Lampiran Neraca Massa dan Panas Prarancangan Pabrik Anilin dari Nitrobenzene.xlsx

8/11/2019 Lampiran Neraca Massa dan Panas Prarancangan Pabrik Anilin dari Nitrobenzene.xlsx

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Kapasitas Produksi =

=

Hari Kerja = 1 =

= 1 =

Basis Bahan Baku = kg/jam

Spesifikasi bahan baku = Nitrobenzen =

= =

= =

= =

Spesifikasi Produk = == =

Tabel Data Masing-masing Komponen

SEPARATOR

2

1

3

Basis = kg/jam

Asumsi = 80% produk Arus 2 (produk yang diinginkan):

Nitrobenzen = kg/jam =

= kg/jam =

Di-Nitrobenzen = kg/jam =

Benzen = kg/jam =

LAMPIRAN A

PERHITUNGAN NERACA MASSA

79.4400

kmol/jam

Air 0.0100

-164 16

0.6459 kmol/jam

Benzen C6H6

A.1

100

H2O 0.0800 0.0044 kmol/jam

0.0800 0.0005 kmol/jam

0.0800 0.0010

123

Benzen 0.0010

Anilin 0.9900

Hidrogen H2 -259.2 2

Di-Nitrobenzen C6H4NO2 301 168

80.1 78

Metana CH4

Anilin C6H5NH2 184.1 93

Komponen Rumus Molekul Titik Didih,oC BM, kg/kmol

Nitrobenzen

62500 ton/tahun

7891.4141 kg/jam

Air H2O 100

C6H5NO2 210.9

0.0010

tahun 330 hari

hari 24 jam

100

0.9930

Air 0.0010

Di-Nitrobenzen

18

Separator


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Arus 1 (umpan):

= kg/jam = kmol/jam

= kg/jam = kmol/jam

Di-Nitrobenzen = kg/jam = kmol/jam

= kg/jam = kmol/jam

Arus 3

Nitrobenzen = kg/jam = kmol/jam

= kg/jam = kmol/jam


= kg/jam = kmol/jam

Tabel Neraca Massa Separator

Di-Nitrobenzen

A.2 REAKTOR

4

2

=

Bahan Baku yang Masuk kedalam Reaktor

C6H5NO2 = = kmol/jam


= = kmol/jam

H2O = = kmol/jam

Perbandingan mol Nitrobezen terhadap H2 = 1:3= kg/jam = kmol/jam

= kg/jam = kmol/jam

Bahan yang Bereaksi

C6H5NO2yang bereaksi = x C6H5NO2yang masuk

= x

99.3000

19.8600

79.4400

Benzen 0.1000 0.0800

0.0200

0.0010

0.0200

0.000002

Konversi

0.98

0.0011

0.0200 0.0001

Total79.6800 19.9200

99.6000 99.6000

0.1000

0.0003

KomponenMasuk (kg/jam) Keluar (kg/jam)

Arus 1 Arus 2 Arus 3

H2O 0.0200

Nitrobenzen 79.4400 19.860099.3000

0.0800

Nitrobenzen 0.8073

0.1000

Benzen 0.1000 0.0013

0.1615

H2O 0.0056

0.1000 0.0006

H2

0.00004

79.4400

C6H6

Benzen 0.0200

H2O 0.1000 0.0800 0.0200

CH4

Konversi 0.98

kg/jam 0.6459

0.0800 kg/jam 0.0044

3.8751 1.9376

0.0800 kg/jam 0.0005

0.0800 kg/jam

Reaktor


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= =

= H2O yang masuk

= kg/jam = kmol/jam

C6H4NO2 = C6H4NO2 yang masuk

= kg/jam = kmol/jam

C6H6 = C6H6yang masuk

= kg/jam =

H2yang bereaksi = (3/1) x C6H5NO2 yang bereaksi

= kg/jam =

= CH4yang masuk= kg/jam =

Reaksi yang Reaksi

C6H5NO2 + C6H5NH2 +

Produk yang Terbentuk

= =

= =

Neraca Massa Total Reaktor

Komponen

Bahan Yang Masuk

C6H5NO2 = kg/jam = kmol/jam


= kg/jam = kmol/jam

= kg/jam = kmol/jam

0.0800

0.0775

0.00004

0.0800 0.0005

H2O 0.0800

C6H6

C6H6

kg/jam

22.7857 kg/jam

79.4400

0.0800

0.0800

0.0800

0.6329 kmol/jam

3.8751

0.00004

-

-

0.0044

0.0800 0.0010

Masuk (kg/jam)

H2O

C6H5NH2

H2O

H2

CH4

Total

22.7857

1.5888 0.0129

83.555283.5552

C6H5NO2

C6H4NO2

1.2659

Sisa 0.0129 0.0388 0.6329 1.2659

CH4

0.08 0.0005

0.08 0.001026

0.00004

-

kmol/jam

3H2 2H2O

-

kmol/jam

3.7976 1.8988 kmol/jam

1.9376

kmol/jam

0.08 0.0044

77.8512 0.6329kg/jam

C6H5NH2

Mula-mula

Bereaksi 0.6329 1.8988

H2O

H2O 1.2659 kmol/jam

0.6459

58.8631

0.000002

0.6329

0.0800

0.0800

Keluar (kg/jam)

1.5888

58.8631


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= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

5

4

6

Komposisi Umpan Masuk

Bahan Yang Masuk



= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

= kg/jam = kmol/jam

Nitrobenzen (C6H5NO2)

x C6H5NO2yang masuk = kg/jam =

Di-Nitrobenzen (C6H4NO2)


Air (H2O)

x H2O yang masuk = kg/jam =

Benzen (C6H6)x C6H6yang masuk = kg/jam =

Gas Hidrogen (H2)

x H2yang masuk = kg/jam =

Gas Metana (CH4)

H2 0.0775 0.0388

CH4 0.0000020.00004

98% 0.0784 0.0010 kmol/jam

100.0% 0.077502 0.0388 kmol/jam

22.408498% 1.2449 kmol/j

0.0792 0.0005

C6H5NH2 58.8631 0.3197

H2O 22.7857 1.2659

kmol/j

Komposisi Bahan yang Teruapkan

98% 1.5570 0.0127 kmol/jam

99%

CH4 0.00004

H2O 0.0800 0.0044

C6H6 0.0800 0.0010

0.000002

0.0388H2 0.0775

58.8631

H2O 22.7857

A.3 Flash Tank

C6

H5

NH2

1.5888

0.3197

1.2659

0.0129

0.0800 0.0005

FlashTan

k


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x CH4yang masuk = kg/jam =

Anilin (C6H

5NH

2)

x C6H5NH2yang masuk = kg/jam =

Komposisi Bahan Cair

Nitrobenzen (C6H5NO2)


Di-Nitrobenzen (C6H4NO2)


Air (H2O)

x H2O yang masuk = kg/jam =

Benzen (C6H6)

x C6H6 yang masuk = kg/jam =

Anilin (C6H5NH2)

x C6H5NH2yang masuk = kg/jam =

Hidrogen (H2)

x H2yang masuk = = kmol/ja

16.344 -0.0241 0.0000

H2O 18.3036 3816.44 -46.13 -

C6H4NO2

C6H5NO2

-

C6H6 15.9008 2788.51 -52.36 - -

-24.246 -4114

-54.494 -2112.3 29.321 -0.0448 0.0000

Total 83.5552 24.2065 59.3487

83.5552

Komponen Antoine

A B C D E

0.0800 0.0792 0.0008

H2O 22.8657 22.4084 0.4573

C6H4NO2

C6H6 0.0800 0.0784 0.0016

H2 0.0775 0.0775 -

CH4 3.87516E-05 3.87516E-05 -

C6H5NH2 58.8631 0.0059 58.8572

Komponen Masuk (kg/jam) Keluar (kg/jam)

V L

2% 0.457314 0.0254 kmol/jam

2% 0.0016 2.05E-05 kmol/jam

99.99% 58.85722 0.6329

1.5888 1.5570 0.0318C6H5NO2

0.000002 km

0.01% 0.0059 0.0001 kmol/j

0.00004

0.00%

km

0.0000 kg/jam 0.00000

2% 0.031776 0.0003 kmol/j

1% 0.0008 km0.000005

100%


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Jadi bisa disimpulkan bahwa suhu pemasukan umpan sebesar 170,11 C

1. C6H5NO2 = x Massa =

2. C6H4NO2 = x Massa =

3. = x Massa =

4. = x Massa =

5. = x Massa =

=

Menentukan Nilai xdi

1. C6H5NO2 = Massa Komponen


3. = Massa Komponen

4. = Massa Komponen

6. = Massa Komponen

1. C6H5NO2 = x =

2. C6H4NO2 = x =

3. = x =

4. = x =

5. = x =

=

Menentukan Nilai xbi



3. = Massa Komponen

C6H5NH2 99% Massa 0.6265 kmol/jam

=

4.71E-06

= 0.0000Massa Total 0.6271

H2O 0.0003

1% Massa 0.0003 kmol/jam

C6H6

=0.0003

= 0.0004Massa Total 0.6271

H2O

Total 0.6271 kmol/jam

99% Massa 2.03.E-05 kmol/jam

C6H6

=

2.05E-07

= 0Massa Total 0.0315

C6H5NH2

=

0.0063

= 0.2010Massa Total 0.031484

Menentukan Massa Bottom

99% Massa 0.0003 kmol/jam

99% Massa 4.71E-06 kmol/jam

2.58E-06

= 8.20552E-05Massa Total 0.0315

=

4.76E-08

= 1.51249E-06Massa Total 0.0315

H2O

=

0.0252

= 0.7989Massa Total 0.0315

kmol/jam

1% 4.76E-08 kmol/jam

H2O 99.00% 0.0252 kmol/jam

kmol/jam

Total 0.0315 kmol/jam

C6H6 1% 2.05E-07 kmol/jam

=

C6H5NH2 1% 0.0063

B. Spesifikasi Hasil Yang Diinginkan

B.1 Distilat

Menentukan Massa Distilat

1% 2.58E-06


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atm = mmHg

C = K

Massa Masuk

Produk =

Faktor Pengali =

135.4209

0.0318

0.0008

H2O

Total

(kg/gr)

0.0016

0.4573

58.8572

C6H5NO2

C6H4NO2

H2O

C6H5NH2

Komponen

2.E-05C6H6

8.E-06 0.0008

Jadi dapat disimpulkan bahwa T bottom adalah 172,5794C

Total 0.6271 1

1.9168

20.90050.0003 0.0004 8254.673 10.86141 0.004401

20.7683

1.0417 58.3071

Massa Keluar

Distilat Bottom

2.E-03

0.4527 0.0046

0.5886 58.2686

0.0003 0.0315

59.3487

1.0000

4.71429E-06 0.0000 10.51353 0.013834 1.04E-07 0.0266

0.0003 0.0004 394.9502 0.519671 0.000212

xi.ki ki/k(HK)

457.1599622

Komponen Massa xi=

Pi

Trial pada T dianggap benar apabila Syi = 1

Pt = 1 760

i =

184.0100

7891.4141

= 135.420958.2732

C6H5NO2

C6H4NO2

T =

(kmol/jam)

0.00035

58.2732

C6H6 2.03.E-05 0.0000 8202.446 10.79269

1.000

59.348759.3487

C6H5NH2 0.6265 0.9991 757.0548 0.996125 0.995275

ki= yi=

m/m total Pi/P


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Arus 1 (umpan):

= kg/jam = kmol/jam

= kg/jam = kmol/jam


= kg/jam = kmol/jam

Arus 3

Nitrobenzen = kg/jam = kmol/jam

= kg/jam = kmol/jam


= kg/jam = kmol/jam

Tabel Neraca Massa Separator

Di-Nitrobenzen

A.2 REAKTOR

4

2

=

Bahan Baku yang Masuk kedalam Reaktor



= = kmol/jam

H2O = = kmol/jam

Perbandingan mol Nitrobezen terhadap H2 = 1:3= kg/jam = kmol/jam

= kg/jam = kmol/jam

Bahan yang Bereaksi

C6H5NO2yang bereaksi = x C6H5NO2yang masuk

= x

CH4 0.00525 0.000328

Konversi

0.98 10757.8363

H2 524.7725 262.3863

C6H6 10.8337 kg/jam 0.0645

10.8337 kg/jam 0.1389

Konversi 0.98

10757.8363 kg/jam 87.4621

10.8337 kg/jam 0.6019

Total10790.3373 2697.5843

13487.9216 13487.9216

13.5421 10.8337 2.7084

Benzen 13.5421 10.8337 2.7084

Nitrobenzen 13447.2954 10757.8363 2689.4591

H2O 13.5421 10.8337 2.7084

KomponenMasuk (kg/jam) Keluar (kg/jam)

Arus 1 Arus 2 Arus 3

H2O 2.7084 0.1505

2.7084 0.0161

Benzen 2.7084 0.0347

13.5421 0.0806

Benzen 13.5421 0.1736

2689.4591 21.8655

Nitrobenzen 13447.2954 109.3276

H2O 13.5421 0.7523

Reaktor


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= =

= H2O yang masuk

= kg/jam = kmol/jam

C6H4NO2 = C6H4NO2 yang masuk

= kg/jam = kmol/jam

C6H6 = C6H6yang masuk

= kg/jam =

H2yang bereaksi = (3/1) x C6H5NO2 yang bereaksi

= kg/jam =

= CH4yang masuk= kg/jam =

Reaksi yang Reaksi

C6H5NO2 + C6H5NH2 +

Produk yang Terbentuk

= =

= =

Neraca Massa Total Reaktor

Komponen

Bahan Yang Masuk



= kg/jam = kmol/jam

= kg/jam = kmol/jam

H2O 10.8337 0.6019

C6H6 10.8337 0.1389

Total 11315.1151 11315.1151

215.1567 1.7492

10.8337 0.0645

C6H5NH2 - 7971.2943

H2O - 3085.6623

H2 524.7725 10.4955

CH4 0.00525 0.00525

H2O 10.8337 10.8337

C6H6 10.8337 10.8337

C6H5NO2 10757.8363 215.1567

C6H4NO2 10.8337 10.8337

H2O 171.4257 kmol/jam 3085.6623 kg/jam

Masuk (kg/jam) Keluar (kg/jam)

Sisa 1.7492 5.2477 85.7128 171.4257

C6H5NH2 85.7128 kmol/jam 7971.2943 kg/jam

Mula-mula 87.4621 262.3863 - -

Bereaksi 85.7128 257.1385 85.7128 171.4257

CH4

0.00525 0.000328 kmol/jam

3H2 2H2O

10.83367 0.0645

10.83367 0.138893 kmol/jam

514.2771 257.1385 kmol/jam

10542.68 kg/jam 85.7128 kmol/jam

H2O

10.83367 0.6019


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4. = Massa Komponen

5. = Massa Komponen

(Kmol/jam)

atm = mmHg

C = K

Jadi dapat disimpulkan bahwa T distilat adalah 182,7943C

D. Perhitungan Suhu Bawah (Bubble point)

1.9179

Total 4.2636 1 0.284

C6H5NH2 0.8570 0.201015166 733.2846 0.9648 0.2083

21.0036

C6H6 2.77786E-05 6.51535E-06 8034.002 10.5711 6.16E-07 21.0129

H2O 3.4061 0.798894751 8030.418 10.5663 0.0756

1.0000

C6H4NO2 6.44861E-06 1.51249E-06 9.967046 0.0131 0.000115 0.0261

C6H5NO2 0.000349848 8.20552E-05 382.3358 0.5031 0.000163

i =

(kmol/jam) m/m total Pi/P yi/ki ki/k(HK)Komponen

Massa yi=Pi

ki= xi=

C. Perhitungan Suhu Atas (Dew point)

Trial pada T akan dianggap benar apabila Sxi = 1

Pt = 1 760

T = 182.7943 455.9443

C6H5NH2 85.7043 99% 84.8472 0.9991

Total 89.1832 84.9197 1.0000

H2O 3.4406 1% 0.0344 0.0004

C6H6 2.78.E-03 99% 2.75.E-03 0.0000

C6H5NO2 0.0350 99% 0.0346 0.0004

C6H4NO2 0.000644861 99% 0.000638413 7.51784E-06

Komponen Massa Bottom

(Kmol/jam) % Massa xbi

C6H5NH2 85.7043 1% 0.8570 0.2010Total 89.1832 4.2636 1.0000

H2O 3.4406 99% 3.4061 0.7989

C6H6 0.002777865 1% 2.77786E-05 0

C6H5NO2 0.0350 1% 0.000349848 8.20552E-05

C6H4NO2 0.000644861 1% 6.44861E-06 1.51249E-06

Komponen Massa Distilat

% Massa xdi

C6H5NH2

=

84.84723

= 0.9991Massa Total 84.91966

C6H6

=

2.8.E-03

= 0.0000Massa Total 84.9197

= = 0.0004Massa Total 84.9197


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2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

= kJ/jam

Q2= Q C6H5NO2+ Q C6H4N2O4+ Q C6H6+ Q H2O

= kJ/jam

3. Menghitung Kebutuhan Pemanas, Q3

0.1736523.15

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 T

298.15 +

=

#######

3 4

Q

523.15

C6H4N2O4

n CpdT298.15

4523.15

0.00192

523.15

+ 523.15 -2

- 298.15 + 8.52E-08

523.15 -

= 0.7523 32.2430 523.15 - 298.15

- 0.47460

523.15 -

+

=

523.15

8744.0538

298.152

- 298.15

Q

0.0806 18.1480 +

1.00E-07523.15

298.15-

+

= 0.0806

=

4

H2O

523.15

18.1480 T + 0.5618 T2 - 3.93E-4T3 + 1.004E-7

T4 - 1.2252E-12 T5

523.15 - 298.15 +

298.15

= 0.1736 -31.3860 523.15

dT298.15

=

298.15

3417.6783

CpdT298.15

+ #######

298.155

+

dT

#######523.15 - 298.15

5855.0194

+ #######

523.15 -

dT

298.15

298.15

0.56182

2

- 298.155

298.15

#######523.15

n523.15

298.15

C6H6

CpdT298.15

1.06E-05+

3

-

Q = n523.15

32.243 T + 1.923E-3 T2 + 1.055E-5 T3 - 3.596E-9 T4

523.15 -

3

= 0.7523523.15

5724098.8721


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2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

= kJ/jam

= 1.7492 -16.2020 412.68 - 298.15

#######412.68 - 298.153 4+

#######412.68 - 298.15 +

+ 0.5618

412.68 - 298.152

- 298.152

= 0.0645 18.1480 412.68 - 298.15

= 0.0645412.68

18.1480 T + 0.5618 T2 - 3.93E-4T3 + 1.004E-7

T4 - 1.2252E-12 T5 dT

298.15

+ #######

412.68 - 298.155

47718.2680

C6H4N2O4

Q = n412.68

CpdT298.15

+ #######

412.68 - 298.155

1.00E-07412.68

+ 0.56182 412.68

- 298.153 4

+ #######

412.68 - 298.15 +

= 0.1389

412.68

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 TdT298.15

1273.1909

C6H6

Q = n412.68

CpdT298.15

8.52E-08412.68 - 298.15

3 4+

#######412.68 - 298.15 +

+ 0.47460

412.68 - 298.152

= 0.1389 -31.3860 412.68 - 298.15

2878.7365

H2O

Q = n412.68

Cp dT298.15

+ #######

412.68 - 298.155

+ 0.00192

412.68 - 298.152

= 0.6019 32.2430 412.68 - 298.15

= 0.6019412.68

32.243 T + 1.923E-3 T2 + 1.055E-5 T3 - 3.596E-9 T4 dT298.15

2350.8332

#######412.68 - 298.15

3 4+

1.06E-05412.68 - 298.15 +


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2. Menghitung Panas Sensibel Keluar Heater, Q2

*Hout

Tin = o

C= K

Tref = o

C= K

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

= kJ/jam

2 2

3.4406444.80

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4

n444.80

CpdT298.15

2626484.8134

298.15

=

Q = n444.80

CpdT

298.153 4

#######

444.80 -

298.152

444.80 - 298.152

Q = n444.80

CpdT

= 0.035 39.47 444.80 - 298.15 + 0.9128

= 3.E-03444.8

-33.6620 T + 0.47430 T2 - 3.61E-3 T3 + 3.82E-6 T4 dT298.15

Q =

298.15 + 0.47212

444.80 -

dT298.15

= 3.4406 18.2964 444.80 -

-

38610.6875

C6H6

+

3 4

298.15 +

1.31E-06

444.80

298.15 + 3.82E-06

444.80 -

298.15

- 298.153 4

298.15

298.15 + 0.47430

444.80 - 298.152

346.4803

= 3.E-03 -33.6620 444.80 -

+ #######

444.80 -

444.80

46.9480 T + 0.9896 T2 - 2.3583E-3 T3 + 2.3296E-6 T4

+ #######

444.80 - 298.15

- 298.152

C6H5NO2

dT298.15

= 85.70 46.9480 444.80 - 298.15

Q = CpdT

+ 2.33E-06

n444.80

298.15

+ 0.9896

444.80

444.80

#### 444.80

25 298.15

C6H5NH2

= 85.70

H2O


68/122


69/122


70/122


71/122


72/122


73/122


74/122


75/122


76/122

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

2 2

3 3 4 4

= 5.E-05412.09

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 T

298.152

#######-

- 298.15 + 0.56182

412.09 -

Q = n412.09

CpdT298.15

#######412.09 - 298.15

5

75.0082

dT298.15

= 5.E-05 18.1480 412.09

dT298.15

= 3.E-03 -16.2020 412.09 - 298.15 + 0.56182

- 298.15 + #######

412.09 -

C6H4N2O4

+ 298.153

Q =

= 3.E-03412.09

412.09 - 298.153 4

104670.8476

1.06E-05412.09 - 298.15 +

#######

Q = n412.09

CpdT298.15

412.09 - 298.15

C6H5NH2

Q = n412.09

-

#######412.09

4

+

+ #######

412.09 - 298.152

1.00E-07

191903.6870

=

3 4

298.152

#######412.09 - 298.15

6.778 -22.0620 412.09 - 298.15

+ #######

412.095

C6H5NO2

298.15

+

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 T

-

dT298.15

+ 0.57313

412.09 -

= 26.94 32.2430 412.09 - 298.15

= 26.94

412.09

32.243 T + 1.923E-3 T2 + 1.055E-5 T3 - 3.596E-9 T4 dT298.15

2

+

CpdT298.15

6.778412.09

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 T

298.15412.09 -

n412.09

CpdT298.15

+ 0.00192

=


77/122

5 5

= kJ/jam

2 2

3 3 4 4

5 5

= kJ/jam

Jadi:

Q3= kJ/jam

c. Panas Sensibel Cairan Reflux, Q4

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

298.152

379.13

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4

46.9480 379.13 - 298.15 +

-

412.09

31.3860 T + 0.4746 T2 - 3.11E-4 T3 + 8.524E-8 T4 - 5.0524E-12 T

2.5398

dT298.15

+ #######

412.09 - 298.15

+ ####### 412.09 - 298.155

8.52E-08412.09 - 298.15

3 4+

#######412.09 - 298.15 +

+ 0.47460

412.09 -

C6H6

Q = n412.09

CpdT298.15

= 2.E-04 -31.3860 412.09 - 298.15

. - .

= 2.E-04

- 298.152

+ #######

379.13

3.

298.15

H2O

.4

296653.0838

379.13 - 298.152

Q = n379.13

0.98961.59

=298.15

379.13

46.9480 T + 0.9896 T2 - 2.3583E-3 T3 + 2.3296E-6 T4 dT

C6H5NH2

1.31E-06379.13 - 298.15

3 4

+ 0.47212

298.15

6.3182 18.2964 379.13 -

Q

298.153

n CpdT

298.15

379.13

dT

38719.7657

298.15

CpdT

=379.13

-

5

1.0011

=

+

4+

#######379.13 - 298.15 +

2.33E-06

1.59

379.13

=

- 298.15

= 6.3182


78/122


79/122

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

= kJ/jam

2 2

3 3 4 4

= kJ/jam

dT

298.15

= 4.E-05 -12.6350 379.13 - 298.15 298.15

298.15

0.8291

379.13 - 298.153 4

+ #######

379.13 - 298.15 +

+ 2.32E-06

379.13 - 298.153 4

+ 1.56240 379.13 -2

+ #######

379.13 -

Q = n379.13

CpdT298.15

298.15

31.6623

C6H4N2O4

Q = n379.13

CpdT

2.01E-06

298.15

= 4.E-05379.13

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4

298.15 +

0.91277

379.13 -2

0.0021379.13

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4 dT298.15

= 0.0021 39.4730 379.13 -

379.13 - 298.15

C6H5NO2

= 5.2.E+00 46.9480 - 298.152

dT298.15

126364.7574

+ 0.9896

84907.2488

C6H5NH2

= 5.2.E+00379.13

46.9480 T + 0.9896 T2 - 2.3583E-3 T3 + 2.3296E-6 T4

379.13

=

2.33E-06379.13 - 298.15

3 4+

#######379.13 - 298.15 +

Q = n379.13

CpdT298.15

- 298.153 4

0.47212379.13 - 298.15

2

+ #######

379.13 - 298.15

20.6200 18.2964 379.13 - 298.15 +

+ 1.31E-06

=

379.13

= 20.6200379.13

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4 dT298.15

298.15


80/122

2 2

3 3 4 4

= kJ/jam

Jadi:

Q5= kJ/jam

e. Panas yang dilepas oleh Pendingin Kondensor, Qc

= Q2+ Q3 - Q4+ Q5

= kJ/jam

Sebagai pendingin digunakan air pada suhu 25oC dan tekanan 1 atm.

Diperkirakan air keluar pada suhu 45oC.

Dari App A.2 Geankoplis, 2003 diperoleh Cp air =

=

Q = m . Cp. T

Cp. T

( 45 - 25 )

Perhitungan Neraca Panas pada Reboiler

a. Panas Sensibel Cairan Masuk MD , Q1

Panas sensibel masuk MD 2 sama dengan panas sensibel cairan keluaranHeater.

Q1= kJ/jam

b. Panas Sensibel Cairan Produk Bawah, Q6

2 2

3 3 4 4

9.4408

3.82E-06379.13 - 298.15

3 4+

#######379.13 - 298.15 +

+ 0.47430

379.13 - 298.152

= 0.0002 -33.6620 379.13 - 298.15

298.15

= 0.0002379.13

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4 dT298.15

C6H6

Q = n379.13

CpdT

+ #######

457.17 - 298.15 +

- 298.152

1.31E-06457.17

Q =

= 0.0344457.17

18.2964 T + 0.47212 T2 - 1.34E-3 T3 + 1.31E-6 T4

- 298.15 + 0.47212

457.17

H2O

- 298.153 4

4.1787 kJ/kgoC

n457.17

CpdT298.15

2666525.0385

dT298.15

=21928.7820

= kg/jam4.1787

0.9987 kkal/kgoC

Qc

21928.7820

mc =Qc

= 0.0344 18.2964 457.17

211313.9385

262.3901


81/122


82/122


83/122


84/122


85/122

6570771.5516 2838811.5810

Total 6572662.0325 6572662.0325

Q C6H4N2O4 27.8001 115.9067

Q C6H5NH2

Q H2O 419.9350 1951.0776

Q pendingin - 3730340.7215

Q C6H6 386.0537 386.0537


86/122


87/122


88/122


89/122


90/122


91/122


92/122


93/122


94/122


95/122


96/122


97/122


98/122


99/122


100/122


101/122


102/122


103/122


104/122


105/122


106/122


107/122


108/122


109/122


110/122


111/122


112/122


113/122


114/122


115/122


116/122


117/122


118/122


119/122

rus rus rus rus rus rus rus rus rus us us us us us us us us us 18

0 0 ## ## ## ## ## ## ## ## ## ## ##

0 0 ## ## ## ## ## ## ## ## ## ## ##

0 0 ## ## ## ## ## ## ## ## ## ## ##

0 0 ## ## ## ## ## ## ## ## ## ## ##

## ## 0 0 0 0 0 ## ## ## ## 0 0

## ## 0 0 0 0 0 ## ## ## ## 0 0

0 0 0 0 0 0 0 ## ## ## ## ##

## ## ## ## ## ## ## ## ## ## ## ## ##

H2

CH4

6H5NH

Total

ompon

Neraca Massa (kg/jam)

6H5NO

6H4N2O

H2O

C6H6


120/122

Arus 1 Arus 2 Arus 3 Arus 4 Arus 5 Arus 6 Arus 7

0 0 10757.8363 10757.8363 10757.8363 2689.4591 10757.8363

0 0 10.8337 10.8337 10.8337 2.7084 10.8337

0 0 10.8337 10.8337 10.8337 2.7084 10.8337

0 0 10.8337 10.8337 10.8337 2.7084 10.8337

524.7725 524.7725 0 0 0 0 00.0052 0.0052 0 0 0 0 0

0 0 0 0 0 0 0

524.7778 524.7778 10790.34 10790.337 10790.337 2697.5843 10790.337

H2CH4

C6H5NH2

Total

Komponen

C6H5NO2

C6H4N2O4

H2O

C6H6


121/122

Arus 8 Arus 9 Arus 10 Arus 11 Arus 12 Arus 13 Arus 14 Arus 15 Arus 16

10757.8363 215.1567 215.1568 215.1568 4.3031 210.8536 4.3031 0.0430 1.6916

10.8337 10.8337 10.8337 10.8337 0.1083 10.7253 0.1083 0.0011 0.0426

10.8337 3096.4960 3096.4960 3096.4960 61.9299 3034.5661 61.9299 61.3106 0.2459

10.8337 10.8337 10.8337 10.8337 0.2167 10.6170 0.2167 0.0022 0.0852

524.7725 10.4955 10.4955 10.4955 0 10 0 0 00.0052 0.0052 0.0052 0.0052 0 0.0052 0 0 0

0.0000 7971.2943 7971.2970 7971.2970 7970.4972 0.7971 7970.4972 79.7050 3133.2230

11315.115 11315.115 11315.118 11315.118 8037.0552 3267.5591 8037.0552 141.06187 3135.2882

Neraca Massa (kg/jam)


122/122

Documents

Lampiran Neraca Massa dan Panas Prarancangan Pabrik Anilin dari Nitrobenzene.xlsx