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17 Example4 In this Example, 330,000 kg/hr rich solvent feed (40) is heated from 32 to 85.40 C. by a process to process heat exchangerandtheresultingstream(41)isfedtothesolvent 5 columnatstage3.Thisfeedpointdividesthesolventcolumn 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 18 the extractive fermentation process. In addition, a small amount of ethanol is assumed to be present in the fermenta tion broth. The mass ratio of ethanol to isobutanol in rich solventstreamisassumedtobe18.5Wt% inthisexample. The separation is realiZed by a similar diameter solvent col umn, and a similar solvent column re-boiler and condenser duties as those of Example 1. Stream 60 is 15.2 Weight per cent ethanol and 82.4 Weight percent isobutanol. 2-BUOH OLEYLOH WATER N4C6 CO2 Mass Frac 9.22E+06 42683.8 27474.046 28000 25033.771 25033.627 682.565 24351.207 25033.771 23760 23737.156 CO2 0.018 0.012 42 43 46 47 48 49 50 60 Stage 1 2 3 4 5 6 7 8 Temperature C. 64.879126 68.490445 69.235774 69.52182 70.066442 72.384545 80.914387 92.794275 Pressure atm 0.986923 0.990448 0.993973 0.997497 1.001022 1.004547 1.008072 1.011596 duty ?oW MJ/hr kg/hr 0 55627.9935 0 57674.293 0 58007.181 0 57817.0513 0 56571.8929 0 52410.0328 0 48063.3543 0 48126.7796 ?ow kghr feed feed feed kghr kghr kg/hr product product kg/hr kg/hr 0 27021.3176 0 0 0 0 0 0 0 0 0 0 0 0 0 0 318.828 324.932 27474.046 28000 1860.063 59185.213 3.65E+07 0.589 2184.987 87185.081 3.67E+07 354.492 1824.399 27021.318 59637.942 9.60E+06 5.46E+07 0.992 2178.891 86659.259 6.38E+07 2-BUOH OLEYLOH WATER N4C6 1 1 0.321 5497.109 27474.046 779.236 1074.133 0.486 0.382 241PPM 166PPM 660 0.054 0.872 0.072 trace trace 100PPM 0.924 0.076 trace Temperature C. Pressure atm VaporFrac Mole Flow kmol/hr Mass Flow kg/hr Volume Flow l/hr EnthalpyMMBtu/hr —896.741 Mass FloW kg/hr 2-BUOH 100 PPM OLEYLOH 0.924 WATER 0.076 N4C6 trace CO2 trace 0.002 0.039 0.487 0.192 trace 256 PPM 94 PPB 42 85.8 1.09 1.05 0 0.003 2389.797 311516.83 370205.91 2646.105 330000 6084625 —947.704 US 8,563,788B2 TABLE 3 Simulated Stream Outputs for Example 1. 11 12 19 20 21 30 33 40 41 Temperature C. Pressure atm Vapor Frac Mole Flow kmol/hr Mass Flow kg/hr Volume Flow l/hr EnthalpyMMBtu/hr —4.76E+01 —61.151 —4.70E+02 —5.31E+02 —6.51E+01 —4.29E+02 —4.94E+02 —986.943 Mass FloW kg/hr 87.6 25 0.99 2 1 0 77.8 0.99 64.9 91.6 0.99 0.99 1 1 87.6 0.99 32 1.04 0 2646.105 330000 390661.04 99.5 1.09 0 2389.797 311516.83 389206.37 —857.501 31.152 287748.52 87.6 0.99 0.664 33062.959 33062.971 4066.919 28996.04 33062.959 17820 14.35 14.35 <0.001 14.35 14.35 287760 28000 1074.133 1074.134 0.559 0.379 242 PPM 165 PPM 0.423 0.287 0.408 0.289 0.092 0.317 0.013 0.012 2-BUOH 31.152 OLEYLOH 287748.52 287760 trace 14.347 0.003 WATER 23737.156 23760 22.7 853.206 24157.721 N4C6 trace 525.936 27471.194 2.87 CO2 trace 660 660.001 368.622 45.511 Mass Frac 17820 48.433 27259.182 5755.356 0.054 0.872 0.072 0.018 0.015 0.806 0.015 0.015 1.68E-11 0.418 0.491 96 PPM 0.491 0.491 1.00E-06 0.525 0.007 0.002 0.007 0.007 2.75E-34 21976.937 294.897 0.151 trace 0.025 0.813 0.011 35 35 35 35 35 100.586873 1 1 1 1 1 1.03626943 1 0 0 0 0 0 23.013 742.353 1419.62 148.471 593.883 239.390326 1257.07 55966.55 29961.461 11193.31 44773.24 17751.9221 5734469 78326.768 31513.163 15665.353 62661.414 24530.4775 —7.017 —194.042 —387.451 —38.808 —155.234 —73.658739 5451.836 21807.345 17740.427 2.869 11.477 11.4774252 170.641 682.565 2.98E-07 5494.239 21976.955 0.0177523 73.724 294.897 4.89E-30 0.487 0.487 0.99935245 256 PPM 256 PPM 0.00064654 TABLE 4 SimulatedBUOH ColumnTra?'lcandLiquidMassCompositionPro?leOutputsforFxamnle1. Heat Liquid Vapor Liquid Vapor Mixed Liquid Vapor 27021.3176 37876.0714 0 39922.3708 0 40255.2588 0 40065.1292 0 38819.9708 0 34658.111 0 30311.432 0 44762.6688 10.5709356 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0.002 tracePDF Image | RECOVERY OF BUTANOL
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