PERHITUNGAN EVAPORATOR PG.
RENDENG KUDUS
OPERASIONA
BASIS KAPASITAS = 1450
% brix NE = 10.50
% brix NK = 61.61
Berat NE = 3126.37 Ton/hari
P Ube = 0.8 ATO
P Badan akhir = 62 CmHg Vac
∆P = 1.61579
Pembagian tekanan menurut HUGOT
Badan ∆P Tekanan
I 0.35547368421 1.4445263158 108.38
II 0.33931578947 1.1052105263 82.97
III 0.32315789474 0.7820526316 58.77
IV 0.307 0.4750526316 35.78
V 0.29084210526 0.1842105263 14
RAW SUGAR DIOLAH PERHARI =
%brix Raw Sugar =
%brix remelt =
Kebutuhan uap di masakan = Berat air masakan + Berat air dita
= 0.0
Kebutuhan uap di VW = 596.9
Badan V = X
Badan IV = X
Badan III = X
Badan II = X +
Badan I = X +
Jumlah = 5X +
Air diuapkan = E= 2593.549 Ton/Hari
E = 5X +
5X = 1996.639
X = 399.32780648 Ton/Hari
BRIX KELUAR TIAP BADAN DAN BRIX RATA - RATA
Badan Air Diuapkan Brix Keluar Brix Rata2
I 996.2 15.41 12.96
II 399.33 18.97 17.19
III 399.33 24.65 21.81
IV 399.33 35.22 29.94
V 399.33 61.61 48.41
Titik Didih = T Uap + KTD hitung + KTD Hidostatis
∆ T = Suhu bahan Penguap - Suhu TD
Badan %brix Rata2 T Uap KTD Hitung
UBE 116.5
I 12.96 109.6 0.306
II 17.19 101.2 0.424
III 21.81 92.5 0.579
IV 29.94 79.5 0.924
V 48.41 58.6 2.522
Kecepatan penguapan dan LP masing - masing badan
Badan ∆T C dessin 0.0006
I 5.61 3.26
II 6.58 2.76
III 6.42 2.21
IV 9.28 1.62
V 11.18 0.79
kecepatan penguapan dibuat sama = 18
Badan 5
TD = 61.1
C = 0.0310 x (T4 - 54)
∆T = T3 -
T4 = 122.3 +
T4 = 86.32
∆T = 17.99
P4 = 0.72 kg/cm2 abs
= 53 CmHg abs
= 23 CmHg Vac
Badan 4
TD = 80.4
C = 0.0420 x (T3 - 54)
∆T = T3 -
T3 = 137.2 +
T3 = 93.94
∆T = 10.72
P3 = 0.91 kg/cm2 abs
= 67 CmHg abs
= 9 CmHg Vac
Badan 3
TD = 93.1
C = 0.0469 x (T2 - 54)
∆T = T2 -
T2 = 148.8 +
2
T2 = 102.66
∆T = 7.88
P2 = 1.222 kg/cm2 abs
= 0.222 ATO
Badan 2
TD = 101.6
C = 0.0497 x (T1 - 54)
∆T = T1 -
T1 = 157.0 +
T1 = 109.55
∆T = 6.52
P1 = 1.51 kg/cm2 abs
= 0.51 ATO
Badan 1
TD = 109.9
C = 0.0522 x (T0 - 54)
∆T = T0 -
T0 = 164.9 +
T0 = 116.41
∆T = 5.52
P0 = 1.85 kg/cm2 abs
= 0.85 ATO
BADAN % brix keluar %brix rata2 TD
I 15.41 12.96 109.9
II 18.97 17.19 101.6
III 24.65 21.81 93.1
IV 35.22 29.94 80.4
V 61.61 48.41 61.1
OR PG.RENDENG KUDUS DESAIN BLEEDING KE MASAKAN DAN JUICE HEATER
OPERASIONAL QUINTIPLE
KAPASITAS 1450 TCD
OLAH RAW SUGAR 0 TON/HARI
TCD
= 135 CmHg Abs T = 116.5 oC -----> LIHAT HUGOT
= 14 CmHg Abs T = 58.6 oC =
Vacum Suhu uap oC
0.44452632 ATO 109.6 -----> LIHAT HUGOT
0.10521053 ATO 101.2
17.23 Vacum 92.5
40.22 Vacum 79.5
62 Vacum 58.6
0 TON
99
60
air masakan + Berat air ditambahkan dimasakan+puteran + air untuk remelt
Ton/hari
Ton/hari
0.0
596.9 + VD II di bleeding ke Juice Heater
596.9
596.9 = 2593.549
KTD Hids KTD Total TD ∆T
0.98 1.29 110.89 5.61
1.4 1.82 103.02 6.58
1.7 2.28 94.78 6.42
2.8 3.72 83.22 9.28
7.2 9.72 68.32 11.18
Air
W (Kec.Penguapan) LP (m2)
diuapkan
18.32 996.2 2265.3241
18.17 399.3 915.91489
14.22 399.3 1170.2259
15.01 399.3 1108.2955
8.82 399.3 1885.9556
7345.7159
kg/m2/jam
68.32
50.3120549651843
-----> LIHAT HUGOT HAL.1034
83.22
50.663200239935
-----> LIHAT HUGOT HAL.1034
94.78
56.5477982275739
-----> LIHAT HUGOT HAL.1034
103.02
62.0681035979159
-----> LIHAT HUGOT HAL.1034
110.89
67.9312567795671
∆T C W LP P Abs
1.85
5.52 3.26 18 2306 1.51
6.52 2.76 18 2306 1.222
7.88 2.28 18 2306 0.91
10.72 1.68 18 2306 0.72
17.99 1.00 18 2306 14
11531
HEATER
-----> LIHAT HUGOT HAL.1034
0.1842 Kg/Cm2
-----> LIHAT HUGOT HAL.1034
Vacum
0.85 ATO
0.51 ATO
0.222 ATO
9 VAC
23 VAC
62 VAC
PERHITUNGAN EVAPORATOR PG.RENDENG KUDUS
OPERASIONA
BASIS KAPASITAS = 4000
% brix NE = 10.50
% brix NK = 61.61
Berat NE = 3126.37 Ton/hari
P Ube = 0.6 ATO
P Badan akhir = 62 CmHg Vac
∆P = 1.41579
Pembagian tekanan menurut HUGOT
Badan ∆P Tekanan
I 0.31147368421 1.2885263158 108.38
II 0.29731578947 0.9912105263 82.97
III 0.28315789474 0.7080526316 58.77
IV 0.269 0.4390526316 35.78
V 0.25484210526 0.1842105263 14
RAW SUGAR DIOLAH PERHARI =
%brix Raw Sugar =
%brix remelt =
Kebutuhan uap di masakan = Berat air masakan + Berat air dita
= 0.0
Kebutuhan uap di VW = 596.9
Badan V = X
Badan IV = X
Badan III = X
Badan II = X +
Badan I = X +
Jumlah = 5X +
Air diuapkan = E= 2593.549 Ton/Hari
E = 5X +
5X = 1996.639
X = 399.32780648 Ton/Hari
BRIX KELUAR TIAP BADAN DAN BRIX RATA - RATA
Badan Air Diuapkan Brix Keluar Brix Rata2
I 996.2 15.41 12.96
II 399.33 18.97 17.19
III 399.33 24.65 21.81
IV 399.33 35.22 29.94
V 399.33 61.61 48.41
Titik Didih = T Uap + KTD hitung + KTD Hidostatis
∆ T = Suhu bahan Penguap - Suhu TD
Badan %brix Rata2 T Uap KTD Hitung
UBE 116.5
I 12.96 109.6 0.306
II 17.19 101.2 0.424
III 21.81 92.5 0.579
IV 29.94 79.5 0.924
V 48.41 58.6 2.522
Kecepatan penguapan dan LP masing - masing badan
Badan ∆T C dessin 0.0006
I 5.61 3.26
II 6.58 2.76
III 6.42 2.21
IV 9.28 1.62
V 11.18 0.79
kecepatan penguapan dibuat sama = 18
Badan 5
TD = 61.1
C = 0.0310 x (T4 - 54)
∆T = T3 -
T4 = 122.3 +
T4 = 86.32
∆T = 17.99
P4 = 0.72 kg/cm2 abs
= 53 CmHg abs
= 23 CmHg Vac
Badan 4
TD = 80.4
C = 0.0420 x (T3 - 54)
∆T = T3 -
T3 = 137.2 +
T3 = 93.94
∆T = 10.72
P3 = 0.91 kg/cm2 abs
= 67 CmHg abs
= 9 CmHg Vac
Badan 3
TD = 93.1
C = 0.0469 x (T2 - 54)
∆T = T2 -
T2 = 148.8 +
2
T2 = 102.66
∆T = 7.88
P2 = 1.222 kg/cm2 abs
= 0.222 ATO
Badan 2
TD = 101.6
C = 0.0497 x (T1 - 54)
∆T = T1 -
T1 = 157.0 +
T1 = 109.55
∆T = 6.52
P1 = 1.51 kg/cm2 abs
= 0.51 ATO
Badan 1
TD = 109.9
C = 0.0522 x (T0 - 54)
∆T = T0 -
T0 = 164.9 +
T0 = 116.41
∆T = 5.52
P0 = 1.85 kg/cm2 abs
= 0.85 ATO
BADAN % brix keluar %brix rata2 TD
I 15.41 12.96 109.9
II 18.97 17.19 101.6
III 24.65 21.81 93.1
IV 35.22 29.94 80.4
V 61.61 48.41 61.1
OR PG.RENDENG KUDUS DESAIN BLEEDING KE MASAKAN DAN JUICE HEATER
OPERASIONAL QUINTIPLE
KAPASITAS 4000 TCD
OLAH RAW SUGAR 0 TON/HARI
TCD
= 135 CmHg Abs T = 116.5 oC -----> LIHAT HUGOT
= 14 CmHg Abs T = 58.6 oC =
Vacum Suhu uap oC
0.28852632 ATO 109.6 -----> LIHAT HUGOT
-0.0087895 ATO 101.2
17.23 Vacum 92.5
40.22 Vacum 79.5
62 Vacum 58.6
0 TON
99
60
air masakan + Berat air ditambahkan dimasakan+puteran + air untuk remelt
Ton/hari
Ton/hari
0.0
596.9 + VD II di bleeding ke Juice Heater
596.9
596.9 = 2593.549
KTD Hids KTD Total TD ∆T
0.98 1.29 110.89 5.61
1.4 1.82 103.02 6.58
1.7 2.28 94.78 6.42
2.8 3.72 83.22 9.28
7.2 9.72 68.32 11.18
Air
W (Kec.Penguapan) LP (m2)
diuapkan
18.32 996.2 2265.3241
18.17 399.3 915.91489
14.22 399.3 1170.2259
15.01 399.3 1108.2955
8.82 399.3 1885.9556
7345.7159
kg/m2/jam
68.32
50.3120549651843
-----> LIHAT HUGOT HAL.1034
83.22
50.663200239935
-----> LIHAT HUGOT HAL.1034
94.78
56.5477982275739
-----> LIHAT HUGOT HAL.1034
103.02
62.0681035979159
-----> LIHAT HUGOT HAL.1034
110.89
67.9312567795671
∆T C W LP P Abs
1.85
5.52 3.26 18 2306 1.51
6.52 2.76 18 2306 1.222
7.88 2.28 18 2306 0.91
10.72 1.68 18 2306 0.72
17.99 1.00 18 2306 14
11531
HEATER
-----> LIHAT HUGOT HAL.1034
0.1842 Kg/Cm2
-----> LIHAT HUGOT HAL.1034
Vacum
0.85 ATO
0.51 ATO
0.222 ATO
9 VAC
23 VAC
62 VAC
MATERIAL BALANCE STASIUN PENGUAPAN (QUINTIPLE EFFECT)
PG. RENDENG KUDUS (TON/JAM)
KAPASITAS 2750 TCD
Air Injeksi 477.11
BLEEDING VW
24.87
Uap Nira V
Ke Kondensor Kondensor
Uap Nira I 16.64 Uap Nira II 16.64 16.64 16.64
Uap Nira III Uap Nira IV
I II III IV V
Uap Bekas 493.75
Air Jatuhan
Nira Kental
Berat = 22.10
Nira Encer Berat = 88.76 Berat = 72.12 Berat = 55.48 Berat = 38.84 Pol = 10.12
Berat = 130.27 %brix = 12.59 %brix = 15.71 %brix = 20.91 %brix = 31.22 Brix = 13.62
Pol = 10.17 Air konden HK = 74.33
Brix = 13.68 Air konden Air konden Air konden Air konden %pol = 45.79
HK = 74.32 Berat = 41.51 Berat = 16.64 Berat = 16.64 Berat = 16.64 Berat = 16.64 %brix = 61.61
%pol = 7.80 OV
Berat = 0.10
Pol = 0.04
Brix = 0.06
HK = 72.00
%pol = 44.36
%brix = 61.61
