Rectifying Section
Upper Feed
D , x D
F U , x F U
Middle Section
Lower Feed
F L , x F L Stripping Section
B , x B
V m ,
L m + 1 ,
y m ,
x m + 1 ,
v h m −1
L h m +1
Stage m F L , x F L , h F L
Ls m ,
s V m −1 ,
y s m −
s x m s ,L h m
1
s ,v h m −1
Stage 2
(V M + B − F L )x I ,m +1 − V M y i ,m − Bx i ,B − F L x i ,F L
=0
L v h v Bh B + F L h F + Q reb = 0 (V m + B − F L )h m +1 − m m − L
V 1s , y 1s , h 1s ,v s
s
s ,L
L 2 , x 2 , h 2
B, x B , h B Reboiler (stage 1)
Q reb = (sh 1v − (s + 1)h 2L + h B )B
Q reb = (DH D + BH B ) − FH F + Q cond − Q 1 − Q 2
(V m s + B )h m s , L 1 − V m s h m s ,v − Bh B + Q reb +
= 0
(V m s + B )h m s ,v − V m s h m s ,v − Bh B + Q reb + Q 1 = 0
(V m s + B )h m s ,v − V m s h m s ,v − Bh B + Q reb + Q 1 + Q 2
= 0
B o u n d a r y V a lu lu e M o d e l
HYSY S
24
24*
U p p e r F e e d L o c a t io io n
6
6*
L o w e r F e e d L o c a t io io n
12
12*
4210
4145
Num ber of Stages
R e b o il e r D u t y ( k W )
Fz
i
x i =
= Vy
+ Lx
i
i
z i
(K i
− 1
f (V/F ) =
)
V
i
+ 1
z i (K i − 1 )
N
∑
y i =
V
(K i
− 1)+ 1
z i V V 1 + 1 − F F K i
= 0
W
=
η P =
n n
− 1
0 . 017
P
in
F
η
P
in
1 −
n − 1
ε
ln F + 0 . 7
n
C o m p on on e en nt Methane
M o le le Fr ac act io n 0.865
Ethane
0.075
Propane
0.035
i-Butane
0.015
n-Butane
0.006
i-Pentane
0.004
Par am e te r
Cond it io n
Temperature ( °C)
25
Pr es s ur e ( bar )
60
Molar Flow Rate ( kmol/h)
Parameter Number of trays Operating pressure (kPa) Pressure drop (kPa)
Condition 25 3000 50
36000
