Trimethylhexamethylenediamine is produced by hydrogenating a trimethylhexamethylenedinitrile-comprising mixture in the presence of at least ammonia and hydrogen and a catalyst in the presence or absence of solvent, wherein the catalyst has the following properties: I. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present: cobalt: 55 to 95 wt %, aluminum: 5 to 45 wt %, chromium: 0 to 3 wt %, and nickel: 0 to 7 wt %, and II. the catalyst is present in the form of irregular particles as granulate and after activation has particle sizes of 1 to 8 mm.

Trimethylhexamethylenediamine is produced by hydrogenating a trimethylhexamethylenedinitrile-comprising mixture in the presence of at least ammonia and hydrogen and a catalyst in the presence or absence of solvent, wherein the catalyst has the following properties: I. after activation the catalyst in its entirety has the following composition in weight percent (wt %), wherein the proportions add up to 100 wt %, based on the metals present: cobalt: 55 to 95 wt %, aluminum: 5 to 45 wt %, chromium: 0 to 3 wt %, and nickel: 0 to 7 wt %, and II. the catalyst is present in the form of irregular particles as granulate and after activation has particle sizes of 1 to 8 mm.

The disclosure provides an improved endothermic hydrocarbon conversion process that comprises reacting a hydrocarbon with a multi-component catalyst bed, and regenerating the catalyst bed with air, where the air used in regeneration step and hydrocarbon are at low air to hydrocarbon ratios and optionally at near-atmospheric pressures.

The disclosure provides an improved endothermic hydrocarbon conversion process that comprises reacting a hydrocarbon with a multi-component catalyst bed, and regenerating the catalyst bed with air, where the air used in regeneration step and hydrocarbon are at low air to hydrocarbon ratios and optionally at near-atmospheric pressures.

A catalyst comprising one or more metal oxides, wherein the catalyst has a total pore volume equal to or greater than 0.3 cm.sup.3/g and a mean pore diameter greater than or equal to 90 Å, where in the pore volume is measured using N.sub.2 adsorption porosimetry and the mean pore diameter is measured using N.sub.2 BET adsorption porosimetry.

A catalyst comprising one or more metal oxides, wherein the catalyst has a total pore volume equal to or greater than 0.3 cm.sup.3/g and a mean pore diameter greater than or equal to 90 Å, where in the pore volume is measured using N.sub.2 adsorption porosimetry and the mean pore diameter is measured using N.sub.2 BET adsorption porosimetry.

The present disclosure relates to metal oxide catalyst materials useful, for example, in the ammoxidation of propylene or isobutylene, processes for making them, and processes for making acrylonitrile and methacrylonitrile using such catalyst materials. In certain aspects, a catalyst material is a fused composite of a metal oxide catalyst and nanoparticulate silica, the nanoparticulate silica comprising in the range of about 40 wt % to about 80 wt % of silica having a particle size in the range of 10 nm to 35 nm, and in the range of about 20 wt % to about 60 wt % of silica having a particle size in the range of 36 nm to 80 nm. The metal oxide catalyst can be, for example, a molybdenum-containing mixed metal oxide catalyst.

The present disclosure relates to metal oxide catalyst materials useful, for example, in the ammoxidation of propylene or isobutylene, processes for making them, and processes for making acrylonitrile and methacrylonitrile using such catalyst materials. In certain aspects, a catalyst material is a fused composite of a metal oxide catalyst and nanoparticulate silica, the nanoparticulate silica comprising in the range of about 40 wt % to about 80 wt % of silica having a particle size in the range of 10 nm to 35 nm, and in the range of about 20 wt % to about 60 wt % of silica having a particle size in the range of 36 nm to 80 nm. The metal oxide catalyst can be, for example, a molybdenum-containing mixed metal oxide catalyst.

The present specification relates to an olefin oligomerization method and specifically to an olefin oligomerization method comprising the step of subjecting an olefin to a multimerization reaction by controlling a reaction temperature such that the weight ratio of 1-hexene to 1-octene within a product comprising 1-hexene and 1-octene has a predetermined value, in the presence of an oligomerization catalyst system comprising a ligand compound, a transition metal compound, and a cocatalyst, wherein the predetermined value for the weight ratio of 1-hexene to 1-octene within the product is selected in a range of 1:0.5 to 1:7. By the method, 1-hexene and 1-octene can be produced in a desired ratio.

Provided is a method for directly preparing dimethyl ether by synthesis gas, the method comprises: the synthesis gas is passed through a reaction zone carrying a catalyst, and reacted under the reaction conditions sufficient to convert at least a portion of the raw materials to obtain the reaction effluent comprising dimethyl ether; and the dimethyl ether is separated from the reaction effluent, wherein the catalyst is zinc aluminum spinel oxide. In the present invention, only one zinc aluminum spinel oxide catalyst is used, which can make the synthesis gas to highly selectively form dimethyl ether, the catalyst has good stability and can be regenerated. The method of the present invention realizes the production of dimethyl ether in one step by the synthesis gas, and reduces the large energy consumption problem caused by step-by-step production.