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US 2011/0162954A1 Jul.7,2011 TABLE 2-continued Conditions Used for Modeling Processes of the Invention Equipment blocks Inputs Decanter(70) Decanterpressure Decantertemperature Combined condenser duty ofthe two columns Orsplit (72) Ratio ofstream (15) to alorganic from decanter (12) Example1 Example2Units 1 1 atm 40 40 degC. —97771 —831 14 MI/hr 0.2 0.2 [0071] Two cases were run to demonstrate the operating feeding itto the solvent column. These parameters can be requirementsoftheprocessesoftheinvention.Foreachcase, manipulatedtoachieveoptimumseparationperformance. a particular modi?cation was made to the rich solvent feed ?ow and compositions from the extractive fermentation pro cesswheretwodifferentaqueousphasetitersweremain tained.Ineachoftheindependentsimulations,columntraf?c and heat exchanger duties will change because of the feed composition change. By comparing the resulting capital investment and operating costs between different cases, the impact of the rich solvent feed ?ow and composition on productrecoveryareaperformancewas quanti?ed.Thesetwo examples, however, should not be regarded as process oper atinglimitsofthisinvention. [0072] Theterm“SolventColumn”issynonymouswiththe term “?rstdistillationcolumn” used above. The term “BUO HCOL” is synonymous with the term “second distillation column” used above. The abbreviation “OLEYLOH” refers tooleylalcohol. [0073] StreamresultsforExample1arelistedinTable3. BUOHCOL columntraf?candliquidmasscompositionpro ?les are listed in Table 4. Solvent column traf?c and liquid mass composition pro?les are listed in Table 5. [0074] StreamresultsforExample2arelistedinTable6. BUOHCOL columntraf?candliquidmasscompositionpro ?les are listed in Table 7. Solvent column traf?c and liquid mass composition pro?les are listed in Table 8. Example 1 [0076] InthisExample,157,778kg/hrrichsolventfeed(9) containing 11.44 weight percent isobutanol is heated from 32.20 C. to 80.60 C. by a process to process heat exchanger and the resulting stream (10) is fed to the solvent column at stage 3. This feed point divides the solvent column into the rectifying and stripping sections. This rich solvent feed con dition corresponds to 20 g/L aqueous phase titer in the fer mentor which is maintained during the extractive fermenta tion process. The separation is realized by a larger diameter solvent column, and higher solvent column re-boiler and condenser duties. Stream (11) contains 92.6 weight percent oleyl alcohol and 7.4 weight percent water. Stream (42) is 99.96weightpercentisobutanol. Example2 [0077] InthisExample,71,097kg/hrrichsolventfeed(9) containing 25.1 weight percent isobutanol is heated from 32.20 C. to 73.20 C. by a process to process heat exchanger and the resulting stream (10) is fed to the solvent column at stage 3. This feed point divides the solvent column into the rectifying and stripping sections. This rich solvent feed con dition corresponds to 40 g/L aqueous phase titer in the fer mentor which is maintained during the extractive fermenta [0075] Otherkeyprocessparametersincludethefollowing: tionprocess.Theseparationisrealizedbyasmallerdiameter 1)thetotalnumberoftheoreticalstagesinthesolventcolumn solventcolumn, andlowersolventcolumnre-boilerandcon andthefeedlocationofthepreheatedrichsolventstream;2) denserduties.Stream(11)contains88.9weightpercentoleyl the split fraction of organic re?ux to solvent column; and 3) alcohol and 11.1 weight percent water. Stream (42) is 99.99 the degree of preheating of the rich solvent stream before weight percent isobutanol. TABLE 3 Simulated Stream Outputs for Example 1. 9 10 Temperature C. 32.2 80.6 Pressure atm 1.09 1.04 VaporFrac 0 0.042 0 0 0 0 0 Mole Flow kmol/hr Mass Flow kg/hr Volume Flow l/hr EnthalpyMMBtu/hr —485.757 —467.491 —375.006 —318.408 —254.726 Mass Flow kg/hr 1041.844 217.297 138285.96 10245.183 164411.35 12587.939 —393.271 —63.682 13.829 8319.561 10169995 1870.528 0 53.784 128102.14 1.31 1319.708 157778.244 188461.269 1319.708 1577782 1041.844 138286 1086.487 51225.914 62939.692 869.189 40980.731 50351.754 1.72E+06 1732979 IiBUOH WATER CO2 OLEYLOH 128107.326 1281073 1281021 6.549 5.239 18055.031 18055.03 13.829 41597.806 33278.245 10218.361 10218.36 10170 9352.639 7482.112 1397.525 1397.525 0 268.919 215.135 11 12 13 14 15 102.3 40 40 42 40 1.09 1 1 1.09 1PDF Image | RECOVERY OFBUTANOL FROM A MIXTURE OF BUTANOL 2011
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