Modeling of Absorption- Stripping Network for Non-ideal Hydrocarbon Mixtures

   The present work is concerned with constructing a simulation computer program of multi –component absorption – stripping network through the use of rigorous method based on Otto Burninghum sum- rates method by using MAT LAB 6.5 package. Two hydrocarbon systems A and B were studied.  The design of equilibrium stage models requires thermodynamic data such as the equilibrium constant and vapor and liquid enthalpies.In this study, the data are predicted by using cubic equation of state namely Peng Robinson equation of state and Soave Redlich Kwong equation of state.The Antoine vapor pressure equation was used to calculate the latent heat of vaporization. The results obtained using SRK-EOS for thermodynamic calculation were compared with results obtained by other references [1, 2] to give the accuracy of the simulation computer program. For the absorber,three hydrocarbon systems A, B, and C were studied and for system C the accuracy of the computer program was 98%, while for the stripper two hydrocarbon systems A and B were studied and for system A the accuracy of the computer program was 99.5%. In this work PR-EOS was used this is because using PR-EOS gives better results in fractional absorbed and stripped for absorption and stripping processes and their networks. The effect of many process variables on the performance of absorption –stripping network were studied. These variables include; number of stages, wet gas feed temperature, operating pressure, and type of the solvent. The effect of the process variables was studied through the total vapor and liquid flow rate profiles, temperature profiles, fraction stripped and vapor mole fraction. The best effect obtained for absorption – stripping network for system A and B ,is by decreasing the number of stages the fraction stripped down to 48.18% for system A and 50% for system B , increasing wet gas feed temperature the fraction stripped down to 48.194 % for system A and 49% for system B, decreasing the operating pressure the fraction stripped down to 47.7% for system A and 49.7% for system B and increasing the carbon number of the solvent the fraction stripped down to 48.4% for system A and 49.75% for system B.