BT3.SEP | This file was created on 23 Jun'03 0:43 by ChemSep v4.50( C:\CHEMSEP\BT3.SEP) |
Column C:\CHEMSEP\BT3.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: Raoult's law K model Antoine Vapour pressure None 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 = 10.00 (-) 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\BT3.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 9.5880E-04 1 4.5167E-02 2 4.9231E-03 3 1.1760E-05 Convergence obtained in 3 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 0.0000 -0.8236 Top -5.873 -0.0000 0.3534 Bottom -5.874 -0.0000 0.4625 Condenser Duty 0.0000 0.0000 Reboiler Duty 0.0000 0.0000 ----------- + ----------- + ----------- + Balance -3.958E-05 0.0000 -0.007768 Thermodynamic efficiency = -0.0000 Component discrepancies (mol/s) Benzene -2.209E-05 Toluene -1.678E-05 Stage Temperature Pressure Flow rates (mol/s) ( C) (bar) Liquid Vapour Feed Product 1 84.11 1.115 58.73 5.873 L 2 84.92 1.115 58.73 64.60 3 86.61 1.115 58.73 64.60 4 89.72 1.115 58.73 64.60 5 94.41 1.115 70.48 64.60 11.75 6 99.53 1.115 70.48 64.60 7 104.8 1.115 70.48 64.60 8 108.8 1.115 70.48 64.60 9 111.3 1.115 70.48 64.60 10 112.7 1.115 64.60 5.874 L Profile for Toluene Stage Liquid (-) Vapour (-) K (-) 1 0.02717 0.01084 0.3990 2 0.06626 0.02717 0.4101 3 0.1445 0.06270 0.4338 4 0.2786 0.1339 0.4805 5 0.4580 0.2557 0.5584 6 0.6282 0.4112 0.6547 7 0.7788 0.5968 0.7663 8 0.8822 0.7612 0.8628 9 0.9418 0.8740 0.9280 10 0.9728 0.9389 0.9652 Profile for Toluene Stage Liquid (-) Vapour (-) K (-) 1 0.02717 0.01084 0.3990 2 0.06626 0.02717 0.4101 3 0.1445 0.06270 0.4338 4 0.2786 0.1339 0.4805 5 0.4580 0.2557 0.5584 6 0.6282 0.4112 0.6547 7 0.7788 0.5968 0.7663 8 0.8822 0.7612 0.8628 9 0.9418 0.8740 0.9280 10 0.9728 0.9389 0.9652 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) 95.60 84.11 112.7 Enthalpy (kJ/kmol) 0.0000 0.0000 0.0000 Entropy (J/kmol/K) 2.352E+05 2.018E+05 2.641E+05 Mole flows (mol/s) Benzene 5.874 5.714 0.1600 Toluene 5.874 0.1596 5.714 Total molar flow 11.75 5.873 5.874 Mole fractions (-) Benzene 0.5000 0.9728 0.02724 Toluene 0.5000 0.02717 0.9728 Mass flows (kg/s) Benzene 0.4588 0.4463 0.01250 Toluene 0.5412 0.01470 0.5265 Total mass flow 1.0000 0.4610 0.5390 Mass fractions (-) Benzene 0.4588 0.9681 0.02319 Toluene 0.5412 0.03189 0.9768
Liquid compositions
Vapor compositions
K-values
Temperatures
Pressures
Flow profiles
Enthalpies
Stripping factors
Key-ratios
Relative volatilities
McCabe-Thiele