<?xml version="1.0" encoding="UTF-8"?><xml><records><record><source-app name="Biblio" version="7.x">Drupal-Biblio</source-app><ref-type>17</ref-type><contributors><authors><author><style face="normal" font="default" size="100%">Michaels, Wesley</style></author><author><style face="normal" font="default" size="100%">Zhang, Hanyu</style></author><author><style face="normal" font="default" size="100%">Luyben, William L.</style></author><author><style face="normal" font="default" size="100%">Baltrusaitis, Jonas</style></author></authors></contributors><titles><title><style face="normal" font="default" size="100%">Design of a separation section in an ethanol-to-butanol process</style></title><secondary-title><style face="normal" font="default" size="100%">Biomass and Bioenergy</style></secondary-title><short-title><style face="normal" font="default" size="100%">Biomass and Bioenergy</style></short-title></titles><dates><year><style  face="normal" font="default" size="100%">2018</style></year><pub-dates><date><style  face="normal" font="default" size="100%">2018/2//</style></date></pub-dates></dates><urls><web-urls><url><style face="normal" font="default" size="100%">https://www.sciencedirect.com/science/article/pii/S096195341730452X</style></url></web-urls></urls><volume><style face="normal" font="default" size="100%">109</style></volume><pages><style face="normal" font="default" size="100%">231 - 238</style></pages><isbn><style face="normal" font="default" size="100%">0961-9534</style></isbn><language><style face="normal" font="default" size="100%">eng</style></language><abstract><style face="normal" font="default" size="100%">AbstractA complete separation scheme has been designed for the effluent of a high-pressure ethanol-to-butanol catalytic reactor, producing 250,000 tonnes of n-butanol per year. The effluent contains water, hydrogen and a diverse range of C2-C4 oxygenates: unconverted ethanol, n-butanol, acetaldehyde, ethyl acetate, and acetal. Fundamental phase equilibrium relationships suggested use of conventional, extractive, and heterogeneous azeotropic distillation units to perform the separations. All reactor effluent species exit the separation process at mole purities of at least 99%. Separation costs are estimated to range from 9.0 to 10.6 MJ/kg n-butanol, which is comparable with the separation costs of n-butanol obtained from established acetone-butanol-ethanol (ABE) separation process.
</style></abstract></record><record><source-app name="Biblio" version="7.x">Drupal-Biblio</source-app><ref-type>17</ref-type><contributors><authors><author><style face="normal" font="default" size="100%">Johnson, Nicole</style></author><author><style face="normal" font="default" size="100%">Baltrusaitis, Jonas</style></author><author><style face="normal" font="default" size="100%">Luyben, William L.</style></author></authors></contributors><titles><title><style face="normal" font="default" size="100%">Design and control of a cryogenic multi-stage compression refrigeration process</style></title><secondary-title><style face="normal" font="default" size="100%">Chemical Engineering Research and Design</style></secondary-title><short-title><style face="normal" font="default" size="100%">Chemical Engineering Research and Design</style></short-title></titles><keywords><keyword><style  face="normal" font="default" size="100%">Compression refrigeration</style></keyword><keyword><style  face="normal" font="default" size="100%">Compressor control</style></keyword><keyword><style  face="normal" font="default" size="100%">Multi-stage cycles</style></keyword><keyword><style  face="normal" font="default" size="100%">Refrigeration dynamic modeling</style></keyword></keywords><dates><year><style  face="normal" font="default" size="100%">2017</style></year><pub-dates><date><style  face="normal" font="default" size="100%">2017/5//</style></date></pub-dates></dates><urls><web-urls><url><style face="normal" font="default" size="100%">http://www.sciencedirect.com/science/article/pii/S026387621730151X</style></url></web-urls></urls><volume><style face="normal" font="default" size="100%">121</style></volume><pages><style face="normal" font="default" size="100%">360 - 367</style></pages><isbn><style face="normal" font="default" size="100%">0263-8762</style></isbn><language><style face="normal" font="default" size="100%">eng</style></language><abstract><style face="normal" font="default" size="100%">AbstractProviding refrigeration at very low cryogenic temperatures requires the use of several stages of compression refrigeration with progressively lower boiling point refrigerants in the various stages. The cascade of cycles ultimately rejects heat to cooling water, but the working fluid at each stage removes heat from a lower-temperature source and rejects this heat plus the compressor work in that stage to a higher-temperature sink. The design of these systems appears to be only qualitatively discussed in the literature, and no discussion of their plantwide dynamic control has been found.
This paper presents a quantitative design of a three-stage compression refrigeration process that uses methane, ethylene and propylene as the working refrigerant fluids in the three stages. Heat is removed in the condenser of a cryogenic distillation column separating carbon monoxide and methane. The bubble-point temperature of carbon monoxide at 13.9 bar is −158 °C. The distillation column condenser is cooled by evaporating boiling liquid methane at −163 °C. The second stage has an evaporator with boiling ethylene at −106.7 °C. The final stage has an evaporator with boiling propylene at −25.9 °C. An effective plantwide control structure is developed and tested.
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