Computation of Isobaric Vapor-Liquid Equilibrium Data for Binary and Ternary Mixtures of Methanol, Water, and Ethanoic Acid from 𝑇, 𝑝, 𝑥, and 𝐻^𝐸_𝑚 Measurements

Table 4

Correlation parameters for activity coefficients, average deviation for studied systems and vapor-phase composition mean absolute deviation from the literatures.

Equation	Parameters or deviations	Methanol (1) + water (2)	Methanol (1) + ethanoic acid (2)	Water (1) + ethanoic acid (2)
	(𝑔12−𝑔11)/J·mol^−1	−436.50	−85.50	−352.42
	(𝑔21−𝑔22)/J·mol^−1	1159.55	0.98	715.43
NRTL^a	𝛼12	0.241	0.30	0.23
	dT/K	0.28	0.51	0.33
	dy	0.0072	0.0054	0.0096
Wilson^a	Λ12/J·mol^−1	389.37	50.46	644.71
	Λ21/J·mol^−1	368.45	95.58	−87.59
	dT/K	0.43	0.47	0.64
	dy	0.0036	0.0059	0.0053
Margules^b	𝐴12	0.95	0.12	0.29
	𝐴21	0.65	−0.46	0.57
	dT/K	0.37	0.32	0.56
	dy	0.0049 (0.0057)^c	0.0075 (0.0234)^c	0.0086 (0.0123)^c
van Laar^b	𝐴12	0.86	0.24	0.32
	𝐴21	0.56	0.03	0.55
	dT/K	0.27	0.58	0.47
	dy	0.0069	0.0078	0.0098

^aWilson’s interaction parameters (J·mol⁻¹), NRTL’s interaction parameters (J·mol⁻¹). ^bMargules and van Laar interaction parameters (dimensionless). 𝑑𝑇=∑|𝑇_exp−𝑇_cal|/𝑁; 𝑁: number of data points; 𝑇_cal: calculated bubble point from model, K; 𝑇_exp: experimental boiling point temperature, K. 𝑑𝑦=∑|𝑦_cal−𝑦_mod|/𝑁; 𝑁: number of data points; 𝑦_cal: calculated vapor-phase mole fraction from Tpx; 𝑦_mol: calculated vapor-phase mole fraction from model. ^cThe values in parentheses from the literatures [38–41].