The vapor compositions predicted by the method of Mixon et al. are in excellent agreement with those predicted by the two-parameter activity coefficient models represented by the Margules model. For example, the calculated values of the vapor compositions by these two methods are given in Tables 6.26.8 for the chosen sets of data. Further, the vapor compositions predicted by the Margules model using the MLH method and the Genetic algorithm are given in Tables 6.9.a 6.9.g. for the chosen sets of data.

III Year B. Tech. Petrochemical Engineering II Sem.Mass Transfer Operation II

Fenske-Underwood-Gilliland (FUG)Presentation byProf. K. V. RaoAcademic Advisor / Visiting ProfessorSchool of Petroleum Courses

Jawaharlal Nehru Technological University Kakinada1Fenske Equation ( minimum trays total reflux)Fenske-Underwood-Gilliland (FUG)

QQxN+1yNx1yo1NTotal CondenserTotal Reboiler2Underwood Equation ( minimum reflux infinite trays)Fenske-Underwood-Gilliland (FUG)

3Gilliland ChartFenske-Underwood-Gilliland (FUG)

4FUG ExampleThe following separation is required for a deethanizeing column operating at 1.25 times the minimum reflux ratio. Determine the theoretical stages required. Flows are in lbmol/ hrComponentFeedDistillateBottomsMethane5.05.0Ethane (LK)35.031.893.11Propylene (HK)15.00.9514.05Propane 20.020.0i-Butane10.00.0n-Butane15.015.0Total100.037.8462.165Assignment 2A multicomponent distillation column should be designed in such a way, that a concentrate stream of Ethane could be separated from a feed stream containing 6 hydrocarbons (hint: separation between Ethane and Propylene). Calculate the required theoretical number of stages and the realistic number of stages when R = 1.25 Rmin.Separation requirements:Mole fraction of Propylene in the Distillate: 0.025Mole fraction of Ethane in the Bottoms: 0.050

Operating conditions:Pressure: p = 27.3 barFeed quality: liquid at the boiling temperature (q = 1)Average plate efficiency coefficient: E = 0.756Feed composition:

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