LAMPIRAN A PERHITUNGAN NERACA MASSA

(1)

LAMPIRAN A

PERHITUNGAN NERACA MASSA

Kapasitas produksi Dimetil Tereftalat (DMT) = 60.000 ton/tahun 1 tahun = 330 hari kerja

1 hari = 24 jam kerja

Kapasitas tiap jam = 60.000 x x x = 7575,7576 kg / jam

Kemurnian dari Dimetil Tereftalat (DMT) adalah 99,7%, maka : Jumlah Dimetil Tereftalat (DMT) = 99,7% x 7575,7576 kg/jam

= 7553,0303 kg/jam

A.1 Penentuan Komposisi Bahan Baku Komposisi Asam Tereftalat :

 98,5% Asam Tereftalat (AT) : 6483,4888 kg/jam

 1,5% Impurities (I) : 98,7333 kg/jam

Total : 6582,2222 kg/jam

Komposisi Metanol

 99,4% Metanol (M) : 2880,3048 kg/jam

 0,6% Air (W) : 17,3861 kg/jam Total : 2897,6909 kg/jam

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(10) (11)

A.2 Perhitungan Neraca Massa A.2.1 Sublimator (SB-01)

Fungsi: Menyublimasi Fresh Asam Terephthalic ( AT ) dan hasil recycle dari Desublimator (DE-01 ) dengan reaktan uap metanol bersuhu tinggi.

Gambar A.1 Aliran Proses pada Sublimator (SB-01)

Neraca Massa Total :

F⁹ + F¹⁰ + F¹¹ = F¹² 58702,5542 + 6582,2221 + 297,7901 = F¹² 65582,5663 kg/jam = F¹²

Neraca Massa Komponen :

AT : = 6582,2221 x 98,5%

= 6483,4888 kg/jam

= 297,7901 x 83,933%

= 249,9455 kg/jam

=

= 6483,4888 + 249,9455

= 6733,4340 kg/jam I : = 6582,2221 x 1,5%

= 98,7333 kg/ jam

SB - 01

M (aq) 99,4%

W(l) 0,6%

AT 98,5%

I 1,5%

AT M W DMT I AT 83,933%

M 0,356%

W 0,029%

DMT 15,682%

(3)

=

= 98,7333 kg/jam M : = 58702,5542 x 99,4%

= 58350,3389 kg/jam

= 297,7901 x 0,356%

= 1,0607 kg/jam

=

= 58350,3389 + 1,0607

= 58351,3996 kg/jam W : = 58702,5542 x 0,6%

= 352,2153 kg/jam

= 297,7901 x 0,029%

= 0,0851 kg/jam

=

= 352,2153 + 0,0851

= 352,3004 kg/jam DMT : = 297,7901 x 15,6892%

= 46,6990 kg/ jam

=

= 46,6990 kg/jam

Tabel A.1 Neraca Massa pada Sublimator (SB-01)

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

Alur 9 Alur 10 Alur 11 Alur 12 Asam Tereftalat 0 6483,4888 249,9455 6733,4340

Metanol 58350,3389 0 1,0607 58351,3996

Air 352,2153 0 0,0851 352,3004

Dimetil Tereftalat 0 0 46,6989 46,6990

Impuritis 0 98,7333 0 98,7333

subtotal 58702,5542 6582,2221 297,7901 65582,5663

total 65582,5663 65582,5663

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A.2.2 Ash Filter (CN-01)

Fungsi : Memisahkan inert berupa logam-logam yang tidak tersublimasi dari uap metanol

Gambar A.2 Aliran Proses pada Ash Filter (CN-01)

F¹² = F¹³+ F¹⁴ 65582,5663 = 98,7333 + F¹⁴ 65483,8330 kg/jam = F¹³

AT : = = 6733,4340 kg/jam I : = = 98,7333 kg/jam M : = = 58351,3996 kg/jam W : = = 352,3004 kg/jam DMT : = = 46,6990 kg/ jam

Tabel A.2 Neraca Massa pada Ash Filter (CN-01)

Alur 12 Alur 13 Alur 14

AT 6733,4340 0 6733,4340

M 58351,3996 0 58351,3996

W 352,3004 0 352,3004

DMT 46,6990 0 46,6990

I 98,7333 98,7333 0

subtotal 65582,5663 98,73333 65483,833

total 65582,5663 65582,5663

CN - 01

AT M W DMT I

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A.2.3 Reaktor (R-01)

Fungsi : Mengesterifikasi Asam Terephthalic dengan Metanol pada fase gas menjadi Dimetil Tereftalat.

Gambar A.3 Aliran Proses pada Reakor (R-01)

Reaksi yang terjadi di dalam Reaktor :

+ 2 → +2

P- C6H4( COOH )2 CH3OH P-C6H4( COOCH3 )2 H2O

XAT = 0,96 =

r₁ = 0,96 x

= 0,96 x 40,5316

= 38,9103 kmol/jam

F¹⁴ = F¹⁵

65582,5663 kg/jam = F¹⁵ Neraca Massa Komponen :

AT : = – ( r1 x

= 6733,4340 – (38,9103 x 166,128)

= 269,3374 kg/jam

=

0,0009

R - 01

AT M W DMT

(6)

M : = – ( 2 x r₁ x

= 58351,3996 – ( 2 x 38,9103 x 32,042 )

= 55857,8695 kg/jam

=

M15=N_M¹⁵

N¹⁵=1743,2704

1881,4180=0,9266 W : = + ( 2 x r1 x

= 352,3004 + (2 x 38,9103 x 18,016)

= 1754,3177 kg/jam

=

0,0518 DMT : = + ( r1 x

= 46,6990 + (38,9103 x 194,18)

= 7602,3084 kg/jam

=

DMT =N_DMT¹⁵

N¹⁵ = 39,1508

1881,4180=0,0208

Tabel A.3 Neraca Massa pada Reaktor (R-01)

Alur 14 Alur 15

AT 6733,4340 269,3374

M 58351,3996 55857,8695

W 352,3004 1754,3177

DMT 46,6990 7602,3084

total 65483,833 65483,833

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A.2.4 Cyclone (CN-03)

Fungsi : Memisahkan Asam Tereftalat yang tidak bereaksi untuk direcycle kembali ke reaktor.

Gambar A.4 Aliran Proses pada Cyclone (CN-03)

Penentuan Dew Point

Untuk menentukan titik dew point, berlaku Yi =Zi dan

Pio Yi Xi P

=

TRIAL T, Suhu

ZA,ZB,ZC,ZD P

APAKAH XA + XB +XC + XD=1 ?

NO

YES ^{T = T DEW}

POINT

PAo, PBo, PCo, PDo

XA, XB, XC, XD

Alogaritma menentukan suhu dew point

CN - 03

AT M W DMT

AT M W DMT AT

M W DMT

(8)

Tekanan Uap Jenuh dapat dihitung dengan menggunakan Persamaan Antoinne sebagai berikut :

T A B P^o = 

ln

P^o 7524T ,1 156

, 20

ln =  , untuk DMT

P^o 16880T

485 , 31

ln =  , untuk AT

29 , 34

55 , 5875 3626

, 18

ln =  

P^o T , untuk Metanol

421 , 19

9 , 421 4770

, 19

ln =  

P^o T , untuk air dengan : P^o = tekanan uap jenuh , mmHg

T = suhu, kelvin

Trial T = 259,85^oC (533 K) ; P = 1,15 atm (874mmHg)

=

= 0,8313 mmHg

AT= P _AT P_AT^o .

AT= 874 0,0009 0,8313

AT= 0,9463 =

=

= 82095,5094 mmHg

M= P _M P_M^o

M= 874 0,9266 82095,5094

M= 0,0099 =

=

= 35421,0933 mmHg

= P P^o

= 874 0,0518 35421,0933

= 0,0013

=

DMT= P _DMT P_DMT^o

(9)

= 419,6788 mmHg

AT= 874 0,0208 419,6788

AT= 0,0433

0,9463 + 0,0099 + 0,0013 + 0,0433

= 1,0008

Suhu dew point berkisar 260^oC , HE-01 digunakan terlebih dahulu untuk

mendinginkan produk gas dari reaktor sebelum produk gas didesublimasi. HE-01 akan menurunkan suhu gas produk dari 330 ^oC sampai suhu 270 ^oC .

Kesetimbangan

Diasumsikan bahwa produk yang keluar dari desublimator telah mencapai kesetimbangan yaitu kesetimbangan 2 fase dan 4 komponen. Sehingga komposisi dan jumlah komponen di fase gas dan fase padat bisa dihitung dengan alogaritma sebagai berikut :

P

mi= Pio dan

( )

LG mi

LG Zi

Xi 



= 1

(10)

TRIAL L/G

ZA,ZB, ZC,ZD

APAKAH XA + XB +XC + XD =1 ?

dan YA + YB + YC + YD =1?

NO

YES Congratulation T,P

PAo, PBo, PCo, PDo

mA, mB, mC, mD

XA, XB, XC, XD

YA, YB, YC, YD

Alogaritama perhitungan kesetimbangan

Trial T = 220^oC (493,15 K) ; P = 1,15 atm (874mmHg) ; L/G = 0,0009485

=

= 0,0643 mmHg

m_AT=P_AT^o P m_AT=0,0643

874 m_AT=0,0001

AT= 0,0009 (1+0,0009485) 0,0001+ 0,0009485

y_AT= m_AT _AT

y_AT= 0,0001

(11)

=

= P_M^o = 43656,5666 mmHg

m_M=P_M^o P

m_M=45656,5666 874 m_M=49,9503

M= 09266 (1+0,0009485) 49,9503+ 0,0009485

y_M= m_M _M

y_M= 0,9274

=

=17097,0560 mmHg

m =P^o P

m =17097,0560 874 m =19,5618

= 0,0518 (1+0,0009485) 19,5618+ 0,0009485

y = m

y = 0,0518

=

=134,1255 mmHg

m_DMT=P_DMT^o P m_DMT=134,1255

874 m_DMT=0,1535

DMT= 0,0208 (1+0,0009485) 0,1535+ 0,0009485

y_DMT= m_DMT _DMT

y_DMT= 0,0207

Σ = 1,0000 Σ = 1,0000

1,6213 + 1743,2704 + 97,3755 + 39,1508

1881,4180^kmol_jam

(12)

Neraca Massa Total : N¹⁷= L¹¹+ ¹⁸

N ¹⁸ = L¹¹

= 0,0009485

= 0,0009485 1881,4180 = 0,0009485 1881,4180 = 1,0009485

1879,6352kmol jam =

L¹¹= N¹⁷ ¹⁸

L¹¹= 1881,4180 1879,6352

1,7828 ^kmol

jam

Neraca Massa Komponen : AT : _AT¹¹= _AT L¹¹ Mr_AT

AT11= 0,8439 1,7828 166,128

AT11= 249,9455 kg/jam

AT18= y_AT ¹⁸ Mr_AT

AT18= 0,0001 1879,6352 166,128

AT18= 19,3919 kg jam

= ^AT

18

Mr_AT=^19,3919_166,128=0,1167^kmol_jam

0,0001

M : _M¹¹= _M L¹¹ Mr_M

M11= 0,0186 1,7828 32,042

M11= 1,0607 kg/jam

M18= y ¹⁸ Mr_M

M18= 0,9274 1879,6352 32,042

M18= 55856,8088 kg jam

= ^M

18

Mr_M=^55856,8088

32,042 =1743,2373^kmol

jam

(13)

0,9274

W : ¹¹= L¹¹ Mr

11= 0,0026 1,7828 18,016

11= 0,0851 kg/jam

18= y ¹⁸ Mr

18= 0,0518 1879,6352 18,016

18= 1754,2326 kg jam

=

18

Mr =^1754,2326

18,016 =97,3708

0,0518

DMT : _DMT¹¹ = _AT L¹¹ Mr_DMT

DMT11 = 0,1349 1,7828 194,18

DMT11 = 46,6989 kg/jam

DMT18 = y_DMT ¹⁸ Mr_DMT

DMT18 = 0,0208 1879,6352 194,18

DMT18 = 7555,6095 kg jam

= ^DMT

18

Mr_DMT=^7555,6095 = 38,9103^kmol_jam

0,0207

Tabel A.4 Neraca Massa pada Cyclone (CN-03)

Asam Tereftalat 269,3374 249,9455 19,3919

Metanol 55857,8695 1,0607 55856,8088

Air 1754,3177 0,0851 1754,2328

Dimetil Tereftalat 7602,3084 46,6990 7555,6095

subtotal 65483,8330 297,7901 65186,0428

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total 65483,8330 65483,8330

A.2.5 Tangki Separator (TS-02)

Fungsi : Untuk memisahkan semua hasil produk DMT dari campuran uap hasil reaktor

Gambar A.5 Aliran Proses pada Tangki Separator (TS-02)

Kesetimbangan

Trial T = 72^oC (345,15 K) ; P = 1,1 atm (836mmHg) ; L/G = 0,281

TS - 02

AT M W DMT

AT M W DMT M

W

(15)

=

= 0,0000 mmHg

m_AT=P_AT^o P m_AT=0,0000

836 m_AT=0,0000

AT= 0,0001 (1+0,281) 0,0000+ 0,281

y_AT= m_AT _AT

y_AT= 0,0000

=

= = 1013,6529 mmHg

m_M=P_M^o P

m_M=1013,6529 836 m_M=1,2125

M= 0,9274 (1+0,281) 1,2125+ 0,281

y_M= m_M _M

y_M= 0,9645

=

= 269,9709 mmHg

m =P^o P

m =269,9709 836 m =0,3229

= 0,0518 (1+0,281) 0,3229+ 0,281

y = m

y = 0,0355

=

= 0,1933 mmHg

m_DMT=P_DMT^o P m_DMT=0,19333

836 m_DMT=0,0002

DMT= 0,0207 (1+0,281) 0,0002+ 0,281

y_DMT= m_DMT _DMT

y_DMT= 0,0000

Σ = 0,9999 Σ = 1,0000

(16)

0,1167 + 1743,2373 + 97,3708 + 38,9103

1879,6352^kmol_jam

Neraca Massa Total : N¹⁹= L²¹+ ²⁰

N ²⁰ = L²¹

= 0,281

= 0,281 1879,6352 = 0,281 1879,6352 = 1,281

1467,3187kmol jam = ²⁰

L²¹= N ²⁰

L²¹= 1879,6352 1467,3187 L²¹ 412,3165 ^kmol

jam

Neraca Massa Komponen : AT : _AT²¹= _AT L²¹ Mr_AT

AT21= 0,0003 412,3165 166,128

AT21= 19,3919 kg/jam

AT20= y_AT ²⁰ Mr_AT

AT20= 0,0000 1467,3187 166,128

AT20= 0,0000 kg jam

M : _M²¹= _M L²¹ Mr_M

M21= 0,7955 412,3165 32,042

M21= 10509,3580 kg/jam

M20= y ²⁰ Mr_M

M20= 0,9645 1467,3187 32,042

M20= 45347,4508 kg jam

(17)

W : ²¹= L²¹ Mr

21= 0,1099 412,3165 18,016

21= 816,2171 kg/jam

20= y ²⁰ Mr

20= 0,0355 1467,3187 18,016

20= 938,0156 kg jam

DMT : _DMT²¹ = _DMT L²¹ Mr_DMT

DMT21 = 0,0943 412,3165 194,18

DMT21 = 7555,6095 kg/jam

DMT20 = y_DMT ²⁰ Mr_DMT

DMT20 = 0,0000 1467,3187 194,18

DMT20 = 0,000 kg jam

Tabel A.5 Neraca Massa pada Tangki Separator (TS-02)

Asam Tereftalat 19,3919 19,3919

Metanol 55856,8088 45347,4508 10509,3580

Air 1754,2328 938,0156 816,2171

Dimetil Tereftalat 7555,6095 7555,6095

subtotal 65186,0428 46285,4664 18900,5765

total 65186,0428 65186,0428

(18)

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A.2.6 Crystalyzer (CR-01)

Fungsi : Mengkristalisasi produk DMT ( Dimethyl Tereftalat ) dari hasil kondensasi CD-01

Gambar A.6 Aliran Proses pada Cooling Crystalizer (CR-01)

Data Kelarutan

Kelarutan Asam Terephthalic dalam g / 100 g metanol

Suhu, ^oC 25 160

Kelarutan 0,1 2,9

(Kirk & Othmer)

Kelarutan Dimethyl Terephthalate dalam g / 100 g metanol

Suhu, ^oC 25 60

Kelarutan 1,0 5,7

(Kirk & Othmer)

Persamaan Clausius-Clapeyron

2

ln

RT H dT

S

d 

=

RT dT S H

dln = ₂

T C R

S H  

= 1

ln

CR - 01

AT M W DMT AT

M W DMT

AT M W DMT

(19)

Dari data kelarutan yang tersedia di plot 1/T (sumbu x) dengan ln S (sumbu y). Maka diperoleh gambar sebagai berikut

Diperoleh persamaan :

AT : 1 8,5014

2219 , 3221

ln =  

S T

DMT : 1 16,5668

3770 , 4939

ln =  

S T T = 72^oC (345,15 K) AT :

5014 , 15 8 , 345 2219 1 , 3221

lnS =  

8314 , 0 lnS =

AT21 ^M²¹^M

100

AT21 ^10537,6821

100

AT21 y = -3221.2219x + 8.5014

-2,5 -2 -1,5 -1 -0,5 0 0,5 1 1,5

0 0,001 0,002 0,003 0,004

ln S

1/T

Kelarutan AT dalam Metanol

y = -4,939.3770x + 16.5668

0 0,5 1 1,5 2

0,0029 0,003 0,0031 0,0032 0,0033 0,0034

ln S

1/T Kelarutan DMT dalam Metanol

(20)

8314 ,

0

=e S

4355 ,

=0 S DMT :

5668 , 15 16 , 345 3770 1 , 4939

lnS =  

2560 , 2 lnS=

2560 ,

e2

S =

5447 ,

=9 S

DMT21 ^M²¹₁₀₀^M²⁶

DMT21 (a )=9,5447 ^10537,6821₁₀₀

DMT21 (a )=670,5276

DMT21 (s)= _DMT²¹ + _DMT²⁶ _DMT²¹ (a )

DMT21 (s)=7555,6095+27,0528 670,5276

DMT21 (s)=6912,1346 T = 10^oC (283,15 K)

AT :

5014 , 15 8 , 283 2219 1 , 3221

lnS =  

8749 , 2 lnS =

8749 ,

2

=e S

0564 ,

=0 S

AT22 ^M²¹₁₀₀^M²⁶

AT22 ^10537,6821₁₀₀

AT22 34

AT22(s)= _AT²¹+ _AT²⁶ _AT²²(a )

AT22(s)=19,3919+3,6707 3,9634

AT22(s)=19,0992 DMT

:

5668 , 15 16 , 283 3770 1 , 4939

lnS =  

8776 , 0 lnS =

8776 ,

0

=e S

4158 ,

=0 S

DMT22 ^M²¹₁₀₀^M²⁶

DMT22 (a )=0,4158 ^10537,6821

100

DMT22 (a )=29,2095

DMT22 (s)= _DMT²¹ (s)+ _DMT²¹ _DMT²² (a )

DMT22 (s)=6912,1346+670,5276 29,2095

(21)

(22) (23)

(25)

DMT22 (s)=7553,4527

Tabel A.6 Neraca Massa pada Crystalyzer (CR-01)

Asam Tereftalat (aq) 19,3919 3,6707 3,9634

Asam Tereftalat (s) 0 0 19,0992

Metanol 10509,3580 28,3241 10537,6821

Air 816,2171 8,1922 824,4093

Dimetil Tereftalat (aq) 670,5276 29,2095

Dimetil Tereftalat_(s) 6912,1346 7553,4527

total 18967,8163 18967,8163

A.2.7 Centrifuge (CF-01)

Fungsi : Memisahkan padatan dari slurry yang berasal dari Cooling Crystalizer ( CR – 01 )

Gambar A.7 Aliran Proses pada Centrifuge (CF-01) Fraksi Massa Cairan

Komponen Alur 22 xi

AT (aq) 3,9624 0,0003

M 10537,6821 0,9247

W 824,4093 0,0723

DMT (aq) 29,2095 0,0027

Σ=11395,2643 Σ=1

CF - 01

AT M W DMT

AT M W AT DMT

M W DMT

(22)

Sisa cairan dalam padatan = 10%

Σ padatan = _AT²(s) + _DMT²² (s)

= 19,0992 + 7553,4527

= 7572,5520 kg/jam 90

Σ padatan= 10 Σ cairan 90

7572,5520= 10 Σ cairan

Σ cairan = 841,3947 kg/jam

Neraca Massa Komponen : AT(aq) = x Σ cairan

= 0,0003 x 841,3947

= 0,2926 kg/jam

=

= 3,9634 0,2926 = 3,6707 kg/jam AT(s) = = 19,0992 kg/jam

M : = x Σ cairan

= 0,9247 x 841,3947 = 778,0732

=

= 10537,6821 – 778,0732 = 9759,6089 kg/jam W : = x Σ cairan

= 0,0723 x 841,3947 = 60,8721

=

= 824,4093 – 60,8721 = 763,5372 kg/jam DMT(aq) = x Σ cairan

= 0,0027 x 841,3947 = 2,1567 kg/ jam

=

= 29,2095– 2,1567 = 27,0528 kg/jam DMT(s) = = 7553,4527 kg/jam

(23)

(24) (26) (27)

Tabel A.7 Neraca Massa pada Centrifuge (CF-01)

Asam Tereftalat (aq) 3,9634 0,2926 3,6707

Asam Tereftalat_(s) 19,0992 19,0992 0

Metanol 10537,6821 778,0732 9759,6089

Air 824,4093 60,8721 763,5372

Dimetil Tereftalat (aq) 29,2095 2,1567 27,0528

Dimetil Tereftalat (s) 7553,4527 7553,4527

Subtotal 18967,8163 8413,9466 10553,8697

Total 18967,8163 18967,8163

A.2.8 Tangki Separator (TS-03)

Fungsi : Memisahkan sisa DMT yang terlarut pada larutan filtrat Centrifuge Filtration (CF-01)

Komponen

Alur 24

Fi Mri N_i= Z_i=

AT 3,6707 166,1280 0,0221 0,0001

M 9759,6089 32,0420 304,5880 0,8774

TS - 03

AT M W DMT

AT M W DMT M

W

(24)

W 763,5372 18,016 42,3811 0,1221

DMT 27,0528 194,18 0,1393 0,0004

Σ 347,1305

Kesetimbangan

Trial T = 75^oC (348,15 K) ; P = 1 atm (760mmHg) ; L/G = 0,00434

=

=4,1406e-08 mmHg

m_AT=P_AT^o P

m_AT=4,1406e 08 760 m_AT=5,45e 11

AT= 0,0001 (1+0,00434) 5,45e 11+ 0,00434

y_AT= m_AT _AT

y_AT= 0,0000

=

= = 1133,2285 mmHg

m_M=P_M^o P

m_M=1133,2285 760 m_M=1,49109

M= 0,8777 (1+0,00434) 1,49109+ 0,00434

y_M= m_M _M

y_M= 0,8787

=

= = 304,1205 mmHg

m =P^o P

m =304,1205 760 m =0,400159

= 0,1218 (1+0,00434) 0,400159+ 0,00434

y = m

y = 0,1213

=

m_DMT=P_DMT^o

P

y_DMT= m_DMT _DMT

y_DMT= 0,0000

(25)

=

= 0,2332 mmHg

m_DMT=0,2332 760 m_DMT=0,0000

DMT= 0,00004 (1+0,00434) 0,000+ 0,00434

Σ = 1,000 Σ = 1,0000

Neraca Massa Total : N²= L²⁶+ ²⁷

N² ²⁷ = L²

= 0,00434

= 0,00434 = 0,00434 = 1,004346

345,6304kmol jam =

L²⁶= N ²⁷

L²⁶= 347,1305 345,6304 L²⁶ 1,5001 ^kmol

jam

(26)

AT : _AT²⁶= _AT L Mr_AT

AT26= 0,0147 1,5001 166,128

AT26= 3,6677kg/jam

AT27= y_AT ²⁷ Mr_AT

AT27= 0,0000 345,6304 166,128

AT27= 0,0000 kg jam

M : _M²⁶= _M L Mr_M

M26= 0,5893 1,5001 32,042

M26= 19,2935 kg/jam

M27= y ²⁷ Mr_M

M27= 0,8787 345,6304 32,042

M27= 9732,2075 kg jam

W : ²⁶= L Mr

26= 0,3031 1,5001 18,016

26= 5,5814 kg/jam

27= y ²⁷ Mr

27= 0,1213 345,6304 18,016

27= 755,5569 kg jam

DMT : _DMT²⁶ = _DMT L Mr_DMT

DMT26 = 0,0929 1,5001 194,18

DMT26 = 27,0303 kg/jam

DMT27 = y_DMT ²⁷ Mr_DMT

DMT27 = 0,0000 345,6304 194,18

DMT27 = 0,000 kg jam

Tabel A.8 Neraca Massa pada Tangki Separator (TS-03)

Asam Tereftalat 3,6707 3,6707 0

Metanol 0 28,3241 9731,2849

Air 9759,6089 8,1922 755,3450

Dimetil Tereftalat 763,5372 27,0528 0

(27)

subtotal 27,0528 67,2398 10486,6298

total 10553,8697 10553,8697

(28)

(25) (29) (28) (31) A.2.9 Rotary Dryer (RD-01)

Fungsi : Untuk mengurangi kadar metanol hasil padatan DMT sampai 0,05

%

Gambar A.9 Aliran Proses pada Rotary Dryer (RD-01) Fraksi Massa

Komponen Alur 25 x_i

AT 19,3919 0,0023

M 778,0732 0,0925

W 60,8721 0,0072

DMT 7555,6095 0,8980

Σ = 8413,9466 Σ=1,0000

Sisa cairan dalam padatan = 0,05%

Σ padatan = _AT²⁵+ _DMT²⁵

= 19,3919 + 7555,6095

= 7575,0014 kg/jam 99,95

Σ padatan= 0,05 Σ cairan 99,95

7575,0014= 0,05 Σ cairan Σ cairan = 3,7894 kg/jam

Udara pengering (0,3% W) = ²⁸ 4,3960 kg/s = 15825,6 kg/jam

28 ²⁸

RD - 01

AT M W DMT

Udara W

AT M W DMT M

W Udara

(29)

28

28 = 47,4768 kg/jam

Neraca Massa Komponen : AT =

= 19,3920 kg/jam

M : = Σ cairan x (

= 778,0732 + 60,8721 – 3,7894 x (

= 774,5587 kg/jam

=

= 778,0732 – 774,5587

= 3,5150 kg/jam

W : = ) +

= 778,0732 + 60,8721 – 774,5587 + 47,4768

= 108,0098

=

= 60,8721 + 47,4768 – 108,0098

= 0,2744 kg/jam DMT =

= 7555,6095 kg/jam

Tabel A.9 Neraca Massa pada Rotary Dryer (RD-01)

Alur 25 Alur 28 Alur 29 Alur 31

Asam Tereftalat 19,3919 0 19,3919 0

Metanol 778,0732 0 3,5144 774,5587

Air 60,8721 47,4768 0,2750 108,0739

Dimetil Tereftalat 7555,6095 0 7555,6095 0

Udara 0 15825,6 0 15825,6

subtotal 8413,9464 15873,077 7578,7908 16708,2327

total 24287,0234 24287,0234

(30)

(32) (33) (34) A.2.10 Tangki Separator (TS-05)

Fungsi : Memisahkan sebagian metanol dari udara pengering yang berasal dari Rotary Dryer RD-01

Komponen

Alur 32

F_i Mr_i Ni = Zi=

M 774,5587 32,0420 24,1732 0,0420

W 108,0739 18,016 5,9988 0,0104

Udara 15825,6 29 545,7103 0,9476

Σ 575,8824

Kesetimbangan

Trial T = -5^oC (268,15 K) ; P = 1 atm (760mmHg) ; L/G = 0,03157

=

= = 21,7616 mmHg

m_M=P_M^o P m_M=21,7616

760 m_M=0,028634

M= 0,0420 (1+0,03157) 0,028634+ 0,03157

y_M= m_M _M

y_M= 0,020595

TS - 05

M W Udara

M W M

W Udara

(31)

=

= 5,0992 mmHg

m =P^o P m =5,0992

760 m =0,00671

= 0,0104 (1+0,03157) 0,00671+ 0,03157

y = m

y = 0,001883

y_dara=0,977523

Σ = 1,0000 Σ = 1,0000

^kmol

jam

(32)

Neraca Massa Total : N³²= L³³+ ³⁴

N³² ³⁴ = L³³

= 0,03157

= 0,03157 575,8824 = 0,03157 575,8824 = 1,03157 558,2581 kmol

jam =

L³³= N ³⁴

L³³= 575,8824 558,2581 L³³ 17,6235 ^kmol

jam

Neraca Massa Komponen : M : _M³³= _M L³³ Mr_M

M33= 0,7192 17,6235 32,042

M33= 406,1685 kg/jam

M34= y ³⁴ Mr_M

M34= 0,020595 558,2581 32,042

M34= 368,3902 kg jam W : ³³= L³³ Mr

33= 0,2807 17,6235 18,016

33= 89,131 kg/jam

34= y ³⁴ Mr

34= 0,001883 558,2581 18,016

34= 18,9429 kg jam

Udara : ³⁴= y_DMT ³⁴ Mr_DMT

34= 0,977523 558,2581 26

34= 15825,6 kg jam

Tabel A.10 Neraca Massa pada Condensor (CD-02)

(33)

(35)

(33)

(41) (20)

(27)

M 774,5587 368,3902 406,1685

W 108,0739 18,9429 89,1310

Udara 15825,6 15825,6 0

subtotal 0 16212,9331 495,2995

total 16708,2327 16708,2327

A.2.11 Menara Destilasi (MD-01)

Fungsi : Merecycle sisa metanol yang tidak bereaksi dengan memperoleh hasil metanol dengan kemurnian 99.4 ( % massa ) pada sisi enriching dan membuang air hasil reaksi esterifikasi pada sisi stripping

Gambar A.11 Aliran Proses pada Menara Destilasi (MD-01)

Neraca massa total :

46285,4664 + 10486,6298 + 495,2995 =

57267,3957 =

57267,3957 - =

MD-01

M W

M W M

W

(34)

(7) (9) (6)

Neraca massa metanol :

M20 + _M²⁷ + _M³³ = ( _M³⁵ ) + ( _M⁴¹ )

45437,4508 + 9731,2849 + 406,1685= 0,994 +( 0,01 (57267,3957 - )

55484,9041 = 0,984 +572,673957

54912,23019 = 0,984

= 55805,112

= 57267,3957 - 55805,112

= 1462,2837

Neraca Massa Komponen

M : = 55805,112 x 99,4%

= 55470,2813 kg/jam

= 1462,2837 x 1%

= 14,6228 kg/jam W : = 55805,112 x 0,6%

= 334,8307 kg/jam

= 1462,2837 x 99%

= 1447,6609 kg/jam

Tabel A.11 Neraca Massa pada Menara Destilasi (MD-01)

Alur 20 Alur 27 Alur 33 Alur 35 Alur 41 Metanol 45347,4508 9731,2849 406,1685 55470,2813 14,6228 Air 938,0156 755,3450 89,1310 334,8307 1447,6609 subtotal 46285,4664 10486,6298 4952995 55805,1120 1462,2837

total 57267,3957 57267,3957

A.2.12 Furnace (FU-01)

Fungsi : Memanaskan vapor metanol ( 99,4 % massa ) dari suhu 96,87 ^oC menjadi 385 ^oC

Gambar A.12 Aliran Proses pada Furnace (FU-01)

FU - 01

M W

M W M

W

(35)

Tabel A.12 Neraca Massa pada Furnace (FU-01)

Metanol 55470,0342 2880,3048 58350,3389

Air 334,8292 17,3861 352,2153

subtotal 55804,8634 2897,6909 58702,5542

total 58702,5542 58702,5542

LAMPIRAN B

PERHITUNGAN NERACA PANAS

Basis Perhitungan : 1 jam operasi Satuan operasi : kJ/jam Temperatur Referensi : 0^oC

Kapasitas produk : 60.000 ton/tahun

LB.1 Perhitungan Kapasitas Panas a) Data perhitungan Cp

Cp x,T = a + bT + cT² + dT³ + eT⁴ Kapasitas panas gas ideal ( Cpig )

Data kapasitas panas gas ideal ( Cpig ) metanol dan steam tersedia dalam Appendix D, (Coulson ,1983 ). Sedangkan Cpig Asam Tereftalat dan Dimetil Tereftalat tidak tersedia di daftar dan harus diestimasi dengan metode Rihani & Doraiswany, ( Coulson,1983 ). Karena campuran gas mendekati sifat ideal maka harga kapasitas panas gas ideal bisa dipakai dalam perhitungan.

Asam Tereftalat

Tabel LB.1 Penentuan Konstanta Asam Tereftalat

Ni Jenis Gugus Ni ai Ni bi Ni ci Ni di

2 -COOH 2(1,4055) 2(3,4632 10^-2) 2(-0,2537 10^-4) 2(0,6886 10^-8) 1 -CH=CH- 1(-3,1210) 1(3,8060 10^-2) 1(-0,2359 10^-4) 1(0,5504 10^-8)

(36)

2 -C=CH- 2(-1,4714) 2(3,3842 10^-2) 2(-0,2371 10^-4) 2(0,6063 10^-8) Sum -3,2518 17,5008 10^-2 -1,2215 10^-4 3,1402 10^-8 Dimetil Tereftalat

Tabel LB.2 Penentuan Konstanta Dimetil Tereftalat Ni Jenis

Gugus Ni ai Ni bi Ni ci Ni di

2 -CH3 2(0,6087) 2(2,1433 10^-2) 2(-0,0852 10^-4) 2(1,1350 10^-8) 2 -COO- 2(2,7350) 2(1,0751 10^-2) 2(0,0667 10^-4) 2(-0,0923 10^-8) 1 -CH=CH- 1(-3,1210) 1(3,8060 10^-2) 1(-0,2359 10^-4) 1(0,5504 10^-8) 2 -C=CH- 2(-1,4714) 2(3,3842 10^-2) 2(-0,2371 10^-4) 2(0,6063 10^-8)

Sum 0,6236 17,011 10^-2 -0,7471 10^-4 2,187 10^-8

3

2 DT

CT BT A

Cp=    dengan

K kJkmol

Cp= 

Harga konstanta A, B, C, dan, D untuk Cpig Asam Tereftalat, Metanol, Steam, dan Dimetil Tereftalat :

Tabel LB.3 Harga konstanta A, B, C, dan, D untuk Cpig

Komponen A B C D

AT -3,2518 17,5008 10^-2 -1,2215 10^-4 3,1402 10^-8 Metanol 21,152 7,0920 10^-2 2,2870 10^-5 -2,851 10^-8 Steam 32,243 1,923 10^-3 1,055 10^-5 -3,596 10^-9 DMT 0,6236 17,011 10^-2 -0,7471 10^-4 2,187 10^-8

Metanol

Cp liquid : 80,57230053 kJ/kmol ^oC

Laten heat : 35278 kJ/kmol

T norm : 337,75 K

H Metanol uap pada saat suhu 64,6 ( : 40482,97061 kJ/kmol

1 ₂ 1 ₃ 1 ₄

(37)

li uid = Cp_{li uid} T

Asam Tereftalat

Heat Sublimation : 199,685856 kJ/kmol

Cp solid : 142000 kJ/kmol ^oC

H fusion : 31600 kJ/kmol

T Sublim : 298,15 K

H AT uap pada saat suhu 25 ^oC ( : 146992,1464 kJ/kmol ^oC

uap =A T+1

2B T²+ 1

3C T³+ 1

4D T⁴+

li uid = Cp_solid T + _usion

solid = Cp_solid T Dimetil Tereftalat

T fusion : 50 ^oC

cp solid : 271,852 kJ/kmol ^oC

H fusion : 31600 kJ/kmol

T nm : 284 ^oC

Panas Laten : 57300 kJ/kmol

(38)

COOH

+ 2 CH₃OH

COOCH₃

+ 2 H₂O

Cp liq : 383,60259 kJ/kmol ^oC

H DMT uap pada saat suhu 284^oC ( : 192255,6061 kJ/kmol

uap =A T+1

2B T²+ 1

3C T³+ 1

4D T⁴+

li uid = Cp_solid T + _usion Cp_{li ud} T

solid = Cp_solid T

LB.1 Fixed Bed Reactor (R-01)

Reaksi esterifikasi Asam Tereftalat dengan Metanol menjadi Dimetil Tereftalat dan Steam :

Asam Tereftalat

Metanol Dimethil

Tereftalat

Steam AT

Metanol H₂O DMT AT

Metanol H2O DMT

597,15 K 602,9 K

(39)

Tabel LB.4 Data panas reaksi tiap komponen Komponen

Hf ^o Solid 25 ^oC (kJ / mol)

Panas sublimasi 25 ^oC (kJ / mol)

Hf ^o Gas 25^oC

(kcal / mol) Sumber

A - 816 142 -161,0899 Kirk Othmer

B - - -48,08 Perry,1984

C - - -57,7979 Perry,1984

D -711 88,4 -148,8049 Kirk Othmer

Notasi yang digunakan:

A = Asam Tereftalat B = Metanol

C = Steam

D = Dimetil Tereftalat

Hr0 adalah perubahan entalphi reaksi pada suhu 25 ^oC ΔHf A

- ΔHf B 2 - ΔHf D ΔHf C

ΔHr₀ =2 ô  ô  ô ô kcal/kmol 7150,9052

- kJ/kmol 3872

, 29919

ΔHr₀ = =

Hr pada berbagai suhu :

=







= ^T

To

T ΔHr cp dT

ΔHr

298

0

∆Hr │327oC = -39993.16688 (kJ/kmol)

Panas Reaksi = ∆Hr │327oC x 308249,5277 kmol Tabel LB.5 . Panas masuk Reaktor pada Alur 14

Q_reaksi =

Input kmol/tahun H (kJ/kmol) Q (kJ/tahun)

AT 321010.2893 162789.4800 52257098080

Metanol 14423041.1578 55085.3340 794498039649.0670

H2O 154874.5039 56111.7220 8690275106

DMT 1904.7059 195380.2508 372141915.1

Sum 14900830.6569 8.55818E+11

(40)

=

= -12,327,874,805.0655 kJ/kmol Tabel LB.6 panas keluar reaktor pada alur 15

Out put kmol/tahun H (kJ/kmol) Q (kJ/tahun)

AT 12840.4116 163160.7185 2095050778

Metanol 13806701.4023 55463.57275 7.65769E+11

H2O 771214.2594 56321.13782 43435664589

DMT 310074.5836 195843.2433 60726012122

Sum 14900830.6569 8.72026E+11

Q = Q_out – (Q_in + Q_reaksi)

= 8,72026 x 10¹¹ – (8,55818 x 10¹¹ +(-12,327,874,805.0655))

= 28,536,035,277.0863 kJ

Massa saturated steam yang dibutuhkan:

m=

= 654,0538 kg/jam

LB.2 Furnace (FU-01)

Tabel B.7 Panas masuk Furnace TINPUT

(K) Input kmol/tahun H

(kJ/ kmol) Q (kJ/tahun) 498,24 Metanol 14422778,9877 48937,7570 705998323546,3320 498,24 H2O 154837,1102 52563,1728 41188489538,4174

Total 14577616.0979 747186813084,7490

Metanol H₂O

Metanol H2O

(41)

=A T+1

2B T²+ 1

3C T³+ 1

4D T⁴+

uapmetanol=21,152 337,75 +1

27,0920 10² 337,75 ²+ 1

32,287 10⁵ 337,75 ³+ 1

4 2,851 10⁸ ( 337,75)⁴+ 40482,97_l

= 48937,7570 kJ/kmol Tabel B.8 Panas Keluar Furnace

T_OUTPUT

(K) Output kmol/tahun H (kJ/kmol) Q (kJ/tahun) 658,15 Metanol 14422778,9877 59209,8815 854188660845,8820 658,15 H2O 154837,1102 58334,2173 45710678610,2246

Total 14577616,0979 899899339456,1060

Total kebutuhan panas = Qout – Qin

= 899899339456,1060 kJ/tahun – 747186813084,7490 kJ/tahun

= 152712526371,3570 kJ/tahun

= 19281884,6428 kJ/jam

(42)

LB.3 Sublimator (SB-01)

Tabel LB.9 Panas masuk Sublimator T

INPUT

oC

Source Input kmol/ tahun H

(kJ/kmol)

H (kJ/tahun)

H (kJ/jam) 25 Fresh pure fresh AT 309094,3829 4992,1464 1543044411 194828.8398

25 Fresh Impurities 0

25 Desublimator recycle AT 11915,9064 4992,1464 59485949.4 7510.852197 25 Desublimator recycle metanol 262,1702 2014,3075 528091.3475 66.67820044 25 Desublimator H2O recycle 37,3936 1882,8000 70404.73922 8.889487275 25 Desublimator recycle DMT 1904,7059 6796,3000 12944952.66 1634.463719 385 Furnace Metanol 14422778,9877 59209,8815 8.53971E+11 107824625.6 385 Furnace H2O 154837,1102 58334,2173 9032301635 1140442.126 SUM 14900830,6569 138221,7991 8.64619E+11 109169117,4514

= Cp_solid T

= 199,685856 25

= 4992,1464 kJ/kmol

Tabel LB.10 Panas keluar Sublimator

Total kebutuhan panas = Qout – Qin

= 109169117,4514 kJ/jam – 108057772,0644 kJ/jam

= 1111345,3870 kJ/jam T output

(K) Out put kmol/tahun H (kJ/kmol) Q, kJ/tahun Q, kJ/jam

597,15

AT 321010,2893 162789,4800 52257098080 6598118.444 Metanol 14423041,1578 55085,3340 7.94498E+11 100315409

H2O 154874,5039 56111,7220 8690275106 1097257 DMT 1904,7059 195380,2508 372141915,1 46987,61554

SUM 108057772,0644 AT

I

AT Metanol H₂O DMT

AT Metanol H₂O DMT Metanol

H₂O

(43)

LB.4 Heat Exchanger (HE-01)

HE-01 A

Tabel B.11 Panas masuk Heat Exchanger

T Input (K) Input kmol/tahun H (kJ/kmol) Q (kJ/tahun)

603,15

AT 12840,4116 163176,9059 2095258631,3318 Metanol 13806701,4023 55480,0686 765996740275,0500 H2O 771214,2594 56330,2509 43442692719,7602 DMT 310074,5836 195863,4514 60732278142,9066

Total 14900830,6569 872266969769,0480

T Input (K) Input kmol/tahun H (kJ/kmol) Q (kJ/tahun)

431,237 Metanol 14426454,4903 45173,5318 651693900369,0480 H2O 783599,7588 50214,3280 39347935296,4790 Total 15210054,2491 90305,8601 691041835665,5270 Tabel B.12 Panas keluar Heat Exchanger

T Output (K) Output kmol/tahun H (kJ/kmol) Q (kJ/tahun)

543,15

AT 12840,4116 159407,7312 2046860876,4828 Metanol 13806701,4023 51643,8547 713031281395,7800 H2O 771214,2594 54162,0459 41770542093,8699 DMT 310074,5836 191202,2673 59286963433,6921

SUM 14900830,6569 816135647799,8250

T Output (K) Input kmol/tahun H (kJ/ Kmol) Q (kJ/tahun) 498,2368 Metanol 14426454,4903 48937,7570 705998323546,3320

H2O 783599,7588 52545,7430 41174831524,6801

Total 15210054,2491 747173155071,0120

AT M W DMT

AT M W DMT M

W

M W