Vapor–Liquid Equilibrium for the 1,1,1-Trifluorotrichloroethane + Sulfuryl Chloride System at 101.3 kPa

Chen, Shuhan; Bao, Zongbi; Lü, Zhengzhang; Yang, Yiwen; Xu, Weiguo; Chen, Zhongmin; Ren, Qilong; Su, Baogen; Xing, Huabin

doi:10.1021/je400544h

Cited by 6 publications

(9 citation statements)

References 16 publications

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“…The experimental data of the boiling point of methanol, ethanol, acetone, and n -hexane at normal pressure is listed in Table compared with the results in ref . The experimental data of the VLE data of acetone (1) + ethanol (2) at 101.33 kPa is listed in Table , which is compared with literature data − in Figure . As can be seen, the agreement is satisfactorily well.…”

Section: Resultsmentioning

confidence: 99%

Isobaric Vapor–Liquid Equilibrium for Nine Binary Systems of Cracking C5 Fraction at 250 kPa

Zhong

et al. 2016

J. Chem. Eng. Data

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The isobaric vapor−liquid equilibrium (VLE) data for nine binary systems of cracking C5 fraction including nhave been measured using a VLE recirculating still. All of the experimental data were checked with the Herington thermodynamic consistency test, which showed thermodynamic consistency. The experimental VLE data were correlated with the Wilson, nonrandom two-liquid (NRTL) and universal quasichemical (UNIQUAC) activity coefficient models. The results show that the calculated values of the vapor-phase mole fraction and boiling temperature by the Wilson, NRTL, and UNIQUAC models agree well with the experimental data. The ideal liquid model was also used to compare with experimental data, which showed a few small differences which indicated the small deviations of these systems from the ideal liquid. The universal quasichemical functional group activity coefficients (UNIFAC) model was also used to predict the VLE data for these systems, which agree well with the experimental data, except cyclopentane + isoprene system which shows a little bigger deviation. ■ INTRODUCTIONThe cracking C5 fraction is the byproduct of ethylene industry, which consist of components such as n-pentane, isopentane, cyclopentane, 2-methyl-2-butene, cyclopentene, and isoprene, etc. These components are a valuable resource in chemical production because of their active chemical properties, which can be used to manufacture petroleum resin and other high value products. Some companies and scholars have conducted relevant research about separation and utilization of the cracking C5 fractions. 1−11 Among the separation methods of these mixtures, distillation is the most widely used method. In the distillation process for the separation of C5 fractions, C5 fractions are usually withdrawn as distillate products. As the boiling point of the C5 fraction at atmospheric pressure is relatively low, weakening the benefit of using cooling water to condense overhead vapor in the condenser of the factory, a sufficiently higher operating pressure of distillation column will be selected. The operating pressure of 250 kPa is a good choice in the distillation process for the separation of C5 fraction. As vapor−liquid equilibrium (VLE) data especially at different pressures are fundamentally important in the design, operation, and optimization of distillation processes, to provide a solid foundation for the design of distillation processes, we focus on the isobaric VLE data of n-pentane + cyclopentane, n-pentane + cyclopentene, isopentane + 2-methyl-2-butene, isopentane + cyclopentene, cyclopentane + 2-methyl-2-butene, cyclopentane + cyclopentene, cyclopentane + isoprene, isoprene + 2-methyl-2-butene, and isoprene + cyclopentene at 250 kPa. However, only few papers have reported the VLE data for these systems, including isobaric VLE data of isopentane + 2-methyl-2-butene at 101.32 kPa, 12 isobaric VLE data of isoprene + 2-methyl-2-butene at 101.6 kPa, 12 101.32 kPa, 13 and 99.66 kPa, 14 and isothermal VLE data of isoprene + 2-methyl-2-butene at 310.93−322.04 ...

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Section: Resultsmentioning

confidence: 99%

Isobaric Vapor–Liquid Equilibrium for Nine Binary Systems of Cracking C5 Fraction at 250 kPa

Zhong

et al. 2016

J. Chem. Eng. Data

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“…High slopes are observed as x 1 ! 0 along with negative values of the natural logarithm of γ 1 for data series other than those referenced [14][15][16]. This is a clear sign of inconsistency.…”

Section: Verification and Selection Of Data Series 31 Acetone + Ethanolmentioning

confidence: 97%

“…There are 10 useful references in literature containing VLE data for the acetone(1) + ethanol(2) system [10][11][12][13][14][15][16][17][18][19] showing a total of 15 experimental series. In Figure 1, seven sets are iso-p (Figure 1(a)), and eight sets are iso-T (Figure 1(b)).…”

Section: Verification and Selection Of Data Series 31 Acetone + Ethanolmentioning

confidence: 99%

A Practical Fitting Method Involving a Trade-Off Decision in the Parametrization Procedure of a Thermodynamic Model and Its Repercussion on Distillation Processes

Sosa¹,

Fernández²,

Gómez³

et al. 2019

Distillation - Modelling, Simulation and Optimization

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The design of processes containing information on phase equilibria must be carried out through a series of steps, experimentation $ verification $ modeling $ simulation. Each of these steps should be rigorously performed to guarantee a good representation of the behavior of the system under study, whose adequate modeling could be used to simulate the corresponding process. To carry out the different previous tasks, two representative systems, extracted from known database, are used. The quality checking of experimental data series is certified through several thermodynamic consistency methods. The modeling is done by applying a multiobjective optimization procedure, which allows to define a solution front (Pareto front) for different sub-models that are established in this work. The fitness of trade-off solutions, obtained from the efficient front, on the design of distillation processes is analyzed through a simulation.

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“…The thermodynamic consistency tests for the two binary systems were based on the Gibbs–Duhem equation , and verified with the Herington area test . The Gibbs–Duhem equation was …”

Section: Thermodynamic Modelingmentioning

confidence: 99%

Investigation on Thermodynamics in Separation for Ethylene Glycol + Neopentyl Glycol System by Azeotropic Distillation

et al. 2016

J. Chem. Eng. Data

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The isobaric vapor−liquid equilibrium (VLE) data for two binary systems of ethylene glycol (EG) + neopentyl glycol (NPG) and NPG + para-xylene (PX) have been measured under pressure of 101.3 kPa, respectively. The thermodynamic consistency of the experimental isobaric VLE data was tested by means of Herington area test. Meanwhile, the experimental isobaric VLE data have been satisfactorily correlated with Wilson, NRTL, and UNIQUAC models. A conventional azeotropic distillation process has been designed to achieve high-purity products based on preceding results. The product purities of EG and NPG can both achieved at 99.9 mol % with minimal total annual cost (TAC) through sequential iterative optimization procedure.

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Vapor–Liquid Equilibrium for the 1,1,1-Trifluorotrichloroethane + Sulfuryl Chloride System at 101.3 kPa

Cited by 6 publications

References 16 publications

Isobaric Vapor–Liquid Equilibrium for Nine Binary Systems of Cracking C5 Fraction at 250 kPa

Isobaric Vapor–Liquid Equilibrium for Nine Binary Systems of Cracking C5 Fraction at 250 kPa

A Practical Fitting Method Involving a Trade-Off Decision in the Parametrization Procedure of a Thermodynamic Model and Its Repercussion on Distillation Processes

Investigation on Thermodynamics in Separation for Ethylene Glycol + Neopentyl Glycol System by Azeotropic Distillation

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