The present invention provides a method of preparing a supported catalyst, preferably a hydrocracking catalyst, the method at least comprising the steps of: a) providing a zeolite Y having a bulk silica to alumina ratio (SAR) of at least 10; b) mixing the zeolite Y provided in step a) with a base, water and a surfactant, thereby obtaining a slurry of the zeolite Y; c) reducing the water content of the slurry obtained in step b) thereby obtaining solids with reduced water content, wherein the reducing of the water content in step c) involves the addition of a binder; d) shaping the solids with reduced water content obtained in step c) thereby obtaining a shaped catalyst carrier; e) calcining the shaped catalyst carrier obtained in step d) at a temperature above 300° C. in the presence of the surfactant of step b), thereby obtaining a calcined catalyst carrier; f) impregnating the catalyst carrier calcined in step e) with a hydrogenation component thereby obtaining a supported catalyst; wherein no heat treatment at a temperature of above 500° C. takes place between the mixing of step b) and the shaping of step d).

A phosphorus-modified MFI-structured molecular sieve is characterized in that the molecular sieve has a K value, satisfying: 70%≤K≤90%; for example, 75%≤K≤90%; further for example, 78%≤K≤85%. The K value is as defined in the specification. A cracking auxiliary or cracking catalyst contains the phosphorus-modified MFI molecular sieve.

Disclosed herein is a fluid catalyst cracking (FCC) catalyst composition that includes a first component and a second component. The first component and second component may be separate microspheroidal FCC catalysts or may be incorporated in a common microspheroidal FCC catalyst. The first component includes zeolite Y and a first matrix that includes gamma-alumina. The second component includes beta zeolite and a second matrix. Also disclosed herein are methods of preparing the FCC catalyst composition and method of using the FCC catalyst composition.

The present invention provides a magnesium-modified ultra-stable rare earth type Y molecular sieve and the preparation method thereof, which method is carried out by subjecting a NaY molecular sieve as the raw material to a rare earth exchange and a dispersing pre-exchange, then to an ultra-stabilization calcination treatment, and finally to a magnesium modification. The molecular sieve comprises 0.2 to 5% by weight of magnesium oxide, 1 to 20% by weight of rare earth oxide, and not more than 1.2% by weight of sodium oxide, and has a crystallinity of 46 to 63%, and a lattice parameter of 2.454 nm to 2.471 nm. In contrast to the prior art, in the molecular sieve prepared by this method, rare earth ions are located in sodalite cages, which is demonstrated by the fact that no rare earth ion is lost during the reverse exchange process. Moreover, the molecular sieve prepared by such a method has a molecular particle size D(v,0.5) of not more than 3.0 μm and a D(v,0.9) of not more than 20 μm. Such a molecular sieve has both high stability and high selectivity for the target product, while cracking catalysts using the molecular sieve as an active component is characterized by a high heavy-oil-conversion capacity and a high yield of valuable target products.

The present invention provides a photocatalyst particle comprising titanium dioxide particles, a zeolite particle, and a carbon layer. The titanium dioxide particles are adsorbed on a part of an external surface of the zeolite particle. The carbon layer coats a part of an external surface of the zeolite particle other than the part of the external surface of the zeolite particle on which the titanium dioxide particles are adsorbed. The carbon layer is in contact with a part of surfaces of the titanium dioxide particles. At least a part of the other part of the surfaces of the titanium dioxide particles is not coated with the carbon layer and are exposed on a surface of the photocatalyst particle. The present invention provides a photocatalyst particle used even in an alkaline aqueous solution.

A method for selectively chemically reducing CO.sub.2 to form CO includes providing a catalyst, and contacting H.sub.2 and CO.sub.2 with the catalyst to chemically reduce CO.sub.2 to form CO. The catalyst includes a metal oxide having a chemical formula of Fe.sub.xCo.sub.yMn(.sub.1-x-y)O.sub.z, in which 0.7≤x≤0.95, 0.01≤y≤0.25, and z is an oxidation coordination number.

A catalyst is provided for production of hydrocarbons including monocyclic aromatic hydrocarbons having a carbon number of 6 to 8 and aliphatic hydrocarbons having a carbon number of 3 to 4 from feedstock in which a 10 vol % distillation temperature is 140° C. or higher and a 90 vol % distillation temperature is 380° C. or lower. The catalyst includes crystalline aluminosilicate including large-pore zeolite having a 12-membered ring structure.

Disclosed is a method for preparing a double end capped glycol ether, the method comprising: introducing into a reactor a raw material comprising a glycol monoether and a monohydric alcohol ether, and enabling the raw material to contact and react with an acidic molecular sieve catalyst to generate a double end capped glycol ether, a reaction temperature being 50-300° C., a reaction pressure being 0.1-15 MPa, a WHSV of the glycol monoether in the raw material being 0.01-15.0 h.sup.−1, and a mole ratio of the monohydric alcohol ether to the glycol monoether in the raw material being 1-100:1. The method of the present invention enables a long single-pass lifespan of the catalyst and repeated regeneration, has a high yield and selectivity of a target product, low energy consumption during separation of the product, a high economic value of a by-product, and is flexible in production scale and application.

The present technology provides a method of making a fluid catalytic cracking (FCC) catalyst, the method includes: in situ crystallizing Y-zeolite on a precursor microsphere to provide the FCC catalyst, wherein the in situ crystallizing includes: mixing the precursor microspheres with sodium silicate, a zeolite initiator (seeding zeolite crystals), and water to form an alkaline slurry; and heating the alkaline slurry to a temperature of about 38° C. (100° F.) to about 93° C. (200° F.) to obtain a zeolitic microsphere material; and wherein the FCC catalyst has a zeolite content of less than or equal to about 30 weight percent (wt.%). The unit cell size of the zeolite Y is 24.60 to 24.70 angstrom.

A modified β zeolite has 0.5-15 wt % of an IVB group metal element in terms of oxide on the dry basis weight of the modified β zeolite. The number of medium strong acid centers of the modified β zeolite accounts for 30-60% of the total acid amount, the number of strong acid centers accounts for 5-25% of the total acid amount, and the ratio of B acid to L acid is 0.8 or more. The ratio of the weight content of the IVB group metal element in the modified β zeolite body phase to the weight content of the IVB group metal element on the surface is 0.1-0.8. The catalytic cracking catalyst containing the modified β zeolite has good selectivity and yield of C4 olefin.