Tabel LB.8 Neraca Panas pada Oil Purifier
Panas Masuk kJ Panas Keluar kJ
Komposisi Alur 16
Alur 17 Alur 18
Minyak Kotoran
Air FFA
5.243.763,076 632,751
7.562,303 93.591,476
- 2.545,525
228,230 -
4.442.760,163 454,830
6.011,364 76.646,806
Panas hilang -
816.902,686
Total 5.345.549,604 5.345.549,604
9. Vacuum Drayer
T = 80 C
-Minyak -Air
-Kotoran -FFA
T = 80 C
-Air 100 18
20 T = 80
C -Minyak
-Air -Kotoran
-FFA
19
Vacuum dryer
Alur 18 :
Q Minyak = 5.277,158 kg x 15,307 kJkg K x 55 K
= 4.442.760,163
kJ Q Kotoran
= 9,376 kg x 4,2164 Jkg K x 55 K =
454,830 kJ
Q Air = 25,922 kg x 4,2164 kJkg K x 55 K
= 6.011,364
kJ Q FFA
= 202,968 kg x 6,866 kJkg K x 55 K =
4.528.646,918 kJ
Panas Keluar : Alur 19 :
Q Air = 51,845 kg x 4,1774 kJkg K x 55 K
= 11.911,752
kJ
Universitas Sumatera Utara
Panas penguapan air dihitung dengan korelasi Watson :
0,38 11
12 1
2
Tr 1
Tr 1
ΔH ΔH
Tr1 = 3
, 647
273 80
= 0,545
Tr2 = 3
, 647
273 80
= 0,545
H1 = Panas penguapan pada titik didih air = 2676 kJkg Hv12 = 2676 x
38 ,
576 ,
1 545
, 1
= 2748,7257 kJkg Panas penguapan
= m x Hv
= 51,845 x 2748,7257 kJ = 142.507,684 kJ
Alur 20 :
Q Minyak = 5.274,430 kg x 15,307 kJkg K x 55 K
= 4.440.463,501
kJ Q Kotoran
= 8,195 kg x 0,882 kJkg K x 55 K =
397,539 kJ
Q Air = 0,109 kg x 4,1774 kJkg K x 55 K
= 25,044
kJ Q FFA
= 180,845 kg x 6,866 kJkg K x 55 K =
68.292,497 kJ
Panas Masuk + Panas dibutuhkan = Panas keluar + Panas penguapan 8.977.873,275 + Panas dibutuhkan = 4.521.090,333 + 142.507,684
Panas dibutuhkan = 4.314.275,258 kJ Entalphi steam pada 70,11 kPa, T 90
C = 2.283,2 kJkg K Saturated steam Maka Steam yang dibutuhkan :
m =
λ dQ
=
kJkg 2.283,2
kJ 258
4.314.275,
= 1889,574 kg
Universitas Sumatera Utara
Tabel LB.9 Neraca Panas pada Vacuum drayer
Panas masuk kJ Panas keluar kJ
Komposisi Alur 18
Alur 19 Alur 20
Minyak Kotoran
Air FFA
Panas Penguapan 4.442.760,163
454,830 6.011,364
4.528.646,918 -
- -
11.911,752 -
142.507,684 4.440.463,501
397,539 25,044
68.292,497 -
Panas dibutuhkan 4.314.275,258
- -
Jumlah 4.663.598,017 154.419,436
4.509.178,581
Total 4.663.598,017 4.663.598,017
10. Depericarper
T = 50 C
-Biji -Ampas
-Air T = 40
C -Ampas
-Biji 11
22 T = 50
C -Biji
-Air -Serat
21
Depericarper
Panas masuk : Alur 11 :
Q Serat = 5.298,330 kg x 1,284 kJkg K x 25 K
= 170.076,393
kJ Q Biji
= 4.202,389 kg x 31,9624 kJkg K x 25 K =
3.357.960,954 kJ
Q Air = 95,967 kg x 4,1840 kJkg K x 25 K
= 10.038,148
kJ Total Panas masuk = 3.538.075,495 kJ
Panas Keluar : Alur 21 :
Q Abu = 5.067,050 kg x 0,882 kJkg K x 15 K
Universitas Sumatera Utara
= 67.037,072
kJ Q Biji
= 211,127 kg x 11,684 kJkg K x 15 K =
37.002,118 kJ
Alur 22 :
Q Biji = 4.175,998 kg x 31,9624 kJkg K x 25 K
= 3.336.872,962
kJ Q Abu
= 43,185 kg x 0,882 kJkg K x 25 K =
952,229 kJ
Q Air = 99,326 kg x 4,1840 kJkg K x 25 K
= 10.389,450
kJ Total Panas Keluar = 3.452.253,831 kJ
Panas Masuk = Panas Keluar + Panas hilang 3.538.075,495 = 3.452.253,831 + Panas Hilang
Panas Hilang = 85.821,664 kJ
Tabel LB.10 Neraca Panas pada Depericarper
Panas Masuk kJ Panas keluar kJ
Komposisi Alur 11
Alur 21 Alur 22
Serat Biji
Air Cangkang
170.076,393 3.357.960,954
10.038,148 -
67.037,072 37.002,118
- -
952,229 3.336.872,962
10.389,450 -
Jumlah 3.538.075,495 104.039,19
3.348.214,641 Panas hilang
- 85.821,664
Total 3.538.075,495 3.538.075,495
Universitas Sumatera Utara
11. Silo Drayer