lampiran neraca panas

7/16/2019 Lampiran Neraca Panas

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LAMPIRAN II

PERHITUNGAN NERACA PANAS

B. Perhitungan Neraca Panas

Data yang diperlukan untuk perhitungan neraca panas adalah :

Kapasitas panas (Cp) untuk masing – masing zat dalam wujud gas maupun

liquid

Cp = A + BT + CT2 + DT3 + ET4 kJ/kgmol K

CpdT = A (T -298) + B/2 (T2 - 2982) + C/3 (T3 - 2983) +

D/4(T4-2984) + E/5(T5-2985)

QF = n. CpdT

Cp Biuret =0,9686 - 0,63339E-2Xc + 0,1104E-4Xc^2 +

(0,3928E-3+0,2834E-4Xc)

T referensi = 25oC + 273oC = 298oC

Keterangan: Xc : Konsentrasi Biuret



Tabel Data Kapasitas Panas pada Gas dan Liquid

Komponen A B C D E

NH3(l) -182,157 3,36E+00 -1,44E-02 2,04E-05

NH3(g) 33,573 -1,26E-02 8,89E-05 -7,18E-08 1,86E-11

CO2(g) 27,437 4,23E-02 -1,96E-05 4,00E-09 -2,99E-13

CO2(l) -3981,02 5,25E+01 -2,27E-01 3,29E-04

H2O(l) 92,053 -4,00E-02 -2,11E-04 5,35E-07

H2O(g) 33,933 -8,42E-03 2,99E-05 -1,78E-08 3,69E-12

O2(g) 29,526 -8,90E-03 3,81E-05 -3,26E-08 8,86E-12

Urea(l) 965,507 -5,10E+00 1,00E-02 -6,38E-06

Urea(g) 24,856 1,44E-01 3,81E-05 -1,10E-07 3,92E-11

(sumber:Yaws,Carl.1999.)



1. Reaktor (DC-101)

REAKTOR

DC - 101

Stripper (DA - 101) :Urea =…………….?

NH3 =…………….?

CO2 =…………….?

H2O =…………….?

Biuret =…………....?

1 2 3

CO2 = 762500,665 Kkal

NH3 = 6284213,542 Kkal

Carbamat

Condenser(EA - 101) :Urea = 3669080,251 Kkal

NH3 = 18131142,680 Kkal

CO2 = 1374427,871 Kkal

H2O = 5258751,261 Kkal

Biuret = 36,974 Kkal

4

Reaksi yang terjadi:

2NH3 + CO2 NH2COONH4

NH2COONH4 NH2CONH2 + H2O

2NH3 + CO2 NH2CONH2 + H2O

Suhu masuk pada aliran umpan NH3 = 148o

C

Suhu masuk pada aliran umpan CO2 = 108oC

Suhu keluar pada aliran Recycle = 180oC

Suhu keluar pada aliran produk ke stripper = 182oC



Aliran umpan NH3

T = 421°K

CpdT NH3 = -182,157 (421 - 298) + 3,36E+00/2 (4212 - 2982) +

-1,44E-02/3 (4213 - 2983) + 2,04E-05/4 (4214-2984)

= 15019,408 KJ/Kmol

QF NH3 = n x CpdT NH3

= 2155,196078 Kmol x 15019,408 KJ/Kmol

= 32369769,22 KJ x 0,239 Kkal/KJ

= 7736374,843 Kkal

Aliran umpan CO2

T = 381°K

CpdT CO2 = 27,437(381 - 298) + 4,23E-02/2 (3812 - 2982) +

-1,96E-05/3 (3813 - 2983) + 4,00E-09/4 (3814-2984) +

-2,99E-13/5 (3815-2985)

= 3293.628 KJ/Kmol

QF CO2 = n x CpdT CO2

= 263,32804 Kmol x 3293,628 KJ/Kmol

= 867304,6057 KJ x 0,239 Kkal/KJ



= 207285,8008 Kkal

Aliran Recycle

T = 453°K

CpdT Urea = 965,507 (453 - 298) + -5,10E+00/2 (4532 - 2982)+

1,00E-02/3 (4533 - 2983) + -6,38E-06/4 (4534-2984)

= 19886,241 KJ/Kmol

QF Urea = n x CpdT Urea

= 690,479175 Kmol x 19886,241 KJ/Kmol

= 13731035,28 KJ x 0,239 Kkal/KJ

= 3281717,432 Kkal

CpdT NH3 = -182,157 (453 - 298) + 3,36E+00/2 (4532 - 2982) +

-1,44E-02/3 (4533 - 2983) + 2,04E-05/4 (4534-2984)

= 22690,232 KJ/Kmol


= 2990,42283 Kmol x 22690,232 KJ/Kmol

= 67853387,79 KJ x 0,239 Kkal/KJ

= 16216959,68 Kkal



CpdT CO2 = 27,437 (453 - 298) + 4,23E-02/2 (4532 - 2982) +

-1,96E-05/3 (4533 - 2983) + 4,00E-09/4 (4534-2984) +

-2,99E-13/5 (4535-2985)

= 6313,484 KJ/Kmol


= 814,7031348 Kmol x 6313,484 KJ/Kmol

= 5143615,206 KJ x 0,239 Kkal/KJ

= 1229324,034 Kkal

CpdT H2O = 92,053 (453 - 298) + -4,00E-02/2 (4532 - 2982)+

-2,11E-04/3 (4533

- 2983

) + 5,35E-07/4 (4534

-2984

)

= 11840,762 KJ/Kmol

QF H2O = n x CpdT H2O

= 1662,069464 Kmol x 11840,762 KJ/Kmol

= 19680168,95 KJ x 0,239 Kkal/KJ

= 4703560,379 Kkal

QF Biuret = n x Cp x dT

= 0,9211165159 Kmol x 0,969 KJ/Kmol °K x ( 453 – 298 )

°K



= 138,3470951 KJ x 0,239 Kkal/KJ

= 33,06495573 Kkal

Aliran Produk ke Stripper

T = 455°K

CpdT Urea = 965,507 (455 - 298) + -5,10E+00/2 (4552 - 2982)+

1,00E-02/3 (4553 - 2983) + -6,38E-06/4 (4554-2984)

= 20114,738 KJ/Kmol


= 1425,251563 Kmol x 20114,738 KJ/Kmol

= 28668561,78 KJ x 0,239 Kkal/KJ

= 6851786,266 Kkal

CpdT NH3 = -182,157 (455 - 298) + 3,36E+00/2 (4552 - 2982) +

-1,44E-02/3 (4553 - 2983) + 2,04E-05/4 (4554 - 2984)

= 23258,594 KJ/Kmol


= 3462,514109 Kmol x 23258,594 KJ/Kmol

= 80533209,88 KJ x 0,239 Kkal/KJ

= 19247437,16 Kkal



CpdT CO2 = 27,437(455 - 298) + 4,23E-02/2 (4552 - 2982) +

-1,96E-05/3 (4553 - 2983) + 4,00E-09/4 (4554-2984) +

-2,99E-13/5 (4555-2985)

= 6399,410 KJ/Kmol


= 263,32804 Kmol x 6399,410 KJ/Kmol

= 1685144,092 KJ x 0,239 Kkal/KJ

= 402749,4381 Kkal

CpdT H2O = 92,053 (455 - 298) + -4,00E-02/2 (455

2

- 298

2

)+

-2,11E-04/3 (4553 - 2983) + 5,35E-07/4 (4554-2984)

= 12001,694 KJ/Kmol


= 2396,196122 Kmol x 12001,694 KJ/Kmol

= 28758412,62 KJ x 0,239 Kkal/KJ

= 6873260,615 Kkal


= 0,598250933 Kmol x 0,969 KJ/Kmol °K x ( 455 – 298 ) °K



= 91,01370919 KJ x 0,239 Kkal/KJ

= 21,7522765 Kkal

Neraca Panas pada reaktor

Komponen Input (Kkal) Output (Kkal)

Aliran NH3

NH3

Aliran CO2

CO2

7736374,843

207285,8008

Aliran Recycle

Urea

NH3

CO2

H2O

Biuret

3281717,43216216959,68 1229324,0344703560,37933,06495573

Aliran produk ke Stripper

Urea

NH3

CO2

H2O

Biuret

6851786,26619247437,16402749,4381

6873260,61521,7522765

Total 33375255,23 33375255,23



2. Stripper (DA-101)

STRIPPER

DA - 101

Carbamat Condenser

(EA - 101) :NH3 = ................ ?

CO2 = ................ ?

H2O = ................ ?

Reaktor (DC - 101) :Urea = 4193841,449 Kkal

NH3 = 24188680,580 Kkal

CO2 = 1481513,510 Kkal

H2O = 5616104,387 Kkal


4 7

HPD ( DA - 201) :Urea = ................ ?

NH3 = ................ ?CO2 = ................ ?

H2O = ................ ?

Biuret = .............. ?

65CO2 Compressor

(GB - 101) :

CO2 = 1361561,539 Kkal

Suhu masuk pada aliran produk dari reaktor = 182oC

Suhu masuk pada aliran umpan CO2 = 108oC

Suhu keluar pada aliran produk ke DA 201 = 171oC

Suhu keluar pada aliran gas ke EA 101 = 184oC

Aliran produk dari reaktor

T = 455°K

CpdT Urea = 965,507 (455 - 298) + -5,10E+00/2 (4552 - 2982)+

1,00E-02/3 (4553 - 2983) + -6,38E-06/4 (4554-2984)

= 20114,738 KJ/Kmol




= 872,368 Kmol x 20114,738 KJ/Kmol

= 17547453,760 KJ x 0,239 Kkal/KJ

= 4193841,449 Kkal

CpdT NH3 = -182,157 (455 - 298) + 3,36E+00/2 (4552 - 2982) +

-1,44E-02/3 (4553 - 2983) + 2,04E-05/4 (4554 - 2984)

= 23258,594 KJ/Kmol


= 4351,418 Kmol x 23258,594 KJ/Kmol

= 101207868,500 KJ x 0,239 Kkal/KJ

= 24188680,580 Kkal

CpdT CO2 = 27,437(455 - 298) + 4,23E-02/2 (4552 - 2982) +

-1,96E-05/3 (4553 - 2983) + 4,00E-09/4 (4554-2984) +

-2,99E-13/5 (4555-2985)

= 6399,410 KJ/Kmol


= 968,652 Kmol x 6399,410 KJ/Kmol

= 6198801,295 KJ x 0,239 Kkal/KJ



= 1481513,510 Kkal

CpdT H2O = 92,053 (455 - 298) + -4,00E-02/2 (4552 - 2982)+

-2,11E-04/3 (4553 - 2983) + 5,35E-07/4 (4554-2984)

= 12001,694 KJ/Kmol


= 1957,919 Kmol x 12001,694 KJ/Kmol

= 23498344,710 KJ x 0,239 Kkal/KJ

= 5616104,387 Kkal


= 0,669 Kmol x 0,969 KJ/Kmol °K x ( 455 –

298 ) °K

= 101,777 KJ x 0,239 Kkal/KJ

= 24,325 Kkal

Aliran Umpan CO2

T = 447,8°K

CpdT CO2 = 27,437(447,8 - 298) + 4,23E-02/2 (447,82 - 2982) +

-1,96E-05/3 (447,83 - 2983) + 4,00E-09/4 (447,84-2984) +

-2,99E-13/5 (447,85-2985)

= 6090,581 KJ/Kmol




= 935,364 Kmol x 6090,581 KJ/Kmol

= 5696910,206 KJ x 0,239 Kkal/KJ

= 1361561,539 Kkal

Aliran produk ke HP Decomposer

T = 444°K

CpdT Urea = 965,507 (444 - 298) + -5,10E+00/2 (4442 - 2982)+

1,00E-02/3 (4443 - 2983) + -6,38E-06/4 (4444-2984)

= 18859,288 KJ/Kmol


= 1225,444 Kmol x 18859,288 KJ/Kmol

= 23111001,320 KJ x 0,239 Kkal/KJ

= 5523529,316 Kkal

CpdT NH3 = -182,157 (444 - 298) + 3,36E+00/2 (4442 - 2982) +

-1,44E-02/3 (4443 - 2983) + 2,04E-05/4 (4444 - 2984)

= 20271,742 KJ/Kmol


= 1129,735 Kmol x 20271,742 KJ/Kmol



= 22901696,450 KJ x 0,239 Kkal/KJ

= 5473505,451 Kkal

CpdT CO2 = -3981,02 (444 - 298) + 5,25E+01/2 (4442 - 2982) +

-2,27E-01/3 (4443 - 2983) + 3,29E-04/4 (4444-2984)

= 189730,002 KJ/Kmol


= 149,431 Kmol x 189730,002 KJ/Kmol

= 28351506,380 KJ x 0,239 Kkal/KJ

= 9327645,600 Kkal

CpdT H2O = 92,053(455 - 298) + -4,00E-02/2 (455

2

- 298

2

)+

-2,11E-04/3 (4553 - 2983) + 5,35E-07/4 (4554-2984)

= 11121,308 KJ/Kmol


= 2066,016 Kmol x 11121,308 KJ/Kmol

= 22976800,270 KJ x 0,239 Kkal/KJ

= 5491455,264 Kkal


= 3,040 Kmol x 0,969 KJ/Kmol °K x ( 444 – 298 ) °K



= 430,081 KJ x 0,239 Kkal/ 1KJ

= 102,789 Kkal

Aliran gas ke Carbamat Condenser

T = 457°K

CpdT NH3 = 33,573(457 - 298) + -1,26E-02/2 (4572 - 2982) +

8,89E-05/3 (457,63 - 2983) + -7,18E-08/4 (457,64-2984) +

1,86E-11/5 (4575-2985)

= 6049,968 KJ/Kmol x 1 Kmol/17kg

= 355,880 KJ/kg

QF NH3 = 54661,080 Kg x 355,880 KJ/kg

= 19452785,150 KJ x 0,239 Kkal/KJ

= 4649215,651 Kkal

CpdT CO2 = 27,437 (457 - 298) + 4,23E-02/2 (4572 - 2982) +

-1,96E-05/3 (4573 - 2983) + 4,00E-09/4 (4574-2984) +

-2,99E-13/5 (4575-2985)


= 147,396 KJ/kg

QF CO2 = 45860,435 kg x 147,396 KJ/kg

= 6759644,677 KJ x 0,239 Kkal/KJ



= 1615555,078 Kkal

CpdT H2O = 33,933 (457 - 298) + -8,42E-03/2 (4572 - 2982) +

2,99E-05/3 (4573 - 2983) + -1,78E-08/4 (4574-2984) +

3,69E-12/5 (4575-2985)


= 301,746 KJ/kg

QF H2O = 5001,805 kg x 301,746 KJ/kg

= 1509274,652 KJ x 0,239 Kkal/KJ

= 360716,642 Kkal



Neraca Panas Pada Stripper

Komponen Input (Kkal) Output (Kkal) Aliran produk dari reactor

Urea

NH3

CO2

H2O

Biuret

4193841,44924188669,570

1481513,5105616104,387

24,325

Aliran umpan segar CO2

CO2 1361561,539

Aliran produk ke DA 201

Urea NH3

CO2

H2O

Biuret

5523529,3165473505,4519327645,6005491455,264

102,789

Aliran gas ke EA 101

NH3

CO2

H2O

Panas yang hilang

4649215,6511615555,078360716,642

4399999,999

Total 36841725,790 36841725,790



3. Carbamat Condenser (EA – 101)

Carbamat

Condenser

EA - 101

HPD (DA - 201) :NH3 = .......... ?

CO2 = .......... ?

H2O = .......... ?

10

8

Ammonia Reservoir ( FA – 104 ) :

NH3 = 5751,379 Kkal

Carbamat ejector

(EE - 101) :Urea = ............... ?

NH3 =…………. ?CO2 =………….. ?

H2O =………….. ?

Biuret = ............. ?

Atmosfer :

NH3 =……... ?H2O =……... ?

Stripper (DA - 101) :

NH3 = 469215,651 KkalCO2 = 1615555,07 Kkal

H2O = 360716,642 Kkal

27

11

CFP (GA - 102A,B) :

Urea = 11349,560 Kkal

NH3 = 2445566,824 Kkal

C2O = 6359426,752 KkalH2O = 1221176,277 Kkal

9

Suhu masuk pada aliran gas dari stripper = 184oC

Suhu masuk pada aliran ammonia reservoir = 30oC

Suhu masuk pada aliran carbamate feed pump = 105oC

Suhu keluar pada aliran produk ke carbamate ejector = 180oC

Suhu keluar pada aliran gas ke HPD = 104oC

Suhu keluar pada aliran gas ke atmosfer = 40°C



Aliran gas dari stripper

T = 457°K

CpdT NH3 = 33,573 (457 - 298) + -1,26E-02/2 (4572 - 2982) +

8,89E-05/3 (457,63 - 2983) + -7,18E-08/4 (457,64-2984) +

1,86E-11/5 (4575-2985)


= 355,880 KJ/kg

QF NH3 = 54661,080 Kg x 355,880 KJ/kg

= 19452785,150 KJ x 0,239 Kkal/KJ

= 4649215,651 Kkal

CpdT CO2 = 27,437 (457 - 298) + 4,23E-02/2 (4572 - 2982) +

-1,96E-05/3 (4573 - 2983) + 4,00E-09/4 (4574-2984) +

-2,99E-13/5 (4575-2985)


= 147,396 KJ/kg

QF CO2 = 45860,435 kg x 147,396 KJ/kg

= 6759644,677 KJ x 0,239 Kkal/KJ

= 1615555,078 Kkal



CpdT H2O = 33,933(457 - 298) + -8,42E-03/2 (4572 - 2982) +

2,99E-05/3 (4573 - 2983) + -1,78E-08/4 (4574-2984) +

3,69E-12/5 (4575-2985)

= 5431,432 KJ/Kmol x 1Kmol/18kg

= 301,746 KJ/kg

QF H2O = 5001,805 kg x 301,746KJ/kg

= 1509274,652 KJ x 0,239Kkal/KJ

= 360716,642 Kkal

Aliran dari ammonia reservoir

T = 303°K

CpdT NH3 = -182,157 (303 - 298) + 3,36E+00/2 (3032 - 2982) +

-1,44E-02/3 (3033 - 2983) + 2,04E-05/4 (3034 - 2984)

= 403,832 KJ/Kmol


= 59,590 Kmol x 403,832 KJ/Kmol

= 24064,349 KJ x 0,239 Kkal/KJ

= 5751,379 Kkal



Aliran masuk dari carbamate feed pump

T = 378°K

CpdT Urea = 965,507 (378 - 298) + -5,10E+00/2 (3782 - 2982)+

1,00E-02/3 (3783 - 2983) + -6,38E-06/4 (3784-2984)

= 11173,576 KJ/Kmol


= 4,25 Kmol x 11173,576 KJ/Kmol

=47487,698 KJ x 0,239 kkal/KJ

= 11349,560 Kkal

CpdT NH3 = -182,157 (378 - 298) + 3,36E+00/2 (3782 - 2982) +

-1,44E-02/3 (3783 - 2983) + 2,04E-05/4 (3784 - 2984)

= 7959,756 KJ/Kmol


= 1285,529 Kmol x 7959,756 KJ/Kmol

= 10232497,170 KJ x 0,239 Kkal/KJ

= 2445566,824 Kkal

CpdT CO2 = -3981,02 (378 - 298) + 5,25E+01/2 (3782 - 2982) +

-2,27E-01/3 (3783 - 2983) + 3,29E-04/4 (3784-2984)



= 47328,786 KJ/Kmol

QF CO2 = n x CpdT CP2

= 562,205 Kmol x 47328,786 KJ/Kmol

= 26608480,130 KJ x 0,239 Kkal/KJ

= 6359426,752 Kkal

CpdT H2O = 92,053 (378 - 298) + -4,00E-02/2 (3782 - 2982)+

-2,11E-04/3 (3783 - 2983) + 5,35E-07/4 (3784-2984)

= 6021,044 KJ/Kmol


= 848,611 Kmol x 6021,044 KJ/Kmol

= 5109524,170 KJ x 0,239 Kkal/KJ

= 1221176,277 Kkal

Aliran keluar produk ke carbamate ejector

T = 453°K

CpdT Urea = 965,507 (453 - 298) + -5,10E+00/2 (4532 - 2982)+

1,00E-02/3 (4533 - 2983) + -6,38E-06/4 (4534-2984)

= 19886,241 KJ/Kmol




= 719,366 Kmol x 19886,241 KJ/Kmol

= 14405465,640 KJ x 0,239 kkal/KJ

= 3419011,069 Kkal

CpdT NH3 = -182,157 (453 - 298) + 3,36E+00/2 (4532 - 2982) +

-1,44E-02/3 (4533 - 2983) + 2,04E-05/4 (4534 - 2984)

= 22690,232 KJ/Kmol


= 3484,330 Kmol x 22690,232 KJ/Kmol

= 79060253,970 KJ x 0,239 Kkal/KJ

= 18895400,700 Kkal

CpdT CO2 = -3981,02 (453 - 298) + 5,25E+01/2 (453 - 2982) +

-2,27E-01/3 (4533 - 2983) + 3,29E-04/4 (4534-2984)

= 189730,002 KJ/Kmol


= 84,878 Kmol x 222008,025 KJ/Kmol

= 18843730,300 KJ x 0,239 Kkal/KJ

= 45036515,540 Kkal



CpdT H2O = 92,053 (453 - 298) + -4,00E-02/2 (4532 - 2982)+

-2,11E-04/3 (4533 - 2983) + 5,35E-07/4 (4534-2984)

= 11840,762 KJ/Kmol


= 1731,603 Kmol x 11840,762KJ/Kmol

= 20503449 KJ x 0,239 Kkal/KJ

= 4900336,261 Kkal


= 0,824 Kmol x 0,969 KJ/Kmol °K x ( 453 – 298 ) °K

= 123,761 KJ x 0,239 Kkal/KJ

= 29,579 Kkal

Aliran gas keluar ke HPD

T = 377°K

CpdT NH3 = 33,573 (377 - 298) + -1,26E-02/2 (3772 - 2982) + 8,89E-

05/3 (3773 - 2983) + -7,18E-08/4 (3774-2984) + 1,86E-11/5

(3775-2985)


= 171,676 KJ/kg

QF NH3 = 319 Kg x 171,676 KJ/kg



= 54764,644 KJ x 0,239Kkal/KJ

= 13088,750 Kkal

CpdT CO2 = 27,437 (377 - 298) + 4,23E-02/2 (3772 - 2982) +

-1,96E-05/3 (3773 - 2983) + 4,00E-09/4 (3774-2984) +

-2,99E-13/5 (3775-2985)


= 71,140 KJ/kg

QF CO2 = 437 kg x 71,140 KJ/kg

= 31088,18 KJ x 0,239 Kkal/KJ

= 7430,075 Kkal

CpdT H2O = 33,933 (377 - 298) + -8,42E-03/2 (3772 - 2982) + 2,99E-

05/3 (3773 - 2983) + -1,78E-08/4 (3774-2984) + 3,69E-12/5

(3775-2985)


= 2675,582 KJ/kg

QF H2O = 36 kg x 2675,582 KJ/kg

= 96320,952 KJ x 0,239 Kkal/KJ

= 23020,708 Kkal



Aliran gas keluar ke atmosfer

T = 313°K

CpdT NH3 = 33,573 (313 - 298) + -1,26E-02/2 (3132 - 2982) + 8,89E-

05/3 (3133 - 2983) + -7,18E-08/4 (3134-2984) + 1,86E-11/5

(3135-2985)


= 31,884 KJ/kg

QF NH3 = 1258,083 Kg x 31,884 KJ/kg

= 40112,718 KJ x 0,239 Kkal/KJ

= 9586,940 Kkal

CpdT CO2 = 27,437 (313 - 298) + 4,23E-02/2 (3132

- 2982

) +

-1,96E-05/3 (3133 - 2983) + 4,00E-09/4 (3134-2984) +

-2,99E-13/5 (3135-2985)


= 13,173 KJ/kg

QF CO2 = 1723,890 Kg x 13,173 KJ/kg

= 22708,803 KJ x 0,239 Kkal/KJ

= 5427,404 Kkal



CpdT H2O = 33,933 (313 - 298) + -8,42E-03/2 (3132 - 2982) + 2,99E-

05/3 (3133

- 2983

) + -1,78E-08/4 (3134

-2984

) + 3,69E-12/5

(3135-2985)


= 28,064 KJ/kg

QF H2O = 142,147 kg x 28,064 KJ/kg

= 3989,213 KJ x 0,239 Kkal/KJ

= 953,422 Kkal



Neraca Panas Pada Carbamat Condenser

Komponen Input (Kkal) Output (Kkal) Aliran gas dari stripper

NH3

CO2

H2O

4649215,6511615555,078360716,642

Aliran masuk dari ammoniareservoir

NH3 5751,379

Aliran produk daricarbamate feed pump

Urea NH3

CO2

H2O

11349,560 2445566,8246359426,7521221176,277

Aliran keluar produk kecarbamat ejector

Urea

NH3

CO2 – H2O –

Biuret

3419011,0691889540,7004503651,5404900336,261

29,579

Aliran gas keluar ke HPD

NH3

CO2

H2O

Aliran gas keluar keatmosfer

NH3

CO2

H2O

Panas yang hilang

13088,7507430,075

23020,708

9586,9405427,404953,422

996681,712

Total 16668758,160 16668758,160



4. HP Decomposer (DA-201)

HPD

DA - 201

Carbamat Condenser

(EA - 101) :NH3 = 13088,750 Kkal

CO2 = 7430,076 KkalH2O = 23020,708 Kkal

Stripper (DA - 101) :Urea = 5523529,316 Kkal

NH3 = 5473505,451 Kkal

CO2 = 9327645,600 Kkal

H2O = 5491455,264 Kkal


13

10

14

15

LPD (DA – 202) :Urea = .............. ?

NH3 = .............. ?

CO2 = .............. ?

H2O = .............. ?Biuret = ............. ?

HPA Lower (EA – 401B) :NH3 = .............. ?

CO2 = .............. ?

H2O = .............. ?

Suhu masuk pada aliran gas dari carbamat condenser = 104 oC

Suhu masuk pada aliran produk dari stripper = 171oC

Suhu keluar pada aliran produk ke LPD = 152

o

C

Suhu keluar pada aliran gas ke HPA Lower = 133oC

Aliran produk dari carbamat condenser

T = 377°K

CpdT NH3 = 33,573 (377 - 298) + -1,26E-02/2 (3772 - 2982) + 8,89E-

05/3 (3773 - 2983) + -7,18E-08/4 (3774-2984) + 1,86E-11/5

(3775-2985)


= 171,676 KJ/kg



QF NH3 = 319 Kg x 171,676 KJ/kg

= 54764,644 KJ x 0,239 Kkal/KJ

= 13088,750 Kkal

CpdT CO2 = 27,437 (377 - 298) + 4,23E-02/2 (3772 - 2982) +

-1,96E-05/3 (3773 - 2983) + 4,00E-09/4 (3774-2984) +

-2,99E-13/5 (3775-2985)


= 71,140 KJ/kg

QF CO2 = 437 Kg x 71,140 KJ/kg

= 31088,180 KJ x 0,239 Kkal/KJ

= 7430,075 Kkal

CpdT H2O = 33,933 (377 - 298) + -8,42E-03/2 (3772 - 2982) + 2,99E-

05/3 (3773 - 2983) + -1,78E-08/4 (3774-2984) + 3,69E-12/5

(3775-2985)


= 2675,582 KJ/kg

QF H2O = 36 Kg x 2675,582 KJ/kg

= 96320,952 KJ x 0,239 Kkal/KJ

= 23020,708 Kkal



Aliran produk dari stripper

T = 444°K

CpdT Urea = 965,507 (444 - 298) + -5,10E+00/2 (4442 - 2982)+

1,00E-02/3 (4443 - 2983) + -6,38E-06/4 (4444-2984)

= 18859,288 KJ/Kmol


= 1225,444 Kmol x 18859,288 KJ/Kmol

= 23111001,32 KJ x 0,239 Kkal/KJ

= 5523529,316 Kkal

CpdT NH3 = -182,157 (444 - 298) + 3,36E+00/2 (444

2

- 298

2

) +

-1,44E-02/3 (4443 - 2983) + 2,04E-05/4 (4444 - 2984)

= 20271,742 KJ/Kmol


= 1129,735 Kmol x 20271,742 KJ/Kmol

= 22901696,450 KJ x 0,239 Kkal/KJ

= 5473505,451 Kkal

CpdT CO2 = -3981,02 (444 - 298) + 5,25E+01/2 (4442 - 2982) + -

2,27E-01/3 (4443 - 2983) + 3,29E-04/4 (4444-2984)



= 189730,002 KJ/Kmol


= 149,431 Kmol x 189730,002 KJ/Kmol

= 28351506,380 KJ x 0,239 Kkal/KJ

= 9327645,600 Kkal

CpdT H2O = 92,053 (455 - 298) + -4,00E-02/2 (4552 - 2982)+

-2,11E-04/3 (4553 - 2983) + 5,35E-07/4 (4554-2984)

= 11121,308 KJ/Kmol


= 2066,016 Kmol x 11121,308 KJ/Kmol

= 22976800,270 KJ x 0,239 Kkal/KJ

= 5491455,264 Kkal


= 3,040 Kmol x 0,969 KJ/Kmol °K x ( 444 – 298 ) °K

= 430,081 KJ x 0,239 Kkal/KJ

= 102,789 Kkal



Aliran produk ke LPD

T = 425°K

CpdT Urea = 965,507 (425 - 298) + -5,10E+00/2 (4252 - 2982)+

1,00E-02/3 (4253 - 2983) + -6,38E-06/4 (4254-2984)

= 16690,194 KJ/Kmol


= 2215,527 Kmol x 16690,194 KJ/Kmol

= 36977567,970 KJ x 0,239 Kkal/KJ

= 8837638,745 Kkal

CpdT NH3 = -182,157 (425 - 298) + 3,36E+00/2 (425

2

- 298

2

) +

-1,44E-02/3 (4253 - 2983) + 2,04E-05/4 (4254 - 2984)

= 15845,708 KJ/Kmol


= 552,667 Kmol x 15845,708 KJ/Kmol

= 8757399,903 KJ x 0,239 Kkal/KJ

= 2093018,577 Kkal

CpdT CO2 = -3981,02 (425 - 298) + 5,25E+01/2 (4252 - 2982) +

-2,27E-01/3 (4253 - 2983) + 3,29E-04/4 (4254-2984)



= 133327,054 KJ/Kmol


= 121,362 Kmol x 133327,054 KJ/Kmol

= 16180868,740 KJ x 0,239 Kkal/KJ

= 3867227,628 Kkal

CpdT H2O = 92,053 (425 - 298) + -4,00E-02/2 (4252 - 2982)+

-2,11E-04/3 (4253 - 2983) + 5,35E-07/4 (4254-2984)

= 9625,275 KJ/Kmol


= 2357,758 Kmol x 9625,275 KJ/Kmol

= 22694072,130 KJ x 0,239 Kkal/KJ

= 5423883,240 Kkal


= 3,260 Kmol x 0,969 KJ/Kmol °K x ( 425 – 298 ) °K

= 401,185 KJ x 0,239 Kkal/KJ

= 95,883 Kkal



Aliran gas ke HPA Lower

T = 406°K

CpdT NH3 = 33,573 (406 - 298) + -1,26E-02/2 (4062 - 2982) + 8,89E-

05/3 (4063 - 2983) + -7,18E-08/4 (4064-2984) + 1,86E-11/5

(4065-2985)

= 4031,975 KJ/Kmol


= 1139,876 Kmol x 4031,975 KJ/Kmol

= 4595951,038 KJ x 0,239 Kkal/KJ

= 1098432,298 Kkal

CpdT CO2 = 27,437 (406 - 298) + 4,23E-02/2 (4062 - 2982) +

-1,96E-05/3 (4063 - 2983) + 4,00E-09/4 (4064-2984) +

-2,99E-13/5 (4065-2985)

= 4325,701 KJ/Kmol


= 1328,217 Kmol x 4325,701 KJ/Kmol

= 5745470,845 KJ x 0,239 Kkal/KJ

= 1373167,532 Kkal



CpdT H2O = 33,933 (406 - 298) + -8,42E-03/2 (4062 - 2982) + 2,99E-

05/3 (4063

- 2983

) + -1,78E-08/4 (4064

-2984

) + 3,69E-12/5

(4065-2985)

= 3668,509 KJ/Kmol


= 931,156 Kmol x 3668,509 KJ/Kmol

= 3415952,908 KJ x 0,239 Kkal/KJ

= 816412,745 Kkal



Neraca Panas Pada HP Decomposer

Komponen Input (Kkal) Output (Kkal) Aliran gas dari carbamatcondenser

NH3

CO2

H2O

13088,7507430,075

23020,708

Aliran produk dari stripper

Urea

NH3

CO2

H2O

Biuret

5523529,3165473505,4519327645,6005491455,264

102,789

Aliran produk ke LPD

Urea

NH3

CO2

H2O

Biuret

8837638,7452093018,5573867227,6285423883,240

95,883

Aliran gas ke recovery

NH3

CO2 H2O

Panas yang hilang

1098432,298

1373167,532816412,745

2349891,320

Total 25859767,950 25859767,320



5. LP Decomposer (DA-202)

LPD

DA - 202

LPA (EA - 402) :

NH3 =…………?

CO2 =…………?

H2O =…………?

Flash Separator (FA - 205) :Urea =…………?

NH3 =…………?

CO2 =……...…?

H2O =………...?

Biuret =………..?

18

HPD ( DA - 201) :Urea = 8837638,745 Kkal

NH3 = 2093018,577 Kkal

CO2 = 3867227,628 Kkal

H2O = 5423883,240 Kkal

Biuret =95,883 Kkal

PCTH2O = 8109,234 Kkal

10

14

17

CO2 Compressor CO2 = 61656,914 Kkal

16

Suhu masuk pada aliran dari PCT = 40

o

C

Suhu masuk pada aliran produk dari HPD = 152oC

Suhu masuk pada aliran gas dari CO2 compressor = 144°C

Suhu keluar pada aliran produk ke Flash Separator = 129oC

Suhu keluar pada aliran gas ke LPA = 114oC

Aliran dari PCT

T = 313°K

CpdT H2O = 92,053 (313 - 298) + -4,00E-02/2 (3132 - 2982)+



-2,11E-04/3 (3133 - 2983) + 5,35E-07/4 (3134-2984)

= 1130,995 KJ/Kmol


= 30 Kmol x 1130,995 KJ/Kmol

= 33929,850 KJ x 0,239 Kkal/KJ

= 8109,234 Kkal

Aliran produk dari HPD

T = 425°K

CpdT Urea = 965,507 (425 - 298) + -5,10E+00/2 (4252 - 2982)+

1,00E-02/3 (425

3

- 298

3

) + -6,38E-06/4 (425

4

-298

4

)

= 16690,194 KJ/Kmol


= 2215,527 Kmol x 16690,194 KJ/Kmol

= 36977567,970 KJ x 0,239 Kkal/KJ

= 8837638,745 Kkal

CpdT NH3 = -182,157 (425 - 298) + 3,36E+00/2 (4252 - 2982) +

-1,44E-02/3 (4253 - 2983) + 2,04E-05/4 (4254 - 2984)

= 15845,708 KJ/Kmol




= 552,667 Kmol x 15845,708 KJ/Kmol

= 8757399,903 KJ x 0,239 Kkal/KJ

= 2093018,577 Kkal

CpdT CO2 = -3981,02 (425 - 298) + 5,25E+01/2 (4252 - 2982) +

-2,27E-01/3 (4253 - 2983) + 3,29E-04/4 (4254-2984)

= 133327,054 KJ/Kmol


= 121,362 Kmol x 133327,054 KJ/Kmol

= 16180868,740 KJ x 0,239 Kkal/KJ

= 3867227,628 Kkal

CpdT H2O = 92,053 (425 - 298) + -4,00E-02/2 (4252 - 2982)+

-2,11E-04/3 (4253 - 2983) + 5,35E-07/4 (4254-2984)

= 9625,275 KJ/Kmol


= 2357,758 Kmol x 9625,275 KJ/Kmol

= 22694072,130 KJ x 0,239 Kkal/KJ

= 5423883,240 Kkal




= 3,260 Kmol x 0,969 KJ/Kmol °K x ( 425 – 298 ) °K

= 401,185 KJ x 0,239 Kkal/KJ

= 95,883 Kkal

Aliran gas dari CO2 compressor

T = 417°K

CpdT CO2 = 27,437 (417 - 298) + 4,23E-02/2 (4172 - 2982) +

-1,96E-05/3 (4173 - 2983) + 4,00E-09/4 (4174-2984) +

-2,99E-13/5 (4175-2985)

= 4785,441 KJ/Kmol x 1Kmol/44 kg

= 108,760 KJ/Kg

QF CO2 = 2372 Kg x 108,760 KJ/Kg

= 257978,720 KJx 0,239 Kkal/KJ

= 61656,914 Kkal

Aliran produk ke Flash Separator

T = 402°K

CpdT Urea = 965,507 (402 - 298) + -5,10E+00/2 (4022 - 2982)+

1,00E-02/3 (4023 - 2983) + -6,38E-06/4 (4024-2984)



= 14033,739 KJ/Kmol X 1Kmol/60 kg

= 233,896 KJ/Kg


= 65746,450 Kg x 233,896 KJ/Kmol

= 15377831,67 KJ x 0,239Kkal/KJ

= 3675301,769 Kkal

CpdT NH3 = -182,157 (402 - 298) + 3,36E+00/2 (4022 - 2982) +

-1,44E-02/3 (4023 - 2983) + 2,04E-05/4 (4024-2984)

= 11525,317 KJ/Kmol x 1Kmol/ 17kg

= 677,960 KJ/Kg


= 761,424 Kg x 677,960 KJ/Kmol

= 516215,015 KJ x 0,239 Kkal/KJ

= 123375,389 Kkal

CpdT CO2 = -3981,02 (402 - 298) + 5,25E+01/2 (4022 - 2982) +

-2,27E-01/3 (4023 - 2983) + 3,29E-04/4 (4024-2984)

= 83108,265 KJ/Kmol x 1 Kmol/44kg

= 1888,824 KJ/Kg



QF CO2 = n x CpdTCO2

=436,551 kg x 1888,824 KJ/Kg

=824568,006 KJ x 0,239 Kkal/KJ

= 197071,753 Kkal

CpdT H2O = 92,053 (402 - 298) + -4,00E-02/2 (4022 - 2982)+

-2,11E-04/3 (4023 - 2983) + 5,35E-07/4 (4024-2984)


= 435,990 KJ/kg


= 34253,941 Kg x 435,990 KJ/kg

= 14934375,74 KJ x 0,239 Kkal/KJ

= 3569315,801 Kkal

QF Biuret = n x CpdT

= 3,124 Kmol x 0,969 KJ/Kmol K x (402 – 298) °K

= 314.824 KJ x 0,239 Kkal/KJ

= 75,243 Kkal



Aliran gas ke LPA

T = 387°K

CpdT NH3 = 33,573 (387 - 298) + -1,26E-02/2 (3872 - 2982) + 8,89E-

05/3 (3873 - 2983) + -7,18E-08/4 (3874-2984) + 1,86E-11/5

(3875-2985)

= 3299,753 KJ/Kmol


= 612,044 Kmol x 3299,753 KJ/Kmol

= 2019594,025 KJ x 0,239 Kkal/KJ

= 482682,972 Kkal

CpdT CO2 = 27,437 (387 - 298) + 4,23E-02/2 (3872 - 2982) +

-1,96E-05/3 (3873 - 2983) + 4,00E-09/4 (3874-2984) +

-2,99E-13/5 (3875-2985)

= 3539,688 KJ/Kmol


= 167,705 Kmol x 3539,688 KJ/Kmol

= 593623,376 KJ x 0,239 Kkal/1KJ

= 141875,987 Kkal



CpdT H2O = 33,933 (387 - 298) + -8,42E-03/2 (3872 - 2982) + 2,99E-

05/3 (3873

- 2983

) + -1,78E-08/4 (3874

-2984

) + 3,69E-12/5

(3875-2985)

= 3017,243 KJ/Kmol


= 259,944 Kmol x 3017,243 KJ/Kmol

= 784314,214 KJ x 0,239 Kkal/KJ

= 187451,097 Kkal



Neraca Panas Pada LP Decomposer

Komponen Input (Kkal) Output (Kkal) Aliran dari PCT

H2O

Aliran produk dari HPD

Urea

NH3

CO2

H2O

Biuret

8109,234

8837638,7452093018,5573867227,6285423883,240

95,883

Aliran gas dari CO2 compressor

CO2 61656,914

Aliran ke flash separator

Urea

NH3

CO2

H2O

Biuret

Aliran gas ke LPA

NH3 CO2

H2O

Panas yang hilang

3675301,769123375,389197071,753

3569315,80175,243

482682,972141875,987187451,097

11914480,190

Total 20291630,200 20291630,200



6. FlashSeparator ( FA-205)

FlashSeparator

FA-205

Flash GasCondenser (EA -506) :NH3 =…………?

CO2 =…………?

H2O = …………?

19

LPD (DA- 202) :Urea = 3675301,769 Kkal

NH3 = 123375,389 Kkal

CO2 = 197071,753 Kkal

H2O = 1569315,801 Kkal


Urea Solution tank(FA-201) :

Urea = .......?NH3 = .......?

CO2 = .......?

H2O = .......?

Biuret = .....?

17

20

Suhu masuk pada aliran produk dari LPD = 129 oC

Suhu keluar pada aliran gas ke Flash Gas Condenser = 96o

C

Suhu keluar pada aliran produk ke Urea Solution Tank = 96 oC

Aliran Produk dari LPD

T = 402°K

CpdT Urea = 965,507 (402 - 298) + -5,10E+00/2 (4022 - 2982)+

1,00E-02/3 (4023 - 2983) + -6,38E-06/4 (4024-2984)

= 14033,739 KJ/Kmol X 1 Kmol/60 kg

= 233,896 KJ/Kg




= 65746,450 Kg x 233,896 KJ/Kmol

= 15377831,670 KJ x 0,239 Kkal/KJ

= 3675301,769 Kkal

CpdT NH3 = -182,157 (402 - 298) + 3,36E+00/2 (4022 - 2982) +

-1,44E-02/3 (4023 - 2983) + 2,04E-05/4 (4024-2984)

= 11525,317 KJ/Kmol x 1 Kmol/17kg

= 677,960 KJ/Kg


= 761,424 Kg x 677,960 KJ/Kmol

= 516215,015 KJ x 0,239 Kkal/KJ

= 123375,389 Kkal

CpdT CO2 = -3981,02 (402 - 298) + 5,25E+01/2 (4022 - 2982) +

-2,27E-01/3 (4023 - 2983) + 3,29E-04/4 (4024-2984)

= 83108,265 KJ/Kmol x 1 Kmol/44kg

= 1888,824 KJ/Kg


=436,551 kg x 1888,824 KJ/Kg



=824568,006 KJ x 0,239 Kkal/KJ

= 197071,753 Kkal

CpdT H2O = 92,053 (402 - 298) + -4,00E-02/2 (4022 - 2982)+

-2,11E-04/3 (4023 - 2983) + 5,35E-07/4 (4024-2984)


= 435,990 KJ/kg


= 34253,941 kg x 435,990 KJ/kg

= 14934375,740 KJ x 0,239 Kkal/KJ

= 1569315,801 Kkal


= 3,124 Kmol x 0,969 KJ/Kmol K x (402 – 298) °K

= 314.824 KJ x 0,239 Kkal/KJ

= 75,243 Kkal

Aliran gas ke Flash Gas Condenser

T = 369°K

CpdT NH3 = 33,573 (369 - 298) + -1,26E-02/2 (3692 - 2982) + 8,89E-

05/3 (3693 - 2983) + -7,18E-08/4 (3694-2984) + 1,86E-11/5

(3695

-2985

)




= 153,852 KJ/kg


= 228,793 kg x 153,852 KJ/kg

= 35200,261 KJ x 0,239 Kkal/KJ

= 8412,862 Kkal

CpdT CO2 = 27,437 (369 - 298) + 4,23E-02/2 (3692 - 2982) +

-1,96E-05/3 (3693 - 2983) + 4,00E-09/4 (3694-2984) +

-2,99E-13/5 (3695-2985)


= 63,742 KJ/kg


=130,247 kg x 63,742 KJ/kg

= 8302,204 KJ x 0,239 Kkal/KJ

= 1984,227 Kkal

CpdT H2O = 33,933 (369 - 298) + -8,42E-03/2 (3692 - 2982) + 2,99E-

05/3 (3693 - 2983) + -1,78E-08/4 (3694-2984) + 3,69E-12/5

(3695-2985)




= 133,488 KJ/kg


= 3928,584 kg x 133,488 KJ/kg

= 524418,821 KJ x 0,239 Kkal/KJ

= 125336,098 Kkal

Aliran produk ke Urea Solution Tank

T = 369°K

CpdT Urea = 965,507 (369 - 298) + -5,10E+00/2 (3692 - 2982)+

1,00E-02/3 (3693 - 2983) + -6,38E-06/4 (3694-2984)

= 10064,104 KJ/Kmol x 1 Kmol/60kg

= 167,735 KJ/kg


= 65746,450 kg x 167,735 KJ/kg

= 11027980,790 KJ x 0,239 Kkal/KJ

= 2635687,409 Kkal

CpdT NH3 = -182,157 (369 -298) + 3,36E+00/2 (3692 - 2982) +

-1,44E-02/3 (3693 - 2983) + 2,04E-05/4 (3694-2984)




= 401,012 KJ/kg


= 532,631 kg x 401,012 KJ/kg

= 213591,022 KJ x 0,239 Kkal/KJ

= 51048,254 Kkal

CpdT CO2 = -3981,02(369 - 298) + 5,25E+01/2 (3692 - 2982) +

-2,27E-01/3 (3693 - 2983) + 3,29E-04/4 (3694-2984)

= 37393,496 KJ/Kmol x 1 Kmol/44kg

= 849,852 KJ/kg


= 306,304 kg x 849,852 KJ/kg

=260313,067 KJ x 0,239 Kkal/KJ

= 62214,823 Kkal

CpdT H2O = 92,053(369 - 298) + -4,00E-02/2 (3692 - 2982)+

-2,11E-04/3 (3693 - 2983) + 5,35E-07/4(3694-2984)


= 296,724 KJ/kg




= 30325,357 kg x 296,724 KJ/kg

= 8998261,230 KJ x 0,239 Kkal/KJ

= 2150584,434 Kkal


= 3,124 Kmol x 0,969 KJ/Kmol K x (369 – 298) K

= 214,928 KJ x 0,239 Kkal/KJ

= 51,368 Kkal

Neraca Panas Pada Flash Separator


Aliran produk dari LPD Urea

NH3

CO2

H2O

Biuret

Aliran gas ke FlashGas Condenser

NH3

CO2

H2O

3675301,769123375,389197071,753

1569315,80175,243

8412,8621984,227

125336,098

Aliran produk ke UreaSolution Tank

Urea

NH3

CO2

H2O

Biuret

Panas yang hilang

2635687,40951048,25462214,823

2150584,43451,368

529820,480

Total 5565139,955 5565139,955



7. Vacuum Concentrator Lower (FA 202 B)

VacuumConcentrator Lower

(FA-202B)

Aliran dari Recovery

Urea = 2419093,284 Kkal

H2O = 800118,257 Kkal


UST(FA-201) :Urea = 2635687,409 Kkal

NH3 = 51048,254 Kkal

CO2 = 62214,823 Kkal

H2O = 2150584,434 Kkal


Heater (EA-201) :Urea = .......?

H2O = .......?

Biuret = .......?

20

21

Aliran menuju PCT :

Urea = ..........?

NH3 = ..........?

CO2 = ..........?

H2O = ...........?

22

23

Suhu masuk pada aliran produk dari Urea Solution Tank = 96oC

Suhu masuk aliran produk dari recovery = 83°C

Suhu keluar pada aliran produk ke Heater = 96

o

C

Suhu keluar pada aliran gas ke PCT = 132oC

Aliran produk dari Urea Solution Tank

T = 369°K

CpdT Urea = 965,507 (369 - 298) + -5,10E+00/2 (3692 - 2982)+

1,00E-02/3 (3693 - 2983) + -6,38E-06/4 (3694-2984)

= 10064,104 KJ/Kmol x 1 Kmol/60kg

= 167,735 KJ/kg




= 65746,450 kg x 167,735 KJ/kg

= 11027980,790 KJ x 0,239 Kkal/KJ

= 2635687,409 Kkal

CpdT NH3 = -182,157 (369 -298) + 3,36E+00/2 (3692 - 2982) +

-1,44E-02/3 (3693 - 2983) + 2,04E-05/4 (3694-2984)


= 401,012 KJ/kg


= 532,631 kg x 401,012 KJ/kg

= 213591,022 KJ x 0,239 Kkal/KJ

= 51048,254 Kkal

CpdT CO2 = -3981,02 (369 - 298) + 5,25E+01/2 (3692 - 2982) +

-2,27E-01/3 (3693 - 2983) + 3,29E-04/4 (3694-2984)

= 37393,496 KJ/Kmol x 1 Kmol/44kg

= 849,852 KJ/kg


= 306,304 kg x 849,852 KJ/kg



=260313,067 KJ x 0,239 Kkal/KJ

= 62214,823 Kkal

CpdT H2O = 92,053 (369 - 298) + -4,00E-02/2 (3692 - 2982)+

-2,11E-04/3 (3693 - 2983) + 5,35E-07/4 (3694-2984)


= 296,724 KJ/kg


= 30325,357 Kg x 296,724 KJ/kg

= 8998261,230 KJ x 0,239 Kkal/KJ

= 2150584,434 Kkal


= 3,124 Kmol x 0,969 KJ/Kmol K x (369 – 298) K

= 214,928 KJ x 0,239 Kkal/KJ

= 51,368 Kkal

Aliran produk dari recovery

T = 356°K

CpdT Urea = 965,507 (356 - 298) + -5,10E+00/2 (3562 - 2982) +

1,00E- 02/3 (3563 - 2983) + -6,38E-06/4 (3564-2984)



= 8413,717 KJ/Kgmol x 1 Kmol/60kg

= 140,229 KJ/kg

QF Urea = 72180 Kg x 140,229 KJ/kg

= 10121729,220 KJ x 0,239 Kkal/KJ

= 2419093,284 Kkal

CpdT H2O = 92,053 (356 - 298) + -4,00E-02/2 (3562 - 2982)+

-2,11E-04/3 (3563 - 2983) + 5,35E-07/4 (3564-2984)


= 242,329 KJ/kg

QF H2O = n xCpdT H2O

= 13815 Kg x 242,329 KJ/kg

= 3347775,135 KJ x 0,239 Kkal/KJ

= 800118,257 Kkal


= 3,385 kg x 0,969 KJ/Kgmol K x (356 – 298) K

= 190,244 KJ x 0,239 Kkal/KJ

= 45,468 Kkal



Aliran Produk ke Heater

T = 369°K

CpdT Urea = 965,507 (369 - 298) + -5,10E+00/2 (3692 - 2982) +

1,00E-02/3 (3693 - 2983) + -6,38E-06/4 (3694-2984)


= 167,735 KJ/kg

QF Urea = 138788,457 kg x 167,735 KJ/kg

= 23279681,830 KJ x 0,239 Kkal/KJ

= 5563843,959 Kkal

CpdT H2O = 92,053 (369 - 298) + -4,00E-02/2 (369

2

- 298

2

)+

-2,11E-04/3 (3693 - 2983) + 5,35E-07/4 (3694-2984)


= 296,724 KJ/kg


= 24866,264 kg x 296,724 KJ/kg

= 7378417,319 KJ x 0,239 Kkal/KJ

= 1763441,739 Kkal




= 15,093 kg x 0,969 KJ/Kgmol K x (369 – 298) K

= 1038,383 KJ x 0,239 Kkal/1KJ

= 248,174 Kkal

Aliran gas keluar ke PCT

T = 405°K

CpdT Urea = 24,856 (405 - 298) + 1,44E-01/2 (4052 - 2982) +

3,81E-05/3 (4053 - 2983) + -1,10E-07/4(4054-2984) +

3,92E-11/5 (4055-2985)


= 135,451 KJ/kg


= 242,329 kg x 135,451 KJ/kg

= 31469,195 KJ x 0,239 Kkal/KJ

= 7521,138 Kkal

CpdT NH3 = 33,573 (405 - 298) + -1,26E-02/2 (4052 - 2982) +

8,89E-05/3 (4053 - 2983) + -7,18E-08/4(4054-2984) +

1,86E-11/5 (4055-2985)




= 234,893 KJ/kg


= 352,479 kg x 234,893 KJ/kg

= 82794,850 KJ x 0,239 Kkal/KJ

= 19787,969 Kkal

CpdT CO2 = 27,437 (405 - 298) + 4,23E-02/2 (4052 - 2982) +

-1,96E-05/3 (4053 - 2983) + 4,00E-09/4 (4054-2984) +

-2,99E-13/5 (4055-2985)


= 97,365 KJ/kg


= 216,627 kg x 97,365 KJ/kg

= 21091,888 KJ x 0,239 Kkal/KJ

= 5040,961 Kkal

CpdT H2O = 33,933(405 - 298) + -8,42E-03/2 (4052 - 2982) +

2,99E-05/3 (4053 - 2983) + -1,78E-08/4(4054-2984) +

3,69E-12/5 (4055-2985)




= 201,898 Kkal


= 17546,627 kg x 201,898 KJ/kg

= 3542628,898 KJ x 0,239 Kkal/KJ

= 846688,307 Kkal

Neraca Panas Vaccum Concentrator Lower


Aliran produk dari UreaSolution Tank

Urea

NH3

CO2

H2O

Biuret

2635687,40951048,25462214,823

2150584,434

51,368

Aliran produk darirecovery

Urea

H2O

Biuret

2419093,284800118,257

45,468

Aliran produk ke Heater

Urea

H2O Biuret

5563843,9591763441,739

248,174

Aliran gas ke PCT

Urea

NH3

CO2

H2O

Panas yang hilang

7521,13819787,969

5040,961846688,307

150056,227

Total 8356628,474 8356628,474



8. Vacum Concentrator Upper (FA 202 A)

Vacuum

Concentrator Upper

(FA-202A)

Final Separator

(FA-203) :Urea = .......?

H2O = .......?

Biuret = .......?

22

Aliran menuju PCT :

Urea = ..........?

NH3 = ..........?

CO2 = ..........?

H2O = ...........?

25

24

Heater (EA-201) :Urea = 5563843,959 Kkal

H2O = 1763441,739 Kkal


Suhu masuk aliran produk dari Heater = 96°C

Suhu keluar pada aliran produk ke Final separator = 138oC


Aliran Produk dari Heater

T = 369°K

CpdT Urea = 965,507 (369 - 298) + -5,10E+00/2 (3692 - 2982) +

1,00E-02/3 (3693 - 2983) + -6,38E-06/4 (3694-2984)


= 167,735 KJ/kg



QF Urea = 138788,457 kg x 167,735 KJ/kg

= 23279681,830 KJ x 0,239 Kkal/KJ

= 5563843,959 Kkal

CpdT H2O = 92,053 (369 - 298) + -4,00E-02/2 (3692 - 2982)+

-2,11E-04/3 (3693 - 2983) + 5,35E-07/4 (3694-2984)


= 296,724 KJ/kg


= 24866,264 kg x 296,724 KJ/kg

= 7378417,319 KJ x 0,239 Kkal/KJ

= 1763441,739 Kkal


= 15,093 kg x 0,969 KJ/Kgmol K x (369 – 298) K

= 1038,383 KJ x 0,239 Kkal/KJ

= 248,174 Kkal



Aliran Produk ke Final separator

T = 411°K

CpdT Urea = 965,507 (411 - 298) + -5,10E+00/2 (4112 - 2982) +

1,00E-02/3 (4113 - 2983) + -6,38E-06/4 (4114-2984)


= 251,332 KJ/kg

QF Urea = 144984,371 kg x 251,332 KJ/kg

= 36439211,93 KJ x 0,239 Kkal/KJ

= 6108971,652 Kkal

CpdT H2O = 92,053(411 - 298) + -4,00E-02/2 (411

2

- 298

2

) +

-2,11E-04/3 (4113 - 2983) + 5,35E-07/4 (4114-2984)


= 474,423 KJ/kg


= 2780,726 kg x 474,423 KJ/kg

= 1319240,371 KJ x 0,239 Kkal/KJ

= 315298,449 Kkal




= 9,008 kg x 0,969 KJ/Kgmol K x (411 – 298) K

= 986,349 KJ x 0,239 Kkal/KJ

= 235,737 Kkal

Aliran gas keluar ke PCT

T = 405 °K

CpdT Urea = 24,856 (405 - 298) + 1,44E-01/2 (4052 - 2982) +

3,81E-05/3 (4053 - 2983) +-1,10E-07/4 (4054-2984)

+ 3,92E-11/5 (4055-2985)


= 135,451 KJ/kg


= 143,745 kg x 135,451 KJ/kg

= 19470,404 KJ x 0,239 Kkal/KJ

= 4653,427 Kkal

CpdT NH3 = 33,573 (405 - 298) + -1,26E-02/2 (4052 - 2982) +

8,89E-05/3 (4053 - 2983) +-7,18E-08/4 (4054-2984)

+ 1,86E-11/5 (4055-2985)




= 234,893 KJ/kg


= 198,269 kg x 234,893 KJ/kg

= 46572 KJ x 0,239 Kkal/KJ

= 11130,708 Kkal

CpdT CO2 = 27,437(405 - 298) + 4,23E-02/2 (4052 - 2982) +

-1,96E-05/3 (4053 - 2983) +4,00E-09/4 (4054-2984) +

-2,99E-13/5 (4055-2985)


= 97,365 KJ/kg


= 153,659 kg x 97,365 KJ/kg

= 14961,009 KJ x 0,239 Kkal/KJ

= 3575,681 Kkal

CpdT H2O = 33,933 (405 - 298) + -8,42E-03/2 (4052 - 2982) +

2,99E-05/3 (4053 - 2983) +-1,78E-08/4(4054-2984) +

3,69E-12/5 (4055-2985)




= 201,898 Kkal


= 16026,762 kg x 201,898 KJ/kg

= 3235771,194 KJ x 0,239 Kkal/KJ

= 773349,315 Kkal

Neraca Panas Vacum Concentrator Upper


Aliran produk dari Heater

Urea

H2O

Biuret

5563843,9591763441,739

248,174

Aliran produk ke FinalSeparator

Urea

H2O

Biuret

Aliran ke EA 202

Urea

NH3

CO2

H2O

Panas yang hilang

6108971,652315298,449

235,737

4653,42711130,708

3575,681773349,315

110318,903

Total 7327533,872 7327533,872



9. Final Separator (FA 203)

Final Separator

(FA-203)

Prilling Tower :Urea = .......?

H2O = .......?

Biuret = .......?

24

Aliran menuju PCT :

Urea = ..........?

NH3 = ..........?

CO2 = ..........?

H2O = ...........?

27

26

Vacuum Concentrator

Upper (FA-202A) :Urea = 6108971,652 Kkal

H2O = 315298,449 Kkal


Suhu masuk aliran produk dari Vacuum Concentrator Upper = 138°C

Suhu keluar pada aliran produk ke Prilling Tower = 138oC


Aliran Produk dari Vacuum Concentrator Upper

T = 411°K

CpdT Urea = 965,507 (411 - 298) + -5,10E+00/2 (4112

- 2982

) +

1,00E-02/3 (4113 - 2983) + -6,38E-06/4 (4114-2984)


= 251,332 KJ/kg



QF Urea = 144984,371 kg x 251,332 KJ/kg

= 36439211,930 KJ x 0,239 Kkal/KJ

= 6108971,652 Kkal

CpdT H2O = 92,053 (411 - 298) + -4,00E-02/2 (4112 - 2982)+

-2,11E-04/3 (4113 - 2983) + 5,35E-07/4 (4114-2984)


= 474,423 KJ/kg


= 2780,726 kg x 474,423 KJ/kg

= 1319240,371 KJ x 0,239 Kkal/KJ

= 315298,449 Kkal


= 9,008 kg x 0,969 KJ/Kgmol K x (411 – 298) K

= 986,349 KJ x 0,239 Kkal/KJ

= 235,737 Kkal

Aliran produk ke Prilling Tower

T = 411°K

CpdT Urea = 965,507 (411 - 298) + -5,10E+00/2 (4112 - 2982) +



1,00E-02/3 (4113 - 2983) + -6,38E-06/4(4114-2984)


= 251,332 KJ/kg

QF Urea = 123660,516 kg x 251,332 KJ/kg

= 31079844,810 KJ x 0,239 Kkal/KJ

= 7428082,909 Kkal

CpdT H2O = 92,053 (411 - 298) + -4,00E-02/2 (4112 - 2982)+

-2,11E-04/3 (4113 - 2983) + 5,35E-07/4 (4114-2984)


= 474,423 KJ/kg


= 249,819 kg x 474,423 KJ/kg

= 118519,879 KJ x 0,239 Kkal/KJ

= 315298,449 Kkal


= 9,608 kg x 0,969 KJ/Kgmol K x (411 – 298) K

= 1052,047 KJ x 0,239 Kkal/KJ

= 251,439 Kkal



Aliran gas ke PCT

T = 411°K

CpdT Urea = 24,856 (411 - 298) + 1,44E-01/2 (4112 - 2982) +

3,81E-05/3 (4113 - 2983) +-1,10E-07/4(4114-2984) +

3,92E-11/5 (4115-2985)


= 143,808 KJ/kg


= 2700,392 kg x 135,451 KJ/kg

= 365770,797 KJ x 0,239 Kkal/KJ

= 87419,220 Kkal

CpdT NH3 = 33,573 (411 - 298) + -1,26E-02/2 (4112 - 2982) +

8,89E-05/3 (4113 - 2983) +-7,18E-08/4 (4114-2984) +

1,86E-11/5 (4115-2985)


= 248,612 KJ/kg


= 694,735 kg x 248,612 KJ/kg

= 172719,458 KJ x 0,239 Kkal/KJ



= 41279,950 Kkal

CpdT CO2 = 27,437(411 - 298) + 4,23E-02/2 (4112 - 2982) +

-1,96E-05/3 (4113 - 2983) + 4,00E-09/4 (4114-2984) +

-2,99E-13/5 (4115-2985)


= 103,051 KJ/kg


= 616,220 kg x 103,051 KJ/kg

= 63502,087 KJ x 0,239 Kkal/KJ

= 15176,999 Kkal

CpdT H2O = 33,933 (411 - 298) + -8,42E-03/2 (4112 - 2982) +

2,99E-05/3 (4113 - 2983) +-1,78E-08/4(4114-2984) +

3,69E-12/5 (4115-2985)


= 213,354 Kj/kg


= 16026,762 kg x 213,354 KJ/kg

= 908913,527 KJ x 0,239 Kkal/KJ



= 217230,333 Kkal

Neraca Panas Final Separator (FA 203)

Komponen Input (Kkal) Output (kg)

Aliran produk

Urea

H2O

Biuret

Aliran ke Prillingtower

Urea

H2O Biuret

6108971,652315298,449

235,737

6028082,909

28326,251251,439

Aliran gas ke PCT

Urea

NH3

CO2

H2O

Panas yang hilang

87419,22041279,95015176,999

217230,333

6738,737

Total 6424505,838 6424505,838



10. Prilling Tower ( IA - 301)

Prilling Tower (IA-301)

Final Separator (FA-203) :Urea = 7428082,909 Kkal

H2O = 315298,449 Kkal

Biuret = 251,439

28

Aliran Urea Produk :Urea = ..........?

H2O = ...........?

Biuret = ........?

31

26

Aliran Udara Masuk :Urea = 83,182 Kkal

H2O = 281535,425 Kkal

Aliran H2O dari PCT :H2O = 275025,678 Kkal

29

Aliran ke ATM :Urea =......?

H2O =......?

32

30

Dust Chamber:Urea = ..........?

H2O = ...........?

Suhu masuk aliran produk dari Final Separator = 138°C

Suhu masuk aliran H2O dari PCT = 50°C

Suhu masuk aliran Udara = 40°C

Suhu keluar pada aliran Urea produk = 138oC

Suhu keluar pada aliran ke Dust chamber = 36oC

Suhu keluar pada aliran gas ke atmosfer = 36°C

Aliran dari Final separator

T = 411°K

CpdT Urea = 965,507 (411 - 298) + -5,10E+00/2 (4112 - 2982) +

1,00E-02/3 (4113 - 2983) + -6,38E-06/4 (4114-2984)




= 251,332 KJ/kg

QF Urea = 123660,516 kg x 251,332 KJ/kg

= 31079844,810 KJ x 0,239 Kkal/KJ

= 7428082,909 Kkal

CpdT H2O = 92,053 (411 - 298) + -4,00E-02/2 (4112 - 2982)+

-2,11E-04/3 (4113 - 2983) + 5,35E-07/4 (4114-2984)


= 474,423 KJ/kg

QF H2O = n xCpdT H2O

= 249,819 kg x 474,423 KJ/kg

= 118519,879 KJ x 0,239 Kkal/KJ

= 315298,449 Kkal


= 9,608 kg x 0,969 KJ/Kgmol K x (411 – 298) K

= 1052,047 KJ x 0,239 Kkal/KJ

= 251,439 Kkal



Aliran H2O dari PCT

T = 323°K

CpdT H2O = 92,053 (323 - 298) + -4,00E-02/2 (3232 - 2982)+

-2,11E-04/3 (3233 - 2983) + 5,35E-07/4 (3234-2984)


= 104,612 KJ/kg


= 11000 kg x 104,612 KJ/kg

= 1150735,056 KJ x 0,239 Kkal/KJ

= 275025,678 Kkal

Aliran udara masuk

T = 313°K

CpdT Urea = 24,856 (313 - 298) + 1,44E-01/2 (3132 - 2982) +

3,81E-05/3 (3133 - 2983) +-1,10E-07/4 (3134-2984) +

3,92E-11/5 (3135-2985)


= 17,402 KJ/kg




= 20 kg x 17,402 KJ/kg

= 348,041 KJ x 0,239 Kkal/KJ

= 83,182 Kkal

CpdT H2O = 33,933 (313 - 298) + -8,42E-03/2 (3132 - 2982) +

2,99E-05/3 (3133 - 2983) + -1,78E-08/4 (3134-2984) +

3,69E-12/5 (3135-2985)


= 28,063 KJ/kg


= 41976 kg x 28,063 KJ/kg

= 1177972,488 KJ x 0,239 Kkal/kJ

= 281535,425 Kkal

Aliran urea produk

T = 411°K

CpdT Urea = 965,507 (411 - 298) + -5,10E+00/2 (4112 - 2982)+

1,00E-02/3 (4113 - 2983) + -6,38E-06/4 (4114-2984)

= 15079,932 KJ/Kmol x 1 Kmol/60kg

= 251,332 KJ/kg




= 123288,589 kg x 251,332 KJ/kg

= 30986393,310 KJ x 0,239Kkal/KJ

= 7405747,762 Kkal

CpdT H2O = 92,053 (411 - 298) + -4,00E-02/2 (4112 - 2982) +

-2,11E-04/3 (4113 - 2983) + 5,35E-07/4 (4114-2984)


= 474,423 KJ/kg


= 249,068 kg x 474,423 KJ/kg

= 118163,588 KJ x 0,239 Kkal/KJ

=28241,097 Kkal

QF biuret = n x CpdT

= 9,579 Kmol x 0,969KJ/Kmol K x (411-298) K

= 1048,872 KJ x 0,239 Kkal/KJ

= 250,673 Kkal

Aliran ke dust chamber

T = 309°K



CpdT Urea = 965,507 (309 - 298) + -5,10E+00/2 (3092 - 2982)+

1,00E-02/3 (3093 - 2983) + -6,38E-06/4 (3094-2984)


= 0,0253 KJ/kg


= 371,917 kg x 0,0253 KJ/kg

= 9,409 KJ x 0,239 Kkal/kJ

= 2,248 Kkal

CpdT H2O = 92,053 (309 - 298) + -4,00E-02/2 (3092 - 2982) +

-2,11E-04/3 (3093

- 2983

) + 5,35E-07/4 (3094

-2984

)


= 46,1002 KJ/kg


= 1484,883 kg x 46,1002 KJ/kg

= 68453,403 KJ x 0,239 Kkal/KJ

= 16,360 Kkal

Aliran ke atmosfer

T = 309°K



CpdT Urea = 24,856 (309 - 298) + 1,44E-01/2 (3092 - 2982) +

3,81E-05/3 (3093 - 2983) + -1,10E-07/4(3094-2984) +

3,92E-11/5 (3095-2985)


= 13,274 KJ/kg


= 30,909 kg x 13,274 KJ/kg

= 410,286 KJ x 0,239 Kkal/kJ

= 98,058 Kkal

CpdT H2O = 33,933 (309 - 298) + -8,42E-03/2 (3092 - 2982) +

2,99E-05/3 (3093 - 2983) + -1,78E-08/4 (3094-2984) +

3,69E-12/5 (3095-2985)


= 20,574 KJ/kg


= 51483,975 kg x 20,574 KJ/kg

= 10599231,302 KJ x 0,239 Kkal/kJ

= 253156,281 Kkal



Neraca Panas Pada Prilling Tower

Komponen Input (Kkal) Output (Kkal) Aliran dari FA 203

Urea

H2O

Biuret

7428082,909315298,449

1251,439

Aliran H2O dari PCT

H2O

275025,678

Aliran udara masuk

Urea

H2O

Aliran urea produk

Urea

Biuret

H2O

83,182

281535,425

7405747,762250,673

28241,097

Aliran ke dust chamber

Urea

H2O

2,248

16,360

Aliran ke atm- Urea- H2O

Panas yang hilang

98,058253156,281

613764,603

Total 8301277,082 8301277,082



Neraca Masa Over All

No. Alat Umpan Masuk

(Kkal)

Umpan Keluar

(Kkal)

1. Seksi Sintesa

− Urea Sintesa Reaktor

− Stripper

− Carbamat Condenser

35480164,250

36841725,790

16668758,160

35480164,250

36841725,790

16668758,160

2. Seksi Purifikasi

− High Pressure Decomposer

− Low Pressure Decomposer

− Flash Separator

25859767,320

20291630,200

5565139,955

25859767,320

20291630,200

5565139,955

4 Seksi Konsentrasi

− Vacuum Concentrator Lower

− Vacuum Concentrator Upper

−

Final Separator

8356628,474

7327533,872

6424505,838

8356628,474

7327533,872

6424505,838

5.. Seksi Prilling

− Prilling Tower 8301277,082 8301277,082

Total 171117130,9 171117130,9

lampiran neraca panas

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