Work Prob. 13.49 for the NRTL equation.

Prob. 13.49

For one of the binary systems listed in Table 13.10, based on Eq. (13.19) and the Wilson equation, make the following calculations:
(a) BUBL T : P = 101.33 kPa, x₁ = 0.3.
(b) DEW T : P = 101.33 kPa, y₁ = 0.3.
(c) P, T − flash: P = 101.33 kPa, T = ½ (T_bubble + T_dew), z₁ = 0.3.
(d) If an azeotrope exists at P =101.33 kPa, find T^az and x^az₁ = y^az_1.

Problems 13.43 through 13.54 require parameter values for the Wilson or NRTL equation for liquid-phase activity coefficients. Table 13.10 gives parameter values for both equations. Antoine equations for vapor pressure are given in Table B.2, Appendix B.

Table 13.10

Table B.2, Appendix B.

 Eq. (13.19)

Transcribed Image Text:

Table 13.10: Parameter Values for the Wilson and NRTL Equations Parameters a12, a21, b12, and baj have units of cal-mol-1, and Vị and V2 have units of cm³-mol-!. Wilson Equation NRTL Equation b12 Vị System V2 a12 b21 a Acetone(1) Water(2) Methanol(1) Water(2) 1-Propanol(1) Water(2) 74.05 291.27 1448.01 631.05 1197.41 0.5343 18.07 40.73 107.38 469.55 -253.88 845.21 0.2994 18.07 75.14 775.48 1351.90 500.40 1636.57 0.5081 18.07 18.07 1696.98 -219.39 548.90 0.2920 Water(1) 1,4-Dioxane(2) 715.96 85.71 Methanol(1) 40.73 504.31 196.75 343.70 314.59 0.2981 Acetonitrile(2) 66.30 Acetone(1) 74.05 -161.88 583.11 184.70 222.64 0.3084 Methanol(2) 40.73 Methyl acetate(1) Methanol(2) 813.18 381.46 79.84 40.73 -31.19 346.54 0.2965 Methanol(1) 40.73 1734.42 183.04 730.09 1175.41 0.4743 Benzene(2) 89.41 1556.45 Ethanol(1) Toluene(2) 58.68 210.52 713.57 1147.86 0.5292 106.85