Vacuum Drayer Depericarper Internal Rate of Return IRR

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