1. August 26, 2010 1 Vapor / Liquid Equilibrium Using HYSYS Prepared by: A.N.Tabish Lab. Engineer / Lecturer Department of Chemical Engineering UET, City Campus, Lahore tabish288@yahoo.com

2. 2 Example # 10.3:* For the system methanol (1) / methyl acetate (2) , the following equations provide a reasonable correlation for the activity coefficient Where, In addition following equations provide vapor pressures: Where T is in kelvin and the vapor pressure are in kPa. * J.M.Smith, H.C.Van Ness and M.M.Abott (2005), “Introduction to Chemical Engineering Thermodynamics”, Ed. 7, pp. 359, McGraw Hill August 26, 2010 tabish288@yahoo.com

3. August 26, 2010 3 CALCULATE: P and {y1}, for T = 318.15 K and {x1}= 0.25 P and {x1}, for T = 318.15 K and {y1}= 0.60 T and {y1}, for P = 101.33kPa and {x1}= 0.85 T and {x1}, for P = 101.33kPa and {y1}= 0.40 tabish288@yahoo.com

5. Define components

6. Select Thermodynamic model.

7. Draw the PFD (material streams)

9. Determine composition using K-Value informationtabish288@yahoo.com

10. August 26, 2010 5 HYSYS: tabish288@yahoo.com

12. Define components (Methanol + Methyl Acetate).tabish288@yahoo.com

16. August 26, 2010 10 BUBL Pressure: P and {y1}, for T = 318.15 K and {x1}= 0.25 73.50 kPa in manual calculations tabish288@yahoo.com

17. August 26, 2010 11 Vapor compositions: y1 = 0.282 y2 = 0.718 y1 = 0.278 y2 = 0.722 tabish288@yahoo.com

18. August 26, 2010 12 DEW Pressure: P and {x1}, for T = 318.15 K and {y1}= 0.60 62.89 kPa in manual calculations tabish288@yahoo.com

19. August 26, 2010 13 Liquid compositions: x1 = 0.8169 x2 = 0.1831 x1 = 0.8099 x2 = 0.1901 tabish288@yahoo.com

20. August 26, 2010 14 BUBL Temperature: T and {y1}, for P = 101.33kPa and {x1}= 0.85 331.20K = 58 oCin manual calculations tabish288@yahoo.com

21. August 26, 2010 15 Vapor compositions: y1 = 0.670 y2 = 0.330 y1 = 0.671 y2 = 0.329 tabish288@yahoo.com

22. August 26, 2010 16 DEW Temperature: T and {x1}, for P = 101.33kPa and {y1}= 0.40 326.70K = 53.7 oC in manual calculations tabish288@yahoo.com

23. August 26, 2010 17 Liquid compositions: x1 = 0.4602 x2 = 0.5398 x1 = 0.4517 x2 = 0.5483 tabish288@yahoo.com

25. Go to the Simulation Environment

26. Go to Tools/Preferences/Extensions and Click on Register an Extension.

27. Find EqPlots.dll and open it. This will remain part of HYSYS or UniSim on your machine until it is Unregistered. Close Preference.

28. Go to Flowsheet/Add Operation. Select the Extensions category and Add Equilibrium Plots. This should open the equilibrium plots extension.

29. For a Binary plot, click the Binary tab at the bottom of the Equilibrium Plots menu, and select the components and the type of plot desired.

30. For an XY plot, specify either T or P, and click on Plot.

31. For a TXY plot, specify P. For a PXY plot, specify T.tabish288@yahoo.com

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35. August 26, 2010 22 Example # 10.4:* For a mixture of 10 mol-% methane, 20 mol-% ethane, and 70 mol-% propane at 50 (oF), determin: The dew point pressure The bubble point pressure * J.M.Smith, H.C.Van Ness and M.M.Abott (2005), “Introduction to Chemical Engineering Thermodynamics”, Ed. 7, pp. 364, McGraw Hill tabish288@yahoo.com

36. August 26, 2010 23 Home Work Task: Assuming the validity of Raoult's law, do the following calculations for the benzene (l)/toluene (2) system: For the system ethyl ethanoate (1) and n-heptane (2)at 343.15 K (70"C) BUBL P calculation for T = 343.15 K (70°C), x1 = 0.05. DEW P calculation for T = 343.15 K (70°C), y1 = 0.05. tabish288@yahoo.com

37. August 26, 2010 24 Home Work Task Contd…. Make the following VLE calculations for the methane (l) / ethylene (2) / ethane (3) system: tabish288@yahoo.com