BT2.SEP | This file was created on 23 Jun'03 0:42 by ChemSep v4.50( C:\CHEMSEP\BT2.SEP) |
Column C:\CHEMSEP\BT2.SEP Components: Benzene Toluene Operation: Simple Distillation Total (Liquid product) Condenser Partial (Liquid product) Reboiler 10 Stages Feeds to stages 5 |----| |------>-----| | | |1 | | |--|------| |--|-| | | |----<-------->- |--|---|--| |--|---|--| ----->----5-|--|---|--| |--|---|--| |--|---|--| | |---|-----<----| |------|--| |--|-| |--->---------->- 10|----| Properties: DECHEMA K model UNIFAC Activity coefficient Antoine Vapour pressure Excess Enthalpy Enthalpy reference state Vapour Enthalpy reference temperature 25.00 ( C) Formation enthalpies Excluded Exergy surroundings temperature 25.00 ( C) Reactions: Specifications: Column pressure Condenser pressure 1.115 (bar) Top pressure 1.115 (bar) Default efficiency = 1.000 (-) Feed 1 Stage 5 Pressure (bar) 1.115 Enthalpy (kJ/kmol) Vapour fraction (-) 0.0000 Temperature ( C) Component flows (mol/s) Benzene 5.874 Toluene 5.874 Condenser Reflux ratio = 2.000 (-) Initialization guess: * Reboiler Bottom product flow rate = 5.874 (mol/s) Initialization guess: * Solve options: Automatic Initialization Newton's method Flow Step limit 0.5000 (-) Temperature Step limit 10.00 ( C) Composition Step limit 1.000 (-) Accuracy = 0.0001 Maximum iterations = 30 Feeds type = Stage below User program = CSW
ChemSep (TM) - Flash/Col2 v4.30s Copyright(c) H.Kooijman and R.Taylor, 1988-2001 Checking data file C:\CHEMSEP\BT2.SEP Reading configuration Reading component property libraries Reading thermodynamic property options Reading specifications Checking Component Data Benzene Toluene Determining feed conditions Generating initial flow profiles Generating initial composition profiles Starting Newtons method Ctrl-Break will terminate execution Iteration Error 0 1.2908E+04 1 9.6881E+01 2 2.1764E-01 Convergence obtained in 2 iterations Generating equilibrium data c:/chemsep/bin/go-col2.exe done
Mass and Energy Balances Stream / Apparatus Mass (mol/s) Energy (MW) Exergy (MW) Feed 1 11.75 -0.2899 -1.114 Top -5.873 0.1479 0.5088 Bottom -5.874 0.1355 0.5933 Condenser Duty -0.5471 -0.09197 Reboiler Duty 0.5536 0.1235 ----------- + ----------- + ----------- + Balance -3.958E-05 1.125E-06 0.01939 Thermodynamic efficiency = 0.3841 Component discrepancies (mol/s) Benzene -2.141E-05 Toluene -1.905E-05 Stage Temperature Pressure Flow rates (mol/s) ( C) (bar) Liquid Vapour Feed Product 1 85.24 1.115 11.75 5.873 L 2 87.54 1.115 11.53 17.62 3 90.49 1.115 11.32 17.41 4 93.61 1.115 11.16 17.20 5 96.30 1.115 22.79 17.03 11.75 6 98.59 1.115 22.65 16.91 7 101.6 1.115 22.53 16.78 8 104.9 1.115 22.46 16.66 9 108.0 1.115 22.44 16.58 10 110.6 1.115 16.57 5.874 L Profile for Toluene Stage Liquid (-) Vapour (-) K (-) 1 0.07929 0.03190 0.4023 2 0.1813 0.07929 0.4373 3 0.3028 0.1469 0.4851 4 0.4202 0.2264 0.5389 5 0.5142 0.3026 0.5886 6 0.5891 0.3730 0.6332 7 0.6806 0.4730 0.6949 8 0.7752 0.5959 0.7688 9 0.8579 0.7236 0.8435 10 0.9206 0.8357 0.9077 Profile for Toluene Stage Liquid (-) Vapour (-) K (-) 1 0.07929 0.03190 0.4023 2 0.1813 0.07929 0.4373 3 0.3028 0.1469 0.4851 4 0.4202 0.2264 0.5389 5 0.5142 0.3026 0.5886 6 0.5891 0.3730 0.6332 7 0.6806 0.4730 0.6949 8 0.7752 0.5959 0.7688 9 0.8579 0.7236 0.8435 10 0.9206 0.8357 0.9077 Stream Feed 1 Top Bottom Stage 5 1 10 Pressure (bar) 1.115 1.115 1.115 Vapour fraction (-) 0.0000 0.0000 0.0000 Temperature ( C) 95.89 85.24 110.6 Enthalpy (kJ/kmol) -2.468E+04 -2.519E+04 -2.307E+04 Entropy (J/kmol/K) 2.353E+05 2.061E+05 2.614E+05 Mole flows (mol/s) Benzene 5.874 5.407 0.4661 Toluene 5.874 0.4657 5.408 Total molar flow 11.75 5.873 5.874 Mole fractions (-) Benzene 0.5000 0.9207 0.07936 Toluene 0.5000 0.07929 0.9206 Mass flows (kg/s) Benzene 0.4588 0.4224 0.03641 Toluene 0.5412 0.04291 0.4983 Total mass flow 1.0000 0.4653 0.5347 Mass fractions (-) Benzene 0.4588 0.9078 0.06810 Toluene 0.5412 0.09222 0.9319
Liquid compositions
Vapor compositions
K-values
Temperatures
Pressures
Flow profiles
Enthalpies
Stripping factors
Key-ratios
Relative volatilities
McCabe-Thiele