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Détail de l'auteur
Auteur William L. Luyben
Documents disponibles écrits par cet auteur
Affiner la rechercheCompressor heuristics for conceptual process design / William L. Luyben in Industrial & engineering chemistry research, Vol. 50 N° 24 (Décembre 2011)
in Industrial & engineering chemistry research > Vol. 50 N° 24 (Décembre 2011) . - pp. 13984-13989
Titre : Compressor heuristics for conceptual process design Type de document : texte imprimé Auteurs : William L. Luyben, Auteur Année de publication : 2012 Article en page(s) : pp. 13984-13989 Note générale : Chimie industrielle Langues : Anglais (eng) Mots-clés : Design Compressor Résumé : Multiple compressors in series with intermediate heat exchangers are frequently used to reduce compressor energy consumption or to limit compressor discharge temperatures when the overall compression ratio (initial suction pressure divided by the required final pressure) is large. The optimum number of stages can be fixed by economics (trade-offbetween capital investment and energy cost) or by equipment and/or process compressor discharge temperature limitations. The chemical engineering design literature contains several conflicting heuristics for designing multistage gas compression systems, and little information about the rationale behind these heuristics is provided. This paper explores several aspects of multistage compression systems including economics, equipment temperature limitations, and process temperature limitations. New heuristics are presented that give either the economic optimum or the temperature-limited number of stages as a function of the overall compression ratio. DEWEY : 660 ISSN : 0888-5885 En ligne : http://cat.inist.fr/?aModele=afficheN&cpsidt=25299866 [article] Compressor heuristics for conceptual process design [texte imprimé] / William L. Luyben, Auteur . - 2012 . - pp. 13984-13989.
Chimie industrielle
Langues : Anglais (eng)
in Industrial & engineering chemistry research > Vol. 50 N° 24 (Décembre 2011) . - pp. 13984-13989
Mots-clés : Design Compressor Résumé : Multiple compressors in series with intermediate heat exchangers are frequently used to reduce compressor energy consumption or to limit compressor discharge temperatures when the overall compression ratio (initial suction pressure divided by the required final pressure) is large. The optimum number of stages can be fixed by economics (trade-offbetween capital investment and energy cost) or by equipment and/or process compressor discharge temperature limitations. The chemical engineering design literature contains several conflicting heuristics for designing multistage gas compression systems, and little information about the rationale behind these heuristics is provided. This paper explores several aspects of multistage compression systems including economics, equipment temperature limitations, and process temperature limitations. New heuristics are presented that give either the economic optimum or the temperature-limited number of stages as a function of the overall compression ratio. DEWEY : 660 ISSN : 0888-5885 En ligne : http://cat.inist.fr/?aModele=afficheN&cpsidt=25299866
in Industrial & engineering chemistry research > Vol. 50 N° 6 (Mars 2011) . - pp. 3382-3389
Titre : Control of an isomerization column / reactor process Type de document : texte imprimé Auteurs : William L. Luyben, Auteur Année de publication : 2011 Article en page(s) : pp. 3382-3389 Note générale : Chimie industrielle Langues : Anglais (eng) Mots-clés : Reactor Isomerization Résumé : The control of a distillation column with a side reactor is studied for the conversion of n-butane into isobutane for use in the alkylation process. Fresh feed of a mixture of propane, isobutane, n-butane, and isopentane is fed to a distillation column. A vapor sidestream is withdrawn in the stripping section of the column and fed to an isomerization reactor in which some of the n-butane is converted to isobutane. Reactor effluent is fed back into the column in the rectifying section. Isopentane is removed in the bottoms, and moderate-purity isobutane is removed in the distillate. The control of the purity of the isobutane product can be achieved in two alternative ways: manipulating sidestream flow rate to the reactor or manipulating reflux ratio. The latter method is demonstrated to be better because manipulating sidestream flow rate presents potential control problems due to the existence of multiple steady states. DEWEY : 660 ISSN : 0888-5885 En ligne : http://cat.inist.fr/?aModele=afficheN&cpsidt=23944505 [article] Control of an isomerization column / reactor process [texte imprimé] / William L. Luyben, Auteur . - 2011 . - pp. 3382-3389.
Chimie industrielle
Langues : Anglais (eng)
in Industrial & engineering chemistry research > Vol. 50 N° 6 (Mars 2011) . - pp. 3382-3389
Mots-clés : Reactor Isomerization Résumé : The control of a distillation column with a side reactor is studied for the conversion of n-butane into isobutane for use in the alkylation process. Fresh feed of a mixture of propane, isobutane, n-butane, and isopentane is fed to a distillation column. A vapor sidestream is withdrawn in the stripping section of the column and fed to an isomerization reactor in which some of the n-butane is converted to isobutane. Reactor effluent is fed back into the column in the rectifying section. Isopentane is removed in the bottoms, and moderate-purity isobutane is removed in the distillate. The control of the purity of the isobutane product can be achieved in two alternative ways: manipulating sidestream flow rate to the reactor or manipulating reflux ratio. The latter method is demonstrated to be better because manipulating sidestream flow rate presents potential control problems due to the existence of multiple steady states. DEWEY : 660 ISSN : 0888-5885 En ligne : http://cat.inist.fr/?aModele=afficheN&cpsidt=23944505
in Industrial & engineering chemistry research > Vol. 48 N° 7 (Avril 2009) . - pp. 3484–3495
Titre : Control of a column/pervaporation process for separating the ethanol/water zeotrope Type de document : texte imprimé Auteurs : William L. Luyben, Auteur Année de publication : 2009 Article en page(s) : pp. 3484–3495 Note générale : Chemical engineering Langues : Anglais (eng) Mots-clés : Pervaporation process Refrigeration Distillation columns Résumé : The pervaporation process features a liquid feed and retentate and a vapor permeate. The phase change produces a temperature decrease as the retentate flows through the unit. Since flux rates decrease with decreasing temperature, the conventional pervaporation unit consists of several membrane modules in series with interstage heating. The vapor permeate must be condensed for recovery and recycle, and refrigeration is usually required. Hybrid systems of distillation columns and pervaporation units are frequently used in situations where distillation alone is impossible or very expensive. Despite the many papers dealing with pervaporation, the issue of dynamic control seems to be almost completely unexplored. That is the purpose of this paper. A hybrid column/pervaporation process is studied that is designed to produce 99.77 wt % ethanol from a feed stream of ethanol/water mixture with composition near the azeotrope. The control objective is to maintain the purity of the ethanol product retentate stream in the face of disturbances in feed flowrate and feed composition. There are two possible manipulated variables: permeate pressure and retentate temperature. Permeate flux is increased by decreasing permeate pressure or increasing retentate temperature. A simplified dynamic pervaporation model is developed that captures the essential features of the process using energy and component balances along with overall pervaporation performance relationships. Dynamic simulations are used to demonstrate the effectiveness of a control structure that uses a cascade composition/temperature structure. A simple process modification is shown to improve controllability. En ligne : http://pubs.acs.org/doi/abs/10.1021/ie801428s [article] Control of a column/pervaporation process for separating the ethanol/water zeotrope [texte imprimé] / William L. Luyben, Auteur . - 2009 . - pp. 3484–3495.
Chemical engineering
Langues : Anglais (eng)
in Industrial & engineering chemistry research > Vol. 48 N° 7 (Avril 2009) . - pp. 3484–3495
Mots-clés : Pervaporation process Refrigeration Distillation columns Résumé : The pervaporation process features a liquid feed and retentate and a vapor permeate. The phase change produces a temperature decrease as the retentate flows through the unit. Since flux rates decrease with decreasing temperature, the conventional pervaporation unit consists of several membrane modules in series with interstage heating. The vapor permeate must be condensed for recovery and recycle, and refrigeration is usually required. Hybrid systems of distillation columns and pervaporation units are frequently used in situations where distillation alone is impossible or very expensive. Despite the many papers dealing with pervaporation, the issue of dynamic control seems to be almost completely unexplored. That is the purpose of this paper. A hybrid column/pervaporation process is studied that is designed to produce 99.77 wt % ethanol from a feed stream of ethanol/water mixture with composition near the azeotrope. The control objective is to maintain the purity of the ethanol product retentate stream in the face of disturbances in feed flowrate and feed composition. There are two possible manipulated variables: permeate pressure and retentate temperature. Permeate flux is increased by decreasing permeate pressure or increasing retentate temperature. A simplified dynamic pervaporation model is developed that captures the essential features of the process using energy and component balances along with overall pervaporation performance relationships. Dynamic simulations are used to demonstrate the effectiveness of a control structure that uses a cascade composition/temperature structure. A simple process modification is shown to improve controllability. En ligne : http://pubs.acs.org/doi/abs/10.1021/ie801428s
in Industrial & engineering chemistry research > Vol. 48 N° 24 (Décembre 2009) . - pp. 11081–11093
Titre : Design and control of an autorefrigerated alkylation process Type de document : texte imprimé Auteurs : William L. Luyben, Auteur Année de publication : 2010 Article en page(s) : pp. 11081–11093 Note générale : Industrial chemistry Langues : Anglais (eng) Mots-clés : Design--Control--Autorefrigerated--Alkylation--Process Résumé : The alkylation of C4 olefins with isobutane to produce high-octane C8 components (“alkylate”) is a very important process in many oil refineries. The Kellogg process uses a sulfuric acid catalyst in a series of agitated reactors, which must operate at temperatures that require refrigeration because of undesirable side reactions that are favored by high temperatures. The reactors are cooled by boiling the liquid in the reactor, compressing the vapor, condensing it, and returning the liquid back to the reactor. A large excess of isobutane is used to suppress undesirable reactions, which requires a large recycle stream. Inert components (propane and n-butane) that enter in the fresh feed streams must be purged from the system. Two distillation columns are used, one of which has a vapor sidestream in addition to distillate and bottoms streams. This paper studies a simplified version of the autorefrigerated alkylation process and demonstrates the design trade-offs and interaction among design optimization variables such as reactor size, reactor temperature, compressor work, and isobutane recycle. Large reactors permit lower temperatures for a given olefin conversion, which improves selectivity. However, low reactor temperatures produce a low reactor pressure, which increases compressor work. Higher isobutane recycle improves selectivity but increases energy consumption and equipment sizes in the separation section. So the optimum economic design must balance the capital costs of reactors and distillation columns with the energy costs of compression and reboiler heat inputs. The location where the fresh feed streams enter the process also affects the design. An effective plantwide control structure is also developed that handles large disturbances in throughput and feed compositions. The structure has several uncommon control features: control of two compositions and one temperature in the sidestream column and a proportional-only temperature control in the other column. ISSN : 0888-5885 En ligne : http://pubs.acs.org/doi/abs/10.1021/ie9012387 [article] Design and control of an autorefrigerated alkylation process [texte imprimé] / William L. Luyben, Auteur . - 2010 . - pp. 11081–11093.
Industrial chemistry
Langues : Anglais (eng)
in Industrial & engineering chemistry research > Vol. 48 N° 24 (Décembre 2009) . - pp. 11081–11093
Mots-clés : Design--Control--Autorefrigerated--Alkylation--Process Résumé : The alkylation of C4 olefins with isobutane to produce high-octane C8 components (“alkylate”) is a very important process in many oil refineries. The Kellogg process uses a sulfuric acid catalyst in a series of agitated reactors, which must operate at temperatures that require refrigeration because of undesirable side reactions that are favored by high temperatures. The reactors are cooled by boiling the liquid in the reactor, compressing the vapor, condensing it, and returning the liquid back to the reactor. A large excess of isobutane is used to suppress undesirable reactions, which requires a large recycle stream. Inert components (propane and n-butane) that enter in the fresh feed streams must be purged from the system. Two distillation columns are used, one of which has a vapor sidestream in addition to distillate and bottoms streams. This paper studies a simplified version of the autorefrigerated alkylation process and demonstrates the design trade-offs and interaction among design optimization variables such as reactor size, reactor temperature, compressor work, and isobutane recycle. Large reactors permit lower temperatures for a given olefin conversion, which improves selectivity. However, low reactor temperatures produce a low reactor pressure, which increases compressor work. Higher isobutane recycle improves selectivity but increases energy consumption and equipment sizes in the separation section. So the optimum economic design must balance the capital costs of reactors and distillation columns with the energy costs of compression and reboiler heat inputs. The location where the fresh feed streams enter the process also affects the design. An effective plantwide control structure is also developed that handles large disturbances in throughput and feed compositions. The structure has several uncommon control features: control of two compositions and one temperature in the sidestream column and a proportional-only temperature control in the other column. ISSN : 0888-5885 En ligne : http://pubs.acs.org/doi/abs/10.1021/ie9012387
in Industrial & engineering chemistry research > Vol. 48 N° 24 (Décembre 2009) . - pp. 11081–11093
Titre : Design and control of an autorefrigerated alkylation process Type de document : texte imprimé Auteurs : William L. Luyben, Auteur Année de publication : 2010 Article en page(s) : pp. 11081–11093 Note générale : Chemical engineering Langues : Anglais (eng) Résumé : The alkylation of C4 olefins with isobutane to produce high-octane C8 components (“alkylate”) is a very important process in many oil refineries. The Kellogg process uses a sulfuric acid catalyst in a series of agitated reactors, which must operate at temperatures that require refrigeration because of undesirable side reactions that are favored by high temperatures. The reactors are cooled by boiling the liquid in the reactor, compressing the vapor, condensing it, and returning the liquid back to the reactor. A large excess of isobutane is used to suppress undesirable reactions, which requires a large recycle stream. Inert components (propane and n-butane) that enter in the fresh feed streams must be purged from the system. Two distillation columns are used, one of which has a vapor sidestream in addition to distillate and bottoms streams. This paper studies a simplified version of the autorefrigerated alkylation process and demonstrates the design trade-offs and interaction among design optimization variables such as reactor size, reactor temperature, compressor work, and isobutane recycle. Large reactors permit lower temperatures for a given olefin conversion, which improves selectivity. However, low reactor temperatures produce a low reactor pressure, which increases compressor work. Higher isobutane recycle improves selectivity but increases energy consumption and equipment sizes in the separation section. So the optimum economic design must balance the capital costs of reactors and distillation columns with the energy costs of compression and reboiler heat inputs. The location where the fresh feed streams enter the process also affects the design. An effective plantwide control structure is also developed that handles large disturbances in throughput and feed compositions. The structure has several uncommon control features: control of two compositions and one temperature in the sidestream column and a proportional-only temperature control in the other column. En ligne : http://pubs.acs.org/doi/abs/10.1021/ie9012387 [article] Design and control of an autorefrigerated alkylation process [texte imprimé] / William L. Luyben, Auteur . - 2010 . - pp. 11081–11093.
Chemical engineering
Langues : Anglais (eng)
in Industrial & engineering chemistry research > Vol. 48 N° 24 (Décembre 2009) . - pp. 11081–11093
Résumé : The alkylation of C4 olefins with isobutane to produce high-octane C8 components (“alkylate”) is a very important process in many oil refineries. The Kellogg process uses a sulfuric acid catalyst in a series of agitated reactors, which must operate at temperatures that require refrigeration because of undesirable side reactions that are favored by high temperatures. The reactors are cooled by boiling the liquid in the reactor, compressing the vapor, condensing it, and returning the liquid back to the reactor. A large excess of isobutane is used to suppress undesirable reactions, which requires a large recycle stream. Inert components (propane and n-butane) that enter in the fresh feed streams must be purged from the system. Two distillation columns are used, one of which has a vapor sidestream in addition to distillate and bottoms streams. This paper studies a simplified version of the autorefrigerated alkylation process and demonstrates the design trade-offs and interaction among design optimization variables such as reactor size, reactor temperature, compressor work, and isobutane recycle. Large reactors permit lower temperatures for a given olefin conversion, which improves selectivity. However, low reactor temperatures produce a low reactor pressure, which increases compressor work. Higher isobutane recycle improves selectivity but increases energy consumption and equipment sizes in the separation section. So the optimum economic design must balance the capital costs of reactors and distillation columns with the energy costs of compression and reboiler heat inputs. The location where the fresh feed streams enter the process also affects the design. An effective plantwide control structure is also developed that handles large disturbances in throughput and feed compositions. The structure has several uncommon control features: control of two compositions and one temperature in the sidestream column and a proportional-only temperature control in the other column. En ligne : http://pubs.acs.org/doi/abs/10.1021/ie9012387
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