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.

Process for the preparation of a catalyst and a catalyst comprising the use of more than one silica source is provided herein. Thus, in one embodiment, the invention provides a particulate FCC catalyst comprising about 5 to about 60 wt % one or more zeolites, about 15 to about 35 wt % quasicrystalline boehmite (QCB), about 0 to about 35 wt % microcrystalline boehmite (MCB), greater than about 0 to about 15 wt % silica from sodium stabilized basic colloidal silica, greater than about 0 to about 30 wt % silica from acidic colloidal silica or polysilicic acid, and the balance clay and the process for making the same. This process results in attrition resistant catalysts with a good accessibility.

The Invention discloses a method for improving the quality of oil products and increasing the yield of low-carbon olefins by catalytic cracking of bio-oil, which takes bio-oil or mixed oil of bio-oil and hydrocarbon oil as raw oil for catalytic cracking reaction. With this method, the octane number of the gasoline in product is obviously increased, simultaneously, the content of propylene and other low-carbon olefins in product is also improved.

A catalyst for hydrocarbon catalytic cracking of the invention contains: a catalyst (a) containing faujasite-type zeolite (A) having a unit cell size in a range of 2.435 nm to 2.455 nm, a matrix component, and rare earths; and a catalyst (b) containing faujasite-type zeolite (B) having a unit cell size in a range of 2.445 nm to 2.462 nm, a matrix component, phosphorus, and magnesium.

In accordance with one or more embodiments of the present disclosure, a catalyst composition includes a catalyst support and at least one hydrogenative component disposed on the catalyst support. The catalyst support includes at least one USY zeolite having a framework substituted with titanium and zirconium. The framework-substituted USY zeolite comprises at least one rare earth element. Methods of making and using such a catalyst in a hydrocracking process are also disclosed.

This invention relates to process for producing biphenyl esters, the process comprising: (a) contacting a feed comprising toluene, xylene or mixtures thereof with hydrogen in the presence of a hydroalkylation catalyst to produce a hydroalkylation reaction product comprising (methylcyclohexyl)toluene, wherein the hydroalkylation catalyst comprises: 1) binder present at 40 wt % or less (based upon weight of final catalyst composition), 2) a hydrogenation component present at 0.2 wt % or less (based upon weight of final catalyst composition), and 3) an acidic component comprising a molecular sieve having a twelve membered (or larger) ring pore opening, channel or pocket and a largest pore dimension of 6.0 angstroms or more present at 60 wt % or more, (based upon weight of final catalyst composition); (b) dehydrogenating the hydroalkylation reaction product using a dehydrogenation catalyst to produce a dehydrogenation reaction product comprising a mixture of methyl-substituted biphenyl compounds; (c) contacting at the dehydrogenation reaction product with an oxidizing gas to convert the methyl-substituted biphenyl compounds to biphenyl carboxylic acids; and (d) reacting the biphenyl carboxylic acids with one or more C.sub.1 to C.sub.14 alcohols to produce biphenyl esters.

A method and apparatus for the cracking of a petroleum oil feedstock to produce a desulfurized full-range gasoline product. The petroleum oil feedstock is contacted with a base cracking catalyst and an FCC additive in an FCC unit, wherein the catalyst includes a stable Y-type zeolite and a rare-earth metal oxide and the additive includes a shape selective zeolite. The catalyst, additive and petroleum oil feedstock can be contacted in a down-flow or riser fluid catalytic cracking unit, that can also include a regeneration zone, a separation zone, and a stripping zone. The FCC unit includes an integrated control and monitoring system that monitors at least one parameter selected from FCC operating parameters, feed rate, feedstock properties, and product stream properties, and adjusts at least one parameter in response to the measured parameter to increase production of desulfurized products.

The present invention relates to a catalyst for isomerization of alkylated aromatics such as mixed xylenes, using xylene isomerization catalyst particles including post-framework modified USY zeolite in which zirconium atoms and/or titanium atoms and/or hafnium atoms form a part of a framework of an ultra-stable Y-type zeolite.

A process for preparing a peptized alumina having increased solids and acid contents and a decreased water content. The process comprising mixing a boehmite or pseudoboehmite alumina and acid with a high intensity, high energy mixer at a ratio of 0.16 to 0.65 moles acid/moles alumina for a time period sufficient to form a substantially free-flowing solid particulate having a solids content of 45 to 65 wt %. When used in catalyst manufacture, peptized alumina produced by the process provides an increased rate in catalyst production and decreased costs due to high solids concentration and the presence of less water to be evaporated.

A molecular sieve of MFI structure has a ratio of n(SiO2)/n(Al2O3) of more than 15 and less than 70. It has a content of phosphorus of 1-15 wt %, calculated as P.sub.2O.sub.5 and based on the dry weight of the molecular sieve and a content of the supported metal in the molecular sieve 1-10 wt % based on the oxide of the supported metal and the dry weight of the molecular sieve. The supported metal is one or two selected from lanthanum and cerium. The volume of mesopores in the molecular sieve represents 40-70% by volume of the total pore volume of the molecular sieve by volume, measured by a nitrogen adsorption BET specific surface area method, and the volume of mesopores means the pore volume of the pores having a diameter of more than 2 nm and less than 100 nm.