The present invention relates to a hybrid iron nanoparticle catalyst comprising: i) 1 to 50 wt. % nanoparticles comprising iron and at least one of a metal M selected from the group consisting of alkali metals, alkaline earth metals, transition metals of groups 3 to 7 and 9 to 11 of the Periodic Table of Elements, lanthanides and combinations of M thereof; and ii) 50 to 99 wt. % of an aluminosilicate or silicoaluminophosphate zeolite, based on the total weight of the catalyst, wherein said nanoparticle has a diameter of about 2 to 50 nm. The present invention also relates to a method of preparing the hybrid iron nanoparticle catalyst and a process for the production of light olefins using the hybrid iron nanoparticle catalyst.

Processes for converting C8 aromatic hydrocarbons. In some embodiments, the process can include feeding a gaseous hydrocarbon feed that can include meta-xylene, ortho-xylene, or both into a conversion zone. The process can also include contacting the gaseous hydrocarbon feed with a catalyst that can include a ZSM-11 zeolite in the conversion zone under conversion conditions to effect isomerization of at least a portion of any meta-xylene, or at least a portion of any ortho-xylene, or both to produce a conversion product rich in para-xylene. In some embodiments, the ZSM-11 zeolite can have an alpha value of 1 to 3,000 and a molar ratio of silica to alumina of from 15 to 200.

Embodiments of catalyst systems and methods of synthesizing catalyst systems are provided. The catalyst system may include a core comprising a zeolite; and a shell comprising a microporous fibrous silica. The shell may be in direct contact with at least a majority of an outer surface of the core. The catalyst system may have a Si/Al molar ratio greater than 5. At least a portion of the shell may have a thickness of from 50 nanometers (nm) to 360 nm.

This invention describes methods of alkylating isobutane which include a catalytic reaction system comprising a crystalline zeolite catalyst and a rare earth-modified molecular sieve adsorbent (RE—MSA). The crystalline zeolite catalyst comprises sodalite cages and supercages, a Si/Al molar ratio of 20 or less, less than 0.5 weight percent alkali metals; and up to 5 wt% of Pt, Pd and or Ni, and acid-site density (including both Lewis and Brønsted acid sites) of at least 100 .Math.mole/gm. The RE-modified molecular sieve adsorbent (Re—MSA) comprising sodalite cages and supercages, a Si/Al molar ratio of 20 or less, less than 1 wt% of alkali metals, RE (rare earth elements) in the range of 10 to 30 wt% and transition metals selected from groups 9-11 in the range from 2 wt% to 10 wt; and acid-site density of no more than 30 .Math.mole/gm. The invention also includes methods of making RE—MSA.

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.

Catalyst composition which comprises a first zeolite having a BEA* framework type and a second zeolite having a MOR framework type and a mesopore surface area of greater than 30 m.sup.2/g is disclosed. These catalyst compositions are used to remove catalyst poisons from untreated feed streams having one or more impurities which cause deactivation of the downstream catalysts employed in hydrocarbon conversion processes, such as those that produce mono-alkylated aromatic compounds.

A process for producing para-xylene and ethylbenzene from C.sub.8 aromatics containing ethylbenzene includes the steps of sending C.sub.8 aromatics containing ethylbenzene to an ethylbenzene liquid-phase adsorption separation device, wherein a suction liquid containing ethylbenzene and a suction residual liquid are obtained after the adsorption separation, and the desorbents in the suction liquid and the suction residual liquid are removed to obtain ethylbenzene and a suction residual oil; sending the suction residual oil to a para-xylene adsorption separation device, and unadsorbed components are discharged as a raffinate from the adsorbent bed; the adsorbent bed is rinsed with a desorbent to desorb the para-xylene therein and obtain an extract; the desorbents in the extract and the raffinate are respectively removed to obtain para-xylene and a raffinate oil; sending the raffinate oil to a xylene isomerization device to carry out xylene isomerization, and the isomerization product is fractionated.

Disclosed are a bifunctional catalyst and a preparation method therefor, the bifunctional catalyst being suitable to produce high-value aromatic hydrocarbons by subjecting alkylaromatic hydrocarbons to a disproportionation/transalkylation/dealkylation reaction while suppressing aromatic loss or subjecting C8 aromatic hydrocarbons to an isomerization reaction while suppressing xylene loss.

A catalyst may include a metallic function derived from a metal constrained within cages and/or channels of a microporous material, wherein the cages and/or channels of the microporous material are defined by 8 tetrahedral atoms or fewer; and an acidic function derived from an additional zeolite having cages and/or channels defined by 10 or more tetrahedral atoms, wherein the microporous material providing the metallic function and additional zeolite providing the acidic function are coupled by a binder.

Embodiments of methods for converting gas condensate into a product stream comprising propylene comprise feeding gas condensate at a top region of a downflow high severity fluidized catalytic cracking reactor (HSFCC), where the gas condensate comprises: at least 50% by weight paraffins, and less than 0.1% by weight olefins. The method further comprises feeding catalyst to the top region of the downflow HSFCC reactor in an amount characterized by a catalyst to gas condensate weight ratio of about 5:1 to about 40:1, where the catalyst comprises nano-ZSM-5 zeolite catalyst having an average particle diameter from 0.01 to 0.2 μm, a Si/Al molar ratio from 20 to 40, and a surface area of at least 20 cm.sup.2/g. The method further comprises cracking the gas condensate in the presence of the catalyst at a reaction temperature of about 500° C. to about 700° C. to produce the product stream comprising propylene.