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Perancangan Reaktor Fixed Bed R-01: F P X Dix

This document summarizes the design of a fixed bed reactor (R-01). Key details include: 1) The reactor is designed to catalyze the reaction of triolein and methanol to produce M-oleate and glycerol with a conversion rate of 95%. 2) Design calculations determine the catalyst bed will be 5.245039 meters in diameter and 3 meters tall, containing 124,138 kg of catalyst. 3) Additional components include support plates, dividers, and inlet/outlet piping sized to accommodate a flow rate of 12,904 kg/hr. 4) The completed reactor design is 8.74824 meters tall with a volume of 38.42935

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Risky Andi
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146 views2 pages

Perancangan Reaktor Fixed Bed R-01: F P X Dix

This document summarizes the design of a fixed bed reactor (R-01). Key details include: 1) The reactor is designed to catalyze the reaction of triolein and methanol to produce M-oleate and glycerol with a conversion rate of 95%. 2) Design calculations determine the catalyst bed will be 5.245039 meters in diameter and 3 meters tall, containing 124,138 kg of catalyst. 3) Additional components include support plates, dividers, and inlet/outlet piping sized to accommodate a flow rate of 12,904 kg/hr. 4) The completed reactor design is 8.74824 meters tall with a volume of 38.42935

Uploaded by

Risky Andi
Copyright
© © All Rights Reserved
We take content rights seriously. If you suspect this is your content, claim it here.
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Download as XLSX, PDF, TXT or read online on Scribd
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PERANCANGAN REAKTOR FIXED BED R-01

diketahui
k 0.0028 Kmol/kgcat.hr konversi 0.95 1.69 lb/ft.jam
_0 14.41701 m^3/jam gc 32.174 lbm.ft/jam fluida 72.92 lb/ft^3
_0 11.9596 kmol/jam dp 0.01 ft
CaO 3350 kg/m^3 0.9

persamaan kecepatan reaksi


_= (
Triolein + 3Metanol 3M-Oleat + Gliserol
_) ^2

penyelesaian
=1/(_0/
_0 ^2 )
1_0^0,99/(1)^2 V bed 37.0562 m
T bed 3m 9.84 ft
L bed 5.245039 m
=(1/
((10,99) ))/(_0
/_0 ^2 )
86401
260.49796 m

Menghitnung preasure drop


5.2048657
1.3717421
2535 213.69743

Ac 21.606645838 m^2 232.48751 ft^2


m 12904.410978 kg/jam 28389.704 lb/jam
G 122.11281478 lb/jam.ft^2

dp 58874.900583 lb/ft^2 286346.11 kg/m2 27.718303 atm

Design Reaktor

Diameter bed katalis (Di) 5.2450391715 m 206.49772 inc


Tinggi bed katalis 3m 118.1103 inc
Konversi reaksi 0.95
Suhu masuk reactor 303 K 320.5
Suhu keluar reactor 338 K
Tekanan masuk reactor 29 atm 426.3 psi
Tekanan keluar reactor 1.2816968057 atm 18.840943 psi

Katalis
Densitas 3350 kg/m^3
volume bed 37.056201746 m^3
Berat Katalis 124138.27585 kg 273677.73 lb

support
A= 43.213291676 m^2
66980.602098 inc^2
P= 4.0859251355 psi
f= 18500 psi
t= 1.3288477586 inci
dipakai 1.5 inci 3 P
Dix x
16 f
Hold down Plate
A= 93772.8429371 inc2
Densitas 72.92 lb/ft2
P= 0.5063888889 psi
t= 0.4678128098 inc
dipakai 0.5 inc

Diiding reaktor
f= 18500
e= 0.8
c= 0.125
P design 228.657518674 psi
t= 1.7351030442 in Pxri
C
dipakai 1.75 in fx 0.6 xP

t= 1.7226458871 in PxDi
C
dipakai 1.75 in 2 xfx 0.2 xP

sf = 2.25
Tinggi head = 107.248858342 in 2.724121 meter

Tinggi reaktor 344.419046684 inc 8.7482438 meter

Volume reaktor 38.4293497904 m3


xDi 2 xDi
(( ) xL ( ))
4 12
xDi 2 xDi
(( ) xL ( ))
Diameter Pipa 4 12
Umpan
Rho masuk 1167.93249047 kg/m3
Rho keluar 920.924906815 kg/m3
G= 12904.4109776 kg/jam
3.5845586049 kg/s
Din 308.311701802 mm 0.3083117 meter 12.138263 in
Dout 315.725282551 mm 0.3157253 meter 12.430136 in
Dipakai Din 1214 60 Sch 20 NPS
Dout 12.5 60 Sch 24 NPS

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