LrgpV1, PascalFrancis, Corpus, bibRecord, 000013

Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology

Identifieur interne : 000013 ( PascalFrancis/Corpus ); précédent : 000012; suivant : 000014

Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology

Auteurs : R. Paulen ; B. Benyahia ; M. A. Latifi ; M. Fikar

Source :

Computers & chemical engineering [ 0098-1354 ] ; 2014.

RBID : Pascal:14-0166144

Descripteurs français

Pascal (Inist)
- Copolymérisation émulsion, Transition vitreuse, Poids, Distribution dimension particule, Vitesse avancement, Emulsion, Productivité, Condition opératoire, Devis descriptif, Structure coeur couche, Polymérisation émulsion, Procédé discontinu, Réacteur chimique, Réacteur polymérisation, Styrène, Température transition, Polymère, Monomère, Programmation dynamique, Modélisation, Masse moléculaire, Optimisation, Paramétrisation, En semi continu, Etude expérimentale, Dispositif alimentation, ..

English descriptors

KwdEn :
- Batch process, Chemical reactor, Core shell structure, Dynamic programming, Emulsion, Emulsion copolymerization, Emulsion polymerization, Experimental study, Feeding device, Glass transition, Modeling, Molecular mass, Monomer, Operating conditions, Optimization, Parameterization, Particle size distribution, Penetration rate, Polymer, Polymerization reactor, Product specification, Productivity, Semicontinuous, Styrene, Transition temperature, Weight.

Abstract

In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.

Notice en format standard (ISO 2709)

Pour connaître la documentation sur le format Inist Standard.

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A14	`03`			`@1 Department of Chemical and Biochemical Engineering, Technische Universität Dortmund, Emil-Figge-Strasse 70 @2 44221 Dortmund @3 DEU @Z 1 aut.`
A14	`04`			`@1 Department of Chemical Engineering, Loughborough University @2 Loughborough, Leicestershire LE11 3TU @3 GBR @Z 2 aut.`
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C01	`01`		`ENG`	@0 In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.
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Format Inist (serveur)

NO :	PASCAL 14-0166144 INIST
ET :	Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology
AU :	PAULEN (R.); BENYAHIA (B.); LATIFI (M. A.); FIKAR (M.); KRASLAWSKI (Andrzej); TURUNEN (Ilkka)
AF :	Laboratoire Reactions et Génie des Procédés CNRS - ENSIC, Université de Lorraine, UPR 6811 CNRS, 1 rue Grandville/Nancy/France (1 aut., 3 aut.); Faculty of Chemical and Food Technology, Slovak University of Technology in Bratislava, Radlinskeho 9/Bratislava/Slovaquie (1 aut., 4 aut.); Department of Chemical and Biochemical Engineering, Technische Universität Dortmund, Emil-Figge-Strasse 70/44221 Dortmund/Allemagne (1 aut.); Department of Chemical Engineering, Loughborough University/Loughborough, Leicestershire LE11 3TU/Royaume-Uni (2 aut.)
DT :	Publication en série; Niveau analytique
SO :	Computers & chemical engineering; ISSN 0098-1354; Coden CCENDW; Royaume-Uni; Da. 2014; Vol. 66; Pp. 233-243; Bibl. 1/4 p.
LA :	Anglais
EA :	In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.
CC :	001D07H; 001D09D02C; 001B60D70K; 001D09D02B
FD :	Copolymérisation émulsion; Transition vitreuse; Poids; Distribution dimension particule; Vitesse avancement; Emulsion; Productivité; Condition opératoire; Devis descriptif; Structure coeur couche; Polymérisation émulsion; Procédé discontinu; Réacteur chimique; Réacteur polymérisation; Styrène; Température transition; Polymère; Monomère; Programmation dynamique; Modélisation; Masse moléculaire; Optimisation; Paramétrisation; En semi continu; Etude expérimentale; Dispositif alimentation; .
ED :	Emulsion copolymerization; Glass transition; Weight; Particle size distribution; Penetration rate; Emulsion; Productivity; Operating conditions; Product specification; Core shell structure; Emulsion polymerization; Batch process; Chemical reactor; Polymerization reactor; Styrene; Transition temperature; Polymer; Monomer; Dynamic programming; Modeling; Molecular mass; Optimization; Parameterization; Semicontinuous; Experimental study; Feeding device
SD :	Copolimerización emulsión; Transición vítrea; Peso; Distribución dimensión partícula; Velocidad penetración; Emulsión; Productividad; Condición operatoria; Presupuesto descriptivo; Estructura núcleo cascarón; Polimerización emulsión; Procedimiento discontínuo; Reactor químico; Reactor polimerización; Estireno; Temperatura transición; Polímero; Monómero; Programación dinámica; Modelización; Masa molecular; Optimización; Parametrización; En semicontinuo; Estudio experimental; Dispositivo alimentación
LO :	INIST-16409.354000507546710180
ID :	14-0166144

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Pascal:14-0166144

Le document en format XML

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<front><div type="abstract" xml:lang="en">In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.</div>
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<inist><standard h6="B"><pA><fA01 i1="01" i2="1"><s0>0098-1354</s0>
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<fA02 i1="01"><s0>CCENDW</s0>
</fA02>
<fA03 i2="1"><s0>Comput. chem. eng.</s0>
</fA03>
<fA05><s2>66</s2>
</fA05>
<fA08 i1="01" i2="1" l="ENG"><s1>Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology</s1>
</fA08>
<fA09 i1="01" i2="1" l="ENG"><s1>Selected papers from ESCAPE-23 (European Symposium on Computer Aided Process Engineering - 23), 9-12 June 2013, Lapeenranta, Finland</s1>
</fA09>
<fA11 i1="01" i2="1"><s1>PAULEN (R.)</s1>
</fA11>
<fA11 i1="02" i2="1"><s1>BENYAHIA (B.)</s1>
</fA11>
<fA11 i1="03" i2="1"><s1>LATIFI (M. A.)</s1>
</fA11>
<fA11 i1="04" i2="1"><s1>FIKAR (M.)</s1>
</fA11>
<fA12 i1="01" i2="1"><s1>KRASLAWSKI (Andrzej)</s1>
<s9>ed.</s9>
</fA12>
<fA12 i1="02" i2="1"><s1>TURUNEN (Ilkka)</s1>
<s9>ed.</s9>
</fA12>
<fA14 i1="01"><s1>Laboratoire Reactions et Génie des Procédés CNRS - ENSIC, Université de Lorraine, UPR 6811 CNRS, 1 rue Grandville</s1>
<s2>Nancy</s2>
<s3>FRA</s3>
<sZ>1 aut.</sZ>
<sZ>3 aut.</sZ>
</fA14>
<fA14 i1="02"><s1>Faculty of Chemical and Food Technology, Slovak University of Technology in Bratislava, Radlinskeho 9</s1>
<s2>Bratislava</s2>
<s3>SVK</s3>
<sZ>1 aut.</sZ>
<sZ>4 aut.</sZ>
</fA14>
<fA14 i1="03"><s1>Department of Chemical and Biochemical Engineering, Technische Universität Dortmund, Emil-Figge-Strasse 70</s1>
<s2>44221 Dortmund</s2>
<s3>DEU</s3>
<sZ>1 aut.</sZ>
</fA14>
<fA14 i1="04"><s1>Department of Chemical Engineering, Loughborough University</s1>
<s2>Loughborough, Leicestershire LE11 3TU</s2>
<s3>GBR</s3>
<sZ>2 aut.</sZ>
</fA14>
<fA20><s1>233-243</s1>
</fA20>
<fA21><s1>2014</s1>
</fA21>
<fA23 i1="01"><s0>ENG</s0>
</fA23>
<fA43 i1="01"><s1>INIST</s1>
<s2>16409</s2>
<s5>354000507546710180</s5>
</fA43>
<fA44><s0>0000</s0>
<s1>© 2014 INIST-CNRS. All rights reserved.</s1>
</fA44>
<fA45><s0>1/4 p.</s0>
</fA45>
<fA47 i1="01" i2="1"><s0>14-0166144</s0>
</fA47>
<fA60><s1>P</s1>
</fA60>
<fA61><s0>A</s0>
</fA61>
<fA64 i1="01" i2="1"><s0>Computers & chemical engineering</s0>
</fA64>
<fA66 i1="01"><s0>GBR</s0>
</fA66>
<fC01 i1="01" l="ENG"><s0>In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.</s0>
</fC01>
<fC02 i1="01" i2="X"><s0>001D07H</s0>
</fC02>
<fC02 i1="02" i2="X"><s0>001D09D02C</s0>
</fC02>
<fC02 i1="03" i2="3"><s0>001B60D70K</s0>
</fC02>
<fC02 i1="04" i2="X"><s0>001D09D02B</s0>
</fC02>
<fC03 i1="01" i2="X" l="FRE"><s0>Copolymérisation émulsion</s0>
<s5>06</s5>
</fC03>
<fC03 i1="01" i2="X" l="ENG"><s0>Emulsion copolymerization</s0>
<s5>06</s5>
</fC03>
<fC03 i1="01" i2="X" l="SPA"><s0>Copolimerización emulsión</s0>
<s5>06</s5>
</fC03>
<fC03 i1="02" i2="X" l="FRE"><s0>Transition vitreuse</s0>
<s5>07</s5>
</fC03>
<fC03 i1="02" i2="X" l="ENG"><s0>Glass transition</s0>
<s5>07</s5>
</fC03>
<fC03 i1="02" i2="X" l="SPA"><s0>Transición vítrea</s0>
<s5>07</s5>
</fC03>
<fC03 i1="03" i2="X" l="FRE"><s0>Poids</s0>
<s5>08</s5>
</fC03>
<fC03 i1="03" i2="X" l="ENG"><s0>Weight</s0>
<s5>08</s5>
</fC03>
<fC03 i1="03" i2="X" l="SPA"><s0>Peso</s0>
<s5>08</s5>
</fC03>
<fC03 i1="04" i2="X" l="FRE"><s0>Distribution dimension particule</s0>
<s5>09</s5>
</fC03>
<fC03 i1="04" i2="X" l="ENG"><s0>Particle size distribution</s0>
<s5>09</s5>
</fC03>
<fC03 i1="04" i2="X" l="SPA"><s0>Distribución dimensión partícula</s0>
<s5>09</s5>
</fC03>
<fC03 i1="05" i2="X" l="FRE"><s0>Vitesse avancement</s0>
<s5>10</s5>
</fC03>
<fC03 i1="05" i2="X" l="ENG"><s0>Penetration rate</s0>
<s5>10</s5>
</fC03>
<fC03 i1="05" i2="X" l="SPA"><s0>Velocidad penetración</s0>
<s5>10</s5>
</fC03>
<fC03 i1="06" i2="X" l="FRE"><s0>Emulsion</s0>
<s5>11</s5>
</fC03>
<fC03 i1="06" i2="X" l="ENG"><s0>Emulsion</s0>
<s5>11</s5>
</fC03>
<fC03 i1="06" i2="X" l="SPA"><s0>Emulsión</s0>
<s5>11</s5>
</fC03>
<fC03 i1="07" i2="X" l="FRE"><s0>Productivité</s0>
<s5>12</s5>
</fC03>
<fC03 i1="07" i2="X" l="ENG"><s0>Productivity</s0>
<s5>12</s5>
</fC03>
<fC03 i1="07" i2="X" l="SPA"><s0>Productividad</s0>
<s5>12</s5>
</fC03>
<fC03 i1="08" i2="X" l="FRE"><s0>Condition opératoire</s0>
<s5>13</s5>
</fC03>
<fC03 i1="08" i2="X" l="ENG"><s0>Operating conditions</s0>
<s5>13</s5>
</fC03>
<fC03 i1="08" i2="X" l="SPA"><s0>Condición operatoria</s0>
<s5>13</s5>
</fC03>
<fC03 i1="09" i2="X" l="FRE"><s0>Devis descriptif</s0>
<s5>14</s5>
</fC03>
<fC03 i1="09" i2="X" l="ENG"><s0>Product specification</s0>
<s5>14</s5>
</fC03>
<fC03 i1="09" i2="X" l="SPA"><s0>Presupuesto descriptivo</s0>
<s5>14</s5>
</fC03>
<fC03 i1="10" i2="X" l="FRE"><s0>Structure coeur couche</s0>
<s5>15</s5>
</fC03>
<fC03 i1="10" i2="X" l="ENG"><s0>Core shell structure</s0>
<s5>15</s5>
</fC03>
<fC03 i1="10" i2="X" l="SPA"><s0>Estructura núcleo cascarón</s0>
<s5>15</s5>
</fC03>
<fC03 i1="11" i2="X" l="FRE"><s0>Polymérisation émulsion</s0>
<s5>16</s5>
</fC03>
<fC03 i1="11" i2="X" l="ENG"><s0>Emulsion polymerization</s0>
<s5>16</s5>
</fC03>
<fC03 i1="11" i2="X" l="SPA"><s0>Polimerización emulsión</s0>
<s5>16</s5>
</fC03>
<fC03 i1="12" i2="X" l="FRE"><s0>Procédé discontinu</s0>
<s5>20</s5>
</fC03>
<fC03 i1="12" i2="X" l="ENG"><s0>Batch process</s0>
<s5>20</s5>
</fC03>
<fC03 i1="12" i2="X" l="SPA"><s0>Procedimiento discontínuo</s0>
<s5>20</s5>
</fC03>
<fC03 i1="13" i2="X" l="FRE"><s0>Réacteur chimique</s0>
<s5>21</s5>
</fC03>
<fC03 i1="13" i2="X" l="ENG"><s0>Chemical reactor</s0>
<s5>21</s5>
</fC03>
<fC03 i1="13" i2="X" l="SPA"><s0>Reactor químico</s0>
<s5>21</s5>
</fC03>
<fC03 i1="14" i2="X" l="FRE"><s0>Réacteur polymérisation</s0>
<s5>22</s5>
</fC03>
<fC03 i1="14" i2="X" l="ENG"><s0>Polymerization reactor</s0>
<s5>22</s5>
</fC03>
<fC03 i1="14" i2="X" l="SPA"><s0>Reactor polimerización</s0>
<s5>22</s5>
</fC03>
<fC03 i1="15" i2="X" l="FRE"><s0>Styrène</s0>
<s2>NK</s2>
<s2>FX</s2>
<s5>23</s5>
</fC03>
<fC03 i1="15" i2="X" l="ENG"><s0>Styrene</s0>
<s2>NK</s2>
<s2>FX</s2>
<s5>23</s5>
</fC03>
<fC03 i1="15" i2="X" l="SPA"><s0>Estireno</s0>
<s2>NK</s2>
<s2>FX</s2>
<s5>23</s5>
</fC03>
<fC03 i1="16" i2="X" l="FRE"><s0>Température transition</s0>
<s5>24</s5>
</fC03>
<fC03 i1="16" i2="X" l="ENG"><s0>Transition temperature</s0>
<s5>24</s5>
</fC03>
<fC03 i1="16" i2="X" l="SPA"><s0>Temperatura transición</s0>
<s5>24</s5>
</fC03>
<fC03 i1="17" i2="X" l="FRE"><s0>Polymère</s0>
<s5>25</s5>
</fC03>
<fC03 i1="17" i2="X" l="ENG"><s0>Polymer</s0>
<s5>25</s5>
</fC03>
<fC03 i1="17" i2="X" l="SPA"><s0>Polímero</s0>
<s5>25</s5>
</fC03>
<fC03 i1="18" i2="X" l="FRE"><s0>Monomère</s0>
<s5>26</s5>
</fC03>
<fC03 i1="18" i2="X" l="ENG"><s0>Monomer</s0>
<s5>26</s5>
</fC03>
<fC03 i1="18" i2="X" l="SPA"><s0>Monómero</s0>
<s5>26</s5>
</fC03>
<fC03 i1="19" i2="X" l="FRE"><s0>Programmation dynamique</s0>
<s5>27</s5>
</fC03>
<fC03 i1="19" i2="X" l="ENG"><s0>Dynamic programming</s0>
<s5>27</s5>
</fC03>
<fC03 i1="19" i2="X" l="SPA"><s0>Programación dinámica</s0>
<s5>27</s5>
</fC03>
<fC03 i1="20" i2="X" l="FRE"><s0>Modélisation</s0>
<s5>28</s5>
</fC03>
<fC03 i1="20" i2="X" l="ENG"><s0>Modeling</s0>
<s5>28</s5>
</fC03>
<fC03 i1="20" i2="X" l="SPA"><s0>Modelización</s0>
<s5>28</s5>
</fC03>
<fC03 i1="21" i2="X" l="FRE"><s0>Masse moléculaire</s0>
<s5>29</s5>
</fC03>
<fC03 i1="21" i2="X" l="ENG"><s0>Molecular mass</s0>
<s5>29</s5>
</fC03>
<fC03 i1="21" i2="X" l="SPA"><s0>Masa molecular</s0>
<s5>29</s5>
</fC03>
<fC03 i1="22" i2="X" l="FRE"><s0>Optimisation</s0>
<s5>30</s5>
</fC03>
<fC03 i1="22" i2="X" l="ENG"><s0>Optimization</s0>
<s5>30</s5>
</fC03>
<fC03 i1="22" i2="X" l="SPA"><s0>Optimización</s0>
<s5>30</s5>
</fC03>
<fC03 i1="23" i2="X" l="FRE"><s0>Paramétrisation</s0>
<s5>31</s5>
</fC03>
<fC03 i1="23" i2="X" l="ENG"><s0>Parameterization</s0>
<s5>31</s5>
</fC03>
<fC03 i1="23" i2="X" l="SPA"><s0>Parametrización</s0>
<s5>31</s5>
</fC03>
<fC03 i1="24" i2="X" l="FRE"><s0>En semi continu</s0>
<s5>33</s5>
</fC03>
<fC03 i1="24" i2="X" l="ENG"><s0>Semicontinuous</s0>
<s5>33</s5>
</fC03>
<fC03 i1="24" i2="X" l="SPA"><s0>En semicontinuo</s0>
<s5>33</s5>
</fC03>
<fC03 i1="25" i2="X" l="FRE"><s0>Etude expérimentale</s0>
<s5>34</s5>
</fC03>
<fC03 i1="25" i2="X" l="ENG"><s0>Experimental study</s0>
<s5>34</s5>
</fC03>
<fC03 i1="25" i2="X" l="SPA"><s0>Estudio experimental</s0>
<s5>34</s5>
</fC03>
<fC03 i1="26" i2="X" l="FRE"><s0>Dispositif alimentation</s0>
<s5>41</s5>
</fC03>
<fC03 i1="26" i2="X" l="ENG"><s0>Feeding device</s0>
<s5>41</s5>
</fC03>
<fC03 i1="26" i2="X" l="SPA"><s0>Dispositivo alimentación</s0>
<s5>41</s5>
</fC03>
<fC03 i1="27" i2="X" l="FRE"><s0>.</s0>
<s4>INC</s4>
<s5>82</s5>
</fC03>
<fN21><s1>209</s1>
</fN21>
<fN44 i1="01"><s1>OTO</s1>
</fN44>
<fN82><s1>OTO</s1>
</fN82>
</pA>
</standard>
<server><NO>PASCAL 14-0166144 INIST</NO>
<ET>Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology</ET>
<AU>PAULEN (R.); BENYAHIA (B.); LATIFI (M. A.); FIKAR (M.); KRASLAWSKI (Andrzej); TURUNEN (Ilkka)</AU>
<AF>Laboratoire Reactions et Génie des Procédés CNRS - ENSIC, Université de Lorraine, UPR 6811 CNRS, 1 rue Grandville/Nancy/France (1 aut., 3 aut.); Faculty of Chemical and Food Technology, Slovak University of Technology in Bratislava, Radlinskeho 9/Bratislava/Slovaquie (1 aut., 4 aut.); Department of Chemical and Biochemical Engineering, Technische Universität Dortmund, Emil-Figge-Strasse 70/44221 Dortmund/Allemagne (1 aut.); Department of Chemical Engineering, Loughborough University/Loughborough, Leicestershire LE11 3TU/Royaume-Uni (2 aut.)</AF>
<DT>Publication en série; Niveau analytique</DT>
<SO>Computers & chemical engineering; ISSN 0098-1354; Coden CCENDW; Royaume-Uni; Da. 2014; Vol. 66; Pp. 233-243; Bibl. 1/4 p.</SO>
<LA>Anglais</LA>
<EA>In this paper dynamic optimization of a lab-scale semi-batch emulsion copolymerization reactor for styrene and butyl acrylate in the presence of a chain transfer agent (CTA) is studied. The mathematical model of the process, previously developed and experimentally validated, is used to predict the glass transition temperature of produced polymer, the number and weight average molecular weights, the monomers global conversion, the particle size distribution, and the amount of residual monomers. The model is implemented within gPROMS environment for modeling and optimization. It is desired to compute feed rate profiles of pre-emulsioned monomers, inhibitor and CTA that will allow the production of polymer particles with prescribed core-shell morphology with high productivity. The results obtained for different operating conditions and various additional product specifications are presented. The resulting feeding profiles are analyzed from the perspective of the nature of emulsion polymerization process and some interesting conclusions are drawn.</EA>
<CC>001D07H; 001D09D02C; 001B60D70K; 001D09D02B</CC>
<FD>Copolymérisation émulsion; Transition vitreuse; Poids; Distribution dimension particule; Vitesse avancement; Emulsion; Productivité; Condition opératoire; Devis descriptif; Structure coeur couche; Polymérisation émulsion; Procédé discontinu; Réacteur chimique; Réacteur polymérisation; Styrène; Température transition; Polymère; Monomère; Programmation dynamique; Modélisation; Masse moléculaire; Optimisation; Paramétrisation; En semi continu; Etude expérimentale; Dispositif alimentation; .</FD>
<ED>Emulsion copolymerization; Glass transition; Weight; Particle size distribution; Penetration rate; Emulsion; Productivity; Operating conditions; Product specification; Core shell structure; Emulsion polymerization; Batch process; Chemical reactor; Polymerization reactor; Styrene; Transition temperature; Polymer; Monomer; Dynamic programming; Modeling; Molecular mass; Optimization; Parameterization; Semicontinuous; Experimental study; Feeding device</ED>
<SD>Copolimerización emulsión; Transición vítrea; Peso; Distribución dimensión partícula; Velocidad penetración; Emulsión; Productividad; Condición operatoria; Presupuesto descriptivo; Estructura núcleo cascarón; Polimerización emulsión; Procedimiento discontínuo; Reactor químico; Reactor polimerización; Estireno; Temperatura transición; Polímero; Monómero; Programación dinámica; Modelización; Masa molecular; Optimización; Parametrización; En semicontinuo; Estudio experimental; Dispositivo alimentación</SD>
<LO>INIST-16409.354000507546710180</LO>
<ID>14-0166144</ID>
</server>
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Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology

Analysis of optimal operation of a fed-batch emulsion copolymerization reactor used for production of particles with core-shell morphology

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