Separation Process Principles- 2n - Seader & Henley - Solutions Manual

595 ethane and 0400 n butane find a bubble point

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Unformatted text preview: ge of a distillation column and passing to a reboiler where all by 50 kmol/h is vaporized to VB. Assumptions: Pressure in reboiler = 758 kPa. S-R-K method for K-values and enthalpies. Find: Compositions and amounts of boilup and bottoms, B, and reboiler duty, QR, from a simulation program Analysis: Use flash module of the CHEMCAD simulator. Feed (L1) temperature is computed from a bubble-point calculation at 758 kPa to be 74.9oC. Flash conditions are P = 758 kPa and V/F = (150 - 50)/150 = 0.6667. The result is a temperature of 87.5oC with a reboiler duty of 2.22 x 106 kJ/h, and compositions as follows in terms of component flow rates: Component: Bottoms, kmol/h Boilup, kmol/h Propane 1.94 13.06 n-Butane 15.39 44.61 n-Pentane 32.67 42.33 Total 50.00 100.00 Exercise 4.39 Subject: Bubble-point and equilibrium flash temperatures for a ternary mixture. Given: Mixture at 50 psia with a composition in mole fractions of 0.005 methane, 0.595 ethane, and 0.400 n-butane. Find: (a) Bubble-point temperature. (b) Temperature and phase compositions for 25 mol% vaporization. Analysis: Instead of using Figs. 2.8 and 2.9 for K-values, use S-R-K method with the CHEMCAD simulator, with the following results: (a) Bubble-point temperature = -61oF. Use of Figs. 2.8 and 2.9 gives -60oF. (b) Flash temperature for 25 mol% vaporization = -43.6oF, with compositions: Component Vapor mole fraction Liquid mole fraction Methane 0.0179 0.0007 Ethane 0.9559 0.4747 n-Butane 0.0262 0.5246 Exercise 4.40 Subject: Heating and expansion of a hydrocarbon mixture. Given: 100 lbmol/h of a mixture at 150oF and 260 psia, with a mole fraction composition of 0.03 ethane, 0.20 propane, 0.37 n-butane, 0.35 n-pentane, and 0.05 n-hexane. Mixture is heated to 260oF at 250 psia, followed by expansion to 100 psia. Assumptions: Expansion is adiabatic. S-R-K method for K-values and enthalpies Find: Using a simulation program, find for each stream in the process, the mol% vapor, and vapor and liquid phase mole fractions. Analysis: Using the CHEMCAD process simulator, the following results are obtained. The feed is all liquid. The streams leaving the heater and the valve are all vapor. The final temperature is 235oF. Exercise 4.41 Subject: Equilibrium vapor and liquid streams leaving the feed stage of a distillation column Given: Feed stream, F, and streams VF+1 and LF-1 as summarized below. Pressure = 785 kPa. Assumptions: VF+1 is at its dew point and LF-1 is at its bubble point. Adiabatic conditions. Find: Composition and amounts of streams VF and LF. Analysis: Using the S-R-K method for K-values, with the CHEMCAD process simulator, the following results are obtained: Stream Temperature, oC Phase condition Flow rate, kmol/h: Propane n-Butane n-Pentane Total F 64.3 Liquid VF+1 73.1 Vapor LF-1 68.5 Liquid VF 70.0 Vapor LF 70.0 Liquid 32.0 64.0 64.0 160.0 58.8 98.0 39.2 196.0 15.0 45.0 40.0 100.0 69.6 89.9 34.5 194.0 36.2 117.1 108.7 262.0 Exercise 4.42 Subject: Adiabatic flash across a valve of a hydrocarbon...
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