Versatile Vapor-Liquid Equilibrium Still

Orr, Virgil; Coates, J.H.

doi:10.1021/ie50601a030

Cited by 18 publications

(7 citation statements)

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“…In the ethyl acetateethanol system, the difference between our data and previous data (5) was relatively large. In the water-1-butanol system, our data differed slightly from previous data (4,13).…”

Section: Procedures and Principlecontrasting

confidence: 99%

New apparatus for isobaric dew and bubble point method. Methanol-water, ethyl acetate-ethanol, water-1-butanol, and ethyl acetate-water systems

Kato¹,

Konishi²,

Hirata³

1970

J. Chem. Eng. Data

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Section: Procedures and Principlecontrasting

confidence: 99%

New apparatus for isobaric dew and bubble point method. Methanol-water, ethyl acetate-ethanol, water-1-butanol, and ethyl acetate-water systems

Kato¹,

Konishi²,

Hirata³

1970

J. Chem. Eng. Data

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“…We now turn toward developing relations similar to eqs 5 and 6 for the vapor−liquid equilibrium (VLE) regions of the phase diagram. Figure 5 compares calculations for the Txy diagram of the binary system at 101.325 kPa to the data of Ellis and Garbett, 24 Orr and Coates, 25 and Kharin, Perelygin and Remizov, 26 and suggests that the model provides an overall satisfactory description of the VLE data. However, as previously pointed out by Mathias,11 Txy diagrams are unable to provide quantitative uncertainty estimates, and for this purpose relative volatility charts are needed.…”

Section: Perturbation Schemementioning

confidence: 76%

“…The combined uncertainties (three standard deviations) of mole fractions in the liquid−liquid equilibrium calculations by the NRTL model in the water-rich and 1-butanol-rich regions are 0.002 out of 0.02 (10%) and 0.01 out of 0.357 (2.8%), respectively. The VLE (specifically relative-volatility) combined uncertainties are demonstrated through Figure 8, which shows base and perturbed activity coefficients calculated by the 24 Orr and Coates, 25 and Kharin, Perelygin, and Remizov, 26 respectively. The solid and dashed lines are the liquid and vapor mole fractions, respectively, from the NRTL model.…”

Section: Perturbation Schemementioning

confidence: 99%

“… Txy diagram of the water +1-butanol at 101.325 kPa. The diamond, square, and circular data points are from Ellis and Garbett, Orr and Coates, and Kharin, Perelygin, and Remizov, respectively. The solid and dashed lines are the liquid and vapor mole fractions, respectively, from the NRTL model.…”

Section: Correlation Of Vapor–liquid–liquid Equilibrium In the 1-buta...mentioning

confidence: 99%

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Effect of Phase-Equilibrium Uncertainties on the Separation of Heterogeneous Azeotropes—Application to the Water + 1-Butanol System

Mathias

2016

J. Chem. Eng. Data

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This paper extends application of the Margules-based phase-equilibrium uncertainty method to a system exhibiting a heterogeneous azeotrope. The author developed the method in order to provide practicing engineers with an intuitive and easy-to-apply procedure to quantitatively relate process-design uncertainties to uncertainties in correlated physical properties, specifically nonideal phase equilibrium. The methodology was first applied to two case studies(1) a propylene–propane superfractionator for which small changes in correlated relative volatilities have a large effect on the design of the distillation column; and (2) a dehexanizer column that separates a mixture containing many close-boiling hydrocarbon componentsand demonstrated that the proposed method provides quantitative insight into the effect of property uncertainties for both these diverse process designs and helps to quantify the safety factors that need to be imposed upon the design. In a subsequent study, the methodology was applied to a distillation train that separates the acetone–chloroform–benzene ternary mixture, which contains one maximum-boiling azeotrope, and showed that the approach quantifies the effect of property uncertainties on utility consumption and also identifies limits on operating variables (specifically minimum recycle flow). In this paper, the Margules perturbation method is applied to the separation of the water + 1-butanol binary mixture. The application is complex because this binary exhibits liquid–liquid equilibrium and forms a minimum-boiling azeotrope, and the typical separation scheme includes a decanter as well as two distillation columns. Further, the chosen activity-coefficient model is unable to correlate the data within measurement uncertainty. Nevertheless, the methodology is demonstrated to provide useful quantitative estimates of the design uncertainty resulting from the combined measurement/model phase-equilibrium uncertainty.

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“…The water content of the distillate stream can be then modified according to the overcooling degree enhancing the separation with a relatively poor cost increase since the condenser temperature allows the use of ambient water as a cooling duty. However, as evidenced by well-established experimental data, 31,32 the aqueous phase composition in the temperature range [0 °C, 91 °C] can only vary from 0.9727 to 0.9838 with an x wat aq = 0.98 value at the boiling point without considerably affecting the thermodynamics of the system. On the contrary, the water content in the organic reflux can significantly change; even though this parameter could improve the separation efficiency from an energetical point of view due to the fact that a lower amount of water circulates through the column, it does not modify the separation thermodynamic feasibility since the reflux stream does not take part in the overall mass balance.…”

Section: Case Studymentioning

confidence: 99%

Exploiting Residue Curve Maps to Assess Thermodynamic Feasibility Boundaries under Uncertain Operating Conditions

Pretoro

Montastruc

Manenti

et al. 2020

Ind. Eng. Chem. Res.

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The very first step of almost any separation process design procedure is the thermodynamic feasibility analysis. In the case of distillation, residue curve maps (RCMs) represent an essential tool to assess whether the separation is feasible or not. However, the analysis is generally carried out by referring to nominal operating conditions and product purities as specification. This means that, when process parameters are likely to undergo fluctuations, the prediction of the system response is not that obvious. An ABE/W (acetone−butanol−ethanol/water) mixture was then selected as a case study since it allows us to discuss several non-ideal thermodynamic behaviors and because of the renewed interest in biorefinery and sustainable processes during recent years. Residue curve mapping was then exploited to determine the thermodynamic feasibility range for multicomponent distillation processes as well as for distillation trains and process-intensified solutions taking into account both product purity and product recovery specifications. The final product of this study is a thorough procedure to determine the flexibility boundaries of feed and product compositions as well as an immediate and intuitive graphical representation from a binary standard distillation column to a complex multicomponent dividing wall column application.

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Versatile Vapor-Liquid Equilibrium Still

Cited by 18 publications

References 0 publications

New apparatus for isobaric dew and bubble point method. Methanol-water, ethyl acetate-ethanol, water-1-butanol, and ethyl acetate-water systems

New apparatus for isobaric dew and bubble point method. Methanol-water, ethyl acetate-ethanol, water-1-butanol, and ethyl acetate-water systems

Effect of Phase-Equilibrium Uncertainties on the Separation of Heterogeneous Azeotropes—Application to the Water + 1-Butanol System

Exploiting Residue Curve Maps to Assess Thermodynamic Feasibility Boundaries under Uncertain Operating Conditions

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