A catalyst can include a phosphorus modified zeolite having partly an ALPO structure. The ALPO structure can be determined by a signal between 35-45 ppm in .sup.27Al MAS NMR spectrum. The zeolite can include at least one ten member ring in the structure thereof. The catalyst can also include a binder and one or more metal oxides. The catalyst can be used in processes in the presence of steam at high temperatures, such as temperatures that are above 300° C. and up to 800° C. The catalyst can be used in alcohol dehydration, olefin cracking, MTO processes, and alkylation of aromatic compounds with olefins and/or alcohols.

A modified Y-type molecular sieve has a unit cell size of 2.420-2.440 nm. It contains a phosphorus content of 0.05-6%, a RE.sub.2O.sub.3 content of 0.03-10%, and an alumina content of less than 22%, and a specific hydroxyl nest concentration of less than 0.35 mmol/g and more than 0.05 mmol/g. The modified Y-type molecular sieve is used as the active component in a catalytic cracking catalyst. The catalytic cracking catalyst maintains a stable activity for a long time, effectively controls the coke yield and increases the heavy oil utilization.

The invention relates to a process for combined ethylbenzene reforming and xylene isomerisation comprising contacting a hydrocarbon feedstock containing ethylbenzene and xylene with a catalyst comprising a catalyst carrier and one or more metal(s) supported on the catalyst carrier, wherein the catalyst carrier is an extrudate comprising (i) a ZSM-48 and/or EU-2 type zeolite and (ii) an alumina binder, the extrudate having a shape with a C/A value of at least 3, where C is the circumference of the extrudate and A is the cross-sectional area of the extrudate. The metal may be platinum and the alumina may be a wide-pore alumina. The process displays high conversion rates whilst maintaining low levels of side-product formation.

The present invention relates to an isomerisation catalyst, in particular a zeolite catalyst. There is provided a method for making a particularly preferred zeolite catalyst by means of modifying catalytic zeolite materials. There is also provided a 5 process for isomerising fatty acids or alkyl esters thereof to produce branched fatty acids employing such an isomerisation catalyst, a composition comprising branched fatty acids, and also use of the isomerisation catalyst.

Embodiments of the disclosure include processes for ring-opening of hydrocarbon species comprising aromatic and cycloparaffinic rings in hydrocarbon feeds to produce ring-opened products. In particular, the process comprises contacting hydrocarbon species comprising aromatic and cycloparaffinic rings with hydrogen in the presence of a ring-opening catalyst comprising a noble metal on a low-acidity crystalline material containing external pockets to facilitate ring-opening of the hydrocarbon species comprising aromatic and cycloparaffinic rings. The processes are useful in the transformation of polynuclear aromatic hydrocarbons (PAHs) to ring-opened products.

The disclosure provides a process to hydrodearylate the non-condensed alkyl-bridged multi-aromatics at the outlet of the clay tower where such multi-aromatics form rather than performing hydrodearylation on the reject stream of the aromatics complex. Hydrodearylation may feature combining a C.sub.8+ hydrocarbon stream from a clay treater with a hydrogen stream over a catalyst bed comprising a support and an acidic component optionally containing Group 8 and/or Group 6 metals.

A process may include contacting an oxygen-containing, halogenide-containing or sulphur-containing organic feedstock in an XTO reactor with a catalyst composite under conditions effective to convert the oxygen-containing, halogenide-containing or sulphur-containing organic feedstock to olefin products. The catalyst composite may include at least 10 weight percent of a modified molecular sieve. The modified molecular sieve may include at least 0.05 weight percent of an alkaline earth metal or a rare earth metal based on a weight of the modified molecular sieve. The modified molecular sieve may include at least 0.3 weight percent of P based on the weight of the modified molecular sieve.

Catalyst composition useful in the catalytic dewaxing of a waxy hydrocarbon feedstock which catalyst composition includes a mixture of zeolite EU-2 and titania and may further include a noble metal. The zeolite EU-2 has a molar bulk ratio of silica-to-alumina (SAR) of greater than 100:1. The zeolite or mixture may have been dealuminated such as by acid leaching using a fluorosilicate salt or by steam treating.

Disclosed are a phosphorus-containing high-silica molecular sieve, its preparation and application thereof, wherein the molecular sieve comprises about 86.5-99.8 wt % of silicon, about 0.1-13.5 wt % of aluminum and about 0.01-6 wt % of phosphorus, calculated as oxides and based on the dry weight of the molecular sieve, the molecular sieve has an XRD pattern with at least three diffraction peaks, the first strong peak is present at a diffraction angle of about 5.9-6.9°, the second strong peak is present at a diffraction angle of about 10.0-11.0°, and the third strong peak is present at a diffraction angle of about 15.6-16.7°. The phosphorus-containing high-silica molecular sieve shows an improved hydrocracking activity in the presence of nitrogen-containing species when used in the preparation of hydrocracking catalysts.

A catalyst system for dewaxing of a hydrocarbon feedstock comprising at least two catalytic sections, the first section comprising a first dewaxing catalyst and a subsequent section comprising a second dewaxing catalyst, wherein the first dewaxing catalyst is a ZSM-12 zeolite based catalyst and the second dewaxing catalyst is a EU-2 and/or ZSM-48 zeolite based catalyst. The catalyst system displays enhanced performance when compared to systems containing either ony ZSM-12 based catalyst or EU-2/ZSM-48 based catalyst only.