ABSTRACT

Aromatic hydrocarbons are usually extracted from reformed naphtha, which are multicomponent mixtures with aliphatic hydrocarbons. These components have very close boiling point, which makes distillation process not so efficient and economically infeasible. For this reason, aromatics compounds are usually separated from aliphatic compounds by intermediate of solvent extraction unit operation. In this work, liquid liquid equilibrium (LLE) data for systems containing decane + toluene + diethylene glycol (DEG) and decane + toluene + triethylene glycol (TEG) at T = (303.15 and 333.15)K and atmospheric pressure were studied. It was observed that temperature hardly influence the size of the two-phase region. Distribution coefficient and selectivity have been calculated from those experimental data. For all systems studied, selectivity parameter showed values greater than 1 indicating that the extraction is possible by using DEG and TEG as extractor solvents. Additionally, selectivity values increase with increasing glycol carbon chain. LLE have been correlated by intermediate of NRTL and UNIQUAC activity coefficients.

Compounds

#	Formula	Name
1	C10H22	decane
2	C7H8	toluene
3	C4H10O3	diethylene glycol
4	C6H14O4	triethylene glycol

Datasets

The table above is generated from the ThermoML associated json file (link above). POMD and RXND refer to PureOrMixture and Reaction Datasets. The compound numbers are included in properties, variables, and phases, if specificied; the numbers refer to the table of compounds on the left.
Type	Compound-#	Property	Variable	Constraint	Phase	Method	#Points
POMD	1	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Pressure, kPa; Liquid		Liquid	Vibrating tube method	1
POMD	2	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Pressure, kPa; Liquid		Liquid	Vibrating tube method	1
POMD	3	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Pressure, kPa; Liquid		Liquid	Vibrating tube method	1
POMD	4	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Pressure, kPa; Liquid		Liquid	Vibrating tube method	1
POMD	2 3 1	Mass fraction - 2 ; Liquid mixture 1	Temperature, K; Liquid mixture 1 Mass fraction - 1; Liquid mixture 1	Pressure, kPa; Liquid mixture 1	Liquid mixture 1 Liquid mixture 2	Density calibration data	25
POMD	2 3 1	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Mass fraction - 1; Liquid Mass fraction - 2; Liquid	Pressure, kPa; Liquid	Liquid	Vibrating tube method	25
POMD	2 3 1	Mass fraction - 1 ; Liquid mixture 2 Mass fraction - 2 ; Liquid mixture 1 Mass fraction - 1 ; Liquid mixture 1	Temperature, K; Liquid mixture 1 Mass fraction - 2; Liquid mixture 2	Pressure, kPa; Liquid mixture 2	Liquid mixture 2 Liquid mixture 1	Density calibration data Density calibration data Density calibration data	10
POMD	2 4 1	Mass fraction - 2 ; Liquid mixture 1	Temperature, K; Liquid mixture 1 Mass fraction - 1; Liquid mixture 1	Pressure, kPa; Liquid mixture 1	Liquid mixture 1 Liquid mixture 2	Density calibration data	29
POMD	2 4 1	Mass density, kg/m3 ; Liquid	Temperature, K; Liquid Mass fraction - 1; Liquid Mass fraction - 2; Liquid	Pressure, kPa; Liquid	Liquid	Vibrating tube method	29
POMD	2 4 1	Mass fraction - 1 ; Liquid mixture 2 Mass fraction - 2 ; Liquid mixture 1 Mass fraction - 1 ; Liquid mixture 1	Temperature, K; Liquid mixture 1 Mass fraction - 2; Liquid mixture 2	Pressure, kPa; Liquid mixture 2	Liquid mixture 2 Liquid mixture 1	Density calibration data Density calibration data Density calibration data	10

Thermodynamics Research Center / ThermoML | Fluid Phase Equilibria

Removal of aromatic hydrocarbons from hydrocarbon mixture using glycols at 303.15 K and 333.15 K and atmospheric pressure: Experimental and calculated data by NRTL and UNIQUAC models

Mesquita, F. M. R.[Francisca Maria Rodrigues], Pinheiro, R. S.[Regiane Silva], Sant Ana, H. B. d.[Hosiberto B. de], Santiago-Aguiar, R. S.[Rilvia S.]

ABSTRACT