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US 2011/0162954A1 Jul.7,2011 rangements Without departing from the spirit of essential attributes of the invention. Reference should be made to the appendedclaims,ratherthantotheforegoingspeci?cation,as Examples,theterm“richsolventstream”issynonymousWith indicatingthescopeoftheinvention. [0066] Theprocessoftheinventioncanbedemonstrated using a computational model of the process. Process model ingisanestablishedmethodologyusedbyengineerstosimu latecomplexchemicalprocesses.ProcessmodelingsoftWare performs 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 BostonofAspentech,Inc.ofBurlington,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 [0067] TheExamplesWereobtainedthroughprocessmod elingusingisobutanolasthebutanolisomerandoleylalcohol as the extractant. Similar results Would be expected for the analogous cases Where 1-butanol or a mixture of 1-butanol and isobutanol Was selected as the butanol isomer, due to the similarity of the physical property data for isobutanol and 1-butanol and the heterogeneous nature of the aZeotrope betWeen Water and these butanol isomers. the term “feed stream” used above. TABLE 1 Feed Compositions (inWeight Percent) ofthe Rich Solvent Stream from the Extractor [0068] Table1liststypicalfeedcompositionsoftherich columnisexpressedintermsofthesplitfractiononthetotal solventstream,obtainedfromextractivefermentation,enter ?oW oftheorganicphase12fromthedecanter. Equipment blocks Solvent Column (50) BUOHCOL Column (80) Inputs Number oftheoretical stages including re-boiler Column top pressure Columnbottompressure Columninternaldiameter Column re-boilerduty Preheated rich solvent feed (10) location Aqueous re?ux from decanter (16) location Organic re?ux from decanter (15) location Mass fraction isobutanol in bottom lean solvent(11) Re?ux stream temperature Preheated rich solvent stream (10) ?oW rate Preheatedrichsolventstream(10)temperature Number oftheoretical stages including re-boiler Column top pressure Columnbottompressure Columninternaldiameter Column re —boiler duty Organic feed from decanter (13) location Organic feed from decanter (13) temperature Water mass fraction in bottom product (42) Example 1 15 1 1.1 3.40 71639 3 1 1 100 40 157778 80.7 10 1 1.05 2.77 Example 2 Units 15 stages 1 bar 1.1 bar 2.82 m 55155 MJ/hr 3 stage 1 stage 1 stage 100 ppm 40 deg C. 71097 kg/hr 73.2 degC. 10 stages 1 bar 1.05 bar 2.75 m ing the isobutanol product recovery area. These compositions Were used in modeling the processes of the invention. In the Feed Compositions Isobutanol Water Carbon dioxide Oleyl alcohol Example 1 11.44% 6.48% 0.89% 81.19% Example 2 25.1% 8.23% 0.94% 65.72% [0069] These composition values for the rich solvent streamWereestablishedbyasimulationofadrygrindfacility usingextractiveinsituproductremovaltechnologyproduc ing50MM gal/yearofisobutanol,andfermenterbrothaque ous phase titers of 20 and 40 g/L respectively. ItWas assumed that the rich solvent stream Was at equilibrium With the fer mentationbrothandthatthesolvent?oW rateWas suf?cientto meetthespeci?edannualcapacity. [0070] Theparametersinputtedforthesimulationsofthe embodiments of the processes of the invention are listed in Table 2 and folloW a process schematic diagram as shoWn in FIG. 2.InFIG. 2,“QED10” referstoaheatstreamrepresent ingprocesstoprocessheatexchangebetWeenthesolvent column feed and bottom product via heat exchangers 52 and 54. Block 60 represents a mixer combining the tWo overhead streams 17 and 18. Certain dimensions and duty results cal culated from the process model are also listed in Table 2. These parameters do not include physical property param eters, and those related to convergence and other computa tional options or diagnostics. The organic re?ux to the solvent TABLE 2 Conditions Used for Modeling Processes of the Invention 33685 33369 1 1 40 40 100 100 MJ/hr stage degC. ppmPDF Image | RECOVERY OFBUTANOL FROM A MIXTURE OF BUTANOL 2011
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