The present discloses an aromatization catalyst, preparation process and application thereof and a low-carbon olefin aromatization process. The aromatization catalyst comprises a microporous material, a binder and a modifier; the microporous material is a zeolite molecular sieve, the binder is alumina, the modifier is phosphorus, and the molar ratio of the aluminum element in the binder to the phosphorus element is more than or equal to 1 and less than 5; the ratio of the acidity of the strongly acidic sites to the acidity of the weakly acidic sites of the olefin aromatization catalyst is less than 1.

The present discloses an aromatization catalyst, preparation process and application thereof and a low-carbon olefin aromatization process. The aromatization catalyst comprises a microporous material, a binder and a modifier; the microporous material is a zeolite molecular sieve, the binder is alumina, the modifier is phosphorus, and the molar ratio of the aluminum element in the binder to the phosphorus element is more than or equal to 1 and less than 5; the ratio of the acidity of the strongly acidic sites to the acidity of the weakly acidic sites of the olefin aromatization catalyst is less than 1.

A process for endothermic dehydrogenation including contacting a catalyst material in a moving bed reactor having at least one reaction zone, the moving bed reactor comprising a heat exchanger containing a heating medium, wherein the catalyst material and the heating medium do not contact one another, and wherein at least 50% of the delta enthalpy of the at least one reaction zone is provided by the heat exchanger; and contacting a feedstock comprising hydrocarbons with the catalyst material in the at least one reaction zone of the moving bed reactor under reaction conditions to convert at least a portion of the hydrocarbons to a first effluent comprising a product comprising alkenes, alkynes, cyclic hydrocarbons, and/or aromatics.

A process and apparatus is disclosed for distributing a gas stream into a downwardly flowing catalyst stream in a vessel by feeding the gas stream into a center of the vessel or the catalyst stream into a hollow cap. The gas stream enters the cap and exits the cap flowing upwardly to contact the catalyst stream.

A process and apparatus is disclosed for distributing a gas stream into a downwardly flowing catalyst stream in a vessel by feeding the gas stream into a center of the vessel or the catalyst stream into a hollow cap. The gas stream enters the cap and exits the cap flowing upwardly to contact the catalyst stream.

According to embodiments, a process of forming a catalyst for aromatizing hydrocarbons may include enhancing a mesoporosity of a zeolite support by a base-leaching treatment, an acid-leaching treatment, or both to form a zeolite support having enhanced mesoporosity, mixing the zeolite support having enhanced mesoporosity with a solution containing zinc or gallium to disperse the zinc or gallium on the zeolite support having enhanced mesoporosity, and calcining the zeolite support having enhanced mesoporosity with zinc or gallium dispersed thereon to form a zinc- or gallium-doped zeolite catalyst having a mesopore volume of greater than 0.09 cm.sup.3/g and less than 0.20 cm.sup.3/g.

According to embodiments, a process of forming a catalyst for aromatizing hydrocarbons may include enhancing a mesoporosity of a zeolite support by a base-leaching treatment, an acid-leaching treatment, or both to form a zeolite support having enhanced mesoporosity, mixing the zeolite support having enhanced mesoporosity with a solution containing zinc or gallium to disperse the zinc or gallium on the zeolite support having enhanced mesoporosity, and calcining the zeolite support having enhanced mesoporosity with zinc or gallium dispersed thereon to form a zinc- or gallium-doped zeolite catalyst having a mesopore volume of greater than 0.09 cm.sup.3/g and less than 0.20 cm.sup.3/g.

The present disclosure relates generally to processes and systems for producing liquid transportation fuels by converting a feed stream that comprises both isopentane and n-pentane, and optionally, some C6+ hydrocarbons. Isopentane and smaller hydrocarbons are separated to form a first fraction while n-pentane and larger components of the feed stock form a second fraction. Each fraction is then catalytically-activated in a separate reaction zone with a separate catalyst, where the conditions maintained in each zone maximize the conversion of each fraction to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. In certain embodiments, the first fraction is activated at a lower temperature than the second fraction. Certain embodiments additionally comprise mixing at least a portion of the two effluents and contacting with an alkylation catalyst to provide enhanced yields of mono-alkylated aromatics that are suitable for use as a blend component of liquid transportation fuels or other value-added chemical products.

The present disclosure relates generally to processes and systems for producing liquid transportation fuels by converting a feed stream that comprises both isopentane and n-pentane, and optionally, some C6+ hydrocarbons. Isopentane and smaller hydrocarbons are separated to form a first fraction while n-pentane and larger components of the feed stock form a second fraction. Each fraction is then catalytically-activated in a separate reaction zone with a separate catalyst, where the conditions maintained in each zone maximize the conversion of each fraction to olefins and aromatics, while minimizing the production of C1-C4 light paraffins. In certain embodiments, the first fraction is activated at a lower temperature than the second fraction. Certain embodiments additionally comprise mixing at least a portion of the two effluents and contacting with an alkylation catalyst to provide enhanced yields of mono-alkylated aromatics that are suitable for use as a blend component of liquid transportation fuels or other value-added chemical products.

A reactor system for aromatization of higher hydrocarbons within a given temperature range T upon bringing a reactant stream including higher hydrocarbons into contact with a catalytic mixture. The reactor system includes a reactor unit arranged to accommodate a catalytic mixture. The catalytic mixture includes a catalyst material and a ferromagnetic material. The catalyst material is arranged to catalyze the aromatization of higher hydrocarbons. The ferromagnetic material is ferromagnetic at least at temperatures up to an upper limit of the given temperature range T, where the temperature range T is the range from between about 400 C. and about 700 C. or a subrange thereof. The reactor system also includes an induction coil arranged to be powered by a power source supplying alternating current, whereby the ferromagnetic material is heated to a temperature within the temperature range T by means of an alternating magnetic field.