A process for dehydrogenating alkane or alkylaromatic compounds comprising contacting the given compound and a dehydrogenation catalyst in a fluidized bed. The dehydrogenation catalyst is prepared from an at least partially deactivated platinum/gallium catalyst on an alumina-based support that is reconstituted by impregnating it with a platinum salt solution, then calcining it at a temperature from 400° C. to 1000° C., under conditions such that it has a platinum content ranging from 1 to 500 ppm, based on weight of catalyst; a gallium content ranging from 0.2 to 2.0 wt %; and a platinum to gallium ratio ranging from 1:20,000 to 1:4. It also has a Pt retention that is equal to or greater than that of a fresh catalyst being used in a same or similar catalytic process.

A catalyst for dehydrogenation of hydrocarbons includes a support including zirconium oxide and alumina. A concentration of the zirconium oxide in the catalyst is in a range of from 1 weight percent (wt. %) to 20 wt. %. The catalyst includes from 0.01 wt. % to 2 wt. % of an alkali metal or alkaline earth metal. The catalyst includes from 1 wt. % to 2 wt. % of tin. The catalyst includes from 0.1 wt. % to 2 wt. % of a platinum group metal. The alkali metal or alkaline earth metal, tin, and platinum group metal are disposed on the support.

A method for operating an acetylene hydrogenation unit of a steam cracking system that integrates a fluidized catalytic dehydrogenation (FCDh) effluent from a fluidized catalytic dehydrogenation (FCDh) system may include separating a cracked gas from the steam cracking system into at least a hydrogenation feed comprising at least acetylene, CO, and hydrogen, introducing the FCDh effluent to the separation system, combining the FCDh effluent with the cracked gas upstream of the separation system, or both. The method may include hydrogenating acetylene in the hydrogenation feed. Elevated CO concentration in the hydrogenation feed due to the FCDh effluent may reduce a reaction rate of acetylene hydrogenation. The acetylene hydrogenation unit may operate at an elevated temperature relative to normal operating temperatures when the portion of the FCDh effluent is not integrated, such that a concentration of acetylene in the hydrogenated effluent is less than a threshold acetylene concentration.

According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

Disclosed are a catalyst and a preparation method therefor, the catalyst being able to maintain a high production yield of C8 aromatic hydrocarbons in the process of converting a feedstock containing alkyl aromatics to C8 aromatic hydrocarbons such as mixed xylene through disproportionation/transalkylation/dealkylation while reducing a content of ethylbenzene in the products.

A method for operating an integrated system for producing olefins may include contacting a hydrogenation feed with a first hydrogenation catalyst to produce a hydrogenated effluent, the hydrogenation feed including at least a portion of a first process effluent from a first olefin production process and at least a portion of a second process effluent from a second olefin production process. The hydrogenation feed may include at least hydrogen, ethylene, carbon monoxide, acetylene, methyl acetylene, and propadiene, and the first hydrogenation catalyst may be a hydrogenation catalyst having a temperature operating range of at least 40° C. The hydrogenated effluent may include methyl acetylene, propadiene, or both. The method may further include contacting at least a portion of the hydrogenated effluent with a second hydrogenation catalyst, which may cause hydrogenation of at least a portion of the methyl acetylene and propadiene to produce an MAPD hydrogenated effluent.

Processes for upgrading a hydrocarbon. The process can include contacting a hydrocarbon-containing feed with fluidized catalyst particles that can include a Group 8-10 element or a compound thereof disposed on a support to effect one or more of dehydrogenation, dehydroaromatization, and dehydrocyclization of at least a portion of the hydrocarbon-containing feed to produce a coked catalyst and an effluent. The process can also include contacting at least a portion of the coked catalyst particles with an oxidant to effect combustion of at least a portion of the coke to produce regenerated catalyst particles. The process can also include contacting an additional quantity of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst particles to produce additional effluent and re-coked catalyst particles.

According to one or more embodiments presently disclosed, a method for processing a chemical stream may include contacting a feed stream with a catalyst in a reactor portion of a reactor system that includes a reactor portion and a catalyst processing portion. Contacting the feed stream with the catalyst may cause a reaction forming an effluent. The method may include separating the effluent stream from the catalyst, passing the catalyst to the catalyst processing portion, and processing the catalyst in the catalyst processing portion. Processing the catalyst may include passing the catalyst to a combustor, combusting a supplemental fuel stream in the combustor to heat the catalyst, and treating the heated catalyst with an oxygen-containing gas. The supplemental fuel stream may include at least 1 mol % of one or more hydrocarbons, and a weight ratio of catalyst to hydrocarbons in the combustor may be at least 300:1.

Reactors and methods of using the reactors to produce 1-butene are disclosed. A feed stream comprising n-butane is flowed to a dehydrogenation compartment of a reactor. The dehydrogenation compartment includes a dehydrogenation catalyst for catalyzing the dehydrogenation of n-butane to produce a dehydrogenation compartment effluent comprising 1-butene, 2-butene, isobutene, and/or unreacted n-butane. The dehydrogenation compartment effluent is flowed to a isomerization compartment of the reactor. The isomerization compartment contains a catalyst for isomerizing 2-butene in the dehydrogenation compartment effluent to produce 1-butene. A heating section is disposed between the dehydrogenation compartment and the isomerization compartment to provide heat for the reactions in both compartments.