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Blocks Inputs BuOH Number oftheoretical Column stagesincludingre-boiler (95) Column top pressure Columnbottompressure Columninternaldiameter Column re-boilerduty Organic feed from solvent column (50) location Organic feed from solvent column (50) temperature Entrainermass fractionin bottomproduct(60) 15 15 1 1 1.05 1.05 3.16 3.16 17366 17396 1 1 40 40 1 1 1 1 15 15 stages 0.1 0.1 bar 0.105 0.105 bar 2.81 2.76 m 7494 6061 MJ/hr 11 stage 40 40 deg C. 11 ppm 11 atm US 8,563,788B2 15 TABLE 2-continued Condition UsedforModelingProcessesoftheInvention Example1 Example2 Example3 Example4 Units 16 Decanter Decanter pressure (85) Decantertemperature 35 35 35 35 deg C. kghr Entrainercirculationrate 28000 28000 28000 28000 Orgsplit Ratio of stream (49) to all 0.2 0.2 0.2 (90) organicfromdecanter(47) Fourcaseswereruntodemonstratetheoperatingrequire- ments of the processes of the invention. Examples 1 and 2 were run to demonstrate the separation of 2-butanol from the richsolventstream.Examples3and4wereruntodemon 25 strate the separation of isobutanol and a small amount of ethanolfromtherichsolventstream.Foreachcase,aparticu larmodi?cationwas made totherichsolventfeed?ow and compositionsfromtheextractivefermentationprocesswhere speci?c aqueous phase titers were maintained. In each of the independentsimulations,columntraf?candheatexchanger dutieswillchangebecauseofthefeedcompositionchange. Bycomparingtheresultingcapitalinvestmentandoperating costs between different cases, the impact of the rich solvent feed?ow andcompositiononproductrecoveryareaperfor mance was quanti?ed. These four examples, however, should not be regarded as process operating limits of this invention. The term “Solvent Column” is synonymous with the term “?rstdistillationcolumn”usedabove.Theterm“BUOH col umn” is synonymous with the term “second distillation col umn” used above. The abbreviation “OLEYLOH” refers to oleyl alcohol. The abbreviation “N-C6” refers to n-hexane. StreamresultsforExample 1arelistedinTable3.BUOH columntraf?candliquidmasscompositionpro?lesarelisted45 in Table 4. Solvent column traf?c and liquid mass composi tion pro?les are listed in Table 5. StreamresultsforExample 2arelistedinTable6.BUOH column traf?c and liquid mass composition pro?les are listed inTable7.Solventcolumntraf?candliquidmasscomposi 50 tion pro?les are listed in Table 8. 0.2 StreamresultsforExample 3arelistedinTable9.BUOH column traf?c and liquid mass composition pro?les are listed in Table 10. Solvent column traf?c and liquid mass compo sitionpro?lesarelistedinTable11. StreamresultsforExample 4arelistedinTable 12.BUOH column traf?c and liquid mass composition pro?les are listed in Table 13. Solvent column traf?c and liquid mass compo sition pro?les are listed in Table 14. 55 In this Example, 330,000 kg/hr rich solvent feed 40 con taining5.4weightpercent2-butanolisheatedfrom32to 85.80 C. by a process to process heat exchanger and the resulting stream 41 is fed to the solvent column at stage 3. Thisfeedpointdividesthesolventcolumnintotherectifying and stripping sections. This rich solvent feed condition cor respondsto10g/L aqueousphasetiterinthefermenterwhich ismaintainedduringtheextractivefermentationprocess.The separation is realized by a larger diameter solvent column, and higher solvent column re-boiler and condenser duties. Stream 60 is 99.94 weight percent 2-butanol. Example2 In this Example, 131,500 kg/hr rich solvent feed 40 con taining 13.84 weight percent 2-butanol is heated from 32 to 76.80 C. by a process to process heat exchanger and the resulting stream 41 is fed to the solvent column at stage 3. Thisfeedpointdividesthesolventcolumnintotherectifying and stripping sections. This rich solvent feed condition cor respondsto40g/literaqueousphasetiterinthefermenter whichismaintainedduringtheextractivefermentationpro cess. The separation is realized by a smaller diameter solvent column, and lower solvent column re-boiler and condenser duties.Stream60is99.99weightpercent2-butanol. Example3 InthisExample, 330,000kg/hrrichsolventfeed40 con taining5.4weightpercentisobutanoland0.54weightpercent ethanol isheated from 32 to 85.80 C. by a process to process heatexchangerandtheresultingstream41isfedtothe solventcolumnatstage3.Thisfeedpointdividesthesolvent column into the rectifying and stripping sections. This rich solvent feed condition is corresponding to 10 g/liter aqueous phase isobutanol titer in the fermenter which is maintained during the extractive fermentation process. In addition, a small amount of ethanol is assumed to be present in the fermentation broth. The mass ratio of ethanol to isobutanol in richsolventstreamisassumedtobe10wt% inthisExample. The separation is realized by a similar diameter solvent col umn,andasimilarsolventcolumnre-boilerandcondenser dutiesasthoseofExample 1.Stream60is8.9weightpercent ethanol and 90.1 weight percent isobutanol. Otherprocessparametersincludethefollowing:1)thetotal number of theoretical stages in the solvent column and the feedlocationofthepreheatedrichsolventstream;2)thesplit fractionoforganicre?uxtosolventcolumn;3)thedegreeof preheating of the rich solvent stream before feeding itto the solventcolumn;and4)theamountofentrainer,water,and65 solventallowedinthe?nalproduct.Theseparameterscanbe manipulated to achieve optimum separation performance. Example 1PDF Image | RECOVERY OF BUTANOL
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