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Stage 1 93.1653 0.986923 MJ/hr kg/hr 48893.429 48356.078 3793191 376501.6 374043.88 372146.27 370805.65 369924.07 369379.04 369063.07 368895.83 368822.36 368806.83 368953.75 309574.58 kghr 77055.272 69318.845 68296.745 329515.25 0 69744.519 0 0 66927.019 0 0 64469.296 0 0 62571.687 0 0 61231.063 0 0 60349.488 0 0 59804.455 0 0 59488.483 0 0 59321.251 0 0 59247.773 0 0 59232.242 0 0 59379.17 0 0 2 96.67048 3 97.13599 4 98.11575 5 98.90471 6 99.57766 7 100.1302 8 100.5749 9 100.9347 10 101.2333 11 101.4906 12 101.7208 13 101.9337 14 102.1355 15 99.51284 0 0 0 0 0 0 0 0 0 0 0 0 0 0 56615.205 14.650976 0 484.74926 Temperature C. Pressure atm Vapor Frac Mole FloW kmol/hr Mass FloW kghr Volume FloW l/hr EnthalpyMMBtu/hr Mass FloW kghr ETOH I-BUOH OLEYLOH 11 12 19 20 21 30 33 40 41 88.8 25 88.8 82.8 58.9 91.5 88.8 32 99.5 0.99 2 0.99 0.99 0.99 0.99 0.99 1.04 1.09 1 0 0.712 0.648 1 1 0.991 0 0 27 TABLE 10-c0ntinued SimulatedBUOH ColumnTra?'lcandLiquidMass Composition Pro?le Outputs for Example 3. 28 8 0 9 0 10 0 11 0 12 0 13 0 14 0 15 0 0 0 0 0 0 0 0 0 0 0 0 0 0 0 19701.091 0 TABLE11 40958.848 39332.283 38067.089 38643.249 39648.378 41563.434 44591.651 19701.091 8255.954 0 0 0 0 0 0 0 C. atm kg/hr kg/hr Simulated Solvent Column Traf?c and Liquid Mass Composition Pro?le Outputs for Example 3. Heat Liquid Vapor Liquid Vapor Temperature Pressure duty floW floW feed feed 0.993973 1.001022 1.008072 1.015121 1.022171 1.02922 1.036269 1.043319 1.050368 1.057418 1.064467 1.071517 1.078566 1.085616 130955.66 US 8,563,788B2 Mixed Liquid Vapor feed product product 1stliquid 2ndliquid Stage kghr kg/hr kghr floWkghr floWkghr 1 0 0 77055.272 2 0 0 0 3 0 0 0 4 0 0 0 5 0 0 0 6 0 0 0 7 0 0 0 8 0 0 0 9 0 0 0 10 0 0 0 11 0 0 0 12 0 0 0 13 0 0 0 14 0 0 0 26.293919 48867.13 26.174428 48329.9 15 0 309574.58 0 312017.73 306968.52 302652.42 299295.74 296884.16 295254.49 294201.36 293542.54 293140.68 292901.21 292762.53 292667.93 0 67301.37 69533.08 71391.46 72850.53 73921.49 74669.58 75177.68 75520.53 75755.15 75921.15 76044.3 76285.83 3095746 TABLE 12 Simulated Stream Outputs for Example 4. 317.756 324.932 2728.966 3053.887 378.959 27381.63 28000 80650.799 108650.32 26333.043 9.23E+06 42683.8 5.77E+07 5.75E+07 1.01E+07 —47.395 —61.151 —666.006 —727.155 —69.229 13027.915 13027.535 1427.108 30174.766 30174.683 1477.034 18.697 18.697 <0.001 2667.763 3046.721 2698.119 2343.146 81699.385 108032.43 330000 307804.64 7.98E+07 8.96E+07 391154.47 384657.78 —614.595 —683.824 —995.721 —842.703 11600.807 13027.915 3284.882 0.007 28697.732 30174.766 17731.273 30.779 18.697 18.697 284685.43 284670.51PDF Image | RECOVERY OF BUTANOL
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