#Input Data Umpan (kg/jam)
#a = Aniline; b= Diphenylamine (DPA); c= Ammonia
FMao = 3997.43585
FMbo = 0
FMco = 0
FMt = FMao+FMbo+FMco
# Trial Ug, Fluid Superficial Velocity (m/s)
# (batasan Ulrich = 0.005 - 1 m/s)
Ugt= 0.21
# Konversi Ugt menjadi m/jam:
Ug=Ugt*3600
# BM komponen (Kg/kmol)
BMa=93.13
BMb=169.23
BMc=17.031
# Mol Flowrate (Kmol/jam)
Fao=FMao/BMa
Fbo=FMbo/BMb
Fco=FMco/BMc
Fto=Fao+Fbo+Fco
# Data input:
xa0=0 # Konversi Inlet
T0=748.15 # Temperature Inlet (K)
P0=7.5*101.325 # Tekanan Inlet (kPa)
BMg=(BMa*(Fao/Fto))+(BMb*(Fbo/Fto))+(BMc*(Fco/Fto)) # BM Campuran Gas
dp=0.000149 # Diameter Katalis (m)
R=0.08206 # Konstanta Gas (atn.m3/kmol.K
rhog=((P0/101.325)*BMg)/(R*T0) # Densitas campuran Gas
(kg/m3)
G=Ug*rhog # kg/jam/m2
A=FMt/G # Luas Penampang Reactor
D=(4*A/3.14)^0.5 # Diameter Reaktor (m)
rhok=3900 # Densitas katalis (kg/m3)
por=0.38+0.073*(1+((D/dp-2)^2/(D/dp)^2)) # Porositas
rhob=rhok*(1-por) # rho bulk katalis (kg/m3)
y=748.15
#profil
#figure (1)
#plot (Z,Y(:,1),'b-')
#title ('Profil Konversi Aniline terhadap Panjang Bed')
#xlabel ('Panjang Bed, meter')
#ylabel ('Konversi Aniline')
#figure (2)
#plot (Z,Y(:,2), 'r-')
#title ('Profil Suhu Bed terhadap Panjang Bed')
#xlabel ('Panjang Bed, meter')
#ylabel ('Suhu Bed, K')
#figure (3)
#plot (Z,Y(:,3), 'g-')
#title ('Profil Tekanan Terhadap Panjang Bed')
#xlabel ('Panjang Bed, meter')
#ylabel ('Tekanan, kPa')
#output
#disp ('Fixed Bed Reactor: Single Bed Catalyst')
#disp ('Detail:')
#fprintf ('Laju Massa Umpan Total = #6.4f kg/jam\n',FMc)
#fprintf ('Fluid Superficial Velocity = #6.4f m/s\n',Ugt)
#fprintf ('Diameter reactor = #6.4f m\n',D)
#fprintf ('Porositas = #6.4f \n',por)
#fprintf ('BM Gas = #6.4f kg/kmol\n',BMg)
#fprintf ('Rho Gas = #6.4f kg/m3\n',rhog)
#fprintf ('rho Bulk = #6.4f kg/m3\n',rhob)
#disp ('profil')
# disp ('Panjang Bed, m Konversi Suhu, K Tekanan, kPa')
# disp ('--------------------- ------------ ---------- ------------------')
#fprintf ( ' #7.4f #6.4f #6,4f #6,4f/n',profil)
#function dy=reactor (z,y)
#global Fao Fbo Fco ya yb yc dp A Fa Fb Fc Ft BMa BMb BMc rhog G por rhob
#dy=zeros (3,1);
# Stoikiometri
Fa=Fao*(2-(748.15*(1)))
Fb=Fbo*Fao*(748.15*(1))
Fc=Fco*Fao*(748.15*(1))
Ft=Fa+Fb+Fc
# Fraksi Mol
ya=Fa/Ft
yb=Fb/Ft
yc=Fc/Ft
# Tekanan Parsial
Pa=ya*(748.15*(3))
Pb=yb*(748.15*(3))
Pc=yc*(748.15*(3))
# Kinetika Reaksi
k1=0.2888407*exp(-760.513/748.15) # cm3/kmol.s
Kp=exp(-264.972/(748.15*8.314)) # Kesetimbangan
rp= (2*k1*Pa)-(k1/Kp)*(Pb)*(Pc) # kmol/m3.jam
# Kapasitas Panas (kJ/kmol.K)
Cpa=-22.1+0.573*(748.15)-4.57*10^-4*(748.15)^2+1.84*10^-7*(748.15)^3-2.99*10^-11*(748.15)^4
#2
Cpb=-119+1.31*(748.15)-1.22*10^-3*(748.15)^2+5.88*10^-7*(748.15)^3-1.14*10^-10*(748.15)^4 #2
Cpc=33.6-1.26*10^-2*(748.15)+8.89*10^-5*(748.15)^2-7.18*10^-8*(748.15)^3+1.86*10^-11*(748.15)^4
#2
# Perhitungan Neraca panas
CpdT=-41.703*(748.15-298.15)+0.147159/2*(748.15^2-298.15^2)-0.0002181/3*(748.15^3-
298.15^3)+1.47617*10^-7/4*(748.15^4-298.15^4)-3.617*10^-11/5*(748.15^5-298.15^5) #2
DHRo=-17.62 # kJ/kmol
minDHR=-(DHRo+CpdT) # kJ/kmol
FiCpi=Fa*Cpa+Fb*Cpb+Fc*Cpc # kJ/jam.K
# Profil konversi
dy1=rp*A/Fao
# Profil Suhu Bed
dy2=rp*A*minDHR/FiCpi
# Viskositas (Yaws, micropoise =1e-6 g/cm.s)
myuA=-19.148+0.3067*(748.15)-0.000053256*(748.15)^2 #2
myuB=-21.162+0.2544*(748.15)-0.000045847*(748.15)^2 #2
myuC=-7.874+0.367*(748.15)-0.00000447*(748.15)^2 #2
myuG=((ya*myuA*BMa^0.5)*(yb*myuB*BMb^0.5)+(yc*myuC*BMc^0.5))/((ya*BMa^0.5)+(yb*BMb^0.5)+
(yc*BMc^0.5))
myuGI=myuG*3.6*10^-4 # micropoise dikonversi jadi (kg/m.jam)
# Profil tekanan (kPa/m)116
gc=127101600 # kg.m/jam2.kgf
gcc=9.807*10^-3 # hasil akhir ergun (kgf/m2/m) dikonversi jadi (kPa/m)
dy=-(G/(rhog*dp*gc))*((1-por)/(por^3))*(150*(1-por)*myuGI/dp+1.75*G)*gcc #3
