CONCEPTUAL DESIGN OF NON-IDEAL MIXTURE SEPARATION WITH LIGHT ENTRAINERS

Shen, W.; Benyounes, H.; Dong, L.; Wei, S.; Li, J.; Gerbaud, V.

doi:10.1590/0104-6632.20160334s20140169

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Brazilian Journal of Chemical Engineering

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Thermodynamics • Braz. J. Chem. Eng. 33 (4) • Oct-Dec 2016 • https://doi.org/10.1590/0104-6632.20160334s20140169 copy

CONCEPTUAL DESIGN OF NON-IDEAL MIXTURE SEPARATION WITH LIGHT ENTRAINERS

Authorship SCIMAGO INSTITUTIONS RANKINGS

Abstract

A method is proposed to study the separation of minimum-, maximum-boiling azeotropic, and low volatility mixtures with a light entrainer, to investigate feasible regions of the key operating parameters reboil ratio (S) and entrainer - feed flowrate ratio (F_E/F) for continuous processes. The thermodynamic topological predictions are carried out for 1.0-2, 1.0-1a, and 0.0-1 Serafimov's class diagrams. It relies upon the knowledge of residue curve maps, along with the univolatility line, and it enables the prediction of possible products at the bottom of the column and limiting values of F_E/F. The profiles of the stripping, extractive, and rectifying sections are calculated by equations considering S and F_E/F, and they bring information about the location of singular points and possible composition profile separatrices that could impair process feasibility. Providing specified product composition and recovery, the approximate calculations are compared with rigorous simulations of extractive distillation processes. Separating non-ideal mixtures using a light entrainer provides more opportunities for the case when it is not easy to find an appropriate heavy or intermediate entrainer.

Keywords:
Conceptual design; Feasibility study; Extractive distillation; Azeotropic mixture; Light entrainer

Classification: 1.0-2; Azeotropic type: Minimum; Volatility order: E>Az>A>B
A	ethanol		ethanol/propanol		MEK		n-butanol
B	water		toluene		benzene		n-butyl-acetate
E	MeOH		acetone		acetone		n-propyl-formate /dipropyl-ether
References	Hunek et al. 1989		Laroche et al. 1992		Rodriguez-Donis et al. 2012a		Lang et al. 1999
	Laroche et al. 1992		Rodriguez-Donis et al. 2012a		Shen and Gerbaud 2013Shen, W. F., Benyounes, H. and Gerbaud, V., Extension of thermodynamic insights on batch extractive distillation to continuous operation. 1. Azeotropic mixtures with a heavy entrainer. Industrial & Engineering Chemistry Research, 52, 4606-4622 (2013a).
	Lang et al. 1999
	Varga et al. 2006b
	Rodriguez-Donis et al. 2012a
	Shen and Gerbaud 2013Shen, W. F., Benyounes, H. and Gerbaud, V., Extension of thermodynamic insights on batch extractive distillation to continuous operation. 1. Azeotropic mixtures with a heavy entrainer. Industrial & Engineering Chemistry Research, 52, 4606-4622 (2013a).
Classification: 1.0-1a; Azeotropic type: Maximum; Volatility order: E>A>B>Az
A	water	acetone				propanoic acid
B	ethyl-enediamine	chloroform				Dimethyl-formamide
E	MeOH	Dichloromethane				MIBK
References	Varga et al. 2006b	Rodriguez-Donis et al. 2012a				Rodriguez-Donis et al. 2012a
	Rodriguez-Donis et al. 2012a					Shen and Gerbaud 2013Shen, W. F., Benyounes, H. and Gerbaud, V., Extension of thermodynamic insights on batch extractive distillation to continuous operation. 1. Azeotropic mixtures with a heavy entrainer. Industrial & Engineering Chemistry Research, 52, 4606-4622 (2013a).
	Shen and Gerbaud 2013Shen, W. F. and Gerbaud, V., Extension of thermodynamic insights on batch extractive distillation to continuous operation. 2. Azeotropic mixtures with a light entrainer. Industrial & Engineering Chemistry Research, 52, 4623-4637 (2013b).
Classification: 0.0-1; Azeotropic type: low alpha; Volatility order E>A>B
A	chlorobenzene			ethyl acetate
B	ethylbenzene			benzene
E	4-methylheptane			acetone
References	Varga et al. 2006b			Rodriguez-Donis et al. 2012a

Specifications	Class 1.0-1a (Fig.7)	Class 1.0.2(Fig. 8a)	Class 1.0-2 (Fig. 8b)	Class 1.0.2 (Fig. 8c)
Tray number, N	65	50	50	100
Entrainer tray, N_FE	60	30	30	60
Feed tray, N_F	20	15	15	10
x_F, mole fraction (A,B,E)	{0.7; 0.3; 0.0}	{0.4; 0.1; 0.5}	{0.225; 0.7; 0.075}	{0.225; 0.275; 0.5}
x_E, mole fraction (A,B,E)	{0.0; 0.0; 1.0}	{0.0; 0.0; 1.0}	{0.0; 0.0;1.0}	{0.0; 0.0; 1.0}

i-j	A_ij	A_ji
ethanol(A) -water (B)	232.00	50.88
ethanol(A)-MeOH(E)	791.80	-482.30
water (B)- MeOH(E)	95.26	-10.38
ethanol(A) -toluene (B)	927.40	-167.20
ethanol(A)-acetone(E)	98.75	94.24
toluene (B)-acetone(E)	-315.30	555.70
butanol(A)-n-butyl acetate (B)	-111.10	279.00
butanol(A)-di-n-propyl-ether(E)	511.70	-203.10
n-butyl acetate (B)-di-n-propyl-ether(E)	-240.20	317.50
MEK(A) -benzene(B)	337.90	-268.10
MEK(A)-acetone(E)	-42.27	12.67
benzene(B)-acetone(E)	-299.80	510.00
water(A) -ED(B)	-798.30	16.43
water(A) -MeOH(E)	95.26	-10.38
ED(B)- MeOH(E)	-121.80	-416.50
acetone(A)-chloroform(B)	-781.60	1566.00
acetone(A)-DCM(E)	-28.34	-135.30
chloroform(B)-DCM(E)	-615.80	1134.00
ethylacetate(A)-benzene(B)	-202.00	204.80
ethylacetate(A)-acetone(E)	-220.70	321.80
benzene(B)-acetone(E)	-299.80	510.60

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