reaktor fixed bed x
DESCRIPTION
panduan perhitungan fixed bedTRANSCRIPT
REAKTOR FIXED BED
PAGE 27
REAKTOR
Tugas =Mereaksikan Toluene dengan udara dengan kecepatann umpan masuk sebesar 16749,61871 kg/jam
Tipe Alat : Reaktor Fix Bed Multitulbular Kondisi operasi : T = 500 oC
P = 5 atm
NERACA MASSA
1. Umpan Masuk : C7H8
= 13,238 kmol/ jam = 1217,918 kg/jam
C6H6 = 0,142 kmol/jam = 11,085 kg/jam
C6H5CHO = 0,0115kmol/jam = 1,2169 kg/jam
O2
= 113,01 kmol/jam = 3616,171 kg/jam
N2 = 425,12kmol/jam = 11903,23 kg/jam +Total = 551,5125kmol/jam = 16749,61871 kg/jam
Reaksi : I. C7H8 + O2 ----------> C6H5CHO + H2O S1 = 0,5
II. C7H8 + 6 O2 ---------> C4H2O3 + 3H2O + 3 CO2 S2 = 0,5
III. C6H6 + 7,5 O2 ---------> 6 CO2 + 3 H2O
Katalis : molybdenum oxide dan uranium oxideKonversi : 0,9 (90 %) terhadap C7H8Reaksi bisa ditulis :
I. A + B -------> C + D
II. A + 6 B------->
E + 3 D + 3 F
III. A + 7,5 B ------->
6 F + 3 DMaka pada saat konversi =
REAKSI 1 :
( C7H8 ) =nAo (1 - XA)
(O2)= nBo - nAo X* (S1 + 6 S2) - 7,5 nGo
(C6H5CHO)= nCo + nAo X S1
(H2O) = nDo + nAo X ( S1 + 3 S2)
(C4H2O3)= nEo + nAo X S2
(CO2)= nFo + nAo X 3 S2REAKSI 3 :
(CO2)= nF + 6 nGo
(H2O) = nD + 3 nGo
Maka pada korversi = 0,9Maka diperoleh hasil reaksi :
C7H8
= 1,324 kmol/ jam = 121,792kg/jam
C6H5CHO= 5,969kmol/jam = 632,681kg/jam
O2
= 70,239kmol/jam = 2247,648kg/jam
N2
= 425,115kmol/jam = 11903,228kg/jam
H2O
= 24,255kmol/jam = 436,593kg/jam CO2
= 18,724kmol/jam = 823,871kg/jam
C4H2O3
= 5,957kmol/jam = 583,806kg/jam
Total
= 551,584kmol/jam = 16749,619kg/jamPENENTUAN KONSTANTA KECEPATAN REAKSI
Reaksi: I. C7H8 + O2 ----------> C6H5CHO + H2O
S1 = 0,5 II. C7H8 + 6 O2 ---------> C4H2O3 + 3H2O + 3 CO2 S2 = 0,5
III. C6H6 + 7,5 O2 ---------> 6 CO2 + 3 H2O
Reaksi diatas dapat disederhanakan menjadi:
I. A + B -------> C + D
II. A + 6 B------->
E + 3 D + 3 F
III. G + 7,5 B ------->
F + 3 D
Persamaan kece patan reaksinya dapat ditulis sebagai berikut:
Kinetika ReaksiReaksi pembentukan Benzene berdasarkan reaksi :
C7H8
+O2(C6H5CHO+H2O
Dari Patent diperoleh data sebagai berikut :
1. Waktu reaksi
=5 dtk
2. Suhu operasi
=500oC
3. Perbandingan mol reaktan C7H8 : O2= 1 : 9.473373
4. Konversi yang dapat dicapai
=0.2
Neraca massa
C7H8
+O2(C6H5CHO+H2O
A
B( C
+ D
Mula-mula: 100 947.3374
Reaksi
: 100 . A 100 . XA 100 . XA 100 . XAHasil
: 100 (1-XA) 947.3374 100 XA 100 . XA 100 . XA
Komposisi awal :
A=100
gmol
B=947.3374gmol
1047.3374
Tekanan=5atm
Suhu
=500oC
Untuk reactor RAP :
dXA
=0.02XA1/Yl
0.0000.2000010.200
0.0200.2049040.820
0.0400.2100120.420
0.0600.2153540.861
0.0800.2209320.442
0.1000.2267640.907
0.1200.2328620.466
0.1400.2392640.957
0.1600.2459720.492
0.1800.2530141.012
0.2000.2604210.260
6.837
Hasil integrasi
= 0.045580391Konsentrasi Awal A (S2)Cao
=
nAo
Pt
nT R T
=
100
5
1047.3374 (82.06 . 773)
=7.52614E-06
gmol/cm3Perbandingan reaktan :
M
=
nBo
nAo
= 9.473374Konversi :
XA
=
0.9
k
=
1
0.045580391
7.52614E-06 5
k
=1211.255209 cm3/gmol.dt
0
Setiap kenaikan suhu 10oC maka kecepatan reaksi menjadi 2 kali lipatnya :
T1=773 oK
(k1 =1211.255209(cm3/gmol)/dt
T2=783 oK
(k2 = 1514.1(cm3/gmol)/dt
Persamaan empiris Arhenius :
Atau
ln1211.255209
=ln A+
B
773
ln1211.255209
=ln A+
B
783
-0.223143551
=
-0.223143551
=B1.65219E-05
B
=-13505.96427
ln1211.255209
=ln A
+-13505.96427
773
7.099412463
=ln A
+-17.47214007
ln A
=24.57155253
A
=46912618686
A=46912618686
B=-13505.96427
kR1=46912618686
exp (-13505.96427 /T)(cm3/gmol) / dtPENYUSUNAN MODEL MATEMATIS PADA ELEMEN VOLUME
1. NERACA MASSA PADA ELEMEN VOLUME
FA z Z Z
FA z+z ZMasuk keluar = akumulasi
FA Z [ FA Z +Z+(-rA) dv ] =Acc
dV = A.Z
dimana A =
Neraca massa elemen volume juga meninjau ruang kosong diantara tumpukan katalis sehingga porositas () berpengaruh. Porositas () didapat dari Brown, fig.219 & 220.
Maka :
dV =
FA Z FA Z +Z-(-rA)
Z = 0
FA Z FA Z +Z
dimana FA = F A0(1-XA)
(FA = -FA0. (XA
(-rA) = kecepatan reaksi = k. CA. CB
CA
=
CB
=
Maka :
...(1)
Dimana :
Perubahan konversi persatuan panjang
Di = Diameter dalam
= porositas tumpukan katalis
F= Kecepatan molar A mula-mula 2. NERACA PANAS PADA ELEMEN VOLUME
T
z z
Qp
z
Masuk keluar = akumulasi
m.cp (Tz -To ) (m.cp (T Z+Z - To) + QR + QP ) = 0
QR= HR.nAO.XA
QP= U.A.T
= U..DO.z.(Ts - T)
m.cp ( T z -T Z+Z) - HR..nAO.XA - U..DO..z. (Ts - T) = 0
m.cp ( T Z - TZ+Z ) = HR..nAO..XA + U..DO. z. (Ts - T)
HR nAO XA +UDO (TS- T )
T Z T Z+Z =
m.Cp
Lim ( z ( 0
.... 2dimana :
dT/dZ = perubahan suhu persatuan panjang katalis
( HR
= panas reaksi
U = over all heat transfer coefficient
Do = diameter luar
T = suhu gas
Ts = suhu penelitian
(m.Cp = kapasitas panas
3. NERACA PANAS UNTUK PENDINGIN PADA ELEMEN VOLUME
Tinjauan : elemen panas
Masuk keluar = akumulasi
mp.Cpp. ( Ts Z+Z - To ) + Qp mp.Cpp. (( Ts Z - To ) = 0
Qp = U.A. T ; dimana : A = .Do.z. dan T = (T Ts)
Sehingga Qp = U.. Do.z. (T Ts)
mp. Cpp. (Ts Z+Z - Ts Z ) = - U.. Do.z. (T Ts)
: mp. Cpp. z
Ts Z+Z - Ts Z U.. Do. (T Ts)
= -
z m. Cpp
PENURUNAN TEKANAN ( PRESSURE DROP )
Penurunan tekanan dalam pipa yang berisi katalisator (fixed bed) menggunakan rumus 11.6 (Chapter 11, Rase) hal 492, Chemical Reactor Design for Process Plants.
fk= faktor friksi
gc= konstanta gravitasi
G= kecepatan aliran massa gas dalam pipa, g/cm3f= densitas gas, g/cm3Dp= diameter partikel katalisator, cm
= porositas tumpukan katalisator
= viskositas gas, g/cm.jam
Sehingga diperoleh 4 persamaan differensial simultan sebagai berikut :
1)
2)
3)
4)
Selanjutnya persamaan differensial simultan tersebut diatas diselesaikan dengan program computer dengan Metode Numeris Runge Kutta.OVERALL HEAT TRANSFER
1. Koefisien transfer panas pipa (hio)
Dari pers. 6-2, Kern diperoleh :
hio =
.(5)
Persamaan diatas berlaku untuk organic liquid, larutan aqueous, dan gas pada Re > 10.000
dimana :
Dp= diameter partikel katalis
Di = diameter dalam pipa
k = konduktivitas thermal
= viskositas gas
Cp= panas jenis gas
Gt= kecepatan massa per satuan luas
hi = koefisien transfer panas pipa dalam
hio = hi.
2. Koefisien transfer panas dinding pipa dalam shell ( ho)
Dari persamaan , Kern :
ho = .(6)
Persamaan diatas berlaku untuk Re antara 2000 1.000.000
dimana :
ho= koefisien transfer panas
De = diameter equivalent
Gp = kecepatan massa pendingin per satuan luas
(p = viskositas pendingin
kp = konduktivitas thermal pendingin
Cpp= panas spesifik pendingin
3. Overall heat transfer coefisient
Ud = overall transfer coefisient pada saat kotor
Uc = overall transfer coefisient pada saat bersih
Rd = faktor tahanan panas pengotor
Maka :
LAY OUT PIPA DALAM REAKTOR ( Kern, 1983, P. 139 )Pipa dalam reaktor disusun secara square pitch, dimana luas penampang 1 pipa menempati luasan sebesar Pt2.
1 pipa menempati luasan = Pt2maka luas total penampang reaktor ( over design 10%)
As = 1,1. Nt.Pt2dimana :
As = Luas penampang shell
Nt = jumlah pipa
Pt = pitch
Alasan penyusunan pipa secara square pitch :
1. mudah pembersihannya.
2. pressure drop kecil.
FLOW AREA DALAM SHELL
As = .(7)
dimana :
B = Jarak buffle, in
C = Clearance, in
Pt = Pitch, in
IDs = Diameter dalam shell, in
As = Flow area shell, in2Diameter EQUIVALEN (De)
Diameter equivalen dapat dipahami sebagai diameter dari area dalam shell, bila dipandang sebagai pipa ( Kern, 1983) p.139
De = =
De = .(8)
DIAMETER SHELL
Diameter shell yang dipakai untuk Nt pipa
Luas shell = As = 1,1.Nt.Pt2 =
Diameter shell :
IDs = ....(9)
KATALISATOR ( Rase, 1977 )
Katalisator yang digunakan berupa molybdenum oxide dan uranium oxide dengan :
Bentuk = pellet
Ukuran
D = 0,3175 cm
H = 0,3175 cm
Bulk density = 1106,13 kg/m3 Formula = PbO2 Mg
(SA, Miller Ernest, 1965)
DIAMETER PARTIKEL ( Dp )
Yaitu diameter partikel katalis yang ekuivalen dengan diameter bola dengan volume yang sama dengan volume katalis ( Rase, 1977, p.493 )
V kat =
=
= 0,025125 cm3V bola= V kat
V Bola =
Maka :
Dp =
=
= 0,36345 cm
PEMILIHAN PIPA
Dalam pemilihan pipa harus diperhatikan faktor perpindahan panas. Pengaruh bahan isian di dalam pipa terhadap koefisien transfer panas konveksi didelik oleh Colburn ( Smith,JM., p.571) dan diperoleh hubungan pengaruh rasio (Dp/Dt) atau perbandingan diameter katalis dengan diameter pipa dengan koefisien transfer panas pipa berisi katalis disbanding transfer panas konveksi pada pipa kosong.
Dp/Dt0.050.010.150.120.25
Hio/h5.5777.57.0
Dimana :
(Dp/Dt)=rasio diameter katalis per diameter pipa
(hio/h)= rasio koefisien transfer panas pipa berisi katalis disbanding koefisien transfer panas pada pipa kosong.
Dari data diatas diperoleh (hio/h)max terjadi pada 7,8 pada (Dp/Dt) = 0,15
= 2,42298 cmDipilih pipa dengan ukuran standar (Kern, table 11) :
NPs = 1 in
OD= 1,32 in
ID= 1,049 in
Sch= 40
JUMLAH PIPA ( Brown, 1950 )
Jumlah pipa ditentukan berdasarkan turbulensi gas dalam pipa berkatalis. Dalam suatu reaksi khusus terjadi tumbukan molekul yang optimum ( well mixed). Keadaan di atas terjadi bila pada keadaan turbulen yaitu bilangan Reynold diatas 3100.
Spherecity (( )=
Luas area bola= (. Dp2= 3,14. 0,36345
= 0,4148 cm2
Luas area katalis
= 0,4748 cm2maka ( =
Dari fig. 223 Brown diperoleh ( = 0,35
KECEPATAN MASSA MASUK REAKTOR
KomponenKgmol/jamKg/jam
O213.14431209.2717
C7H8124.52053984.6553
N2468.434213116.1572
C6H5CHO0.01231.2990
C6H60.139910.9158
Total606.251118322.2988
Kecepatan massa= 18322.2988 Kg/j
= 5089.5278 g/dt
BM rata-rata
= 30.22
Suhu Umpan (T)= 773 oK
Tekanan Umpan (P)= 2 atm
Densitas gas(rho)= 0.000953 g/cm3
Viskositas gas= 0.000973 g/cm dt
Digunakan pipa Standard
ID pipa = 1.049 in = 2.664 cm
OD pipa = 1.320 in = 3.353 cm
BWG = 16 in
A. Jumlah pipa maximum :
1. Menghitung Gt :
= 18866.13 Gt
Gt = 0.217321 g/cm2 dt
2. Menghitung Luas penampang pipa :
= 2.0063 cm2
3. Menghitung Luas penampang total :
= 23419.4434 cm2
Menghitung Jumlah pipa maximum :
= 11673.0938 pipa
B. Jumlah pipa minimum :
1. Menghitung Kecepatan maximum :
= 771.5457 cm/dt2. Menghitung Kecepatan Volume Umpan :
= 5341104.5000 cm3/dt
3. Menghitung Luas penampang total :
= 6922.6025 cm2 Menghitung Jumlah pipa minimum :
= 3450.4744 pipa
C. Jumlah pipa :
1. Menghitung Gt :
diambil bilangan Reynold (Re) = 7000
= 18866.13 Gt
Gt
= 7000 / 18866.13 g/cm2 dt
= 0.371035 g/cm2 dt
2. Menghitung Luas penampang pipa :
= 2.0063 cm2
3. Menghitung Luas penampang total :
= 13717.1025 cm2
Menghitung Jumlah pipa :
= 6837 pipa
SIFAT FISIS
a) Spesifik Heat
Cp = A + BT + CT2 +DT
KomponenCp ( joule/mol.K )
ABCD
O26,7130,879.10-64,170.10-6-2,544.10-9
N27,4400,324.10-26.400.10-6-2,790.10-9
CO24,7281,754.10-2-1,338.10-54,097.10-9
H2O7,7014,595.10-42,521.10-6-0,859.10-9
C4H2O3-3,1238,32.10-2-5,22.10-51,16.10-8
C7H8-5,8171,22.10-1-6,61.10-51,17.10-8
C6H6-8,1071,13.10-1-7,21.10-51,70.10-8
C6H5CHO-2,91,19.10-1-6,79.10-51,23.10-8
Cp = Cpi . yi
b) Viskositas
= A + BT + CT2
Komponen ( micropoise.K )
TcPc
O2154,649,8
N2126,233,5
CO2304,272,8
H2O647,3217,6
C4H2O3--
C7H8591,7406
C6H6562,1483
C6H5CHO69546
*Sumber: Robert C. Reid Sifat gas dan zat cair Gramedia Pustaka 1991
c) Konduktivitas Thermal
k = ((14,54 . T/Tc ) 5,14 )2/3 . Cp/i . 106
KomponenTcPc
O2154,649,8
N2126,233,5
CO2304,272,8
H2O647,3217,6
C4H2O3--
C7H8591,7406
C6H6562,1483
C6H5CHO69546
d) Sifat Pendingin
Cp = 0,509 Btu/lboK
= 0,40 micropoise.K
k = 0,68 Btu/jam.ft.oK
PANAS REAKSI
T
HT To
H298HT = H298 + Cp dT
KomponenHf
O20
N20
CO2-94,05
H2O-68,315
C4H2O3-112,08
C7H811,95
C6H619,82
C6H5CHO-8,79
*sumber: Dimana :
H298= Hfp HfR
= -205,02 -103,6
= -101,42 kjoule/mol
= -24239,38 kkal/kmol
Cp = + T + T2 = AP AR = BP BR
= CP CR
KomponenCp ( joule/mol.K )
ABCD
O26,7130,879.10-64,170.10-6-2,544.10-9
N27,4400,324.10-26.400.10-6-2,790.10-9
CO24,7281,754.10-2-1,338.10-54,097.10-9
H2O7,7014,595.10-42,521.10-6-0,859.10-9
C4H2O3-3,1238,32.10-2-5,22.10-51,16.10-8
C7H8-5,8171,22.10-1-6,61.10-51,17.10-8
C6H6-8,1071,13.10-1-7,21.10-51,70.10-8
C6H5CHO-2,91,19.10-1-6,79.10-51,23.10-8
= 64,374 ( 11,591 + 45,780 )
= 7,003 joule/mol.K
= 6,4776.10-2 ( 3,2301.10-1 + 2,1034.10-2 )
= 2,2286.10-2 joule/mol.K
= 3,5143.10-4 (-1,3067.10-4 + 1,2484.10-4 )
= 3,5726.10-4 joule/mol.K
Sehingga :
= = = -101,42 kjoule/mol + 7,003 ( 298 - 513 ) + + joule/molPenyelesaian persamaan defferensial secara numeris dengan metode Runge Kutta :
CLS
N = 6837 'jml pipa
MS = 15
Ptek = 2
'massa pendingin
C = 500 'suhu operasi
TC1 = C
TcC = C
D = 490 'suhu keluar
td0 = D
DOU = 1.32 * 2.54 'diameter luar pipa
DI = 1.049 * 2.54 'diameter dalam pipa
Pt = 1.25 * DOU 'pitch
CL = Pt - DOU 'clearence
DE = (4 * (Pt ^ 2 - (3.14 * DOU ^ 2 / 4))) / (3.14 * DOU) 'diameter aquivalen
Ass = N * Pt ^ 2 * 1.15 'luas penampang shell
ID = (4 * Ass / 3.14) ^ .5 'diameter dalam shell
BS = ID / 5 'jarak buffle
AT = 3.14 / 4 * DI ^ 2: 'luas penampang pipa
ASi = ID * CL * BS / Pt 'flow area dlm shell
PRINT " "
PRINT " R E A K T O R F I X E D B E D M U L T I T U B E "
PRINT " "
PRINT USING " Jumlah pipa = #### pipa"; N
PRINT USING " Diameter luar pipa = #.### cm"; DOU
PRINT USING " Diameter dalam pipa = #.### cm"; DI
PRINT USING " Pitch = #.### cm"; Pt
PRINT USING " Diameter Shell = #.### m"; ID / 100
PRINT USING " Jumlah pendingin = ######.### Kg/j"; MS * N * 3.6
PRINT 'MS * N * .373 * (536.6 - 504.8)
PRINT : PRINT : PRINT
Dp = .5723
BMB = 32 'O2
BMA = 92 'C7H8
BMC = 28 'N2
BMD = 18 'H20
BME = 106 'C6H5CHO
BMF = 78 'C6H6
BMG = 98 'C4H2O3
BMH = 44 'CO2
'KECEPATAN MASUK MASING-MASING GAS (KGMOL/JAM)
FAIO = 1209.2717# / BMA 'C7H8
FBIO = 3984.6553# / BMB 'O2
FCIO = 13116.1569# / BMC 'N2
FDIO = 0 / BMD 'H2O
FEIO = 1.299 / BME 'C6H5CHO
FFIO = 10.9158 / BMF 'C6H6
FGIO = 0 / BMG 'C4H2O3
FHIO = 0 / BMH 'CO2
FAo = FAIO / 3.6:
FBo = FBIO / 3.6:
FCo = FCIO / 3.6:
FDo = FDIO / 3.6:
FEo = FEIO / 3.6:
FFo = FFIO / 3.6:
FGo = FGIO / 3.6:
FHo = FHIO / 3.6:
FTO = FAo + FBo + FCo + FDo + FEo + FFo + FGo + FHo
bmrt = (FAo / FTO) * BMA + (FBo / FTO) * BMB + (FCo / FTO) * BMC + (FDo / FTO) * BMD + (FEo / FTO) * BME + (FFo / FTO) * BMF + (FGo / FTO) * BMG + (FHo / FTO) * BMH
GT = FTO * bmrt / AT: GS = MS * N / ASi
PRINT " KECEPATAN MASSA MASUK REAKTOR"
PRINT " "
PRINT " Komponen Kgmol /jam Kg / jam "
PRINT " "
PRINT USING " O2 #####.#### ######.#### "; FBIO; FBIO * BMB
PRINT USING " C7H8 #####.#### ######.#### "; FAIO; FAIO * BMA
PRINT USING " N2 #####.#### ######.#### "; FCIO; FCIO * BMC
PRINT USING " H2O #####.#### ######.#### "; FDIO; FDIO * BMD
PRINT USING " C6H5CHO #####.#### ######.#### "; FEIO; FEIO * BME
PRINT USING " C6H6 #####.#### ######.#### "; FFIO; FFIO * BMF
PRINT USING " C4H203 #####.#### ######.#### "; FGIO; FGIO * BMG
PRINT USING " CO2 #####.#### ######.#### "; FHIO; FHIO * BMH
PRINT " "
PRINT USING " Total #####.#### ######.#### "; FTO * 3.6; FTO * bmrt * 3.6
INPUT "", A$
PRINT " KECEPATAN MASSA GAS KELUAR REAKTOR"
XA = .9
XA1 = 1 / .9 * XA
S1 = .5
S2 = .5
FA = FAo * (1 - XA) 'C7H8
FB = FBo - FAo * XA * (S1 + 6 * S2) - 7.5 * FFo * XA1 'O2
FC = FCo 'N2
FD = FDo + FAo * XA * (S1 + 3 * S2) + 3 * FFo * XA1 'H2O
FE = FEo + FAo * XA * S1 'C6H5CHO
FF = FFo - FFo * XA1 'C6H6
FG = FGo + FAo * XA * S2 'C4H2O3
FH = FHo + 3 * FAo * XA * S2 + 6 * FFo * XA1 'CO2
FT = FA + FB + FC + FD + FE + FF + FG + FH + FI
YA = FA / FT: YB = FB / FT: YC = FC / FT: YD = FD / FT: YE = FE / FT:
YF = FF / FT: YG = FG / FT: YH = FH / FT: YI = FI / FT
m = BMA * YA + BMB * YB + BMC * YC + BMD * YD + BME * YE + BMF * YF + BMG * YG + BMH * YH + BMI * YI
PRINT " "
PRINT " Komponen Kgmol /jam Kg / jam "
PRINT " "
PRINT USING " O2 #####.#### ######.#### "; FB * 3.6; FB * 3.6 * BMB
PRINT USING " C7H8 #####.#### ######.#### "; FA * 3.6; FA * 3.6 * BMA
PRINT USING " N2 #####.#### ######.#### "; FC * 3.6; FC * 3.6 * BMC
PRINT USING " H2O #####.#### ######.#### "; FD * 3.6; FD * 3.6 * BMD
PRINT USING " C6H5CHO #####.#### ######.#### "; FE * 3.6; FE * 3.6 * BME
PRINT USING " C6H6 #####.#### ######.#### "; FF * 3.6; FF * 3.6 * BMF
PRINT USING " C4H2O3 #####.#### ######.#### "; FG * 3.6; FG * 3.6 * BMG
PRINT USING " CO2 #####.#### ######.#### "; FH * 3.6; FH * 3.6 * BMH
PRINT " "
PRINT USING " Total #######.#### ######.#### "; FT * 3.6; FT * 3.6 * m
INPUT "", A$
PRINT " Enthalpi Umpan Masuk Reaktor :"
m = bmrt
FA = FAo
FB = FBo
FC = FCo
FD = FDo
FE = FEo
FF = FFo
FG = FGo
FH = FHo
GOSUB 7000
Qo1 = QTOT
INPUT "", P$
PRINT " Reaksi yang terjadi :"
PRINT " C7H8 + O2 -----------> C6H5CHO + H2O"
PRINT " C7H8 + 6 O2 -----------> C4H2O3 + 3 H2O + 3 CO2 "
PRINT " C6H6 + 7.5 O2 -----------> 6 CO2 + 3 H2O"
INPUT "", A$
PRINT : PRINT " KONDISI AWAL"
A = 0: B = 0: E = Ptek: F = 1
E1 = E
PRINT " "
PRINT USING " Suhu gas masuk = ###.# C "; C
PRINT USING " Suhu pendingin keluar = ###.# C "; D
PRINT USING " Tekanan awal = ##.# atm "; E
PRINT USING " Increment tebal katalis = #.## cm "; F
PRINT " "
PRINT : INPUT "", P$
' Perhitungan RUNGA KUTTA
PRINT " "
PRINT " L(cm) Xa T(c) Td (c) P(atm) "
PRINT " "
PRINT USING " #### #.#### ###.## ###.# ##.### "; A; B; C; D; E
NO = 0
620 GA = A: GB = B: GC = C: GD = D: GE = E: GF = F: GG = G: GH = H
GOSUB 910
K1 = DX * F
L1 = T * F
EM1 = S * F
N1 = P * F
GB = B + K1
GC = C + L1
GD = D + EM1
GE = E + N1
GOSUB 910
K2 = DX * F
L2 = T * F
EM2 = S * F
N2 = P * F
GB = B + (K2 / 2)
GC = C + (L2 / 2)
GD = D + (EM2 / 2)
GE = E + (N2 / 2)
GOSUB 910
K3 = DX * F
L3 = T * F
EM3 = S * F
N3 = P * F
GB = B + (K3 / 2)
GC = C + (L3 / 2)
GD = D + (EM3 / 2)
GE = E + (N3 / 2)
GOSUB 910
K4 = DX * F
L4 = T * F
EM4 = S * F
N4 = P * F
GB2 = B + 1 / 6 * (K1 + 2 * K2 + 2 * K3 + K4)
GC2 = C + 1 / 6 * (L1 + 2 * L2 + 2 * L3 + L4)
GD2 = D + 1 / 6 * (EM1 + 2 * EM2 + 2 * EM3 + EM4)
GE2 = E + 1 / 6 * (N1 + 2 * N2 + 2 * N3 + N4)
710 A = A + F
C = GC2
B = GB2
D = GD2
E = GE2
NO = NO + 1
Qre = Q1 * F * N + Qre
Ql = Q2 * F * N + Ql
790 IF B >= .9 THEN 870
IF NO = 10 THEN 800
GOTO 620
800 PRINT USING " #### #.#### ###.## ###.# ##.### "; A; B; C; D; E: NO = 0
860 GOTO 620
870 PRINT USING " #### #.#### ###.## ###.# ##.### "; A; B; C; D; E
PRINT " "
PRINT " KECEPATAN MASSA GAS KELUAR REAKTOR"
XA = .9
XA1 = 1 / .9 * XA
S1 = .5
S2 = .5
FA = FAo * (1 - XA) 'C7H8
FB = FBo - FAo * XA * (S1 + 6 * S2) - 7.5 * FFo * XA1 'O2
FC = FCo 'N2
FD = FDo + FAo * XA * (S1 + 3 * S2) + 3 * FFo * XA1 'H2O
FE = FEo + FAo * XA * S1 'C6H5CHO
FF = FFo - FFo * XA1 'C6H6
FG = FGo + FAo * XA * S2 'C4H2O3
FH = FHo + 3 * FAo * XA * S2 + 6 * FFo * XA1 'CO2
FT = FA + FB + FC + FD + FE + FF + FG + FH + FI
YA = FA / FT: YB = FB / FT: YC = FC / FT: YD = FD / FT: YE = FE / FT:
YF = FF / FT: YG = FG / FT: YH = FH / FT: YI = FI / FT
m = BMA * YA + BMB * YB + BMC * YC + BMD * YD + BME * YE + BMF * YF + BMG * YG + BMH * YH + BMI * YI
PRINT " "
PRINT " Komponen Kgmol /jam Kg / jam "
PRINT " "
PRINT USING " O2 #####.#### ######.#### "; FB * 3.6; FB * 3.6 * BMB
PRINT USING " C7H8 #####.#### ######.#### "; FA * 3.6; FA * 3.6 * BMA
PRINT USING " N2 #####.#### ######.#### "; FC * 3.6; FC * 3.6 * BMC
PRINT USING " H2O #####.#### ######.#### "; FD * 3.6; FD * 3.6 * BMD
PRINT USING " C6H5CHO #####.#### ######.#### "; FE * 3.6; FE * 3.6 * BME
PRINT USING " C6H6 #####.#### ######.#### "; FF * 3.6; FF * 3.6 * BMF
PRINT USING " C4H2O3 #####.#### ######.#### "; FG * 3.6; FG * 3.6 * BMG
PRINT USING " CO2 #####.#### ######.#### "; FH * 3.6; FH * 3.6 * BMH
PRINT " "
PRINT USING " Total #######.#### ######.#### "; FT * 3.6; FT * 3.6 * m
INPUT "", A$
PRINT " Enthalpi Hasil reaksi :"
GOSUB 7000
Qo2 = QTOT
INPUT "", A$
PRINT " NERACA PANAS :"
PRINT " MASUK : KELUAR : "
PRINT " 1. Enthalpi Umpan Masuk Reaktor 1. Enthalpi hasil reaksi:"
PRINT USING " Qs1 = #########.#### Kcal/jam Qs2 = #########.#### Kcal/jam"; Qo1; Qo2
Qll = Qo1 + (Qre * 3.6) - Qo2
Qp = MS * N * 3.6 * .373 * (td0 - D)
Qloss = Qll - Qp
PRINT " 2. Panas Reaksi 2. Panas dibawa pendingin"
PRINT USING " Qr = #########.#### Kcal/jam Qp = #########.#### Kcal/jam"; Qre * 3.6; Qp
PRINT " 3. Panas Hilang"
PRINT USING " Qloss = #########.#### Kcal/jam"; Qloss
tpIN = td0 - (Ql - Qloss) / (MS * 3.6 * N * .373)
PRINT " -------------------------------- --------------------------------- "
PRINT USING " #########.#### Kcal/jam #########.#### Kcal/jam"; Qo1 + Qre * 3.6; (Qo2 + Qp + Qloss)
INPUT "", A$
PRINT " Dari hasil perhitungan Reaktor diperoleh :"
PRINT USING " Jumlah pipa = #### pipa"; N
PRINT USING " Diameter Shell = #.### m"; ID / 100
PRINT USING " Jumlah pendingin = ###### Kg/j"; MS * N * 3.6
PRINT USING " Panjang terhitung = ###.# m"; A / 100
PRINT USING " = ###.# ft"; A / 100 / .3048
HH = 40
PRINT USING " Panjang Pipa = ###.# m"; HH * .3048
PRINT USING " = ###.# ft"; HH
PRINT USING " Tinggi Head reaktor = #.### m"; ID / 100 / 2
PRINT USING " Tinggi reaktor = ##.### + 2 . #.### m"; HH * .3048; ID / 100 / 2
PRINT USING " = ###.# m"; HH * .3048 + ID / 100 / 2
CLOSE
900 END
910 'KOMPOSISI GAS (GMOL/JAM)
XA = GB
XA1 = 1 / .2 * XA
S1 = .5
S2 = .5
FA = FAo * (1 - XA) 'C7H8
FB = FBo - FAo * XA * (S1 + 6 * S2) - 7.5 * FFo * XA1 'O2
FC = FCo 'N2
FD = FDo + FAo * XA * (S1 + 3 * S2) + 3 * FFo * XA1 'H2O
FE = FEo + FAo * XA * S1 'C6H5CHO
FF = FFo - FFo * XA1 'C6H6
FG = FGo + FAo * XA * S2 'C4H2O3
FH = FHo + 3 * FAo * XA * S2 + 6 * FFo * XA1 'CO2
FT = FA + FB + FC + FD + FE + FF + FG + FH + FI
YA = FA / FT: YB = FB / FT: YC = FC / FT: YD = FD / FT: YE = FE / FT:
YF = FF / FT: YG = FG / FT: YH = FH / FT: YI = FI / FT
m = BMA * YA + BMB * YB + BMC * YC + BMD * YD + BME * YE + BMF * YF + BMG * YG + BMH * YH + BMI * YI
'KAPASITAS PANAS GAS (CAL/GMOL.K) (Reid,1979)
CPA = 6.713 + -8.79E-07 * (GC + 273) + 4.17E-06 * (GC + 273) ^ 2 + -2.54E-09 * (GC + 273) ^ 3
CPB = -5.817 + .122 * (GC + 273) + -.0000661 * (GC + 273) ^ 2 + 1.17E-08 * (GC + 273) ^ 3
CPC = 7.44 + -.00324 * (GC + 273) + .0000064 * (GC + 273) ^ 2 + -2.79E-09 * (GC + 273) ^ 3
CPD = 7.701 + .00046 * (GC + 273) + 2.52E-06 * (GC + 273) ^ 2 + -8.59E-10 * (GC + 273) ^ 3
CPE = 2.9 + .119 * (GC + 273) + -.0000679 * (GC + 273) ^ 2 + 1.23E-08 * (GC + 273) ^ 3
CPF = 8.107 + .113 * (GC + 273) + -.0000721 * (GC + 273) ^ 2 + 1.7E-08 * (GC + 273) ^ 3
CPG = -3.123 + .0832 * (GC + 273) + -.0000522 * (GC + 273) ^ 2 + 1.16E-08 * (GC + 273) ^ 3
CPH = 4.728 + .0175 * (GC + 273) + -.0000134 * (GC + 273) ^ 2 + 4.1E-09 * (GC + 273) ^ 3
CPM = (YA * CPA + YB * CPB + YC * CPC + YD * CPD + YE * CPE + YF * CPF + YG * CPG + YH * CPH + YI * CPI) / m
'KAPASITAS pendingin (CAL/GMOL.K)
CPP = .373
'RAPAT MASSA CAMPURAN GAS
RM = E * m / (GC + 273) / 82.06
'VISKOSITAS GAS (gr/dt.cm)
TcA = 154.6: PcA = 49.8
TcB = 591.7: PcB = 40.6
TcC = 126.2: PcC = 33.5
TcD = 647.3: PcD = 217.6
TcE = 695: PcE = 46
TcF = 562.1: PcF = 483
TcG = 500: PcG = 20
TcH = 304.2: PcH = 72.8
VA = (.00036 * (4.61 * ((GC + 273) / TcA) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcA)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcA)) + .1) / (TcA ^ (1 / 6) * BMA ^ (-.5) * PcA ^ (-2 / 3))) / 100
VB = (.00036 * (4.61 * ((GC + 273) / TcB) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcB)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcB)) + .1) / (TcB ^ (1 / 6) * BMB ^ (-.5) * PcB ^ (-2 / 3))) / 100
VC = (.00036 * (4.61 * ((GC + 273) / TcC) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcC)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcC)) + .1) / (TcC ^ (1 / 6) * BMC ^ (-.5) * PcC ^ (-2 / 3))) / 100
VD = (.00036 * (4.61 * ((GC + 273) / TcD) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcD)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcD)) + .1) / (TcD ^ (1 / 6) * BMD ^ (-.5) * PcD ^ (-2 / 3))) / 100
VE = (.00036 * (4.61 * ((GC + 273) / TcE) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcE)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcE)) + .1) / (TcE ^ (1 / 6) * BME ^ (-.5) * PcE ^ (-2 / 3))) / 100
VF = (.00036 * (4.61 * ((GC + 273) / TcF) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcF)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcF)) + .1) / (TcF ^ (1 / 6) * BMF ^ (-.5) * PcF ^ (-2 / 3))) / 100
VG = (.00036 * (4.61 * ((GC + 273) / TcG) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcG)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcG)) + .1) / (TcG ^ (1 / 6) * BMG ^ (-.5) * PcG ^ (-2 / 3))) / 100
VH = (.00036 * (4.61 * ((GC + 273) / TcG) ^ .618 - 2.04 * EXP(-.449 * ((GC + 273) / TcG)) + 1.94 * EXP(-4.058 * ((GC + 273) / TcG)) + .1) / (TcG ^ (1 / 6) * BMG ^ (-.5) * PcG ^ (-2 / 3))) / 100
VM = YA * VA * SQR(BMA) + YB * VB * SQR(BMB) + YC * VC * SQR(BMC)
VM = VM + YD * VD * SQR(BMD) + YE * VE * SQR(BME) + YF * VF * SQR(BMF)
VM = VM + YG * VG * SQR(BMG) + YH * VH * SQR(BMH) + YI * VI * SQR(BMI)
VBAH = YA * SQR(BMA) + YB * SQR(BMB) + YC * SQR(BMC)
VBAH = VBAH + YD * SQR(BMD) + YE * SQR(BME) + YF * SQR(BMF)
VBAH = VBAH + YG * SQR(BMG) + YH * SQR(BMH) + YI * SQR(BMI)
VR = VM / VBAH
'VISKOSITAS pendingin (gr/dt.cm)
VP = (35.5898 - .04212 * D) * .01
'THERMAL KONDUKTIVITAS (Cal/dt.cm.K)
TIA = TcA ^ (1 / 6) * BMA ^ (1 / 2) / PcA ^ (2 / 3)
TIB = TcB ^ (1 / 6) * BMB ^ (1 / 2) / PcB ^ (2 / 3)
TIC = TcC ^ (1 / 6) * BMC ^ (1 / 2) / PcC ^ (2 / 3)
TID = TcD ^ (1 / 6) * BMD ^ (1 / 2) / PcD ^ (2 / 3)
TIE = TcE ^ (1 / 6) * BME ^ (1 / 2) / PcE ^ (2 / 3)
TIF = TcF ^ (1 / 6) * BMF ^ (1 / 2) / PcF ^ (2 / 3)
TIG = TcG ^ (1 / 6) * BMG ^ (1 / 2) / PcG ^ (2 / 3)
TIH = TcG ^ (1 / 6) * BMG ^ (1 / 2) / PcG ^ (2 / 3)
jp = .000001
KA = ((14.52 * (GC + 273) / TcA) - 5.14) ^ (2 / 3) * (jp / TIA) * CPA
KB = ((14.52 * (GC + 273) / TcB) - 5.14) ^ (2 / 3) * (jp / TIB) * CPB
KC = ((14.52 * (GC + 273) / TcC) - 5.14) ^ (2 / 3) * (jp / TIC) * CPC
KD = ((14.52 * (GC + 273) / TcD) - 5.14) ^ (2 / 3) * (jp / TID) * CPD
KE = ((14.52 * (GC + 273) / TcE) - 5.14) ^ (2 / 3) * (jp / TIE) * CPE
KF = ((14.52 * (GC + 273) / TcF) - 5.14) ^ (2 / 3) * (jp / TIF) * CPF
KG = ((14.52 * (GC + 273) / TcG) - 5.14) ^ (2 / 3) * (jp / TIG) * CPG
KH = ((14.52 * (GC + 273) / TcG) - 5.14) ^ (2 / 3) * (jp / TIG) * CPG
KM = YA * KA * (BMA ^ .333) + YB * KB * (BMB ^ .333) + YC * KC * (BMC ^ .333)
KM = KM + YF * KF * (BMF ^ .333) + YD * KD * (BMD ^ .333) + YE * KE * (BME ^ .333)
KM = KM + YG * KG * (BMG ^ .333) + YH * KH * (BMH ^ .333) + YI * KI * (BMI ^ .333)
BAWAH = YA * (BMA ^ .333) + YB * (BMB ^ .333) + YC * (BMC ^ .333)
BAWAH = BAWAH + YD * (BMD ^ .333) + YE * (BME ^ .333) + YF * (BMF ^ .333)
BAWAH = BAWAH + YG * (BMG ^ .333) + YH * (BMH ^ .333) + YI * (BMI ^ .333)
KM = KM / BAWAH
'KONDUKTIVITAS pendingin (CAL/JAM.M.K)
KP = (.84333 - .0005807 * (GD + 273))
'PERHITUNGAN KOEFISIEN TRANSFER PANAS
RE = 50 * GT / N * Dp / VR
HI = (.27 * KM * (RE) ^ .8 * (CPM * VR / KM) ^ (1 / 3)) / DI
HI = 7.8 * HI
HIO = HI * DI / DOU
Rs = DE * GS / VP
PR = CPP * VP / KP
HO = .46 * KP / DE * Rs ^ .55 * PR ^ .333
UC = (HIO * HO) / (HIO + HO)
UD = UC / (11.06557 * UC + 1) / 100
'KECEPATAN REAKSI DAN PANAS REAKS
kx = 4691261868600# * EXP(-13505.96427# / (GC + 273))
'PANAS REAKSI
HR1 = -79310 + 3.905 * ((GC + 273) - 298)
HR1 = HR1 + (1 / 2) * (-.00344) * ((GC + 273) ^ 2 - 298 ^ 2)
HR1 = HR1 + (1 / 3) * (-3.539E-06) * ((GC + 273) ^ 3 - 298 ^ 3)
HR1 = HR1 + (1 / 4) * (2.295E-09) * ((GC + 273) ^ 4 - 298 ^ 4)
HR2 = -579550 + -.297 * ((GC + 273) - 298)
HR2 = HR2 + (1 / 2) * (.0148) * ((GC + 273) ^ 2 - 298 ^ 2)
HR2 = HR2 + (1 / 3) * (-4.372E-05) * ((GC + 273) ^ 3 - 298 ^ 3)
HR2 = HR2 + (1 / 4) * (2.481E-08) * ((GC + 273) ^ 4 - 298 ^ 4)
HR3 = -757490 + 9.2305 * ((GC + 273) - 298)
HR3 = HR3 + (1 / 2) * (-.00667) * ((GC + 273) ^ 2 - 298 ^ 2)
HR3 = HR3 + (1 / 3) * (-3.193E-05) * ((GC + 273) ^ 3 - 298 ^ 3)
HR3 = HR3 + (1 / 4) * (2.406E-08) * ((GC + 273) ^ 4 - 298 ^ 4)
HR = .75 * HR1 + .2 * HR2 + .05 * HR3
'PERSAMAAN DIFFERENSIAL
' (dx/dz)
RR = 82.06
TT = GC + 273
MM = FBo / FAo
CA0 = FAo / FTO * E1 / RR / TT
RC = kx * CA0 ^ 2 * (1 - GB) * (MM - GB)
DX = (3.14 * DI ^ 2 * RC * .36) / (4 * (FAo / N))
' (dT/dz)
Q1 = (-HR) * DX * FAo / N ' (cal/gmol) (1/cm) (gmol/dt) = cal/dt cm
Q2 = (UD * 3.14 * DOU * (GC - GD)) ' (cal/cm2 oC dt) (cm) (oC) = cal/dt cm
MCPR = FA * CPA + FB * CPB + FC * CPC + FD * CPD + FE * CPE + FF * CPF + FG * CPG + FH * CPH
T = (Q1 - Q2) / (MCPR / N)
' (dTs/dz)
S = -((UD * 3.14 * DOU * (GC - GD)) / (MS * CPP))
' (dP/dz)
fk = (150 * (1 - .36) / RE + 1.75) / 10000
P = (GT / N) ^ 2 * (1 - .36) * fk
P = -.00001 '((P / ((Dp) * (RM) * 981 * .36 ^ 3)))
RETURN
7000
FT = FA + FB + FC + FD + FE + FF + FG + FH
TC = C
GOSUB 8000
RETURN
8000
XX = (TC + 273) - 298
YY = (TC + 273) ^ 2 - 298 ^ 2
ZZ = (TC + 273) ^ 3 - 298 ^ 3
WW = (TC + 273) ^ 4 - 298 ^ 4
CPA = 6.713 * XX + -8.79E-07 / 2 * YY + 4.17E-06 / 3 * ZZ + -2.54E-09 / 4 * WW
CPB = -5.817 * XX + .122 / 2 * YY + -.0000661 / 3 * ZZ + 1.17E-08 / 4 * WW
CPC = 7.44 * XX + -.00324 / 2 * YY + .0000064 / 3 * ZZ + -2.79E-09 / 4 * WW
CPD = 7.701 * XX + .00046 / 2 * YY + 2.52E-06 / 3 * ZZ + -8.59E-10 / 4 * WW
CPE = 2.9 * XX + .119 / 2 * YY + -.0000679 / 3 * ZZ + 1.23E-08 / 4 * WW
CPF = 8.107 * XX + .113 / 2 * YY + -.0000721 / 3 * ZZ + 1.7E-08 / 4 * WW
CPG = -3.123 * XX + .0832 / 2 * YY + -.0000522 / 3 * ZZ + 1.16E-08 / 4 * WW
CPH = 4.728 * XX + .0175 / 2 * YY + -.0000134 / 3 * ZZ + 4.1E-09 / 4 * WW
QS1 = FA * CPA * 3.6
QS2 = FB * CPB * 3.6
QS3 = FC * CPC * 3.6
QS4 = FD * CPD * 3.6
QS5 = FE * CPE * 3.6
QS6 = FF * CPF * 3.6
QS7 = FG * CPG * 3.6
QS7 = FH * CPG * 3.6
QTOT = QS1 + QS2 + QS3 + QS4 + QS5 + QS6 + QS7 + QS8
PRINT USING " Suhu operasi = ###.## C"; TC
PRINT " Suhu refferensi = 25 C "
PRINT " "
PRINT " Komponen Kgmol /jam Cp dT Qs = m Cp dT "
PRINT " "
PRINT USING " O2 #####.#### #####.## ########.#### "; FA * 3.6; CPA; QS1
PRINT USING " C7H8 #####.#### #####.## ########.#### "; FB * 3.6; CPB; QS2
PRINT USING " N2 #####.#### #####.## ########.#### "; FC * 3.6; CPC; QS3
PRINT USING " H2O #####.#### #####.## ########.#### "; FD * 3.6; CPD; QS4
PRINT USING " C6H5CHO #####.#### #####.## ########.#### "; FE * 3.6; CPE; QS5
PRINT USING " C6H6 #####.#### #####.## ########.#### "; FF * 3.6; CPF; QS6
PRINT USING " C4H2O3 #####.#### #####.## ########.#### "; FG * 3.6; CPG; QS7
PRINT USING " CO2 #####.#### #####.## ########.#### "; FH * 3.6; CPH; QS8
PRINT " "
PRINT USING " Total #######.#### ########.#### "; FT * 3.6; QTOT
RETURN
Hasil Running Program computer
R E A K T O R F I X E D B E D M U L T I T U B E
Jumlah pipa = 6837 pipa
Diameter luar pipa = 3.353 cm
Diameter dalam pipa = 2.664 cm
Pitch = 4.191 cm
Diameter Shell = 4.194 m
Jumlah pendingin = 369198.000 Kg/j
KECEPATAN MASSA MASUK REAKTOR
Komponen Kgmol /jam Kg / jam
O2 124.5205 3984.6553
C7H8 13.1443 1209.2717
N2 468.4342 13116.1572
H2O 0.0000 0.0000
C6H5CHO 0.0123 1.2990
C6H6 0.1399 10.9158
C4H203 0.0000 0.0000
CO2 0.0000 0.0000
Total 606.2511 18322.2988
KECEPATAN MASSA GAS KELUAR REAKTOR
Komponen Kgmol /jam Kg / jam
O2 82.0665 2626.1272
C7H8 1.3144 120.9272
N2 468.4342 13116.1563
H2O 24.0795 433.4310
C6H5CHO 5.9272 628.2800
C6H6 0.0000 0.0000
C4H2O3 5.9149 579.6617
CO2 18.5844 817.7147
Total 606.3211 18322.2988
Enthalpi Umpan Masuk Reaktor :
Suhu operasi = 500.00 C
Suhu refferensi = 25 C
Komponen Kgmol /jam Cp dT Qs = m Cp dT
O2 13.1443 3571.98 46951.0313
C7H8 124.5205 19696.54 2452622.0000
N2 468.4342 3395.24 1590446.2500
H2O 0.0000 4065.76 0.0000
C6H5CHO 0.0123 22865.14 280.2058
C6H6 0.1399 23612.95 3304.5408
C4H2O3 0.0000 13115.67 0.0000
CO2 0.0000 5110.12 0.0000
Total 606.2511 4093604.0000
Reaksi yang terjadi :
C7H8 + O2 -----------> C6H5CHO + H2O
C7H8 + 6 O2 -----------> C4H2O3 + 3 H2O + 3 CO2
C6H6 + 7.5 O2 -----------> 6 CO2 + 3 H2O
KONDISI AWAL
Suhu gas masuk = 500.0 C
Suhu pendingin keluar = 490.0 C
Tekanan awal = 2.0 atm
Increment tebal katalis = 1.00 cm
L(cm) Xa T(c) Td (c) P(atm)
0 0.0000 500.00 490.0 2.000
10 0.0208 504.25 489.9 2.000
20 0.0428 508.35 489.8 2.000
30 0.0661 512.33 489.6 2.000
40 0.0905 516.15 489.4 2.000
50 0.1159 519.82 489.1 1.999
60 0.1422 523.32 488.9 1.999
70 0.1693 526.63 488.6 1.999
80 0.1971 529.73 488.2 1.999
90 0.2254 532.60 487.9 1.999
100 0.2540 535.20 487.5 1.999
110 0.2826 537.52 487.1 1.999
120 0.3111 539.52 486.6 1.999
130 0.3394 541.18 486.2 1.999
140 0.3671 542.49 485.7 1.999
150 0.3940 543.41 485.2 1.998
160 0.4201 543.95 484.7 1.998
170 0.4451 544.11 484.2 1.998
180 0.4690 543.89 483.7 1.998
190 0.4916 543.31 483.2 1.998
200 0.5130 542.39 482.7 1.998
210 0.5330 541.16 482.2 1.998
220 0.5517 539.65 481.8 1.998
230 0.5691 537.91 481.3 1.998
240 0.5852 535.97 480.8 1.998
250 0.6002 533.87 480.4 1.997
260 0.6141 531.65 479.9 1.997
270 0.6269 529.34 479.5 1.997
280 0.6388 526.98 479.1 1.997
290 0.6498 524.59 478.7 1.997
300 0.6599 522.21 478.4 1.997
310 0.6694 519.85 478.0 1.997
320 0.6782 517.53 477.7 1.997
330 0.6864 515.27 477.4 1.997
340 0.6940 513.07 477.1 1.997
350 0.7011 510.95 476.8 1.996
360 0.7078 508.92 476.5 1.996
370 0.7141 506.97 476.2 1.996
380 0.7201 505.12 476.0 1.996
390 0.7257 503.35 475.8 1.996
400 0.7310 501.68 475.5 1.996
410 0.7360 500.10 475.3 1.996
420 0.7408 498.60 475.1 1.996
430 0.7454 497.19 475.0 1.996
440 0.7498 495.87 474.8 1.996
450 0.7539 494.62 474.6 1.995
460 0.7579 493.45 474.5 1.995
470 0.7618 492.36 474.3 1.995
480 0.7655 491.33 474.2 1.995
490 0.7691 490.36 474.0 1.995
500 0.7725 489.46 473.9 1.995
510 0.7759 488.61 473.8 1.995
520 0.7791 487.82 473.7 1.995
530 0.7823 487.08 473.5 1.995
540 0.7853 486.39 473.4 1.995
550 0.7883 485.74 473.3 1.994
560 0.7912 485.13 473.2 1.994
570 0.7940 484.56 473.1 1.994
580 0.7967 484.02 473.0 1.994
590 0.7994 483.52 473.0 1.994
600 0.8020 483.04 472.9 1.994
610 0.8045 482.60 472.8 1.994
620 0.8070 482.18 472.7 1.994
630 0.8095 481.79 472.6 1.994
640 0.8119 481.42 472.6 1.994
650 0.8142 481.07 472.5 1.993
660 0.8165 480.74 472.4 1.993
670 0.8187 480.42 472.4 1.993
680 0.8209 480.13 472.3 1.993
690 0.8231 479.85 472.2 1.993
700 0.8252 479.58 472.2 1.993
710 0.8273 479.33 472.1 1.993
720 0.8294 479.09 472.1 1.993
730 0.8314 478.86 472.0 1.993
740 0.8334 478.64 472.0 1.993
750 0.8354 478.43 471.9 1.992
760 0.8373 478.23 471.9 1.992
770 0.8392 478.04 471.8 1.992
780 0.8410 477.85 471.8 1.992
790 0.8429 477.68 471.7 1.992
800 0.8447 477.51 471.7 1.992
810 0.8464 477.34 471.6 1.992
820 0.8482 477.18 471.6 1.992
830 0.8499 477.03 471.5 1.992
840 0.8516 476.89 471.5 1.992
850 0.8533 476.74 471.4 1.991
860 0.8549 476.61 471.4 1.991
870 0.8566 476.47 471.3 1.991
880 0.8582 476.34 471.3 1.991
890 0.8598 476.22 471.3 1.991
900 0.8613 476.10 471.2 1.991
910 0.8629 475.98 471.2 1.991
920 0.8644 475.86 471.2 1.991
930 0.8659 475.75 471.1 1.991
940 0.8673 475.64 471.1 1.991
950 0.8688 475.54 471.0 1.990
960 0.8702 475.43 471.0 1.990
970 0.8717 475.33 471.0 1.990
980 0.8731 475.23 470.9 1.990
990 0.8744 475.13 470.9 1.990
1000 0.8758 475.04 470.9 1.990
1010 0.8771 474.95 470.8 1.990
1020 0.8785 474.85 470.8 1.990
1030 0.8798 474.76 470.8 1.990
1040 0.8811 474.68 470.7 1.990
1050 0.8823 474.59 470.7 1.989
1060 0.8836 474.51 470.7 1.989
1070 0.8849 474.42 470.6 1.989
1080 0.8861 474.34 470.6 1.989
1090 0.8873 474.26 470.6 1.989
1100 0.8885 474.19 470.6 1.989
1110 0.8897 474.11 470.5 1.989
1120 0.8908 474.03 470.5 1.989
1130 0.8920 473.96 470.5 1.989
1140 0.8931 473.89 470.4 1.989
1150 0.8943 473.81 470.4 1.988
1160 0.8954 473.74 470.4 1.988
1170 0.8965 473.67 470.4 1.988
1180 0.8976 473.61 470.3 1.988
1190 0.8986 473.54 470.3 1.988
1200 0.8997 473.47 470.3 1.988
1203 0.9000 473.45 470.3 1.988
KECEPATAN MASSA GAS KELUAR REAKTOR
Komponen Kgmol /jam Kg / jam
O2 82.0665 2626.1272
C7H8 1.3144 120.9272
N2 468.4342 13116.1563
H2O 24.0795 433.4310
C6H5CHO 5.9272 628.2800
C6H6 0.0000 0.0000
C4H2O3 5.9149 579.6617
CO2 18.5844 817.7147
Total 606.3211 18322.2988
Enthalpi Hasil reaksi :
Suhu operasi = 473.45 C
Suhu refferensi = 25 C
Komponen Kgmol /jam Cp dT Qs = m Cp dT
O2 1.3144 3359.46 4415.7666
C7H8 82.0665 18267.09 1499115.5000
N2 468.4342 3197.49 1497813.5000
H2O 24.0795 3823.43 92066.2578
C6H5CHO 5.9272 21285.38 126162.1016
C6H6 0.0000 22025.61 0.0000
C4H2O3 5.9149 12185.40 226458.5938
CO2 18.5844 4789.26 0.0000
Total 606.3211 3446031.7500
NERACA PANAS :
MASUK : KELUAR :
1. Enthalpi Umpan Masuk Reaktor 1. Enthalpi hasil reaksi:
Qs1 = 4093604.0000 Kcal/jam Qs2 = 3446031.7500 Kcal/jam
2. Panas Reaksi 2. Panas dibawa pendingin
Qr = 2518927.2500 Kcal/jam Qp = 2716473.5000 Kcal/jam
3. Panas Hilang
Qloss = 450026.0000 Kcal/jam
-------------------------------- ---------------------------------
6612531.5000 Kcal/jam 6612531.0000 Kcal/jam
Dari hasil perhitungan Reaktor diperoleh :
Jumlah pipa = 6837 pipa
Diameter Shell = 4.194 m
Jumlah pendingin = 369198 Kg/j
Panjang terhitung = 12.0 m
= 39.5 ft
Panjang Pipa = 12.2 m
= 40.0 ft
Tinggi Head reaktor = 2.097 m
Tinggi reaktor = 12.192 + 2 . 2.097 m
= 14.3 m
1. Menghitung tebal shell
Digunakan bahan Carbon steel SA 178 grade C
Tekanan design (p) = 17.64 psi
Allowable stress = 18750 psi
efisiensi sambungan = 0.85
faktor korosi = 0.125 in
Jari-jari tangki = 82.56 in
Tebal Shell :
p .ri
t shell = + c
S . e - 0.4 . p
17.64 . 82.56
= + 0.125
18750.00 . 0.85 - 0.4 . 17.64
= 0.216 in
Dipakai tebal shell 1/4 in
2. Menghitung tebal head
Bentuk head : Elliptical Dished Head
Digunakan bahan Carbon steel SA 178 grade C
Tekanan design (p) = 32.24 psi
Allowable stress = 18750 psi
efisiensi sambungan = 0.85
faktor korosi = 0.125 in
Jari-jari tangki = 82.56 in
Tebal Head :
0.885 . p .d
t head = + c
2 . S . e - 0.2 . p
0.885 . 32.24 . 165.12
= + 0.125
2 . 18750.00 . 0.85 - 0.2 . 32.24
= 0.273 in
Dipilih tebal head 1/4 in
3. Menghitung ukuran pipa
Diameter Optimum pipa berdasarkan Pers. 15 Peters, hal.525
a. Pipa pemasukan Umpan Reaktor :
Kecepatan Umpan = 40309.059 lb/j
Densitas Umpan = 0.1684 lb/ft^3
Di = 2.2 . ( G/1000 )^ 0.45 . den ^ (-0.31)
= 2.2 . ( 40309.059 / 1000 )^ 0.45 . 0.1684 ^ (-0.31)
= 20.171 in
Dipakai pipa dengan ukuran : 20.00 in
b. Pipa pengeluaran hasil Reaktor :
Kecepatan hasil = 40309.059 lb/j
Densitas hasil = 0.1673 lb/ft^3
Di = 2.2 . ( G/1000 )^ 0.45 . den ^ (-0.31)
= 2.2 . ( 40309.059 / 1000 )^ 0.45 . 0.1673 ^ (-0.31)
= 20.212 in
Dipakai pipa dengan ukuran : 20.00 in
c. Pipa pemasukan dan pengeluaran pemanas:
Kecepatan HITEC = 812235.6250 lb/j
Densitas HITEC = 54.6624 lb/ft^3
Di = 2.2 . ( L/1000 )^ 0.45 . den ^ (-0.31)
= 2.2 . ( 812235.625 / 1000 )^ 0.45 . 54.6624 ^ (-0.31)
= 12.975 in
Dipakai pipa dengan ukuran : 12.00 in
4. Menghitung tebal Isolasi
Diameter shell = 13.76 ft
Tinggi shell = 40.00 ft
Tebal shell = 0.018 ft
Luas permukaan head = 356.70 ft
Luas permukaan shell = 1728.24 ft
Total luas permukaan = 2084.94 ft
Suhu permukaan isolasi = 140.00 F = 600.00 R
Suhu dalam reaktor = 956.39 F = 1416.39 R
Suhu udara lingkungan = 86.00 F = 546.00 R
Konduktifitas thermal diding shell = 28.0000 Btu ft/(j ft F)
Digunakan Isolasi Fine Diatomaceous earth powder
Konduktifitas thermal isolasi = 0.1250 Btu ft/(j ft F)
Koeffisien transfer panas konveksi (hc) :
0.25
hc = 0.3 Tw - Tu
0.25
= 0.3 140.00 - 86.00
= 0.8132418 Btu/j ft F
Koeffisien transfer panas Radiasi (hr) :
4 4
k e (Tw/100) - (Tu/100)
hr = ---------------------------------
[ Tw - Tu ]
4 4
0.178 . 0.8 6.00 - 5.46
= ---------------------------------
[ 600.00 - 546.00 ]
= 5.8827672 Btu/j ft F
A . (T1 - Tu)
Q loss = -----------------------------
t1 t2 1
---- + ---- + ---------
k1 k2 (hr + hc)
2084.940 . (956.39 - 86.00)
= --------------------------------------------
0.018 T is 1
------- + -------- + ------------------
28.00 0.125 0.8132 + 5.8828
0.018 T is 1 2084.940 (956.39 - 86.00)
------- + -------- + -------- = ---------------------------
28.00 0.125 6.6960 450026.000
0.018 T is 1
------- + -------- + -------- = 4.032
28.00 0.125 6.6960
T is
0.00064 + -------- + 0.1493 = 4.032
0.1250
T is
-------- = 3.882
0.1250
T isolasi = 0.485 ft
= 5.824 in
Kesimpulan :1. Tugas
2. Type alat = Reaktor Fixed Bed Multitube, karena reaksinya sangat eksotermis3. Kondisi operasi
4. Katalis
5. Pipa reactor6. Ukuran reaktor
Jumlah pipa = 6837 pipa
Diameter Shell = 4.194 m
Jumlah pendingin = 369198 Kg/j
Panjang terhitung = 12.0 m
= 39.5 ft
Panjang Pipa = 12.2 m
= 40.0 ft
Tinggi Head reaktor = 2.097 m
Tinggi reaktor = 12.192 + 2 . 2.097 m
= 14.3 m
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
EMBED Equation.3
= (-rA) EMBED Equation.3
EMBED Equation.3 Z
QR
z
T z+z
: EMBED Equation.3 z
..(3)
.(4)
B
C
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