HIGHLY ACTIVE ALKANE DEHYDROGENATION CATALYST AND METHOD OF PRODUCTION THEREOF Russian patent published in 2020 - IPC B01J23/24 B01J23/04 B01J21/18 B01J35/10 B01J37/04 B01J37/18 B01J37/08 C07C5/333 C07C5/48 C07C11/02 

FIELD: chemistry.

SUBSTANCE: present invention discloses a novel method of producing a highly active and selective dehydrogenation catalyst, a catalyst obtained using said method, and a method of alkane dehydrogenation, which involves contacting a stream of starting material containing light paraffins or a mixture of paraffins and diluents with a catalyst, wherein the ratio of alkane to diluent ranges from 1:0.1 to 1:10. Method of producing catalyst for dehydrogenation of alkane involves: (a) wet grinding of carbonaceous material to obtain paste of ground carbon material; (b) adding aluminium oxide to the organic acid solution while stirring for 15 to 20 minutes to obtain an aluminium oxide gel and aging gel for 15 to 20 minutes; (c) preparing an aqueous solution of Group IA metal salts and Group VIB using suitable metal salts; (d) adding crushed carbonaceous material paste obtained at step (a), and aqueous solution of metal salts obtained at step (c) into aluminium oxide gel obtained in step (b) to obtain a homogeneous catalyst suspension; (e) drying the catalyst suspension obtained in step (d) at temperature of 100 to 150 °C for 12 to 16 hours to obtain a dry catalyst briquette; (f) crushing dry catalyst briquette obtained at step (e) and sieving to obtain catalyst particles from 0.5 to 1.0 mm for operation in fixed bed and particles of 20 to 200 mcm for operation in fluidised bed; (g) calcination of catalyst particles obtained at step (f) at temperature of 600 to 650 °C and heating at rate of 2.0 °C/min for two hours in the presence of air; and (h) reducing the catalyst obtained in step (g), in a fixed bed/fixed fluid bed reactor using gaseous hydrogen at temperature of 600–800 °C and a controlled flow rate to obtain a final catalyst. Catalyst contains: (i) from 0.01 to 20 wt. % of Group VIB metal; (ii) from 0.001 to 5 wt. % of group IA metals; (iii) optionally from 0.001 to 5 wt. % of group VIII metals and (iv) aluminium oxide, wherein the weight percentage is determined with respect to the total weight of the catalyst. Availability of active centres and dispersion of metal oxides are improved by adding during production of catalyst carbonaceous material, such as coke, obtained from coal, or oil coke, or any other form of carbon, and its combustion during calcination.

EFFECT: technical result is high activity and selectivity with respect to light olefins.

12 cl, 1 dwg, 4 tbl, 3 ex