Disclosed are processes for conversion of a feedstock comprising C.sub.8+ aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C.sub.8+ aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam.

The invention relates to a catalyst comprising at least one metal selected from the group formed by metals of group VIB and of group VIII of the periodic table, used alone or as a mixture, and a support comprising at least one zeolite NU-86, at least one zeolite Y and at least one porous mineral matrix containing at least aluminum and/or at least silicon. The invention also relates to a process for hydrocracking of hydrocarbon feeds employing said catalyst.

The invention relates to a catalyst comprising at least one metal selected from the group formed by metals of group VIB and of group VIII of the periodic table, used alone or as a mixture, and a support comprising at least one zeolite NU-86, at least one zeolite Y and at least one porous mineral matrix containing at least aluminum and/or at least silicon. The invention also relates to a process for hydrocracking of hydrocarbon feeds employing said catalyst.

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.

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.

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.

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.

A selective catalytic reduction catalyst for the treatment of an exhaust gas stream of a passive ignition engine, the catalyst comprising a porous wall-flow filter substrate comprising an inlet end, an outlet end, a substrate axial length (w) extending between the inlet end and the outlet end, and a plurality of passages defined by porous internal walls of the porous wall flow filter substrate; wherein the catalyst further comprises a first coating, said first coating extending over x % of the substrate axial length from the inlet end toward the outlet end of the substrate, x being in the range of from 10 to 100, wherein the first coating comprises copper and an 8-membered ring pore zeolitic material; wherein the catalyst further comprises a second coating, the second coating extending over y % of the substrate axial length from the outlet end toward the inlet end of the substrate, y being in the range of from 20 to 90, wherein the second coating comprises copper, and optionally an 8-membered ring pore zeolitic material; wherein the catalyst optionally further comprises a third coating; wherein x+y is at least 90; wherein y % of w from the outlet end toward the inlet end of the substrate define the outlet zone of the coated substrate and (100−y) % of w from the inlet end toward the outlet end of the substrate define the inlet zone of the coated substrate; wherein the ratio of the loading of copper in the inlet zone, Cu(in), calculated as CuO, relative to the loading of copper in the outlet zone, Cu(out), calculated as CuO, Cu(in):Cu(out), is less than 1:1.

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.

A catalyst for the conversion of NO.sub.X and N.sub.2O comprising iron chabazite and iron beta zeolite. A method of simultaneously reducing the NO.sub.X and N.sub.2O concentration in a process gas stream comprising contacting the process gas stream with a catalyst comprising iron chabazite and iron beta zeolite under conversion conditions.