The Experts below are selected from a list of 4023 Experts worldwide ranked by ideXlab platform
Yinglong Wang - One of the best experts on this subject based on the ideXlab platform.
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separation of Azeotropic Mixture isopropyl alcohol ethyl acetate by extractive distillation vapor liquid equilibrium measurements and interaction exploration
Fluid Phase Equilibria, 2020Co-Authors: Yi Zhang, Hui Yang, Jun Gao, Lianzheng Zhang, Yinglong WangAbstract:Abstract Isopropyl alcohol and ethyl acetate can be used to produce degradable and renewable fuel. Since isopropyl alcohol + ethyl acetate can form an Azeotropic Mixture, it is a tough task to separate the binary Mixture by general distillation. In this work, extractive distillation process with N, N-dimethylformamide and dimethyl sulfoxide as entrainers was adopted to separate this azeotrope. The binary and ternary vapor-liquid equilibrium data for (isopropyl alcohol + N, N-dimethylformamide), (ethyl acetate + dimethyl sulfoxide), (isopropyl alcohol + ethyl acetate + N, N-dimethylformamide) and (isopropyl alcohol + ethyl acetate + dimethyl sulfoxide) were determined under 101.3 kPa. Meanwhile, the interaction energies between the molecules were calculated to provide the theoretical insight into the separation of the azeotrope of (EA + IPA) by the entrainers. In addition, the NRTL, UNIQUAC and Wilson models were used to fit the determined binary VLE data. The ternary VLE data for (isopropyl alcohol + ethyl acetate + N, N-dimethylformamide) and (isopropyl alcohol + ethyl acetate + dimethyl sulfoxide) were predicted using the NRTL, UNIQUAC and Wilson models with the parameters regressed from the experimental data.
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separation of Azeotropic Mixture 2 2 3 3 tetrafluoro 1 propanol water by extractive distillation entrainers selection and vapour liquid equilibrium measurements
The Journal of Chemical Thermodynamics, 2019Co-Authors: Xianglin Meng, Jun Gao, Xiaowei Liu, Yinglong WangAbstract:Abstract For separating the azeotrope of 2, 2, 3, 3-tetrafluoro-1-propanol (TFP) and water by extractive distillation, N-methyl pyrrolidone (NMP), N-methyl formamide (NMF) and N, N-dimethyl formamide (DMF) were selected as entrainers using the COSMO-SAC model based on solvent capacity. And the charge density surface of entrainers and each component in the azeotrope system were calculated. The vapour-liquid equilibrium (VLE) data for the Mixtures (TFP + NMP), (TFP + NMF) and (TFP + DMF) were measured by a modified Rose-type recirculating still at the pressure 101.3 kPa. The thermodynamic consistency for the VLE data was validated using the Herington and van Ness methods. The VLE data were correlated with NRTL, Wilson and UNIQUAC models, and the interaction parameters of thermodynamic models were fitted. Meanwhile, the effect of the entrainers on the VLE for TFP and water was explored. Compared with NMF and DMF, NMP was adopted as the suitable entrainer for separation of the Azeotropic Mixture TFP and water by extractive distillation.
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ternary liquid liquid equilibrium of an Azeotropic Mixture hexane methanol with different imidazolium based ionic liquids at t 298 15 k and 101 325 kpa
Fluid Phase Equilibria, 2018Co-Authors: Guilin Wen, Yinglong Wang, Wenting Bai, Fengbin Zheng, Juan A Reyeslabarta, Jun GaoAbstract:Abstract The recovery and purification of methanol from its Mixtures is of great importance; to this end, liquid-liquid extraction is an effective method for the separation of azeotropes. In this work, three imidazolium-based ionic liquids were used to separate a hexane-methanol Azeotropic Mixture, and the ternary liquid-liquid equilibria (LLE) data for the systems of hexane + methanol + [MIM][HSO4] (1-methylmidazole hydrogen sulfate), [BMIM][HSO4] (1-Butyl-3-methylimidazolium hydrogen sulfate), [BMIM][OTf] (1-Butyl-3-methylimidazolium trifluoromethansulfonate) were measured at 298.15 K and atmospheric pressure. The separation factor and distribution coefficient were calculated from the experimental LLE data to evaluate the separation performance. The influence of the anions and mono-/di-substituted hydrocarbon chains on the imidazolium cation ring of the LLE was investigated. The experimental LLE data were successfully correlated by non-random two liquid (NRTL) and universal quasi-chemical (UNIQUAC) models, and the binary interaction parameters were obtained.
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effect of solvent flow rates on controllability of extractive distillation for separating binary Azeotropic Mixture
Industrial & Engineering Chemistry Research, 2015Co-Authors: Yinglong Wang, Shisheng Liang, Wei Liu, Zhen Zhang, Zhaoyou ZhuAbstract:The Mixture of n-heptane and isobutanol creates a minimum-boiling azeotrope under atmospheric conditions. Extractive distillation was used for separating n-heptane and isobutanol. A sequential iterative optimization procedure optimized the steady state extractive distillation process to obtain a minimal total annual cost (TAC). The dynamic control of the optimal extractive distillation process showed poor controllability. It was found that the dynamic control performance could be improved if the solvent flow rate was increased properly with a small increase in TAC. Hence, the choice of the optimal extractive distillation process for separating a binary Azeotropic Mixture should be considered from the perspectives of both TAC and the dynamic control performance.
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control of heat integrated pressure swing distillation process for separating Azeotropic Mixture of tetrahydrofuran and methanol
Industrial & Engineering Chemistry Research, 2015Co-Authors: Yinglong Wang, Zhen Zhang, Huan Zhang, Qing ZhangAbstract:Dynamic control of a pressure-swing-distillation process for separation of Azeotropic Mixture of tetrahydrofuran and methanol is explored. The pressure-swing-distillation processes involved with no, partial, and full heat integration are simulated using Aspen Plus Dynamics. The influences of the selection of the sensitive temperature stage in the low-pressure column on the dynamic responses in the pressure-swing distillation with different heat integration were investigated. The results indicate that a suitable temperature control stage in the low-pressure column is crucial to achieve efficient control of the process. In addition, more time is needed to reach the quality specifications under feed disturbances for both components when heat integration is added in the distillation sequence.
Jixin Qian - One of the best experts on this subject based on the ideXlab platform.
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Adding rectifying/stripping section type heat integration to a pressure-swing distillation (PSD) process
Applied Thermal Engineering, 2008Co-Authors: Kejin Huang, Lan Shan, Qunxiong Zhu, Jixin QianAbstract:This paper studies the economical effect of considering rectifying/stripping section type heat integration in a pressure-swing distillation (PSD) process separating a binary homogeneous pressure-sensitive azeotrope. The schemes for arranging heat integration between the rectifying section and the stripping section of the high- and low-pressure distillation columns, respectively, are derived and an effective procedure is devised for the conceptual process design of the heat-integrated PSD processes. In terms of the separation of a binary Azeotropic Mixture of acetonitrile and water, intensive comparisons are made between the conventional and heat-integrated PSD processes. It is demonstrated that breaking a pressure-sensitive Azeotropic Mixture can be made more economical than the current practice with the conventional PSD process. For boosting further the thermodynamic efficiency of a PSD process, it is strongly suggested to consider simultaneously the condenser/reboiler type heat integration with the rectifying/stripping section type heat integration in process synthesis and design.
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adding rectifying stripping section type heat integration to a pressure swing distillation psd process
Applied Thermal Engineering, 2008Co-Authors: Kejin Huang, Lan Shan, Qunxiong Zhu, Jixin QianAbstract:This paper studies the economical effect of considering rectifying/stripping section type heat integration in a pressure-swing distillation (PSD) process separating a binary homogeneous pressure-sensitive azeotrope. The schemes for arranging heat integration between the rectifying section and the stripping section of the high- and low-pressure distillation columns, respectively, are derived and an effective procedure is devised for the conceptual process design of the heat-integrated PSD processes. In terms of the separation of a binary Azeotropic Mixture of acetonitrile and water, intensive comparisons are made between the conventional and heat-integrated PSD processes. It is demonstrated that breaking a pressure-sensitive Azeotropic Mixture can be made more economical than the current practice with the conventional PSD process. For boosting further the thermodynamic efficiency of a PSD process, it is strongly suggested to consider simultaneously the condenser/reboiler type heat integration with the rectifying/stripping section type heat integration in process synthesis and design.
Huiyuan Wang - One of the best experts on this subject based on the ideXlab platform.
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A new entrainer for separation of tetrahydrofuran–water Azeotropic Mixture by extractive distillation
Chemical Engineering and Processing, 2006Co-Authors: Huiyuan WangAbstract:Abstract A new entrainer for separation of tetrahydrofuran–water Azeotropic Mixture by extractive distillation was introduced in this article. 1,2-Propanediol was used as the entrainer instead of 1,4-butanediol, which decreased the reboiler energy and entrainer consumption. Tetrahydrofuran–water extractive binary column distillation system was simulated with the HYSYS software platform. 1,2-Propanediol and 1,4-butanediol are used as solvent in the simulation respectively. Simulation results showed that there are a lot of advantages when 1,2-propanediol was entrainer. The results were then corroborated in a batch experimental column for the selected entrainer.
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a new entrainer for separation of tetrahydrofuran water Azeotropic Mixture by extractive distillation
Chemical Engineering and Processing, 2006Co-Authors: Huiyuan WangAbstract:Abstract A new entrainer for separation of tetrahydrofuran–water Azeotropic Mixture by extractive distillation was introduced in this article. 1,2-Propanediol was used as the entrainer instead of 1,4-butanediol, which decreased the reboiler energy and entrainer consumption. Tetrahydrofuran–water extractive binary column distillation system was simulated with the HYSYS software platform. 1,2-Propanediol and 1,4-butanediol are used as solvent in the simulation respectively. Simulation results showed that there are a lot of advantages when 1,2-propanediol was entrainer. The results were then corroborated in a batch experimental column for the selected entrainer.
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separation of tetrahydrofuran water Azeotropic Mixture by batch extractive distillation process
Chemical Engineering Research & Design, 2006Co-Authors: Huiyuan WangAbstract:Tetrahydrofuran and water formed a minimum azeotrope at 64°C, which contains water 6.7% in mass fraction. We could not use conventional distillation to separate these two components. In this work, a systematic study of the separation of the tetrahydrofuran–water Mixture with a new en trainer by batch extractive distillation was performed. Based upon the lots of computation, 1,2-propanediol was chosen to be the entrainer. It broke the original binary azeotrope. The process feasibility analysis was validated by rigorous simulation with chemical process simulation software—HYSYS. Plant 2.2 and DISTIL 4.1. Simulation results were then corroborated in a batch experimental packing column with the selected entrainer. The experimental and simulation results agreed well.
Kejin Huang - One of the best experts on this subject based on the ideXlab platform.
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Adding rectifying/stripping section type heat integration to a pressure-swing distillation (PSD) process
Applied Thermal Engineering, 2008Co-Authors: Kejin Huang, Lan Shan, Qunxiong Zhu, Jixin QianAbstract:This paper studies the economical effect of considering rectifying/stripping section type heat integration in a pressure-swing distillation (PSD) process separating a binary homogeneous pressure-sensitive azeotrope. The schemes for arranging heat integration between the rectifying section and the stripping section of the high- and low-pressure distillation columns, respectively, are derived and an effective procedure is devised for the conceptual process design of the heat-integrated PSD processes. In terms of the separation of a binary Azeotropic Mixture of acetonitrile and water, intensive comparisons are made between the conventional and heat-integrated PSD processes. It is demonstrated that breaking a pressure-sensitive Azeotropic Mixture can be made more economical than the current practice with the conventional PSD process. For boosting further the thermodynamic efficiency of a PSD process, it is strongly suggested to consider simultaneously the condenser/reboiler type heat integration with the rectifying/stripping section type heat integration in process synthesis and design.
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adding rectifying stripping section type heat integration to a pressure swing distillation psd process
Applied Thermal Engineering, 2008Co-Authors: Kejin Huang, Lan Shan, Qunxiong Zhu, Jixin QianAbstract:This paper studies the economical effect of considering rectifying/stripping section type heat integration in a pressure-swing distillation (PSD) process separating a binary homogeneous pressure-sensitive azeotrope. The schemes for arranging heat integration between the rectifying section and the stripping section of the high- and low-pressure distillation columns, respectively, are derived and an effective procedure is devised for the conceptual process design of the heat-integrated PSD processes. In terms of the separation of a binary Azeotropic Mixture of acetonitrile and water, intensive comparisons are made between the conventional and heat-integrated PSD processes. It is demonstrated that breaking a pressure-sensitive Azeotropic Mixture can be made more economical than the current practice with the conventional PSD process. For boosting further the thermodynamic efficiency of a PSD process, it is strongly suggested to consider simultaneously the condenser/reboiler type heat integration with the rectifying/stripping section type heat integration in process synthesis and design.
Jun Gao - One of the best experts on this subject based on the ideXlab platform.
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separation of Azeotropic Mixture isopropyl alcohol ethyl acetate by extractive distillation vapor liquid equilibrium measurements and interaction exploration
Fluid Phase Equilibria, 2020Co-Authors: Yi Zhang, Hui Yang, Jun Gao, Lianzheng Zhang, Yinglong WangAbstract:Abstract Isopropyl alcohol and ethyl acetate can be used to produce degradable and renewable fuel. Since isopropyl alcohol + ethyl acetate can form an Azeotropic Mixture, it is a tough task to separate the binary Mixture by general distillation. In this work, extractive distillation process with N, N-dimethylformamide and dimethyl sulfoxide as entrainers was adopted to separate this azeotrope. The binary and ternary vapor-liquid equilibrium data for (isopropyl alcohol + N, N-dimethylformamide), (ethyl acetate + dimethyl sulfoxide), (isopropyl alcohol + ethyl acetate + N, N-dimethylformamide) and (isopropyl alcohol + ethyl acetate + dimethyl sulfoxide) were determined under 101.3 kPa. Meanwhile, the interaction energies between the molecules were calculated to provide the theoretical insight into the separation of the azeotrope of (EA + IPA) by the entrainers. In addition, the NRTL, UNIQUAC and Wilson models were used to fit the determined binary VLE data. The ternary VLE data for (isopropyl alcohol + ethyl acetate + N, N-dimethylformamide) and (isopropyl alcohol + ethyl acetate + dimethyl sulfoxide) were predicted using the NRTL, UNIQUAC and Wilson models with the parameters regressed from the experimental data.
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separation of Azeotropic Mixture 2 2 3 3 tetrafluoro 1 propanol water by extractive distillation entrainers selection and vapour liquid equilibrium measurements
The Journal of Chemical Thermodynamics, 2019Co-Authors: Xianglin Meng, Jun Gao, Xiaowei Liu, Yinglong WangAbstract:Abstract For separating the azeotrope of 2, 2, 3, 3-tetrafluoro-1-propanol (TFP) and water by extractive distillation, N-methyl pyrrolidone (NMP), N-methyl formamide (NMF) and N, N-dimethyl formamide (DMF) were selected as entrainers using the COSMO-SAC model based on solvent capacity. And the charge density surface of entrainers and each component in the azeotrope system were calculated. The vapour-liquid equilibrium (VLE) data for the Mixtures (TFP + NMP), (TFP + NMF) and (TFP + DMF) were measured by a modified Rose-type recirculating still at the pressure 101.3 kPa. The thermodynamic consistency for the VLE data was validated using the Herington and van Ness methods. The VLE data were correlated with NRTL, Wilson and UNIQUAC models, and the interaction parameters of thermodynamic models were fitted. Meanwhile, the effect of the entrainers on the VLE for TFP and water was explored. Compared with NMF and DMF, NMP was adopted as the suitable entrainer for separation of the Azeotropic Mixture TFP and water by extractive distillation.
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ternary liquid liquid equilibrium of an Azeotropic Mixture hexane methanol with different imidazolium based ionic liquids at t 298 15 k and 101 325 kpa
Fluid Phase Equilibria, 2018Co-Authors: Guilin Wen, Yinglong Wang, Wenting Bai, Fengbin Zheng, Juan A Reyeslabarta, Jun GaoAbstract:Abstract The recovery and purification of methanol from its Mixtures is of great importance; to this end, liquid-liquid extraction is an effective method for the separation of azeotropes. In this work, three imidazolium-based ionic liquids were used to separate a hexane-methanol Azeotropic Mixture, and the ternary liquid-liquid equilibria (LLE) data for the systems of hexane + methanol + [MIM][HSO4] (1-methylmidazole hydrogen sulfate), [BMIM][HSO4] (1-Butyl-3-methylimidazolium hydrogen sulfate), [BMIM][OTf] (1-Butyl-3-methylimidazolium trifluoromethansulfonate) were measured at 298.15 K and atmospheric pressure. The separation factor and distribution coefficient were calculated from the experimental LLE data to evaluate the separation performance. The influence of the anions and mono-/di-substituted hydrocarbon chains on the imidazolium cation ring of the LLE was investigated. The experimental LLE data were successfully correlated by non-random two liquid (NRTL) and universal quasi-chemical (UNIQUAC) models, and the binary interaction parameters were obtained.
