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.

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.

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 catalytic cracking catalyst contains 10-70 wt % of a cracking active component, 10-60 wt % of a binder and 10-70 wt % of a clay. The cracking active component has 5-100 wt % of a first Y-type molecular sieve and 0-95 wt % of a second molecular sieve. The first Y-type molecular sieve is a modified molecular sieve based on the crystal modification of kaolin and has the sodium oxide content of less than 2 wt %. The process for preparing the catalyst includes the steps of vigorously mixing and stirring a cracking active component comprising a modified molecular sieve based on the crystal modification of kaolin, a binder and a clay with water; spray drying; washing; filtering; and drying. The catalyst is used in the catalytic cracking reaction of heavy oils, and has a good coke selectivity, as well as a higher heavy oil conversion rate.

A catalytic cracking catalyst contains 10-70 wt % of a cracking active component, 10-60 wt % of a binder and 10-70 wt % of a clay. The cracking active component has 5-100 wt % of a first Y-type molecular sieve and 0-95 wt % of a second molecular sieve. The first Y-type molecular sieve is a modified molecular sieve based on the crystal modification of kaolin and has the sodium oxide content of less than 2 wt %. The process for preparing the catalyst includes the steps of vigorously mixing and stirring a cracking active component comprising a modified molecular sieve based on the crystal modification of kaolin, a binder and a clay with water; spray drying; washing; filtering; and drying. The catalyst is used in the catalytic cracking reaction of heavy oils, and has a good coke selectivity, as well as a higher heavy oil conversion rate.

Methods and corresponding catalysts are provided for conversion of an aromatic feed containing C.sub.8+ aromatics (particularly C.sub.9+ aromatics) to form a converted product mixture comprising, e.g., benzene and/or xylenes. The aromatic feed can be converted in the presence of a catalyst that includes a silica binder, a mixture of a first zeolite having an MEL framework (such as ZSM-11 and/or an MFI framework (such as ZSM-5), and a second zeolite having an MOR framework, such as mordenite, particularly a mordenite synthesized using TEA or MTEA as a structure directing agent, and a metal. The catalyst can further include one or more metals supported on the catalyst.

Methods and corresponding catalysts are provided for conversion of an aromatics feed containing C.sub.8+ aromatics, particularly C.sub.9+ aromatics, to form a converted product mixture comprising, e.g., benzene and/or xylenes. The aromatic feed can be converted in the presence of a catalyst that includes a mixture of a first zeolite having an MEL framework, such as ZSM-11, and a second zeolite having a MOR framework, such as mordenite, particularly a mordenite synthesized using TEA or MTEA as a structure directing agent. The weight ratio of the first zeolite to the second zeolite in the catalyst can be from 0.3 to 1.2, or from 0.3 to 1.1, or from 0.3 to 1.0. The catalyst can further include one or more metals supported on the catalyst, such as a combination of metals.

The present disclosure recognizes a correlation between zeolitic surface area (ZSA) of a catalyst composition and its catalytic activity. Particularly, the disclosure provides catalyst articles for diesel NO.sub.x abatement, including a substrate and a washcoat layer containing metal-promoted molecular sieves, wherein the zeolitic surface area (ZSA) of the catalyst article is about 100 m.sup.2/g or greater, the volumetric surface area is about 900 m.sup.2/in.sup.3 or greater, and/or the total zeolitic surface area (tZSA) is about 1200 m.sup.2 or greater. The disclosure further relates to methods for evaluating ZSA, volumetric ZSA, and tZSA, e.g., including the steps of coating a catalyst composition comprising metal-promoted molecular sieves onto a substrate; calcining and aging the catalyst composition; determining the ZSA (or volumetric ZSA or tZSA) thereof; and correlating the ZSA (or volumetric ZSA or tZSA) with catalyst composition NO.sub.x abatement activity to determine whether the catalyst composition is suitable for an intended use.

The present disclosure recognizes a correlation between zeolitic surface area (ZSA) of a catalyst composition and its catalytic activity. Particularly, the disclosure provides catalyst articles for diesel NO.sub.x abatement, including a substrate and a washcoat layer containing metal-promoted molecular sieves, wherein the zeolitic surface area (ZSA) of the catalyst article is about 100 m.sup.2/g or greater, the volumetric surface area is about 900 m.sup.2/in.sup.3 or greater, and/or the total zeolitic surface area (tZSA) is about 1200 m.sup.2 or greater. The disclosure further relates to methods for evaluating ZSA, volumetric ZSA, and tZSA, e.g., including the steps of coating a catalyst composition comprising metal-promoted molecular sieves onto a substrate; calcining and aging the catalyst composition; determining the ZSA (or volumetric ZSA or tZSA) thereof; and correlating the ZSA (or volumetric ZSA or tZSA) with catalyst composition NO.sub.x abatement activity to determine whether the catalyst composition is suitable for an intended use.

Methods and systems for producing pyrolysis products from a mixed plastics stream are described herein. The method may include conducting pyrolysis of a plastic feedstock to produce a stream of plastic pyrolysis oil; feeding a catalytic cracking feed stream and a catalyst from a catalyst regenerator into a fluidized bed reactor, where the catalytic cracking feed stream comprises the plastic pyrolysis oil; cracking the catalytic cracking feed stream in the fluidized bed reactor to produce a product stream and a spent catalyst; and transporting the spent catalyst to the catalyst regenerator and regenerating the catalyst in the catalyst regenerator. The product stream comprises olefins having a carbon number of C.sub.2-C.sub.4 and distillate fuel.