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US 2011/0162954A1 Jul.7,2011 30 Wt %, or from about 16 to about 30 Weight percent, Water and may further comprise less than about 0.001 Weight per cent of residual extractant Which comes overhead in column 500. The fraction of extractant in the butanol phase can be minimized by use of a recti?cation section in column 500. The liquid aqueous phase includes less than about 10 Wt %, or fromabout3toabout10Weightpercentbutanol.Thedecanter may beofanyconventionaldesign. condensed in a condenser 850 to produce a second conden sate stream 185 comprising butanol and Water. The condenser 850may beofanyconventionaldesign.Atleastaportionof thesecondcondensatestream185may beintroducedintothe ?rst mixed condensate stream, for example by feeding the second condensate steam 185 into decanter 700. The com bined ?rst mixed condensate stream and second condensate streamarethenalloWedtoseparateintoaliquidbutanolphase andaliquidaqueousphase,andnon-condensablegascanbe [0053] Whenanon-condensablegassuchascarbondiox ideispresentinthefeed,thenon-condensablegasispresent purgedaspreviouslydescribedhereinabove. in stream 170 and in stream 175. At least a portion of the gas phase comprising the non-condensable gas can be purged from the process, as shoWn in FIG. 1, in Which purge stream 210comprisingthenon-condensablegasisshoWnleavingthe decanter 700. [0054] Fromthedecanter700,atleastaportionofthe aqueous phase 160 is introduced to the ?rst distillation col umn 500. The aqueous phase 160 may be introducedasre?ux to the column and Will typically include all of the aqueous phase separated in the decanter. Introducing stream 160 into column 500 loWers the column temperature and ensures that Water is present in the bottoms stream. This is advantageous because higher column temperatures can result in degrada tion of the extractant in the column bottoms, particularly in thecaseWherefermentationbyproductssuchasorganicacids are present and the extractant contains functional groups, suchasunsaturatedcarbon-carbonbondsinthecaseofoleyl alcohol. Degradation of the extractant should be avoided as it can cause decreased ef?ciency in the extractive fermentation process. [0059] Thevaporousoverheadstream180mayfurther comprise volatile fermentation byproducts such as acetalde hyde. Optionally, at least a portion of stream 180 may be purged from the process (not shoWn) to remove volatile fer mentation byproducts from the butanol recovery process. [0060] Amixtureofhigherboilingextractantsisexpected to behave in a fundamentally similar Way to a single extrac tant provided that the boiling point of the mixture, or the boilingpointoftheloWestboilingsolventofthemixture,is signi?cantly higher than the boiling points of Water and butanol,forexampleatleastabout30degreeshigher. [0061] Thepresentprocessesforseparatingorrecovering butanol provide butanol knoWn to have an energy content similar to that of gasoline and Which can be blended With any fossil fuel. Butanol is favored as a fuel or fuel additive as it yieldsonlyCO2 andlitleorno SO,CorNO,CWhenburnedin the standard internal combustion engine. Additionally, butanol is less corrosive than ethanol, the most preferred fuel additive to date. [0062] Inadditiontoitsutilityasabiofuelorfueladditive, thebutanolrecoveredaccordingtothepresentprocesseshas thepotentialofimpactinghydrogendistributionproblemsin the emerging fuel cell industry. Fuel cells today are plagued by safety concerns associated With hydrogen transport and [0055] Theprocessmayoptionallyfurthercompriseintro ducing at least a portion of the aqueous phase from the decanter into a fermentation vessel (not shoWn). This can provide a means to recycle some ofthe Water from the butanol recoveryprocessbacktotheextractivefermentationprocess. distribution.Butanolcanbeeasilyreformedforitshydrogen HoWever, itisnormallypreferredtorecycleWatertothe fermenter via stream 110, in Which the butanol content is loWer. [0056] Thebutanolphase120leavingthedecanterissplit plantderivedcarbonsources,avoidingthenegativeenviron intotWoportions.A ?rstportionofthebutanolphase,stream 130, is introduced into a second distillation column 800, Whichhasastrippingsection,atafeedpointabovethestrip ping section. The stream 130 is distilled to provide a second bottoms stream 420 comprising butanol and a second vapor ous overhead stream 180 comprising butanol and Water. The second distillation column is operated so as to provide the bottoms stream 420 substantially free ofWater. By “substan tially free of Water” it is meant that the bottoms 420 include less than about 0.01 Weight percent Water. The distillation column 800 can be any conventional column having at least a feed inlet, an overhead vapor outlet, a bottoms stream outlet, a heating means, a stripping section, and a suf?cient number ofstagestoeffectthedesiredseparation.Column 800 should have at least 6 stages a including re-boiler. mental impact associated With standard petrochemical pro cesses for butanol production. [0063] Oneadvantageofthepresentprocessesforsepara tionorrecoveryofbutanolisthatbyreturningaportionofthe aqueous phase from the decanter to the ?rst column, the temperature in the ?rst column is kept relatively loW, for example beloW about 1400 C. under any conditions, and inthe case of operation at atmospheric pressure, closer to 1000 C. LoWer temperatures avoid or reduce fouling of the heat exchangers associated With the column, as can occur When the extractant in the bottoms stream degrades, for example throughreactionsWithorcatalyZedbyfermentationbyprod uctscontainedinthebottomsstream.LoWercolumntempera tures also make the recovery process more economical. [0064] Anadditionaladvantageisthatthe?rstbottoms streamcomprisingtheextractantissubstantiallyfreeofthe [0057] A secondportionofthebutanolphase,stream150, isintroducedintothe?rstdistillationcolumn500.Stream150 butanolproduct,Whichcontributestohighyieldintherecov may be introduced as re?ux to the column. Introducing stream 150 into column 500 as re?ux Will suppress extractant loss in vaporous stream 170 of column 500. The ratio of stream 150 over stream 120 can range from 0.1 to 50 Weight percent. eryprocess.Beingsubstantiallyfreeofbutanolalsoenables optional recycling of the ?rst bottoms stream to the fermen tativeprocess. Italso simpli?es itsdisposition, should itnot berecycled. [0065] Althoughparticularembodimentsofthepresent [0058] Thevaporousoverheadstream180fromthesecond inventionhavebeendescribedintheforegoingdescription,it distillationcolumn 800 includes about 66.5 Weight percent Willbeunderstoodbythoseskilledintheartthattheinvention butanol and about 32.5 Weight percent Water. Stream 180 is iscapable ofnumerous modi?cations, substitutions, and rear contentandcanbedistributedthroughexistinggasstationsin the purity required for either fuel cells or vehicles. Further more, the present processes recover butanol obtained fromPDF Image | RECOVERY OFBUTANOL FROM A MIXTURE OF BUTANOL 2011
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