A catalyst composition comprising (a) carrier comprising (i) 5 to 95 wt % mordenite type zeolite having a mean crystallite length parallel to the direction of the 12-ring channels of 60 nm or less and a mesopore volume of at least 0.10 cc/gram, (ii) 5 to 95 wt % ZSM-5 type zeolite; and (iii) 10 to 60 wt % inorganic binder; and (b) 0.001 to 10 wt % of one or more catalytically active metals, wherein the inorganic binder comprises titania, its preparation and its use in alkylaromatic conversion.

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm.sup.3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

Embodiments of processes for producing propylene utilize a dual catalyst system comprising a mesoporous silica catalyst impregnated with metal oxide and a mordenite framework inverted (MFI) structured silica catalyst downstream of the mesoporous silica catalyst, where the mesoporous silica catalyst includes a pore size distribution of at least 2.5 nm to 40 nm and a total pore volume of at least 0.600 cm.sup.3/g, and the MFI structured silica catalyst has a total acidity of 0.001 mmol/g to 0.1 mmol/g. The propylene is produced from the butene stream via metathesis by contacting the mesoporous silica catalyst and subsequent cracking by contacting the MFI structured silica catalyst.

A catalyst for selective catalytic reduction of NO.sub.x having one or more transition metals selected from Cr, Mn, Fe, Co, Ce, Ni, Cu, Zn, Ga, Mo, Ru, Rh, Pd, Ag, In, Sn, Re, Ir, Pt, and mixtures thereof supported on a support, wherein the support has a molecular sieve having at least one intergrowth phase having at least two different small-pore, three-dimensional framework structures.

A method for making a hydroisomerization catalyst having improved thermal stability and metal dispersion characteristics, the catalyst prepared therefrom, and a process for making a base oil product using the catalyst are disclosed. The catalyst is prepared from a composition comprising an SSZ-91 molecular sieve and a rare earth modified alumina, with the composition being modified to contain a Group 8-10 metal, typically through impregnation of a Group 8-10 metal composition. The catalyst may be used to produce dewaxed base oil products by contacting the catalyst under hydroisomerization conditions with a hydrocarbon feedstock.

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 Bronsted acid sites) of at least 100 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 mole/gm. The invention also includes methods of making RE-MSA.

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.

A magnesium modified Y-type molecular sieve has a rare earth oxide content of about 4% to about 11% by weight, a magnesium oxide content of about 0.1% to about 4% by weight, a sodium oxide content of about 0.3% to about 0.8% by weight, a total pore volume of about 0.33 mL/g to about 0.39 mL/g, a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of the modified Y-type molecular sieve of about 10% to about 30%, a lattice constant of about 2.440 nm to about 2.455 nm, a percentage of non-framework aluminum content to the total aluminum content of the modified Y-type molecular sieve of no more than about 20%, and a lattice collapse temperature of not lower than about 1045 C.

An extruded, solid honeycomb body comprises a copper-promoted, small pore, crystalline molecular sieve catalyst for converting oxides of nitrogen in the presence of a reducing agent, wherein the crystalline molecular sieve contains a maximum ring size of eight tetrahedral atoms, which extruded, solid honeycomb body comprising: 20-50% by weight matrix component comprising diatomaceous earth, wherein 2-20 weight % of the extruded, solid honeycomb body is diatomaceous earth; 80-50% by weight of the small pore, crystalline molecular sieve ion-exchanged with copper; and 0-10% by weight of inorganic fibres.

A hydrocarbon feed stream may be cracked by a method including contacting the hydrocarbon feed stream with a cracking catalyst in a reactor unit. The hydrocarbon feed stream has an API gravity of at least 40 degrees. The cracking catalyst may include one or more binder materials, one or more matrix materials, *BEA framework type zeolite, FAU framework type zeolite, and MFI framework type zeolite.