Nomenclature


6. Conclusions

separation operation.

Acknowledgements

support received.

Nomenclature

gE

g ð Þ i-j

The different theoretical and practical settings related to azeotropy within the context of chemical engineering, have been described taking into account the experience of our research group in this area. The relationship between the presence of azeotropes, the non-ideality of the solution and the difference in vapor pressures of the pure compounds has been exposed. This information, together with some additional knowledge about the compounds involved in a

The combination of direct and indirect measuring techniques, together with suitable treatment of the results, is an excellent way to generate experimental data on which to base the studies. On the other hand, the polynomial equation proposed and used here would seem to be the best option to model the systems, provided that the parameters are optimized using all the

For the prediction of azeotropes, COSMO-RS method produces the best results, although in some cases the quantitative values produced by UNIFAC-DM approximate real values. Simulation of a process by pressure-swing-distillation and another by extractive-distillation allow verify the impact of the modeling and selection of the design parameters on the results of the

This work was supported by MINECO from Spanish Government, Grant CTQ2015-68428-P. One of us (AS) is grateful to the ACIISI (from Canaries government, No. 2015010110) for the

Bii, Bij, m3 mol�<sup>1</sup> second Virial coefficient for pure component "i" and ij-pair for mixtures

<sup>k</sup> coefficients for molar Gibbs excess energy model in Eq. (17) for binary i-j

C<sup>n</sup> ternary parameters for molar Gibbs excess model in Eq. (18)

   

� <sup>100</sup>=<sup>f</sup> exp )

solution, can be used to estimate the appearance of the azeotrope.

166 Laboratory Unit Operations and Experimental Methods in Chemical Engineering

experimental data available by means of a combined correlation procedure.

ARDf relative deviations in absolute value (� <sup>f</sup> exp � <sup>f</sup> est

n,N excess molar Gibbs function given by Eq. (15)

Gij interaction parameters of NRTL model

FS feed stage in distillation column

<sup>g</sup>E, J�mol�<sup>1</sup> excess molar Gibbs function

