Vapour-liquid equilibria—III. Total vapour pressure measurements for binary mixtures of methanol, ethanol, 1-propanol and 1-butanol with benzene, toluene and p-xylene at 313.15 K

Oracz, Paweł; Kolasińska, G.

doi:10.1016/0378-3812(87)80016-x

Cited by 63 publications

(19 citation statements)

References 61 publications

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“…(a) Benzene (2) : VLE at (□) T = 313 K [56], (○) T = 373 K [57] and (∆) T = 453 K [57]. (b) Toluene (2) : VLE at (□) T = 313 K [58,59]. (c) Benzene (2) : h E under P = 0.101 MPa and at (□) T = 298 K [60] and (◊) T = 318 K [61].…”

Section: List Of Symbolsmentioning

confidence: 99%

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

Neau¹,

Raspo²,

Escandell³

2016

Fluid Phase Equilibria

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The goal of this study is to propose a modification of the NRTL-PR EoS for the prediction of phase equilibria and excess enthalpies in mixtures containing methanol with hydrocarbons; indeed, with these systems, the original equation is confronted to many difficulties arising from the simultaneous prediction of liquid-liquid equilibria together with vapor-liquid and enthalpy data. For this purpose, an additional term is included in the EoS excess Gibbs energy, E EoS g , of the Peng-Robinson equation to account for the self-association of methanol. The resulting NRTL-PRA EoS is successfully used for the prediction of both liquid-liquid and vapor-liquid equilibria, as well as excess enthalpies, in mixtures of methanol with hydrocarbons, light gases and associating compounds. Results are comparable to those obtained with other predictive EoS (VTPR and SAFT), but with the main advantage to predict all thermodynamic properties with a simple cubic equation.

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Section: List Of Symbolsmentioning

confidence: 99%

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

Neau¹,

Raspo²,

Escandell³

2016

Fluid Phase Equilibria

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“…Isobaric vapor-liquid equilibrium data for 1-butanol-p-xylene system have not been reported to date at 97.3 kPa, whereas isothermal vapor-liquid equilibrium data at 308.15 K [1] and 313.15 K [2] and bubble temperature measurements at 95.1 kPa [3] have been reported earlier for the system studied. The experimental data generated in this study is comparable to the earlier reported data.…”

Section: Introductionmentioning

confidence: 72%

Isobaric Vapor–Liquid Equilibria of 1-Butanol–p-Xylene System

2006

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Isobaric vapor-liquid equilibrium data were obtained for 1-butanol-p-xylene system at 97.3 kPa using a vapor recirculating type (modified Othmer's) equilibrium still. The activity coefficients were obtained by taking into consideration vapor-phase imperfections. The experimental data for this system were tested for thermodynamic consistency and were correlated by various equations. The system forms a minimum boiling azeotrope.

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“…Ethanol was modeled with the (a) 2B scheme and (b) 2C scheme. Experimental data are from ◇ ref and ● ref .…”

Section: Resultsmentioning

confidence: 99%

A Quadrupolar SAFT-VR Mie Approach to Modeling Binary Mixtures of CO₂ or Benzene with n-Alkanes or 1-Alkanols

2020

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SAFT-VR Mie is extended to quadrupolar molecules and their mixtures by incorporating an explicit Helmholtz contribution for quadrupole−quadrupole interactions. Two quadrupolar terms are considered: the quadrupolar theory of Larsen and coworkers, and that of Gross, yielding VRM-L and VRM-G, respectively. Each model requires an additional parameter for quadrupolar molecules. The two quadrupolar models are evaluated by means of their ability to model the following binary systems: CO 2 or benzene with n-alkanes or 1-alkanols and binary mixtures of quadrupolar molecules. VRM-L and VRM-G offer significant improvements over nonpolar SAFT-VR Mie in describing the VLE of the CO 2 + n-alkane systems, while only the benzene + n-hexane system requires the additional quadrupolar term for accurate description. Cross-association in CO 2 + 1-alkanol systems is accounted for by fine-tuning the association parameters of CO 2 , resulting in an improved description of these systems using VRM-G. Less promising results are obtained with VRM-L. VRM-L and VRM-G can describe benzene + 1-alkanol systems without cross-association. The quadrupolar models can qualitatively represent the VLLE of CO 2 + n-alkane and CO 2 + 1-alkanol systems. Good predictions of the CO 2 + benzene system are obtained with both VRM-L and VRM-G when only CO 2 is modeled as quadrupolar.

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Vapour-liquid equilibria—III. Total vapour pressure measurements for binary mixtures of methanol, ethanol, 1-propanol and 1-butanol with benzene, toluene and p-xylene at 313.15 K

Cited by 63 publications

References 61 publications

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

Isobaric Vapor–Liquid Equilibria of 1-Butanol–p-Xylene System

A Quadrupolar SAFT-VR Mie Approach to Modeling Binary Mixtures of CO₂ or Benzene with n-Alkanes or 1-Alkanols

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Vapour-liquid equilibria—III. Total vapour pressure measurements for binary mixtures of methanol, ethanol, 1-propanol and 1-butanol with benzene, toluene and p-xylene at 313.15 K

Cited by 63 publications

References 61 publications

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

The NRTL-PRA group contribution EoS for the simultaneous prediction of LLE, VLE and h of hydrocarbon mixtures with associating compounds

Isobaric Vapor–Liquid Equilibria of 1-Butanol–p-Xylene System

A Quadrupolar SAFT-VR Mie Approach to Modeling Binary Mixtures of CO2 or Benzene with n-Alkanes or 1-Alkanols

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A Quadrupolar SAFT-VR Mie Approach to Modeling Binary Mixtures of CO₂ or Benzene with n-Alkanes or 1-Alkanols