a. Shell side
s e
10 2
s s
s D
10 22
. 5
1 N
D G
f 2
1 P
φ ⋅
⋅ ⋅
⋅ +
⋅ ⋅
⋅ ⋅
= Δ
Kern, 1965
untuk R
e
= 15168,8576 , f = 0.002 ft
2
in
2
Fig.29, Kern, 1965 N+1 = LB
Kern, 1965 = 144 2.67 = 53,93
ΔP
s
yang diperbolehkan adalah ≤ 10 psi, maka ΔP
s
dapat diterima.
b. Tube side
t 10
2 t
t
s ID
10 22
. 5
N L
G f
P φ
⋅ ⋅
⋅ ⋅
⋅ ⋅
⋅ =
Δ Kern, 1965
untuk R
e
= 63715,744 , f = 0.0001 ft
2
in
2
Fig.26, Kern, 1965
231 ,
7 1
1 0,6212
10 22
, 5
4 12
077 ,
2015623 0.0001
10 2
= ⋅
⋅ ⋅
⋅ ⋅
⋅ ⋅
= Δ
t
P
psi
2 r
g 2
V s
n 4
P ⋅
= Δ
untuk G
t
= 077
, 2015623
,
2
g 2
V
= 0,3 Fig.27, Kern, 1965
4 ,
2 0,3
1 4
4 =
⋅ ⋅
= Δ
r
P psi
r t
T
P P
P Δ
+ Δ
= Δ
psi P
T
631 ,
9 =
Δ
ΔP
T
yang diperbolehkan adalah ≤ 10 psi, maka ΔP
T
dapat diterima.
LC.14 Tangki Penampung Distilat T-103
Jenis sambungan : Double welded butt joints
Tabel Komposisi Distilat
Komp. F ρ V V
ρ camp EtOH 3677.94 0.789
4661.5209 0.9681
0.7638 H2O 153.29 0.998
153.5972 0.0319 0.0318
Total 3831.23 4815.1181 1 0.7956
psi 4467
, 1
1.2 08
. 10
22 .
5 93
, 53
8 227802,865
002 .
5 .
10 2
= ⋅
⋅ ⋅
⋅ ⋅
⋅ ⋅
× =
Δ
s
P
Kondisi operasi : Temperatur
= 81.14 °C Tekanan
= 1 atm Laju alir massa
= 3831,23 kgjam Kebutuhan perancangan= 5 menit
Faktor kelonggaran = 15
Densitas campuran = 0.795 kgL = 49,6301 lbft
3
Perhitungan:
a. Volume tangki
Volume larutan, V
l
=
3
kgm 795
mnt 60
jam 1
mnt x 5
x kgjam
3831,23 = 0.401m
3
Volume tangki, V
t
= 1 + 0.15 × 0.401 m
3
= 0.461 m
3
Fraksi volum = 0.401 0.461 = 0.8698
Untuk Fraksi volum 0.8698 maka HD = 0.815 Tabel 10.64, Perry, 1999 Volume
tangki, V
t
= ⎟
⎠ ⎞
⎜ ⎝
⎛ α
α −
α cos
sin 30
. 57
LR
2
Perry, 1999 Dimana cos
α = 1-2HD cos
α = 1-20.815 cos
α = -0.63 α = 129,05 derajat
Asumsi panjang
tangki L
t
= 2 m Maka, volume tangki, V
t
= ⎟
⎠ ⎞
⎜ ⎝
⎛ α
α −
α cos
sin 30
. 57
LR
2
0.461 =
⎟ ⎠
⎞ ⎜
⎝ ⎛
− 05
. 129
cos 05
, 129
sin 30
. 57
05 ,
129 2
2
R R radius = 0.588 m
D diameter = 1.176 m = 46,2991 in H
s
tinggi cairan = 0,956 m = 3,1364 ft
b. Spesifikasi Tangki
Tebal shell, Cc
1,2P 2SE
PD t
+ −
= Peters, 2003
P = P
operasi
+ P
h
P
h
= 6301
, 49
144 1
- 3,1364
× = 0.7363 psi
P = 14.694 + 0.7363 × 1.15 = 17.747 psi faktor
kelonggaran 15
Joint efficiency E = 0.85
Peters, 2003 Allowable stress S
= 18750 psi Brownell,1959
Allowable corrosion Cc = 0.125 in10 thn
Peters, 2003 Maka, tebal shell:
in t
0.151 125
. psi
1,217.747 psi0,85
218750 in
49,2991 psi
17.747 =
+ −
=
Tebal shell standar yang digunakan = 316 in Brownell,1959 Tebal head,
Diameter tutup = diameter tangki
= 1.176 m Ratio axis
= L:D = 1: 4
L
h
= 176
. 1
4 1
Hh ×
⎟ ⎠
⎞ ⎜
⎝ ⎛
= ×
⎟ ⎠
⎞ ⎜
⎝ ⎛
D D
= 0.294 m L
t
panjang tangki = L
s
+ L
h
L
s
panjang shell = 2 m – 20.294 m = 1.412 m
Tutup atas tangki terbuat dari bahan yang sama dengan shell sehingga tebal tutup 14 in.
LC.15 Pompa Refluks Destilasi P-105
Jenis : centrifugal pump
Kondisi operasi Temperatur
= 81,14
C Densitas larutan
ρ = 0,7956 kgL = 49,6301 lbmft
3
Viskositas larutan μ
= 0,420 cp
= 0,00028 lb
m
ft ⋅s
Laju alir massa F =
3713,19 kgjam = 2,0629 lb
m
s
psi ,
144 1
H Ph
s
ρ −
=
Laju alir volumetrik, Q = ρ F
=
3
lbmft 49,6301
lbms 2,0629
= 0,0415 ft
3
s
0,13 0,45
f opt
i,
ρ 3,9Q
D =
0,13 3
0,45 3
lbmft 49,6301
s ft
3,90,0415 =
= 1,5475 in = 0,1289 ft
Ukuran spesifikasi pipa :Appendix A-5 Geankoplis Ukuran pipa nominal
= 1,5 in
Schedule pipa
= 40
Diameter dalam ID =
1,61 in = 0,13417 ft
Diameter luar OD =
1,9 in = 0,15833 ft
Luas penampang dalam A
t
= 0,01414ft
2
Kecepatan linier, =
=
t
A Q
v
2 3
ft 0,0141
s ft
0,0415
= 2,9349 fts Bilangan Reynold,
69812,4602 lbmft
0,00028 ft
0,1342 fts
2,9349 ft
49,6301lbm μ
D v
ρ N
3 Re
= ⋅
= =
Karena N
Re
2100, maka aliran turbulen. Untuk pipa sainless steel diperoleh
0,25 Nre
0,079 f
=
= 0,00486 esposito, 1994 Instalasi pipa:
Pipa lurus 16 ft ; ft
0,1342 .s
lbm.ftlbf 32,174
ft 16
2 fts
2,9349 20,00486
F
2
= = 0,3100 ft.lbflbm
1 gate valve, 2
.s lbm.ftlbf
32,174 2
fts 2,9349
10,19 F
2
= = 0,0087 ft.lbflbm
1 Tee, 2
.s lbm.ftlbf
32,174 2
fts 2,9349
1,8 F
2
= = 0,0821 ft.lbflbm
1 kontraksi, 2
.s lbm.ftlbf
32,174 21
fts 2,9349
0,55 F
2
= = 0,0251 ft.lbflbm
1 ekspansi, 2
.s lbm.ftlbf
32,174 21
fts 2,9349
11 F
2
= = 0,0456 ft.lbflbm
Total Friksi : Σ F = 0,4715 ft.lbflbm
Kerja pompa : F
Σ Pv
Δ c
g α
2 2
v Δ
c g
g ΔZ
W +
+ ⎟
⎟ ⎠
⎞ ⎜
⎜ ⎝
⎛ +
= peters, 2004
Tinggi pemompaan, Δz = 13,5 ft
Static head ,
m f
c
lb lb
ft 13,5
g g
Δz ⋅
= Velocity head
, g
2 Δv
c 2
= ; Pressure head, ρ
P Δ
= 0 Maka : W = 13,9715 ft.lbflbm
Daya pompa : 28,7764
ft 49,6301lbm
s ft
0,0415 ft.lbflbm
13,9715 ρ
Q W
P
3 3
= =
= efisiensi pompa 80
: Hp
0,0654 8
, 550
28,7764 P
= =
x Digunakan pompa dengan daya standar 0,1 Hp.
Daya motor : 0,11765Hp
85 ,
0,1Hp =
= : digunakan motor 0,12 Hp
LC.16 Pompa I Destilasi P-106
Jenis : centrifugal pump
Kondisi operasi Temperatur
= 81,14
C Densitas larutan
ρ = 0,795 kgL = 49,6301 lbmft
3
Viskositas larutan μ
= 0,420 cp
= 0,00028 lb
m
ft ⋅s
Laju alir massa F =
118,036 kgjam = 0,0656 lb
m
s Laju alir volumetrik, Q = ρ
F =
3
lbmft 49,6301
lbms 0,0656
= 0,0013 ft
3
s
0,13 0,45
f opt
i,
ρ 3,9Q
D =
0,13 3
0,45 3
lbmft 49,6301
s ft
3,90,0013 =
= 0,3257 in = 0,0271 ft Ukuran spesifikasi pipa : Appendix A-5 Geankoplis
Ukuran pipa nominal =
1,25 in
Schedule pipa
= 40
Diameter dalam ID =
1,38 in = 0,115 ft
Diameter luar OD =
1,66 in = 0,1383 ft
Luas penampang dalam A
t
= 0,01040 ft
2
Kecepatan linier,
= =
t
A Q
v
2 3
ft 0,01040
s ft
0,0013
= 0,125 fts Bilangan Reynold,
7143 ,
2545 lbmft
0,00028 ft
0,1149 fts
0,125 ft
49,6301lbm μ
D v
ρ N
3 Re
= ⋅
= =
Karena N
Re
2100, maka aliran turbulen. Untuk pipa sainlessl steel diperoleh
0,25 Nre
0,079 f
=
= 0,0111 esposito, 1994 Instalasi pipa:
Pipa lurus 20 ft ; ft
0,1149 .s
lbm.ftlbf 32,174
ft 20
2 fts
0,125 20,0111
F
2
= = 0,0018 ft.lbflbm
3 elbow 90 ,
2 .s
lbm.ftlbf 32,174
2 fts
0,125 30,75
F
2
= = 0,0044 ft.lbflbm
1 gate valve, 2
.s lbm.ftlbf
32,174 2
fts 0,125
10,19 F
2
= = 0,00037 ft.lbflbm
1 kontraksi, 2
.s lbm.ftlbf
32,174 21
fts 0,125
0,55 F
2
= = 0,0011 ft.lbflbm
1 ekspansi, 2
.s lbm.ftlbf
32,174 21
fts 0,125
11 F
2
= = 0,002 ft.lbflbm
Total Friksi : Σ F = 0,00967 ft.lbflbm
Kerja pompa : F
Σ Pv
Δ c
g α
2 2
v Δ
c g
g ΔZ
W +
+ ⎟
⎟ ⎠
⎞ ⎜
⎜ ⎝
⎛ +
= peters, 2004
Tinggi pemompaan, Δz = 13 ft
Static head ,
m f
c
lb lb
ft 13
g g
Δz ⋅
=
Velocity head ,
g 2
Δv
c 2
= ; Pressure head, ρ
P Δ
= 0 Maka : W = 13,00967 ft.lbflbm
Daya pompa : 8394
, ft
49,6301lbm s
ft 0,0013
ft.lbflbm 13,00967
ρ Q
W P
3 3
= =
= efisiensi pompa 80
: 0,002Hp
8 ,
550 0,8394
P =
= x
Digunakan pompa dengan daya standar 0,05 Hp. Daya motor :
0,058Hp 85
, 0,05Hp
= =
: digunakan motor 0,06 Hp
LC.17 Pompa II Destilasi P-107
Jenis : centrifugal pump
Kondisi operasi Temperatur
= 92,61
C Densitas larutan
ρ = 1,102 kgL = 68,7954 lbmft
3
Viskositas larutan μ
= 0,171 cp
= 0,00011 lb
m
ft ⋅s
Laju alir massa F =
1349,738 kgjam = 0,7498 lb
m
s Laju alir volumetrik, Q = ρ
F =
3
lbmft 68,7954
lbms 0,7498
= 0,0109 ft
3
s
0,13 0,45
f opt
i,
ρ 3,9Q
D =
0,13 3
0,45 3
lbmft 68,7954
s ft
3,90,0109 =
= 0,8847 in = 0,0737 ft
Ukuran spesifikasi pipa : Appendix A-5 Geankoplis Ukuran pipa nominal
= 0,5 in
Schedule pipa
= 40
Diameter dalam ID =
0,622 in = 0,0518 ft
Diameter luar OD =
0,84 in = 0,0699 ft
Luas penampang dalam A
t
= 0,304 in
= 0,00211 ft
2
Kecepatan linier,
= =
t
A Q
v
2 3
ft 0,00211
s ft
0,0109
= 5,1659 fts Bilangan Reynold,
3636 ,
167356 lbmft
0,00012 ft
0,0518 fts
5,1659 lbmft
68,7954 μ
D v
ρ N
3 Re
= ⋅
= =
Karena N
Re
2100, maka aliran turbulen. Untuk pipa sainlessl steel diperoleh
0,25 Nre
0,079 f
=
= 0,0039 esposito, 1994
Instalasi pipa: Pipa lurus 15 ft ;
ft 0,0518
.s lbm.ftlbf
32,174 ft
15 2
fts 5,1659
20,0039 F
2
= = 1,8719 ft.lbflbm
1 elbow 90 ,
2 .s
lbm.ftlbf 32,174
2 fts
5,1659 10,75
F
2
= = 0,0602 ft.lbflbm
1 gate valve, 2
.s lbm.ftlbf
32,174 2
fts 5,1659
10,19 F
2
= = 0,0152 ft.lbflbm
1 kontraksi, 2
.s lbm.ftlbf
32,174 21
fts 5,1659
0,55 F
2
= = 0,0441 ft.lbflbm
1 ekspansi, 2
.s lbm.ftlbf
32,174 21
fts 5,1659
11 F
2
= = 0,0802 ft.lbflbm
Total Friksi : Σ F = 2,0716 ft.lbflbm
Kerja pompa : F
Σ Pv
Δ c
g α
2 2
v Δ
c g
g ΔZ
W +
+ ⎟
⎟ ⎠
⎞ ⎜
⎜ ⎝
⎛ +
= peters, 2004
Tinggi pemompaan, Δz = 5 ft
Static head ,
m f
c
lb lb
ft 5
g g
Δz ⋅
=
Velocity head ,
g 2
Δv
c 2
= ; Pressure head, ρ
P Δ
= 0 Maka : W = 7,0716 ft.lbflbm
Daya pompa : 3027
, 5
ft 68,7954lbm
s ft
0,0109 ft.lbflbm
7,0716 ρ
Q W
P
3 3
= =
= efisiensi pompa 80
: 0,0120Hp
8 ,
550 5,3027
P =
= x
Digunakan pompa dengan daya standar 0,05 Hp. Daya motor :
0,05882Hp 85
, 0,05Hp
= =
: digunakan motor 0,06 Hp
LC.18 Reboiler RB-101
Jenis : shell and tube exchanger
Deskripsi :
Tabel LC.. Deskripsi
Reboiler
DESCRIPTION Unit
SHELL SIDE TUBE SIDE
Cold Fluid Hot Fluid
1
Fluid Type Camp. etanol
steam In Out In Out
Temperature T °C 92.61
97.23 200 200
2 °F
198.698 207 392 392 3
Total Flow W
kgh 5180.964 8813,20
lbh 11398.121 19389,04 kJh
21646,987 4
Total Heat Transfer Q
Btuh 20517,304
5
Pass
1 2
Length L
ft - 12
6 in
- 144
7 OD Tubes
in - 1
8
BWG -
10 9
Pitch Square
in - 1.25
Mencari Δt
1 2
1 2
t t
ln t
t LMTD
Δ Δ
Δ −
Δ =
Kern, 1965
F LMTD
o
190 198.698
392 207
392 ln
198.698 392
207 392
= ⎟⎟⎠
⎞ ⎜⎜⎝
⎛ −
− −
− −
=
Koreksi LMTD CMTD CMTD
Δt = LMTD × Ft
1 2
2 1
t t
T T
R −
− =
= 198.698
207 392
392 =
− −
1 1
1 2
t T
t t
S −
− =
= 0.04
198.698 392
198.698 207
= −
−
R = 0, maka Ft = 1 CMTD
Δt = 190 × 1 = 190 F
Caloric Temperature T
c
dan t
c
392 2
392 392
2 T
T T
2 1
c
= +
= +
=
F
202.85 2
198.698 207
2 t
t t
2 1
c
= +
= +
=
F
Menghitung jumlah tubes yang digunakan
Dari Tabel 8. Kern, 1965, reboiler untuk fluida dingin light organic dan fluida panas steam, diperoleh U
D
=100 – 200, faktor pengotor R
d
= 0,003 Diambil U
D
= 100 Btujam ⋅ft
2
⋅°F a. Luas permukaan untuk perpindahan panas,
2 D
ft 0798
, 1
190 100
20517,304 Δt
U Q
A =
× =
× =
Luas permukaan luar a ″ = 0.2618 ft
2
ft Tabel 10. Kern, 1965
Jumlah tube, 344
, ft
ft 0.2618
ft 12
ft 1,0798
a L
A N
2 2
t
= ×
= ×
= buah
Nilai terdekat adalah 16 buah dengan ID shell = 8 in Tabel 9. Kern, 1965 b. Koreksi U
D
Koefisien menyeluruh kotor t
A Q
U
D
Δ ⋅
= dimana,
Nt L
a A
× ×
=
A = 0.2618 × 12 × 2 = 6,2832 ft
2
186 ,
17 190
6,2832 20517,304 =
⋅ =
D
U Btu h ft
2
F Penentuan R
D
design:
1. Flow Area a
a. shell side
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