4473 2.2903819 2064.249993175 1388
T= k (25ᵒC) 0.1694 0.1432 0.36 0.607 1.2796
Tmax 751 490 719 833 633 3426
Vapor Pressure (P) Yaws, pers 7-1 hal. 159. Vapor Pressure Organic and Inorganic Compound log P= A+(B/T)+(C log T)+(D*T)+(E*T^2) (P=mmHg , T=K)
T=
Komponen C2H5OH C12H14O4 H2O
A 71.2535 23.8442 29.8605
B -5.50E+03 -2.86E+03 -3.15E+03
C -2.14E+01 -5.47E+00 -7.30E+04
D 3.81E-10 3.74E-11 2.42E-09
E 5.03E-06 2.74E-07 1.81E-06
log P 1.41E+00 1.47E+00 -1.84E+05
ρ (g/cm^3) 1.25419 0.73262 1.0578 0.9757 1.7647 2.4495
ρ (kg/m^3) fv (m3/jam) 1254.19 732.62 1057.8 975.7 1764.7 2449.5
Cp 25 (g/cm^3) 264.72 107.4 374.9 75.55 139.95
Cp (kg/m^3) fv (m3/jam) 2.77E+02 1.26E+02 4.15E+02 7.71E+01 1.52E+02
log µ
µ
0.8250 -0.3582 0.3009 0.7564 -0.4531 -3.9551 -2.8841605583
333
fraksi mol 6.6828 0.4384 1.9992 5.7068 0.3523 0.0001 15.1795426745
K
k 0.157550286 0.1594126978 0.1397125053 2.6693365175 3.1199624425 6.2459744491
fraksimol
333 K
P 2.56E+01 2.92E+01 0.00E+00
NERACA MASSA PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan ETYL ALKOHOL KAPASITAS 30.000 TON/TH Kapasitas produksi
= = =
kemurnian produk impuritis
30000.0000 30000.0000 3787.8788 0.9900 0.0100
ton/tahun ton/th x 1 th/330 hari x 1 hari/24 j x 1000 kg/ton kg/j 17.0625 C12H14O4 3750.0000 H20 37.8788 3787.8788
REAKTOR reaksi yang terjadi C8H4O3
+
DEP Terbentuk Etanol 20% berlebihan
=
komposisi bahan terbentuk / berx DEP Terbentuk H2O terbentuk PA brx EA brx
NETRALIZER Reaksi: M R S M R S Kebutuhan NaOH= H2O (Impurities NaOH)= Neraca Massa Netralizer Komponen
kg/jam 16.8919
= = = = = = =
kg/jam 3750 304.0540540541 2500 1554.0540540541 kg/jam
21.1149 0.1602399754 42.2297297297 50.6756756757 6.8160265529 0.637755102 0.070861678 kmol/jam
= = = = = =
3750.0000
16.8919 16.8919 16.8919 33.7837837838 kmol/jam
Komposisi Bahan Keluar PA MA EA H2O H2SO4 DEP
C12H14O4
kmol/jam = = = =
Komposisi Bahan Masuk Reaktor PA masuk reaktor MA masuk reaktor EA stci EA masuk reaktor H2O dalam EA H2SO4 MR H2O dalam H2SO4
2 C2H5OH kmol/jam
3125.00000 15.70352 1942.56757 2331.08108 122.68848 62.50000 1.27551 5623.433509
EA recycle= EA (FF)= H2O impurities EA FF=
H2O dari recycle (Asumsi 2% H2O
kg/jam
4.2230 0.1602 16.8918918919 21.8446 0.637755102 16.8919
625.0000 15.7035 777.0270 393.2030 62.5000 3750.0000 5623.4335085886
H2SO4 0.637755102 0.637755102 0 C6H4(CO)2O 4.2229730 4.2229730 0 10.0419361008 24.1750313538
+2NaOH 1.2755102041 1.2755102041 0 +2NaOH 8.4459459459 8.4459459459 0 kmol/jam kmol/jam
----->
= =
0 0.637755102 0.637755102 C8H4Na2O4 0 4.2229730 4.2229730 401.67744403 435.15056437
BM
Masuk
kg/j
Keluar
---->
Na2SO4
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 DECANTER Komponen MA DEP H2O EA Na2SO4 C8H4Na2O4 C4H2Na2O4
148.0000 98.0000 222.000 18.0000 98.0000 46.000 40.0000 142.0000 210.0000 160
4.2230 0.1602 16.8919 46.0196 0.637755102 16.8918918919 10.0419361008 0 0 0
98.0000 222.000 18.0000 46.000 142.0000 210.0000 160
Masuk Decanter 0.0000 16.8919 51.6783636159 16.8919 0.6378 4.2230 0.1602400
BM
625 0 15.7035175879 0.0000 3750 16.8919 828.3535283417 51.6784 62.5 0 777.027027027 16.891891892 401.6774440321 0 0 0.637755102 0 4.2229730 0 0.1602 6460.2615 kg/j Densitas 0 0.185 3750 1.0578 930.2105450857 0.9757 777.027027027 0.73262 90.5612244898 2.4495 886.8243243243 2.34 25.6383960619 2.2 6460.2615169888
Hasil Atas Decanter Asumsi H2O sebagai hasil atas decanter sebesar 2% H2O terbentuk di reaktor Komponen BM kmol/jam kg/j Densitas DEP 222.000 16.8919 3750 1.0578 EA 46.000 16.8919 777.027027027 0.73262 H2O 18.0000 2.4422 43.9598689599 0.9757 4570.9868959869 Hasil Bawah Decanter Komponen BM kmol/jam kg/j Densitas H2O 18.0000 49.2361 886.2506761258 0.9757 Na2SO4 142.0000 0.6378 90.5612244898 2.4495 C8H4Na2O4 210.0000 4.2230 886.8243243243 2.34 C4H2Na2O4 160 0.1602400 25.6383960619 2.4 1889.2746210019 KELUAR DECANTER 6460.2615169888 EVAPORATOR Bahan Masuk Evaporator 0.953358709 Komponen BM kmol/jam kg/j DEP 222.000 16.8919 3750 EA 46.000 16.8919 777.027027027 H2O 18.0000 2.4422 43.9598689599 4570.9868959869 Evaporator dijalankan pada suhu 85 C TD Bahan MA 202 C Berdasarkan titik didih bahan maka komponen yang menja DEP 295 C dan yang menjadi hasil bawah evaporator adalah DEP dan EA 78.29 C H2O 100 C Hasil Atas Evaporator Komponen BM kmol/jam kg/j EA 46.000 16.8919 777.027027027 H2O 18.0000 0.3378 6.0810810811 783.1081081081 Hasil Bawah Evaporator
Komponen DEP H2O
BM
kmol/jam 222.000 18.0000
kg/j 16.8919 2.1044
KELUAR EVAPORATOR MIXER Komponen Masuk Mixer Komponen PA MA EA H2O Komponen Keluar Mixer Komponen PA MA EA H2O
BM
kmol/jam 148.0000 98.0000 46.000 18.0000
BM
21.1149 0.1602399754 50.6757 4.8819
kmol/jam 148.0000 98.0000 46.0000 18.0000
21.1149 0.1602399754 50.6756756757 4.8818555398
3750 37.8787878788 3787.8787878788 4570.9868959869
kg/j 3125 15.7035175879 2331.0810810811 87.8733997155 5559.6579983845 kg/j 3125 15.7035175879 2331.0810810811 87.8733997155 5559.6579983845
AS 30.000 TON/TH KOMPONEN C8H4O3 C2H5OH C12H14O4 H2SO4 NaOH Na2SO4 H2O MA C8H4Na2O4
hari/24 j x 1000 kg/ton kg/jam kg/jam
+
16.8919 kmol/jam 2.1044 kmol/jam
H2O
x=
C8H4O3 + 21.1148649 16.8919 4.2230
0.8000 2 C2H5OH 50.6756757 33.7837838 16.8918919 EA keluar reaktor= EA masuk reaktor=
O impurities EA FF=
16.8918919 kmol/jam 33.7837838 kmol/jam 81.7923186 kg/jam
O dari recycle (Asumsi 2% H2O terbentuk )=
+2H2O 0 1.2755102041 1.2755102041 +H2O 0 4.2229730 4.222972973 kg/jam kg/jam kg/j
M R S
BM 148.0000 46.000 222.000 98.0000 40.0000 142.0000 18.0000 98.0000 210.0000
C12H14O4
+
0 16.8919 16.8919 16.8918918919 kmol/jam 50.6756756757 kmol/jam
2331.08108 777.027027 kg/jam 1554.05405 kg/jam 4.5440177 kmol/jam 0.33783784 kmol/jam
6.0810810811 kg/jam
C4H2O3 + 2NaOH ---> 0.1602 0.3204799508 0.1602 0.3204799508 0 0
C4H2Na2O4 0 0.1602 0.1602
0 0 3750 930.21054509 0 777.02702703 0 90.56122449 886.82432432 25.638396062 6460.261517 Data Kelarutan Bahan MA bereaksi menjadi maleic acid DEP 1g/100mL H2O tercampur dengan etanol EA tercampur dengan air Na2SO4 13,9g/100mL C8H4Na2O sedikit larut dalam air
volume 3545.0935905 1060.6139977 45.054698124 4650.7622863 densitas rata-rata= volume 908.32292316 36.971310263 378.98475398 10.682665026 densitas rata-rata= 1334.9616524
0.98284681
1.41522763
han maka komponen yang menjadi hasil atas evaporator adalah EA dan H2O wah evaporator adalah DEP dan MA
Tabel Neraca Massa Total Komponen FF PA MA EA H2O DEP H2SO4 NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL Neraca Massa Overall Komponen PA MA EA H2O H2SO4 NaOH DEP Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
MIXER Masuk (kg/jam) RC 3125.0000 15.7035 1554.0541 777.0270 81.7923 6.0811
5559.6580 Masuk (kg/jam) Katalis
FF 3125.0000 15.7035 1554.0541 81.7923
1.2755 62.5000
5677.1534
Kemurnian Bahan Baku PA EA H2SO4 NaOH
99.50% 95% 98% 48%
H2O x= 0.3378378378 16.8919 17.2297
0.8000
777.027027027 2331.0810810811
Tabel Neraca Massa Reaktor Komponen
MF
PA MA EA H2SO4 H2O DEP TOTAL
Masuk (kg/jam) Katalis 3125.00000 15.70352 2331.08108 87.87340 5623.4335
Keluar (kg/jam)
62.50000 1.27551
625.0000 15.7035 777.0270 62.5000 393.2030 3750.0000 5623.4335
+ H2O 0 0.1602 0.1602
Tabel Neraca Massa Netralizer Komponen
Masuk (kg/jam) Keluar Reaktor Penetral
Keluar (kg/jam)
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
625.0000 15.7035 0 3750.0000 3750 393.2030 435.1505643681 930.2105450857 62.5000 777.0270 777.027027027 401.6774440321 90.5612244898 886.8243243243 25.6383960619 6460.2615 6460.261516989
Tabel Neraca Massa Dekanter Komponen C4H2Na2O4 DEP H2O EA Na2SO4 C8H4Na2O4 TOTAL
Masuk (kg/jam) 25.6383960619 3750 930.2105450857 777.027027027 90.5612244898 886.8243243243 6460.2615169888
Keluar (kg/jam) Hasil Atas Hasil Bawah 0 25.6383960619 3750 43.9598689599 886.2506761258 777.027027027 90.5612244898 886.8243243243 6460.2615169888
Tabel Neraca Massa Evaporator Komponen DEP EA
Masuk (kg/jam) 3750 777.027027027
Keluar (kg/jam) Hasil Atas Hasil Bawah 3750 777.027027027
H2O TOTAL
43.9598689599 4570.9868959869
Tabel Neraca Massa Mixer Komponen
FF
PA MA EA H2O TOTAL
MIXER Keluar (kg/jam) 3125.0000 15.7035 2331.0811 87.8734
5559.6580
uk (kg/jam)
677.1534
6.0810810811 37.8787878788 4570.9868959869
MF
Masuk (kg/jam) Keluar (kg/jam) RC 3125 3125 15.7035175879 15.7035175879 1554.0540540541 777.027027027 2331.081081081 81.7923186344 6.0810810811 87.8733997155 5559.6579983845 5559.657998385
REAKTOR NETRALIZER Masuk (kg/jam) Masuk (kg/jam) Keluar (kg/jam) Katalis Keluar Reaktor Penetral 3125.0000 625.0000 625.0000 15.7035 15.7035 15.7035 2331.0811 777.0270 777.0270 87.8734 1.2755 393.2030 393.2030 435.1506 3750.0000 3750.0000 62.5000 62.5000 62.5000 401.6774
5623.4335
5623.4335
Keluar (kg/jam) Hasil Bawah Dekanter Produk
Penetral
435.1506
886.2507
37.8788
401.6774 3750.0000 90.5612 886.8243 25.6384 5677.1534
6460.2615
TRALIZER Keluar (kg/jam)
DECANTER Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
0.0000 777.0270 930.2105 3750.0000
0.0000 777.0270 930.2105 3750.0000
90.5612 886.8243 25.6384 6460.2615
90.5612 886.8243 25.6384 6460.2615
0.0000 777.0270 43.9599 3750.0000
886.2507
EVAPORATOR Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah 0.0000 777.0270 43.9599 3750.0000
0.0000 777.0270 6.0811
37.8788 3750.0000
90.5612 886.8243 25.6384 6460.2615
4570.9869
4570.9869
PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan ETYL ALKOHOL KAPASITAS PRODUKSI 30.000 TON/TH H2SO4
62.500
H2O
1.2755 63.7755
EA= H2O=
777.027027027 6.0810810811 783.1081081081
EA= 1554.05405405 H2O= 81.7923186344 1635.8464 PA=
3125
MA=
15.7035
Mixer 1 atm
3140.7035
PA=
3125
Reaktor 1 atm
MA= 15.703518
PA=
625.0000
EA= 2331.0811
MA=
15.7035
87.8734
EA=
777.0270
5559.658
H2SO4=
62.5000
H2O=
393.2030
DEP=
3750.0000
H2O=
NaOH= 401.677444032 H2O= 435.150564368
3750
H2O=
43.9598689599
EA=
777.027027027 4570.98690
Evaporator 1 atm
5623.4335
836.8280084 FF+RC Katalis+MF RP+Netral UPL+HADec HAEvap+P
DEP=
Netralizer 1 atm
5559.6580 5623.4335 6460.2615 6460.26152 4570.9869
Produk :
Decanter 1 atm
DEP=
DEP=
3750
H2O=
930.2105
H2O=
EA=
777.0270
Na2SO4=
90.5612
C8H4Na2O4=
886.8243
C4H2Na2O4=
25.6384
Na2SO4=
90.5612244898
6460.2615
C4H2Na2O4=
25.6383960619
C8H4Na2O4=
886.8243243243
ke UPL H20=
886.2506761258
1889.2746210019
Evaporator 1 atm
3750 37.8788 3787.8788
NERACA MASSA PABRIK DIETYL PHTHALATE dari PHTHALIC ANHYDRIDE dan 2-ETYL ALKOHOL KAPASITAS 25.000 TON/TH Kapasitas produksi
= = =
kemurnian produk impuritis
25000.0000 25000.0000 3156.5657 0.9900 0.0100
ton/tahun ton/th x 1 th/330 hari x 1 hari/24 j x 1000 kg/ton kg/j 14.2188 C12H14O4 3125.0000 H20 31.5657 3156.5657
REAKTOR reaksi yang terjadi C8H4O3
+
DEP Terbentuk Etanol 20% berlebihan
=
komposisi bahan terbentuk / berx DEP Terbentuk H2O terbentuk PA brx EA brx
NETRALIZER Reaksi: M R S M R S Kebutuhan NaOH= H2O (Impurities NaOH)= Neraca Massa Netralizer Komponen
kg/jam 14.0766
= = = = = = =
kg/jam 3125 253.3783783784 2083.3333333333 1295.0450450451 kg/jam
17.5957 0.1335333128 35.1914414414 42.2297297297 5.6800221274 0.531462585 0.0590513983 kmol/jam
= = = = = =
3125.0000
14.0766 14.0766 14.0766 28.1531531532 kmol/jam
Komposisi Bahan Keluar PA MA EA H2O H2SO4 DEP
C12H14O4
kmol/jam = = = =
Komposisi Bahan Masuk Reaktor PA masuk reaktor MA masuk reaktor EA stci EA masuk reaktor H2O dalam EA H2SO4 MR H2O dalam H2SO4
2 C2H5OH kmol/jam
2604.16667 13.08626 1618.80631 1942.56757 102.24040 52.08333 1.06293 4686.194590
EA recycle= EA (FF)= H2O impurities EA FF=
H2O dari recycle (Asumsi 2% H2O
kg/jam
3.5191 0.1335 14.0765765766 18.2038 0.531462585 14.0766
520.8333 13.0863 647.5225 327.6691 52.0833 3125.0000 4686.1945904905
H2SO4 0.531462585 0.531462585 0 C6H4(CO)2O 3.5191441 3.5191441 0 8.368280084 20.1458594615
+2NaOH 1.0629251701 1.0629251701 0 +2NaOH 7.0382882883 7.0382882883 0 kmol/jam kmol/jam
----->
= =
0 0.531462585 0.531462585 C8H4Na2O4 0 3.5191441 3.5191441 334.73120336 362.62547031
BM
Masuk
kg/j
Keluar
---->
Na2SO4
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 DECANTER Komponen MA DEP H2O EA Na2SO4 C8H4Na2O4 C4H2Na2O4
148.0000 98.0000 222.000 18.0000 98.0000 46.000 40.0000 142.0000 210.0000 160
3.5191 0.1335 14.0766 38.3497 0.531462585 14.0765765766 8.368280084 0 0 0
98.0000 222.000 18.0000 46.000 142.0000 210.0000 160
Masuk Decanter 0.0000 14.0766 43.0653030132 14.0766 0.5315 3.5191 0.1335333
BM
520.8333333333 0 13.0862646566 0.0000 3125 14.0766 690.2946069514 43.0653 52.0833333333 0 647.5225225225 14.076576577 334.7312033601 0 0 0.531462585 0 3.5191441 0 0.1335 5383.5513 kg/j Densitas 0 0.185 3125 1.0578 775.1754542381 0.9757 647.5225225225 0.73262 75.4676870748 2.4495 739.0202702703 2.34 21.3653300516 2.2 5383.5512641573
Hasil Atas Decanter Asumsi H2O sebagai hasil atas decanter sebesar 2% H2O terbentuk di reaktor Komponen BM kmol/jam kg/j Densitas DEP 222.000 14.0766 3125 1.0578 EA 46.000 14.0766 647.5225225225 0.73262 H2O 18.0000 2.0352 36.6332241332 0.9757 3809.1557466558 Hasil Bawah Decanter Komponen BM kmol/jam kg/j Densitas H2O 18.0000 41.0301 738.5422301048 0.9757 Na2SO4 142.0000 0.5315 75.4676870748 2.4495 C8H4Na2O4 210.0000 3.5191 739.0202702703 2.34 C4H2Na2O4 160 0.1335333 21.3653300516 1574.3955175016 KELUAR DECANTER 5383.5512641573 EVAPORATOR Bahan Masuk Evaporator Komponen BM kmol/jam kg/j DEP 222.000 14.0766 3125 EA 46.000 14.0766 647.5225225225 H2O 18.0000 2.0352 36.6332241332 3809.1557466558 Evaporator dijalankan pada suhu 120 C TD Bahan MA 202 C Berdasarkan titik didih bahan maka komponen yang menja DEP 295 C dan yang menjadi hasil bawah evaporator adalah DEP dan EA 78.29 C H2O 100 C Hasil Atas Evaporator Komponen BM kmol/jam kg/j EA 46.000 14.0766 647.5225225225 H2O 18.0000 0.2815 5.0675675676 652.5900900901 Hasil Bawah Evaporator
Komponen DEP H2O
BM
kmol/jam 222.000 18.0000
kg/j 14.0766 1.7536
KELUAR EVAPORATOR MIXER Komponen Masuk Mixer Komponen PA MA EA H2O Komponen Keluar Mixer Komponen PA MA EA H2O
BM
kmol/jam 148.0000 98.0000 46.000 18.0000
BM
17.5957 0.1335333128 42.2297 4.0682
kmol/jam 148.0000 98.0000 46.0000 18.0000
17.5957 0.1335333128 42.2297297297 4.0682129498
3125 31.5656565657 3156.5656565657 3809.1557466558
kg/j 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963 4633.0483319871 kg/j 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963 4633.0483319871
ITAS 25.000 TON/TH KOMPONEN C8H4O3 C2H5OH C12H14O4 H2SO4 NaOH Na2SO4 H2O MA C8H4Na2O4
hari/24 j x 1000 kg/ton kg/jam kg/jam
+
14.0766 kmol/jam 1.7536 kmol/jam
H2O
x=
C8H4O3 + 17.5957207 14.0766 3.5191
0.8000 2 C2H5OH 42.2297297 28.1531532 14.0765766 EA keluar reaktor= EA masuk reaktor=
O impurities EA FF=
14.0765766 kmol/jam 28.1531532 kmol/jam 68.1602655 kg/jam
O dari recycle (Asumsi 2% H2O terbentuk )=
+2H2O 0 1.0629251701 1.0629251701 +H2O 0 3.5191441 3.5191441441 kg/jam kg/jam kg/j
M R S
BM 148.0000 46.000 222.000 98.0000 40.0000 142.0000 18.0000 98.0000 210.0000
C12H14O4
+
0 14.0766 14.0766 14.0765765766 kmol/jam 42.2297297297 kmol/jam
1942.56757 647.522523 kg/jam 1295.04505 kg/jam 3.78668142 kmol/jam 0.28153153 kmol/jam
5.0675675676 kg/jam
C4H2O3 + 2NaOH ---> 0.1335 0.2670666256 0.1335 0.2670666256 0 0
C4H2Na2O4 0 0.1335 0.1335
0 0 3125 775.17545424 0 647.52252252 0 75.467687075 739.02027027 21.365330052 5383.5512642 Data Kelarutan Bahan MA bereaksi menjadi maleic acid DEP 1g/100mL H2O tercampur dengan etanol EA tercampur dengan air Na2SO4 13,9g/100mL C8H4Na2O sedikit larut dalam air
volume 2954.2446587 883.84499812 37.54558177 3875.6352386 densitas rata-rata=
0.98284681
volume 756.9357693 30.809425219 315.82062832 1103.5658228 densitas rata-rata=
1.42664396
han maka komponen yang menjadi hasil atas evaporator adalah EA dan H2O wah evaporator adalah DEP dan MA
Tabel Neraca Massa Total Komponen
MIXER Masuk (kg/jam) FF RC 2604.166666667 13.0862646566 1295.045045045 647.5225225225 68.1602655287 5.0675675676
PA MA EA H2O DEP H2SO4 NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL Neraca Massa Overall Komponen PA MA EA H2O H2SO4 NaOH DEP Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
4633.0483319871
Masuk (kg/jam) FF Katalis 2604.166666667 13.0862646566 1295.045045045 68.1602655287 1.06293 52.08333
4730.9611740672
Kemurnian Bahan Baku PA EA H2SO4 NaOH
99.50% 95% 98% 48%
H2O x= 0.2815315315 14.0766 14.3581
0.8000
647.5225225225 1942.5675675676
Tabel Neraca Massa Reaktor Komponen
Masuk (kg/jam) MF
PA MA EA H2SO4 H2O DEP TOTAL
Katalis 2604.16667 13.08626 1942.56757 73.22783
52.08333 1.06293
4686.1946
Keluar (kg/jam) 520.8333 13.0863 647.5225 52.0833 327.6691 3125.0000 4686.1946
+ H2O 0 0.1335 0.1335
Tabel Neraca Massa Netralizer Komponen
Masuk (kg/jam) Keluar Reaktor Penetral
Keluar (kg/jam)
PA MA DEP H2O H2SO4 EA NaOH Na2SO4 C8H4Na2O4 C4H2Na2O4 TOTAL
520.8333 13.0863 0 3125.0000 3125 327.6691 362.62547 775.1754542381 52.0833 647.5225 647.5225225225 334.731203 75.4676870748 739.0202702703 21.3653300516 5383.5513 5383.551264157
Tabel Neraca Massa Dekanter Komponen C4H2Na2O4 DEP H2O EA Na2SO4 C8H4Na2O4 TOTAL
Masuk (kg/jam) 21.3653300516 3125 775.1754542381 647.5225225225 75.4676870748 739.0202702703 5383.5512641573
Keluar (kg/jam) Hasil Atas Hasil Bawah 0 21.3653300516 3125 36.6332241 738.5422301048 647.522523 75.4676870748 739.0202702703 5383.5512641573
Tabel Neraca Massa Evaporator Komponen DEP EA
Masuk (kg/jam)
Keluar (kg/jam) Hasil Atas Hasil Bawah
3125 647.5225225225 647.522523
3125
H2O TOTAL
36.6332241332 5.06756757 31.5656565657 3809.1557466558 3809.1557466558
Tabel Neraca Massa Mixer Komponen
Masuk (kg/jam)
PA MA EA H2O TOTAL
2604.1666666667 2604.166666667 13.0862646566 13.0862646566 1295.0450450451 647.522523 1942.567567568 68.1602655287 5.06756757 73.2278330963 4633.0483319871 4633.048331987
MIXER Keluar (kg/jam) 2604.1666666667 13.0862646566 1942.5675675676 73.2278330963
4633.0483319871
uk (kg/jam)
9611740672
Penetral
362.6254703067
Keluar (kg/jam)
RC
FF
MF
REAKTOR NETRALIZER Masuk (kg/jam) Masuk (kg/jam) Keluar (kg/jam) Katalis Keluar Reaktor Penetral 2604.16667 520.8333 520.8333 13.08626 13.0863 13.0863 1942.56757 647.5225 647.5225 73.22783 1.06293 327.6691 327.6691 362.625470307 3125.0000 3125.0000 52.08333 52.0833 52.0833 334.73120336
4686.1946
4686.1946
Keluar (kg/jam) Hasil Bawah Dekanter Produk
738.5422301048 31.5656566
334.7312033601 3125 75.4676870748 739.0202702703 21.3653300516 4730.9611740672
5383.5513
TRALIZER Keluar (kg/jam) 0 647.5225225225 775.1754542381 3125
75.4676870748 739.0202702703 21.3653300516 5383.5513
DECANTER Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
EVAPORATOR Keluar (kg/jam) Masuk (kg/jam) Hasil Atas Hasil Bawah
0 0 0 0 647.5225225225 647.52252 647.5225225225 647.52252 775.1754542381 36.633224 738.542230105 36.6332241332 5.0675676 31.565656566 3125 3125 3125 3125
75.4676870748 739.0202702703 21.3653300516 5383.5512641573
75.4676870748 739.02027027 21.3653300516 5383.5512641573 3809.155746656
3809.15575
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