An object of the present invention is to provide a method for regenerating a catalyst for butadiene production, for removing a coke-like substance which is generated by oxidative dehydrogenation of n-butene in the presence of a catalyst for butadiene production and which is attached to the catalyst and the inside of a reactor. After the catalyst is used in oxidative dehydrogenation of butenes, the catalyst regeneration method of the present invention removes a coke-like substance in a reactor which is charged with the catalyst for butadiene production, the catalyst having a prescribed composition before being used in the oxidative dehydrogenation.

An object of the present invention is to provide a method for regenerating a catalyst for butadiene production, for removing a coke-like substance which is generated by oxidative dehydrogenation of n-butene in the presence of a catalyst for butadiene production and which is attached to the catalyst and the inside of a reactor. After the catalyst is used in oxidative dehydrogenation of butenes, the catalyst regeneration method of the present invention removes a coke-like substance in a reactor which is charged with the catalyst for butadiene production, the catalyst having a prescribed composition before being used in the oxidative dehydrogenation.

The invention relates to a process for the production of 1,3-butadiene from ethanol and acetaldehyde with catalyst regeneration comprising a) reacting a feed comprising ethanol and acetaldehyde in a reactor having at least one adiabatic reaction zone comprising a supported catalyst, and b) regenerating the supported catalyst. Regeneration stage b) comprises stripping step i. at a temperature of 300 to 400? C., ii. first and second combustion steps ii. and iii. at a temperature of 350 to 400? ? C. and 400 to 550? C. respectively, and stripping step iv. at a temperature of 550? C. to 300? ? C. The gas flows to each of regeneration steps b)i. to b)iv. are first heated and then contact the supported catalyst.

The invention relates to a process for the production of 1,3-butadiene from ethanol and acetaldehyde with catalyst regeneration comprising a) reacting a feed comprising ethanol and acetaldehyde in a reactor having at least one adiabatic reaction zone comprising a supported catalyst, and b) regenerating the supported catalyst. Regeneration stage b) comprises stripping step i. at a temperature of 300 to 400? C., ii. first and second combustion steps ii. and iii. at a temperature of 350 to 400? ? C. and 400 to 550? C. respectively, and stripping step iv. at a temperature of 550? C. to 300? ? C. The gas flows to each of regeneration steps b)i. to b)iv. are first heated and then contact the supported catalyst.

A phenol alkylation catalyst exhibiting a desirable combination of activity, selectivity, and regenerability is prepared from a catalyst precursor that includes specific amounts of magnesium oxide, copper oxide or a copper oxide precursor, a hydrous magnesium aluminosilicate-containing binder, a pore-former, a lubricant, and water. Methods of forming and regenerating the catalyst, as well as a phenol alkylation method, are described.

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst.

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst.

A method to regenerate and reactivate catalysts used for a carbon and syngas production reaction including a DRM or CARGEN reaction is developed. Carbon dioxide (CO.sub.2) is used as the regeneration and activation media. This method of a single step regeneration and activation using CO.sub.2 is more effective than the existing conventional two-step process that includes separate reduction and oxidation steps. This method produces pure carbon monoxide (CO) as a byproduct from the regeneration process by utilizing CO.sub.2 and carbon.

A method to regenerate and reactivate catalysts used for a carbon and syngas production reaction including a DRM or CARGEN reaction is developed. Carbon dioxide (CO.sub.2) is used as the regeneration and activation media. This method of a single step regeneration and activation using CO.sub.2 is more effective than the existing conventional two-step process that includes separate reduction and oxidation steps. This method produces pure carbon monoxide (CO) as a byproduct from the regeneration process by utilizing CO.sub.2 and carbon.

A counter-current catalyst regenerator with at least two stages of counter-current contact along with a regenerator riser is proposed. Each stage may comprise a permeable barrier that allows upward passage of oxygen-containing gas and downward passage of coked catalyst into each stage, but inhibits upward movement of catalyst to mitigate back mixing and approximate true counter-current contact and efficient combustion of coke from catalyst. The regenerator riser may provide a passage to transport the catalyst and may serve as a secondary stage for coke combustion to provide the regenerated catalyst.