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Estela Lladosa - One of the best experts on this subject based on the ideXlab platform.
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separation of di n Propyl ether and n Propyl Alcohol by extractive distillation and pressure swing distillation computer simulation and economic optimization
Chemical Engineering and Processing, 2011Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Abstract Azeotropic mixtures are impossible to separate by ordinary distillation. Two of the most common methods for separating a binary homogeneous azeotrope are pressure-swing distillation (PSD) and extractive distillation (ED). The PSD process is effective if the azeotropic composition changes significantly with pressure. The ED process is effective if a suitable solvent can be found. This paper compares these two alternatives to separate a mixture made up of 50 mol% of di-n-Propyl ether and 50 mol% of n-Propyl Alcohol by means of a practical case of a plant to treat 12,000 Tm/year of this mixture. The simulation has been carried out satisfactorily by mean of a package of commercial software (Aspen Hysys ® ) using the thermodynamic model UNIQUAC with binary parameters obtained experimentally by us in previous papers. The two processes evaluated have been optimized independently from each other and the best configurations have been evaluated economically. Results show that, for this particular case, the PSD is more attractive than the extractive distillation.
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Isobaric Vapor−Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
Journal of Chemical & Engineering Data, 2009Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Roberto BavieraAbstract:Consistent vapor−liquid equilibrium data at 101.3 kPa have been determined for the ternary system diisoPropyl ether (1) + 2-Propyl Alcohol (2) + n-butyl propionate (3) and two constituent binary systems: diisoPropyl ether (1) + n-butyl propionate (3) and 2-Propyl Alcohol (2) + n-butyl propionate (3). The diisoPropyl ether (1) + n-butyl propionate (3) system does not present deviation from ideal behavior, and the 2-Propyl Alcohol (2) + n-butyl propionate (3) system shows light positive deviation from Raoult’s law. The activity coefficients of the solutions were correlated with their compositions by the Wilson, NRTL, and UNIQUAC models. Wisniak−Tamir equations were used to correlate the boiling points of the solutions with its composition. The binary VLE data measured in the present study passed the thermodynamic consistency test of Fredeslund et al. The ternary system is very well predicted from binary interaction parameters and passed both the Wisniak L−W and McDermott−Ellis consistency tests. The change ...
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isobaric vapor liquid equilibria for binary and ternary mixtures of diisoPropyl ether 2 Propyl Alcohol and n butyl propionate at 101 3 kpa
Journal of Chemical & Engineering Data, 2009Co-Authors: Estela Lladosa, Juan B. Montón, Cruz M Burguet, Roberto BavieraAbstract:Consistent vapor−liquid equilibrium data at 101.3 kPa have been determined for the ternary system diisoPropyl ether (1) + 2-Propyl Alcohol (2) + n-butyl propionate (3) and two constituent binary systems: diisoPropyl ether (1) + n-butyl propionate (3) and 2-Propyl Alcohol (2) + n-butyl propionate (3). The diisoPropyl ether (1) + n-butyl propionate (3) system does not present deviation from ideal behavior, and the 2-Propyl Alcohol (2) + n-butyl propionate (3) system shows light positive deviation from Raoult’s law. The activity coefficients of the solutions were correlated with their compositions by the Wilson, NRTL, and UNIQUAC models. Wisniak−Tamir equations were used to correlate the boiling points of the solutions with its composition. The binary VLE data measured in the present study passed the thermodynamic consistency test of Fredeslund et al. The ternary system is very well predicted from binary interaction parameters and passed both the Wisniak L−W and McDermott−Ellis consistency tests. The change ...
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isobaric vapour liquid liquid equilibrium data for di n Propyl ether n Propyl Alcohol water and diisoPropyl ether isoPropyl Alcohol water systems at 100 kpa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
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Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
Journal of Chemical & Engineering Data, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Consistent vapor−liquid equilibrium data for the binary and ternary systems diisoPropyl ether (1) + 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) are reported at 101.3 kPa. The diisoPropyl ether (1) + 3-methyl-1-butanol (3) system shows positive deviations from ideal behavior, and the 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) system exhibits slight deviations from ideal behavior. The activity coefficients and the boiling points were correlated with their compositions by the Wilson, NRTL, UNIQUAC, and Wisniak−Tamir equations. It is shown that these models allow a very good prediction of the phase equilibria of the ternary system using the pertinent parameters of the binary systems. 3-Methyl-1-butanol eliminates the diisoPropyl ether (1) + 2-Propyl Alcohol (2) binary azeotrope. The change of phase equilibria behavior is significant; therefore, this solvent seems to be an effective agent for the separation of the azeotropic mixture by extractive distillation.
Rosa Muñoz - One of the best experts on this subject based on the ideXlab platform.
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phase equilibria involved in extractive distillation of diPropyl ether 1 Propyl Alcohol using 2 ethoxyethanol as entrainer
Fluid Phase Equilibria, 2007Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Rosa MuñozAbstract:Abstract Consistent vapour–liquid equilibrium data at 101.3 kPa have been determined for the ternary system diPropyl ether + 1-Propyl Alcohol + 2-ethoxyethanol and two constituent binary systems: diPropyl ether + 2-ethoxyethanol and 1-Propyl Alcohol + 2-ethoxyethanol. The diPropyl ether + 2-ethoxyethanol system shows positive deviations from ideal behaviour and 1-Propyl Alcohol + 2-ethoxyethanol system exhibits no deviation from ideal behaviour. The activity coefficients and the boiling points were correlated with their compositions by the Wilson, NRTL and UNIQUAC equations. It is shown that the models allow a very good prediction of the phase equilibria of the ternary system using the pertinent parameters of the binary systems. The parameters obtained from binary data were utilized to predict the phase behaviour of the ternary system. The results showed a good agreement with the experimental values. Moreover, the entrainer capabilities of 2-ethoxyethanol were compared with 1-pentanol, butyl propionate and N,N-dimethylformamide, concluding that N,N-dimethylformamide is the best entrainer.
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phase equilibria involved in extractive distillation of diPropyl ether 1 Propyl Alcohol using n n dimethylformamide as entrainer
Journal of Chemical & Engineering Data, 2007Co-Authors: Estela Lladosa, Juan B. Montón, And M. Cruz Burguet, Rosa MuñozAbstract:Consistent vapor−liquid equilibrium data for the binary and ternary systems diPropyl ether (1) + 1-Propyl Alcohol (2) + N,N-dimethylformamide (3) are reported at 101.3 kPa. The results indicate that diPropyl ether (1) + N,N-dimethylformamide (3) system exhibits a positive deviation from ideal behavior and that 1-Propyl Alcohol (2) + N,N-dimethylformamide (3) system deviates negatively from ideality. The activity coefficients of the solutions were correlated by the Wilson, NRTL, and UNIQUAC models. It is shown that these models allow a very good prediction of the phase equilibrium of the ternary system using the pertinent parameters of the binary systems. In addition, the Wisniak−Tamir relations were used for correlating bubble-point temperatures.
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Phase equilibria involved in extractive distillation of diPropyl ether + 1-Propyl Alcohol using 2-ethoxyethanol as entrainer
Fluid Phase Equilibria, 2007Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Rosa MuñozAbstract:Abstract Consistent vapour–liquid equilibrium data at 101.3 kPa have been determined for the ternary system diPropyl ether + 1-Propyl Alcohol + 2-ethoxyethanol and two constituent binary systems: diPropyl ether + 2-ethoxyethanol and 1-Propyl Alcohol + 2-ethoxyethanol. The diPropyl ether + 2-ethoxyethanol system shows positive deviations from ideal behaviour and 1-Propyl Alcohol + 2-ethoxyethanol system exhibits no deviation from ideal behaviour. The activity coefficients and the boiling points were correlated with their compositions by the Wilson, NRTL and UNIQUAC equations. It is shown that the models allow a very good prediction of the phase equilibria of the ternary system using the pertinent parameters of the binary systems. The parameters obtained from binary data were utilized to predict the phase behaviour of the ternary system. The results showed a good agreement with the experimental values. Moreover, the entrainer capabilities of 2-ethoxyethanol were compared with 1-pentanol, butyl propionate and N,N-dimethylformamide, concluding that N,N-dimethylformamide is the best entrainer.
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Phase equilibria involved in extractive distillation of diPropyl ether + 1-Propyl Alcohol using N,N-dimethylformamide as entrainer
Journal of Chemical & Engineering Data, 2007Co-Authors: Estela Lladosa, Juan B. Montón, And M. Cruz Burguet, Rosa MuñozAbstract:Consistent vapor−liquid equilibrium data for the binary and ternary systems diPropyl ether (1) + 1-Propyl Alcohol (2) + N,N-dimethylformamide (3) are reported at 101.3 kPa. The results indicate that diPropyl ether (1) + N,N-dimethylformamide (3) system exhibits a positive deviation from ideal behavior and that 1-Propyl Alcohol (2) + N,N-dimethylformamide (3) system deviates negatively from ideality. The activity coefficients of the solutions were correlated by the Wilson, NRTL, and UNIQUAC models. It is shown that these models allow a very good prediction of the phase equilibrium of the ternary system using the pertinent parameters of the binary systems. In addition, the Wisniak−Tamir relations were used for correlating bubble-point temperatures.
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isobaric vapor liquid equilibria for binary and ternary mixtures of diPropyl ether 1 Propyl Alcohol and butyl propionate
Journal of Chemical & Engineering Data, 2006Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Rosa MuñozAbstract:Consistent vapor−liquid equilibrium (VLE) data at 101.3 kPa have been determined for the ternary system diPropyl ether + 1-Propyl Alcohol + butyl propionate and two constituent binary systems: diPropyl ether + butyl propionate and 1-Propyl Alcohol + butyl propionate. The diPropyl ether + butyl propionate system exhibits ideal behavior, and the 1-Propyl Alcohol + butyl propionate system shows positive deviations from Raoult's law. No additional azeotropes are present. The activity coefficients of the solutions were correlated with its composition by the Wilson, NRTL, and UNIQUAC models. The ternary system is well-predicted from binary interaction parameters. Butyl propionate breaks the diPropyl ether/1-Propyl Alcohol binary azeotrope. However, the change of phase equilibria behavior is small; therefore, this solvent is not such an effective agent to this azeotrope mixture separation. In fact, the mean relative volatility on a solvent-free basis is 0.82 (close to unity).
Juan B. Montón - One of the best experts on this subject based on the ideXlab platform.
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separation of di n Propyl ether and n Propyl Alcohol by extractive distillation and pressure swing distillation computer simulation and economic optimization
Chemical Engineering and Processing, 2011Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Abstract Azeotropic mixtures are impossible to separate by ordinary distillation. Two of the most common methods for separating a binary homogeneous azeotrope are pressure-swing distillation (PSD) and extractive distillation (ED). The PSD process is effective if the azeotropic composition changes significantly with pressure. The ED process is effective if a suitable solvent can be found. This paper compares these two alternatives to separate a mixture made up of 50 mol% of di-n-Propyl ether and 50 mol% of n-Propyl Alcohol by means of a practical case of a plant to treat 12,000 Tm/year of this mixture. The simulation has been carried out satisfactorily by mean of a package of commercial software (Aspen Hysys ® ) using the thermodynamic model UNIQUAC with binary parameters obtained experimentally by us in previous papers. The two processes evaluated have been optimized independently from each other and the best configurations have been evaluated economically. Results show that, for this particular case, the PSD is more attractive than the extractive distillation.
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Isobaric Vapor−Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
Journal of Chemical & Engineering Data, 2009Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Roberto BavieraAbstract:Consistent vapor−liquid equilibrium data at 101.3 kPa have been determined for the ternary system diisoPropyl ether (1) + 2-Propyl Alcohol (2) + n-butyl propionate (3) and two constituent binary systems: diisoPropyl ether (1) + n-butyl propionate (3) and 2-Propyl Alcohol (2) + n-butyl propionate (3). The diisoPropyl ether (1) + n-butyl propionate (3) system does not present deviation from ideal behavior, and the 2-Propyl Alcohol (2) + n-butyl propionate (3) system shows light positive deviation from Raoult’s law. The activity coefficients of the solutions were correlated with their compositions by the Wilson, NRTL, and UNIQUAC models. Wisniak−Tamir equations were used to correlate the boiling points of the solutions with its composition. The binary VLE data measured in the present study passed the thermodynamic consistency test of Fredeslund et al. The ternary system is very well predicted from binary interaction parameters and passed both the Wisniak L−W and McDermott−Ellis consistency tests. The change ...
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isobaric vapor liquid equilibria for binary and ternary mixtures of diisoPropyl ether 2 Propyl Alcohol and n butyl propionate at 101 3 kpa
Journal of Chemical & Engineering Data, 2009Co-Authors: Estela Lladosa, Juan B. Montón, Cruz M Burguet, Roberto BavieraAbstract:Consistent vapor−liquid equilibrium data at 101.3 kPa have been determined for the ternary system diisoPropyl ether (1) + 2-Propyl Alcohol (2) + n-butyl propionate (3) and two constituent binary systems: diisoPropyl ether (1) + n-butyl propionate (3) and 2-Propyl Alcohol (2) + n-butyl propionate (3). The diisoPropyl ether (1) + n-butyl propionate (3) system does not present deviation from ideal behavior, and the 2-Propyl Alcohol (2) + n-butyl propionate (3) system shows light positive deviation from Raoult’s law. The activity coefficients of the solutions were correlated with their compositions by the Wilson, NRTL, and UNIQUAC models. Wisniak−Tamir equations were used to correlate the boiling points of the solutions with its composition. The binary VLE data measured in the present study passed the thermodynamic consistency test of Fredeslund et al. The ternary system is very well predicted from binary interaction parameters and passed both the Wisniak L−W and McDermott−Ellis consistency tests. The change ...
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isobaric vapour liquid liquid equilibrium data for di n Propyl ether n Propyl Alcohol water and diisoPropyl ether isoPropyl Alcohol water systems at 100 kpa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
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Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
Journal of Chemical & Engineering Data, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Consistent vapor−liquid equilibrium data for the binary and ternary systems diisoPropyl ether (1) + 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) are reported at 101.3 kPa. The diisoPropyl ether (1) + 3-methyl-1-butanol (3) system shows positive deviations from ideal behavior, and the 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) system exhibits slight deviations from ideal behavior. The activity coefficients and the boiling points were correlated with their compositions by the Wilson, NRTL, UNIQUAC, and Wisniak−Tamir equations. It is shown that these models allow a very good prediction of the phase equilibria of the ternary system using the pertinent parameters of the binary systems. 3-Methyl-1-butanol eliminates the diisoPropyl ether (1) + 2-Propyl Alcohol (2) binary azeotrope. The change of phase equilibria behavior is significant; therefore, this solvent seems to be an effective agent for the separation of the azeotropic mixture by extractive distillation.
M C Burguet - One of the best experts on this subject based on the ideXlab platform.
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separation of di n Propyl ether and n Propyl Alcohol by extractive distillation and pressure swing distillation computer simulation and economic optimization
Chemical Engineering and Processing, 2011Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Abstract Azeotropic mixtures are impossible to separate by ordinary distillation. Two of the most common methods for separating a binary homogeneous azeotrope are pressure-swing distillation (PSD) and extractive distillation (ED). The PSD process is effective if the azeotropic composition changes significantly with pressure. The ED process is effective if a suitable solvent can be found. This paper compares these two alternatives to separate a mixture made up of 50 mol% of di-n-Propyl ether and 50 mol% of n-Propyl Alcohol by means of a practical case of a plant to treat 12,000 Tm/year of this mixture. The simulation has been carried out satisfactorily by mean of a package of commercial software (Aspen Hysys ® ) using the thermodynamic model UNIQUAC with binary parameters obtained experimentally by us in previous papers. The two processes evaluated have been optimized independently from each other and the best configurations have been evaluated economically. Results show that, for this particular case, the PSD is more attractive than the extractive distillation.
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Isobaric Vapor−Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
Journal of Chemical & Engineering Data, 2009Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Roberto BavieraAbstract:Consistent vapor−liquid equilibrium data at 101.3 kPa have been determined for the ternary system diisoPropyl ether (1) + 2-Propyl Alcohol (2) + n-butyl propionate (3) and two constituent binary systems: diisoPropyl ether (1) + n-butyl propionate (3) and 2-Propyl Alcohol (2) + n-butyl propionate (3). The diisoPropyl ether (1) + n-butyl propionate (3) system does not present deviation from ideal behavior, and the 2-Propyl Alcohol (2) + n-butyl propionate (3) system shows light positive deviation from Raoult’s law. The activity coefficients of the solutions were correlated with their compositions by the Wilson, NRTL, and UNIQUAC models. Wisniak−Tamir equations were used to correlate the boiling points of the solutions with its composition. The binary VLE data measured in the present study passed the thermodynamic consistency test of Fredeslund et al. The ternary system is very well predicted from binary interaction parameters and passed both the Wisniak L−W and McDermott−Ellis consistency tests. The change ...
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isobaric vapour liquid liquid equilibrium data for di n Propyl ether n Propyl Alcohol water and diisoPropyl ether isoPropyl Alcohol water systems at 100 kpa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
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Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of DiisoPropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
Journal of Chemical & Engineering Data, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C BurguetAbstract:Consistent vapor−liquid equilibrium data for the binary and ternary systems diisoPropyl ether (1) + 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) are reported at 101.3 kPa. The diisoPropyl ether (1) + 3-methyl-1-butanol (3) system shows positive deviations from ideal behavior, and the 2-Propyl Alcohol (2) + 3-methyl-1-butanol (3) system exhibits slight deviations from ideal behavior. The activity coefficients and the boiling points were correlated with their compositions by the Wilson, NRTL, UNIQUAC, and Wisniak−Tamir equations. It is shown that these models allow a very good prediction of the phase equilibria of the ternary system using the pertinent parameters of the binary systems. 3-Methyl-1-butanol eliminates the diisoPropyl ether (1) + 2-Propyl Alcohol (2) binary azeotrope. The change of phase equilibria behavior is significant; therefore, this solvent seems to be an effective agent for the separation of the azeotropic mixture by extractive distillation.
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Isobaric (vapour + liquid + liquid) equilibrium data for (di-n-Propyl ether + n-Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) systems at 100 kPa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
Javier De La Torre - One of the best experts on this subject based on the ideXlab platform.
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isobaric vapour liquid liquid equilibrium data for di n Propyl ether n Propyl Alcohol water and diisoPropyl ether isoPropyl Alcohol water systems at 100 kpa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
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Isobaric (vapour + liquid + liquid) equilibrium data for (di-n-Propyl ether + n-Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) systems at 100 kPa
The Journal of Chemical Thermodynamics, 2008Co-Authors: Estela Lladosa, Juan B. Montón, M C Burguet, Javier De La TorreAbstract:Abstract Isobaric (vapour + liquid + liquid) equilibria were measured for the (di- n -Propyl ether + n -Propyl Alcohol + water) and (diisoPropyl ether + isoPropyl Alcohol + water) system at 100 kPa. The apparatus used for the determination of (vapour + liquid + liquid) equilibrium data was an all-glass dynamic recirculating still with an ultrasonic homogenizer couple to the boiling flask. The experimental data demonstrated the existence of a heterogeneous ternary azeotrope for both ternary systems. The (vapour + liquid + liquid) equilibria data were found to be thermodynamically consistent for both systems. The experimental data were compared with the estimation using UNIQUAC and NRTL models and the prediction of UNIFAC model.
