The present disclosure relates to a method for preparing a ceria-zirconia composite oxide, a ceria-zirconia composite oxide, and a catalyst including the same.

The present disclosure relates to a method for preparing a ceria-zirconia composite oxide, a ceria-zirconia composite oxide, and a catalyst including the same.

A supported non-oxidative alkane dehydrogenation catalyst and a method for making and using the same is disclosed. The supported non-oxidative alkane dehydrogenation catalyst can include a vanadium oxide, a rare earth metal oxide, an alkali metal oxide, and a support containing silica and alumina.

A supported non-oxidative alkane dehydrogenation catalyst and a method for making and using the same is disclosed. The supported non-oxidative alkane dehydrogenation catalyst can include a vanadium oxide, a rare earth metal oxide, an alkali metal oxide, and a support containing silica and alumina.

Processes and apparatus for reforming hydrocarbons to reduce the impact of contaminants created by non-catalyst coking. The reaction zone receives sulfur to inhibit the impact, and a control index is used to control the determine conditions with generally lower pressures. Additionally, a compression zone, pressure control zone and combustion zone operation are provided for the operation of the reaction zone at the generally lower pressures.

Processes and apparatus for reforming hydrocarbons to reduce the impact of contaminants created by non-catalyst coking. The reaction zone receives sulfur to inhibit the impact, and a control index is used to control the determine conditions with generally lower pressures. Additionally, a compression zone, pressure control zone and combustion zone operation are provided for the operation of the reaction zone at the generally lower pressures.

A catalyst for non-oxidative dehydrogenation of alkanes and a method for making and using the same is disclosed. The catalyst can include vanadium oxide derived from vanadyl oxalate. More particularly the catalyst is prepared by a method comprising the steps of: (a) contacting a transition alumina support with an aqueous solution comprising a vanadium carboxylate material solubilized therein; (b) heating the contacted alumina support to remove the water and produce a catalyst precursor material in solid form; and (c) heating the solid catalyst precursor material in the presence of an oxidizing source at a temperature of 500 to 800° C. to produce an alumina supported catalytic material comprising vanadium oxide. The catalyst can be further modified with an alkali metal oxide like potassium oxide, the precursor thereof being introduced with the impregnation solution.

A catalyst for non-oxidative dehydrogenation of alkanes and a method for making and using the same is disclosed. The catalyst can include vanadium oxide derived from vanadyl oxalate. More particularly the catalyst is prepared by a method comprising the steps of: (a) contacting a transition alumina support with an aqueous solution comprising a vanadium carboxylate material solubilized therein; (b) heating the contacted alumina support to remove the water and produce a catalyst precursor material in solid form; and (c) heating the solid catalyst precursor material in the presence of an oxidizing source at a temperature of 500 to 800° C. to produce an alumina supported catalytic material comprising vanadium oxide. The catalyst can be further modified with an alkali metal oxide like potassium oxide, the precursor thereof being introduced with the impregnation solution.

The invention relates to a process, unit and reaction system of low-carbon alkane dehydrogenation, which comprises the following steps: C3-C5 low-carbon alkane feed gas, together with CO and/or CO.sub.2 process gas, get into reactor after being preheated to 200-500° C., contact with a Cr—Ce—Cl/Al.sub.2O.sub.3 dehydrogenation catalyst, a Cu—Ce—Ca—Cl/Al.sub.2O.sub.3 thermal generating agent and thermal storage/support inert alumina balls, and convert to dehydrogenation products for 5-30 minutes under the conditions: temperature, 500-700° C., pressure, 10-100 kPa and weight hourly space velocity (WHSV), 0.1-5 hours.sup.−1. The products formed enter the downstream separation unit for separating out the low-carbon alkenes. The periodic regeneration process of the catalyst bed includes steam purging, hot air regenerating, bed heating, evacuating and reducing at 560 to 730° C. and 0.01 to 1 MPa. Each cycle needs about 10-70 minutes. With such dehydrogenation process, the reaction heat balance is moderated, and temperature gradient and reaction severity in the catalyst bed are reduced. As a consequence, the catalytic conversion, product selectivity, operation cycle and service life are improved. The system energy consumption is reduced.

The invention relates to a process, unit and reaction system of low-carbon alkane dehydrogenation, which comprises the following steps: C3-C5 low-carbon alkane feed gas, together with CO and/or CO.sub.2 process gas, get into reactor after being preheated to 200-500° C., contact with a Cr—Ce—Cl/Al.sub.2O.sub.3 dehydrogenation catalyst, a Cu—Ce—Ca—Cl/Al.sub.2O.sub.3 thermal generating agent and thermal storage/support inert alumina balls, and convert to dehydrogenation products for 5-30 minutes under the conditions: temperature, 500-700° C., pressure, 10-100 kPa and weight hourly space velocity (WHSV), 0.1-5 hours.sup.−1. The products formed enter the downstream separation unit for separating out the low-carbon alkenes. The periodic regeneration process of the catalyst bed includes steam purging, hot air regenerating, bed heating, evacuating and reducing at 560 to 730° C. and 0.01 to 1 MPa. Each cycle needs about 10-70 minutes. With such dehydrogenation process, the reaction heat balance is moderated, and temperature gradient and reaction severity in the catalyst bed are reduced. As a consequence, the catalytic conversion, product selectivity, operation cycle and service life are improved. The system energy consumption is reduced.