<?xml version="1.0" encoding="ISO-8859-1"?><article xmlns:mml="http://www.w3.org/1998/Math/MathML" xmlns:xlink="http://www.w3.org/1999/xlink" xmlns:xsi="http://www.w3.org/2001/XMLSchema-instance">
<front>
<journal-meta>
<journal-id>0120-100X</journal-id>
<journal-title><![CDATA[Revista ION]]></journal-title>
<abbrev-journal-title><![CDATA[Rev. ion]]></abbrev-journal-title>
<issn>0120-100X</issn>
<publisher>
<publisher-name><![CDATA[Universidad Industrial de Santander]]></publisher-name>
</publisher>
</journal-meta>
<article-meta>
<article-id>S0120-100X2020000200049</article-id>
<article-id pub-id-type="doi">10.18273/revion.v33n2-2020004</article-id>
<title-group>
<article-title xml:lang="es"><![CDATA[Estimación del equilibrio líquido-vapor del sistema binario acetona-cloroformo mediante el modelo termodinámico de Van Laar y Peng Robinson]]></article-title>
<article-title xml:lang="en"><![CDATA[Prediction of vapour-liquid equilibrium of the binary system acetonechloroform through Van Laar and Peng Robinson thermodynamic model]]></article-title>
<article-title xml:lang="pt"><![CDATA[Estimativa do equilíbrio líquido-vapor do sistema binário acetona-clorofórmio usando o modelo termodinâmico de Van Laar e Peng Robinson]]></article-title>
</title-group>
<contrib-group>
<contrib contrib-type="author">
<name>
<surname><![CDATA[Sandoval Martínez]]></surname>
<given-names><![CDATA[María Isabel]]></given-names>
</name>
<xref ref-type="aff" rid="Aff"/>
</contrib>
<contrib contrib-type="author">
<name>
<surname><![CDATA[Muñoz Navarro]]></surname>
<given-names><![CDATA[Samuel Fernando]]></given-names>
</name>
<xref ref-type="aff" rid="Aff"/>
</contrib>
<contrib contrib-type="author">
<name>
<surname><![CDATA[Martinez Jiménez]]></surname>
<given-names><![CDATA[Humberto Jose]]></given-names>
</name>
<xref ref-type="aff" rid="Aff"/>
</contrib>
</contrib-group>
<aff id="Af1">
<institution><![CDATA[,Universidad Industrial de Santander Escuela de ingeniería de Petróleos ]]></institution>
<addr-line><![CDATA[ ]]></addr-line>
<country>Colombia</country>
</aff>
<aff id="Af2">
<institution><![CDATA[,Universidad Industrial de Santander Escuela de ingeniería de Petróleos ]]></institution>
<addr-line><![CDATA[ ]]></addr-line>
<country>Colombia</country>
</aff>
<aff id="Af3">
<institution><![CDATA[,Universidad Industrial de Santander Escuela de ingeniería de Petróleos ]]></institution>
<addr-line><![CDATA[ ]]></addr-line>
<country>Colombia</country>
</aff>
<pub-date pub-type="pub">
<day>00</day>
<month>12</month>
<year>2020</year>
</pub-date>
<pub-date pub-type="epub">
<day>00</day>
<month>12</month>
<year>2020</year>
</pub-date>
<volume>33</volume>
<numero>2</numero>
<fpage>49</fpage>
<lpage>60</lpage>
<copyright-statement/>
<copyright-year/>
<self-uri xlink:href="http://www.scielo.org.co/scielo.php?script=sci_arttext&amp;pid=S0120-100X2020000200049&amp;lng=en&amp;nrm=iso"></self-uri><self-uri xlink:href="http://www.scielo.org.co/scielo.php?script=sci_abstract&amp;pid=S0120-100X2020000200049&amp;lng=en&amp;nrm=iso"></self-uri><self-uri xlink:href="http://www.scielo.org.co/scielo.php?script=sci_pdf&amp;pid=S0120-100X2020000200049&amp;lng=en&amp;nrm=iso"></self-uri><abstract abstract-type="short" xml:lang="es"><p><![CDATA[Resumen La determinación del equilibrio líquido-vapor de diferentes sistemas es información muy importante para la caracterización de las mezclas y los procesos de separación de estas. El equilibrio es estimado de forma experimental; sin embargo, su ejecución tiene altos costos por la precisión que se demanda en dichas pruebas. Una solución viable a la problemática planteada es el uso modelos termodinámicos que permitan obtener el equilibrio de fases. El presente artículo muestra la metodología para la estimación del equilibrio líquido-vapor de un sistema binario no ideal azeotropo, tomando como ejemplo la mezcla de acetona y cloroformo, en la herramienta software Matlab 9.0. Para dar cumplimiento al principal objetivo de la investigación, se elaboró la curva de rocío y burbuja usando la ecuación cúbica de Peng Robinson para calcular los coeficientes de fugacidad, y el modelo termodinámico de Van Laar para los coeficientes de actividad. Las curvas resultantes fueron comparadas con las curvas obtenidas experimentalmente a una temperatura de 50 °C y 35,17 °C, mostrando un buen ajuste, con errores relativos promedios inferiores a 3,9%. Adicionalmente, los resultados fueron comparados con los estimados a través del simulador de procesos químicos Aspen HYSYS y con un programa comercial (VLE Cal) alcanzando porcentajes de error promedio inferiores al 1%.]]></p></abstract>
<abstract abstract-type="short" xml:lang="en"><p><![CDATA[Abstract The Determination of the liquid-vapor equilibrium of different systems is very important information for the mixtures characterization and its separation processes. Equilibrium is estimated experimentally; however, its execution has high costs due to the precision demanded in said tests. A good solution to this problem is to employ thermodynamic models that allow obtaining phase equilibrium. This article shows the methodology for estimating the liquid-vapor balance of a non-ideal azeotrope binary system, taking as an example the mixture of acetone and chloroform, in the Matlab 9.0 software tool. To reach the main objective of the research, the dew and bubble curve was developed, using the cubic equation of Peng Robinson to calculate the fugacity coefficients, and the thermodynamic model of Van Laar for the activity coefficients. The resulting curves were compared with the curves obtained experimentally at a temperature of 50 °C and 35.17 °C, showing a well fit, with average relative errors of less than 3.9%. Additionally, the results were compared with those estimated through the Aspen HYSYS chemical process simulator and with a commercial program (VLE Cal), reaching average error percentages of less than 1%.]]></p></abstract>
<abstract abstract-type="short" xml:lang="pt"><p><![CDATA[Resumo A determinação do equilíbrio líquido-vapor de diferentes sistemas é uma informação muito importante para a caracterização de misturas e seus processos de separação. O equilíbrio é estimado experimentalmente; no entanto, sua execução apresenta altos custos devido à precisão exigida nos referidos testes. Uma solução viável para o problema proposto é o uso de modelos termodinâmicos que permitem obter o equilíbrio de fases. Este artigo mostra a metodologia para estimar o equilíbrio líquido-vapor de um sistema binário azeotrópico não ideal, tomando como exemplo a mistura de acetona e clorofórmio, na ferramenta de software Matlab 9.0. Para cumprir o objetivo principal da pesquisa, foi desenvolvida a curva de orvalho e bolha, usando a equação cúbica de Peng Robinson para calcular os coeficientes de fugacidade e o modelo termodinâmico de Van Laar para os coeficientes de atividade. As curvas resultantes foram comparadas com as curvas obtidas experimentalmente a uma temperatura de 50 °C e 35,17 °C, mostrando um bom ajuste, com erros relativos médios inferiores a 3,9%. Além disso, os resultados foram comparados com os estimados através do simulador de processo químico Aspen HYSYS e com um programa comercial (VLE cal), atingindo percentuais médios de erro inferiores a 1%.]]></p></abstract>
<kwd-group>
<kwd lng="es"><![CDATA[Equilibrio Líquido-Vapor]]></kwd>
<kwd lng="es"><![CDATA[Acetona-Cloroformo]]></kwd>
<kwd lng="es"><![CDATA[Modelo Van Laar]]></kwd>
<kwd lng="es"><![CDATA[Coeficiente de Actividad]]></kwd>
<kwd lng="es"><![CDATA[Coeficiente de Fugacidad]]></kwd>
<kwd lng="en"><![CDATA[Liquid-Gas Equilibrium]]></kwd>
<kwd lng="en"><![CDATA[Acetone-Chloroforme]]></kwd>
<kwd lng="en"><![CDATA[Van Laar Model]]></kwd>
<kwd lng="en"><![CDATA[Fugacity Coefficient]]></kwd>
<kwd lng="en"><![CDATA[Activity Coefficient]]></kwd>
<kwd lng="pt"><![CDATA[Equilíbrio Líquido-Vapor]]></kwd>
<kwd lng="pt"><![CDATA[Acetona-Clorofórmio]]></kwd>
<kwd lng="pt"><![CDATA[Modelo de Van Laar]]></kwd>
<kwd lng="pt"><![CDATA[Coeficiente de Atividade]]></kwd>
<kwd lng="pt"><![CDATA[Coeficiente de Fugacidade]]></kwd>
</kwd-group>
</article-meta>
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