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13 volatilityofWater,Whichleadstolessboilupbeingrequired to operate the second column compared to the case Without an entrainer. Althoughparticularembodimentsofthepresentinvention have been described in the foregoing description, it Will be understood by those skilled in the art that the invention is capable of numerous modi?cations, substitutions, and rear rangements Without departing from the spirit of essential attributes of the invention. Reference should be made to the appendedclaims,ratherthantotheforegoingspeci?cation,as indicatingthescopeoftheinvention. The process of the invention can be demonstrated using a computational model of the process. Process modeling is an establishedmethodologyusedbyengineerstosimulatecom plex chemical processes. Process modeling softWare per forms many fundamental engineering calculations, for examplemassandenergybalances,vapor/liquidequilibrium and reaction rate computations. The modeling of distillation columns is particularity Well established. Calculations based on experimentally determined binary vapor/liquid equilib rium and liquid/liquid equilibrium data can predict reliably the behavior of multi-component mixtures. This capability hasbeenexpandedtoalloWmodelingofcomplexmulti-stage, multi-component distilationcolumns using rigorous algo rithms like the “inside-out” algorithm developed by Joseph Boston ofAspentech, Inc. of Burlington, Mass. Commercial modeling softWare, such as Aspen Plus® from Aspentech, canbeusedinconjunctionWithphysicalpropertydatabases, such as DIPPR, available from the American Institute of Chemical Engineers, Inc., of NeW York, N.Y., to develop accurate models and assessments of processes. EXAMPLES Examples 1 and 2 Were obtained through process modeling using 2-butanol as the butanol isomer, oleyl alcohol as the extractant, and n-hexane as the entrainer. Examples 3 and 4 Were obtained through process modeling using isobutanol as thebutanolisomer,oleylalcoholastheextractant,andn-hex aneastheentrainer.A smallamountofethanolWasincluded in the feed stream for Examples 3 and 4. Similar results Would be expected for the analogous cases Where l-butanol or mixtures of l-butanol, 2-butanol, and/or isobutanol Were selected as the butanol isomer. 14 Table 1 lists typical feed compositions of the rich solvent stream, obtained from extractive fermentation, entering the alcoholproductrecoveryarea.ThesecompositionsWereused inmodelingtheprocessesoftheinvention.IntheExamples, the term “rich solvent stream” is synonymous With the term “feed stream” used above. TABLE 1 Feed Compositions (inWeight Percent) ofthe Rich Solvent Stream from the Extractor FeedCompositions Example1 Example2 Example3 Example4 Blocks Solvent Column (65) Inputs US 8,563,788B2 30 iso-butanol 2-butanol ethanol Water Carbon dioxide Oleyl alcohol i 5.40% i 7.20% 0.20% 87.2% i 5.4% 13.84% i i 0.54% 9.58% 7.2% 0.75% 0.2% 75.83% 86.66% 5.375% i 0.9954% 7.164% 0.199% 86.27% These composition values for the rich solvent stream Were established by a simulation of a dry grind facility using extractive in situ product removal technology producing 50 MMgal/yearof2-butanolorisobutanol,andfermenterbroth aqueous phase titers of 10 and 40 g/L 2-butanol or 10 g/L isobutanol respectively. ItWas assumed that the rich solvent stream Was at equilibrium With the fermentation broth and thatthesolvent?oW rateWas suf?cienttomeetthespeci?ed annualcapacity. Theparametersinputtedforthesimulationsoftheembodi ments of the processes of the invention are listed in Table 2 and folloW a process schematic diagram as shoWn in FIG. 2. In FIG. 2, “EM10” refers to a heat stream representing pro cess to process heat exchange betWeen the solvent column feedand bottomproductviaheatexchangers. Block 80 rep resents a mixer combining the tWo streams 12 and 19. Block 35 40 TABLE 2 Conditions Used for Modeling Processes of the Invention Example1 Example2 Example3 Example4 Units 70 represents a mixer combining the tWo streams 30 and 21. Block 75 represents amodeling artifactWhere allentraineris takenoutoftheprocess sothatthecorrectamount ofentrainer can be added to the decanter. Certain dimensions and duty results calculated from the process model are also listed in Table 2. These parameters do not include physical property parameters, and those related to convergence and other com putational options or diagnostics. The organic re?ux to the solvent column is expressed in terms of the split fraction on thetotal?oW oftheorganicphase47fromthedecanter. 15 15 15 15 stages 1 bar 1.1 bar 4.39 m Number oftheoretical stagesincludingre-boiler Column top pressure Columnbottompressure Columninternaldiameter Column re-boilerduty Preheated rich solvent feed(43)location Organic re?ux from decanter(48)location Mass fractionWaterin bottom stream (49) Re?ux streamtemperature Preheatedrichsolvent 330000 stream (42) ?oW rate Preheatedrichsolvent 85.8 76.8 98.7 98.3 degC. stream (42) temperature 1 1 1 1.1 1.1 1.1 4.46 2.83 4.44 92577 48300 99716 3 3 3 101471 3 1 1 MJ/hr stage stage ppm deg C. kg/hr 1 1 1 1 1 1 40 40 40 131500 330000 330000 40PDF Image | RECOVERY OF BUTANOL
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