ABSTRACT
In this study, optimizations on separation of Toluene and 1-Butanol mixture is carried out by pressure swing distillation process. New heat integration methods are applied and compared to conventional PSD process by using vapor recompression technique combined with pressure swing distillation process. New heat integration methods show positive results to decrease the utilities used in the process. A simulator Aspen HYSYS V8.4 is used for simulating all processes. Cost analysis is also performed and Aspen HYSYS V8.4 optimizer program is used for optimizing profit for the process. Pressure is also optimized for minimum heat duty requirements in the process and the ultimate concern is to minimize the total reboiler heat duties and overall operating cost for the system which results into increasing profit.
Nomenclature
T | = | = Absolute temperature (K) |
P | = | = Pressure (kPa) |
R | = | = Gas constant (J/gmole-K) |
N | = | = Number of components |
V | = | = molar volume (m3/gmol) |
PSD | = | = Pressure swing distillation |
LP | = | = Low pressure |
HP | = | = High pressure |
xi and yi | = | = liquid and vapour phase mole fraction of component i and j |
= | = binary coefficients in NRTL model | |
= | = Experimental and calculated dew point temperatures | |
= | = Cost of toluene and 1-butanol components in feed | |
= | = Flow rate of toluene and 1-butanol components in feed | |
= | = Cost of toluene and 1-butanol components in product | |
= | = Flow rate of toluene and 1-butanol components in product | |
= | = Utility cost | |
= | = Equipment capital cost | |
= | = Depreciation factor |