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15 99.54878 1.085616 131183.53 307804.64 59460.559 00 Mixed Liquid Vapor feed product product 1stliquid 2ndliquid Stage kghr kghr kg/hr ?oWkghr ?oWkg/hr 9 10 11 12 13 14 15 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 21466.802 0 TABLE 14 43249.936 39494.953 39676.2 40017.329 40932.433 43270.946 21466.802 0 0 0 0 0 0 0 US 8,563,788B2 31 TABLE 13-continued SimulatedBUOH ColumnTraf?candLiquidMass CompositionPro?leOutputsforExample4. 32 Simulated Solvent Column Tral?c and Liquid Mass CompositionPro?leOutputsforExample4. Heat Liquid Vapor Liquid Vapor Pressure duty ?oW ?oW feed feed Stage C. atm MJ/hr kg/hr kg/hr kg/hr kghr Temper- ature 1 91.49881 2 96.14796 3 96.78605 4 97.91872 5 98.79444 6 99.51716 7 100.0975 1.02922 8 100.558 1.036269 9 100.9262 1.043319 10 101.2293 1.050368 11 101.4888 1.057418 12 101.7201 1.064467 13 101.9335 1.071517 14 102.1354 1.078566 0 48598.116 81699.385 59485.237 18.791886 0 47557.727 70793.473 0 487.25557 0 378241.44 69265.827 329512.74 0 0 375236.53 70436.828 0 0 0 372628.96 67431.944 0 0 0 3706229 64824.22 0 0 0 369210.81 62818.008 0 0 0 368286.26 61405.939 0 0 0 367717.06 60481.46 0 0 0.986923 0.993973 1.001022 1.008072 1.015121 1.022171 0 3673882 59912.283 0 367214.33 59583.436 0 367137.63 59409.628 0 367120.55 59332.935 0 367265.35 59315.849 0 0 0 0 0 0 0 0 0 0 1 0 0 2 0 0 3 0 0 4 0 0 5 0 0 6 0 0 7 0 0 8 0 0 9 0 0 10 0 0 11 0 0 12 0 0 13 0 0 14 0 0 15 0 307804.64 81699.385 0 29.815222 48568301 29.22518 47528501 Whatisclaimedis: 1.A processcomprising: a)introducingafeedcomprising: (i)aWater-immiscibleorganicextractant; (i)Water; (i)atleastone isomer ofbutanol; (iv)optionallyanon-condensablegas; (v) ethanol; and (vi)optionallyfermentationby-products into a ?rst distillation column, Wherein the ?rst distillation column comprises a stripping section and optionally a rectifying section at an intro ductionpointabovethestrippingsection,the?rstdistil lation column having an operating temperature T1 and an operating pressure P 1 in the stripping section; Wherein T1 and P1 are selected to produce a ?rst bottoms stream and a ?rst vaporous overhead stream, the ?rst bottoms stream comprising the Water-immiscible organicextractantandWaterandbeingsubstantiallyfree ofbutanol,andthe?rstvaporousoverheadstreamcom prisingWater,butanol,ethanol,optionallytheextractant, 0 311969.16 0 306458.19 0 301822.64 0 298254 0 2957096 0 294002.43 0 292906.65 0 292225.62 0 291812.73 0 291568.16 0 291427.41 0 291332.35 0 0 66272.288 68778339 70806.313 72368896 73501.208 74283.833 74810.408 75162.582 75401.603 75569.473 75693.14 75932.999 307804.64 50 55 andoptionallythenon-condensablegas; b) introducing a Water-immiscible organic entrainerto at 60 65 leastone process stream orvessel; c) condensing the ?rst vaporous overhead stream to pro duce a gas phase and recover a ?rst mixed condensate; Wherein the ?rst mixed condensate comprises: (i) an organic phase comprising butanol, ethanol, entrainer, and Water; and (i)an aqueous phase comprising Water, butanol, and ethanol; and Wherein the ?rst mixed condensate comprises suf?cient entrainertoprovidephase separationoftheorganic and the aqueous phases;PDF Image | RECOVERY OF BUTANOL
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