OP-II-3

MODELING OF CFTALYTIC α-OLEFINS OLIGOMERIZATIONIN THE FLOW-TYPE REACTORTsvetkov O.N.PP-II-48VNII NP, 11116, Moscow, Aviamotornaya Str., 6, (495) 361-11-51, paom@rambler.ruThe possibility of modeling the α-olefin oligomerization reaction in a column flowtypereactor with a mechanical mixing device representing a multi-tier mixer withplane vanes has been discussed. The dependence of the mean residence time of thereaction mass in the apparatus on the space velocity of the flow has beenexperimentally found. It has been shown that the description of the oligomerizationprocess in the said reactor by several logically acceptable kinetic models includingthose of: ideal reactor displacement, cascade of ideal mixing reactors, diffusionalmodel, ideal displacement and ideal mixing reactors in succession, and visa verse,does not reveal any substantial difference in the final degree of α-olefin conversion tooligomers between the models under consideration. The reason of this may beattributed to the fact that in these computations the observed mean residence time,being a corrective factor while modeling is taken. For example, while using the idealdisplacement reactor kinetic model on the kinetic parameters of decene-1oligomerization at different temperatures a rather adequate approximation of theexperimental and calculated values of the total olefin conversion to oligomers hasbeen obtained. Given a sufficient experimental data base is available, thedependence of the yield, oligomer mean molecular mass and viscosity on theprocess conditions may by described by regressive equations and can be combinedinto a unified computer system permitting to control the oligomerization process in aflow-type reactor to produce oligomers with desired molecular-mass and viscositycharacteristics. The reactor under discussion proves to be versatile for α-olefinoligomerization in the presence of pseudo-homogeneaus and homogeneaus catalyst.One of the definite advantages of the reactor consists in the combination of intensivereaction mass mixing being especially important while using pseudo-homogeneauscatalysts, providing for the required mean residence time to attain maximum possiblemonomer conversion.421