THERMAL-DIST Interface

Optimal Separation Sequences based on Thermally Coupled Distillation.
DATA
Parameters
Benzene
Toluene
EthylBenzene
Styrene
alpha-Methylstyrene
A
B
C
D
E
Relative Volatility*
10.50
4.04
1.76
1.31
1.00
Feed mole fraction
0.30
0.20
0.10
0.20
0.20
Molecular weight - g/mol
78.00
92.00
106.00
104.00
118.00
Vaporization enthalpy - kJ/mol
30.77
33.19
35.58
36.83
38.30
* Relative volatility of component i to the less volatile component (alpha-Methylstyrene ).

Total Feed Flow - Kmol/h
200
Nominal pressure - atm
0.50
Maximum number of trays
58
Molecular weight - g/mol
96.80
Recovery of each component in a column
0.98
Feed temperature - ° C
85.12
Cost of Steam - $/GJ †
5.09
Cost of Water - $/GJ †
0.19
† Assumed Operation time: 8000 h/yr.

RESULTS
Costs ($/yr)
Total Energy Cost 1994406.55
Total Investment Cost 105173.43
Total Cost 2099579.98

Specifications
State exists*
ABCDE
ABCD
BCDE
BCD
CD
DE
Number of trays
7
16
28
19
53
58
Column (pseudo-column) diameter - m
2.38
1.58
1.64
1.57
2.28
2.28
Heat load of the Reboiler - kW †
(BCDE ) 5318
(DE ) 2664
(E ) 5187
Heat load of the Condenser - kW †
(ABCD ) 4847
(A ) 2004
(B ) 2117
(C ) 2736
Separation task exists
ABCD/BCDE
A/BCD
BCD/DE
B/CD
C/D
D/E
        * A,B,C,D,E states always exist.
        † Value between parentheses represents the state to which reboiler/condenser is associated.

Optimal Solution
TAC1
GAMS LIST FILE