OP-II-3

PP-II-44NONISOTHERMAL MATHEMATICAL MODELS FOR FISCHER –TROPSCH PROCESS IN THREE – PHASE FLUIDIZED BEDACCOUNTING FOR GAS DISSOLVED COMPONENTSCONCENTRATIONS CHANGE IN SUSPENTION DURING THEREACTION. THE PROFIT OF PRELIMINARY INERT LIQUIDPRESATURATION BY SYNTHESIS – GAS AND USE THE SPATIALPACKING FOR GAS – LIQUID FLOW HYDRODYNAMICSIMPROVEMENTZhukova Olga 1 , Stefoglo Evgeny 21 Siberian State Technology University, Krasnoyarsk, Russia, zhukovolga@yandex.ru,2 ALCAR Chemical Group, Versher, Canada, stefevg@aol.comIn the last Reports concerning methanol synthesis in slurry bubble column reactor(SBCR) with an inherently high heat removal capability.This is a new concept to couple SBCR installation with coal-based integratedgasification combined cycle (IGCC) facility to co produce electric power andmethanol. Methanol produced by coal-based IGCC operations should be lower costthan methanol produced by conventional methanol - only units, and cold displacehigher priced methanol from other sources. In such kind of reactors high ratio CO/H 2can utilize which are produced by new syngas generators.Advances in kinetics studies are going on, and improvements in establishedlaboratory kinetics models and expansion in the mechanism searching space arestressed. Considerable data have been obtained both in experimental and theoreticalfields. A key aspect of an F-T catalyst is that it must promote CO activation.Two columns were utilized for hydrodynamic studying 10 and 20 of diameter and2 lengths. Special packing proposed of 2% specific volume and isotropiccharacteristic. Industrial powder catalyst, glass balls and sound as solid phase wereused. Gas and solid phases hold up were measured in bubble column, three-phasefluidized bed with and without packing. By tracer technique axial dispersion isdetermined. It was found considerable effect by using packing, especially at high gasflow rate. The equations were found for solid hold up and Pe in liquid are proposed. Forstudying initial condition in gas - liquid processes on solid suspended catalyst 1 litervolume batch in liquid reactor were used. Commercial processes of catalytichydrogenation on Pd/C powder catalyst at the range of temperatures 20-250 °C andpressures 1-40 bar were studied. Stirrer speed and gas flow rate also changed.414