Zeolite-containing catalyst, process for its preparation and a process for converting aliphatic hydrocarbons C2-C12 aromatic hydrocarbons or in a high-octane gasoline components

摘要

1.u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0438u0439 catalyst u0434u043bu00a0 u043fu0440u0435u0432u0440u0430u0449u0435u043du0438u00a0 c2 to c12 aliphatic hydrocarbons, aromatic hydrocarbons, or u0432u044bu0441u043eu043au043eu043eu043au0442u0430u043du043eu0432u044bu0439 component in mixture gas, the u0436u0430u0449u0438u0439 u0446u0435u043eu043bu0438u0442 group u043fu0435u043du0442u0430u0441u0438u043bu0430 with residual content of u043du0430u0442u0440u0438u00a0, u0441u0432u00a0u0437u0443u044eu0449u0438u0439 component and oxides of u0446u0438u0440u043au043eu043du0438u00a0, u043du0438u043au0435u043bu00a0 and zinc, u043eu0442u043bu0438u0447u0430u044eu0449u0438u0439u0441u00a0 orderwhat u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0438u0439 catalyst contains u0446u0435u043eu043bu0438u0442 zsm - 5 u0441u0438u043bu0438u043au0430u0442u043du044bu043c module SiO2 / Al2u043e3 = 60 to 80 mol / mol and residual content of u043du0430u0442u0440u0438u00a0 0.02 - 0.05% oxides of u0446u0438u0440u043au043eu043du0438u00a0 mas. and u043du0438u043au0435u043bu00a0 as elements of structure u0446u0435u043eu043bu0438u0442u043du043eu0433u043e component, as well as a promoter or zinc oxide with the following components: content, mas.;u0446u0435u043eu043bu0438u0442 65.00 is 80.00 per;zro2 0 - 4.00;NiO 0 1.00;ZnO 0 5.00 per;Na2O 0.02 - 0.05;u0441u0432u00a0u0437u0443u044eu0449u0438u0439 component of the rest.;2.method u043fu043eu043bu0443u0447u0435u043du0438u00a0 u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst comprising operation u0441u043cu0435u0448u0435u043du0438u00a0 reagents, hydrothermal synthesis, washing, drying and u043fu0440u043eu043au0430u043bu0438u0432u0430u043du0438u0435 sediment, remember u0449u0438u0439u0441u00a0, the reaction mixture obtained by u0441u043cu0435u0448u0435u043du0438u00a0 aqueous salt solutions u0430u043bu044eu043cu0438u043du0438u00a0, u0446u0438u0440u043au043eu043du0438u00a0, u043du0438u043au0435u043bu00a0, u0433u0438u0434u0440u043eu043eu043au0441u0438u0434u0430 u043du0430u0442u0440u0438u00a0, u0441u0438u043bu0438u043au0430u0433u0435u043bu00a0 and / or acid u043au0440u0435u043cu043du0438 eva waterthe crystal structure of u0437u0430u0442u0440u0430u0432u043eu0447u043du044bu0445 u0446u0435u043eu043bu0438u0442u0430 zsm - 5 in na or h shape, u0441u0442u0440u0443u043au0442u0443u0440u043eu043eu0431u0440u0430u0437u043eu0432u0430u0442u0435u043bu00a0, e.g. n - butanol, transferred to the autoclave, in which u043fu0440u043eu0432u043eu0434u00a0u0442 u0433u0438u0434u0440u043eu0442u0435u0440u043cu0430u043b u044cu043du044bu0439 fusion at a temperature of 160 190u0441 for 10 to 20 hours in u043fu043eu0441u0442u043eu00a0u043du043du043eu043c u043fu0435u0440u0435u043cu0435u0448u0438u0432u0430u043du0438u0438, after u0437u0430u0432u0435u0440u0448u0435u043du0438u00a0 hydrothermal synthesis u043fu0443u043bu044cu043fu0443 na form u0446u0435u043eu043bu0438u0442u0430 filter.the residue is washed u0445u043eu0437u00a0u0439u0441u0442u0432u0435u043du043du043e - drinking water and u043du0430u043fu0440u0430u0432u043bu00a0u044eu0442 the salt ion exchange by processing the u0430u043cu043cu043eu043du0438u00a0 chloride water solution when heated and u043fu0435u0440u0435u043cu0435u0448u0438u0432u0430u043du0438u0438 pulp obtained after the salt ion exchange u043fu0443u043bu044cu043fu0443 filtered, washed u0445u043eu0437u00a0u0439u0441u0442u0432u0435u043du043du043e - drinking water and then washed with water u0434u0435u043cu0438u043du0435u0440u0430u043bu0438u0437u043eu0432u0430u043du043du043eu0439 to residual u0441u043eu0434u0435u0440u0436u0430u043du0438u00a0 oxide u043du0430u0442u0440u0438u00a0 0.02 - 0.05 mas.%, in terms of dried and u043fu0440u043eu043au0430u043bu0435u043du043du044bu0439 product washed residue u0430u043cu043cu043eu043du0438u0439u043du043eu0439 form u0446u0435u043eu043bu0438u0442u0430 u043du0430u043fu0440u0430u0432u043bu00a0u044eu0442 operation input promoter or - zinc, and u043fu0440u0438u0433u043eu0442u043eu0432u043bu0435u043du0438u00a0 swung mash mass by u0441u043cu0435u0448u0435u043du0438u00a0 u0430u043cu043cu043eu043du0438u0439u043du043eu0439 form u0446u0435u043eu043bu0438u0442u0430 modified zinc, with the active u0433u0438u0434u0440u043eu043eu043au0441u0438u0434u043eu043c u0430u043bu044eu043cu0438u043du0438u00a0 received u043au0430u0442u0430u043bu0438u0437u0430u0442u043eu0440u043du0443u044e mass are the extrusion and u0433u0440u0430u043du0443u043bu0438u0440u043eu0432u0430u043du0438u044e,granules of dried at a temperature of 100 110u0441 and u043fu0440u043eu043au0430u043bu0438u0432u0430u044eu0442 at 550 - 650u0441, u043fu0440u043eu043au0430u043bu0435u043du043du044bu0435 granules u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst are classified, u043eu0442u0434u0435u043bu00a0u044eu0442 fraction is u0446u0435u043eu043bu0438u0442 a catalyst, a fraction of the granules are 2.5 mm to the homogenous powder and returned to operation u043fu0440u0438u0433u043eu0442u043eu0432u043bu0435u043du0438u00a0 u043au0430u0442u0430u043bu0438u0437u0430u0442u043eu0440u043du043eu0439 mass.;3. method u043fu0440u0435u0432u0440u0430u0449u0435u043du0438u00a0 aliphatic hydrocarbons in gasoline by u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e u0432u044bu0441u043eu043au043eu043eu043au0442u0430u043du043eu0432u044bu0439 component catalyst comprising heating and passes we u0441u044bu0440u044cu00a0 through u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0438u0439 catalyst, u043eu0442u043bu0438u0447u0430u044eu0449u0438u0439u0441u00a0, as u0441u044bu0440u044cu00a0 using pairs of u043fu0440u00a0u043cu043eu0433u043eu043du043du043eu0439 u0431u0435u043du0437u0438u043du043eu0432u043eu0439 fraction oil which miss you by the fixed layer u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst according to p.1, heated to the temperature of 300 to 420u0441 in load catalyst on the feedstock 2 h - 1.;4. method u043fu0440u0435u0432u0440u0430u0449u0435u043du0438u00a0 aliphatic hydrocarbons in a mixture of aromatic hydrocarbons by u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst comprising heating and passes we u0441u044bu0440u044cu00a0 through u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0438u0439 catalyst, u043eu0442u043bu0438u0447u0430u044eu0449u0438u0439u0441u00a0, as u0441u044bu0440u044cu00a0 using gaseous mixture of saturated hydrocarbons c2 - c4, which u043fu0440u043eu043fu0443u0441 quarters through the stationary layer u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst according to p.1, heated to a temperature of 550 600u0441 under load u0446u0435u043eu043bu0438u0442u0441u043eu0434u0435u0440u0436u0430u0449u0435u0433u043e catalyst to feedstock 100 - 200 h - 1.