A nano-sized mesoporous zeolite beta composition and processes for the synthesis and use of the nano-sized mesoporous zeolite beta. The nano-sized mesoporous zeolite beta is synthesized using a hydrothermal treatment without drying and calcination of the zeolite prior to or after hydrothermal treatment. A process for hydrocracking a hydrocarbon feedstock using the nano-sized mesoporous zeolite beta is also provided.

A nano-sized mesoporous zeolite beta composition and processes for the synthesis and use of the nano-sized mesoporous zeolite beta. The nano-sized mesoporous zeolite beta is synthesized using desilication without the addition of a structure directing agent (SDA). A process for hydrocracking a hydrocarbon feedstock using the nano-sized mesoporous zeolite beta is also provided

A nano-sized mesoporous zeolite beta composition and processes for the synthesis and use of the nano-sized mesoporous zeolite beta. The nano-sized mesoporous zeolite beta is synthesized using desilication without the addition of a structure directing agent (SDA). A process for hydrocracking a hydrocarbon feedstock using the nano-sized mesoporous zeolite beta is also provided

Zeolite catalysts and systems and methods for preparing and using zeolite catalysts having the CHA crystal structure are disclosed. The catalysts can be used to remove nitrogen oxides from a gaseous medium across a broad temperature range and exhibit hydrothermal stable at high reaction temperatures. The zeolite catalysts include a zeolite carrier having a silica to alumina ratio from about 15:1 to about 256:1 and a copper to alumina ratio from about 0.25:1 to about 1:1.

Zeolite catalysts and systems and methods for preparing and using zeolite catalysts having the CHA crystal structure are disclosed. The catalysts can be used to remove nitrogen oxides from a gaseous medium across a broad temperature range and exhibit hydrothermal stable at high reaction temperatures. The zeolite catalysts include a zeolite carrier having a silica to alumina ratio from about 15:1 to about 256:1 and a copper to alumina ratio from about 0.25:1 to about 1:1.

An organotemplate-free synthetic process for the production of a zeolite of TON framework type structure is provided. The process includes the steps of: (1) preparing a mixture comprising: (a) an alumina-coated silica; (b) a source of an alkali metal; (c) an alcohol; (d) a source of hydroxide ions; (e) seed crystals comprising a zeolitic material having a TON framework type structure; and (f) water; and (2) crystallizing the mixture obtained in step (1).

An organotemplate-free synthetic process for the production of a zeolite of TON framework type structure is provided. The process includes the steps of: (1) preparing a mixture comprising: (a) an alumina-coated silica; (b) a source of an alkali metal; (c) an alcohol; (d) a source of hydroxide ions; (e) seed crystals comprising a zeolitic material having a TON framework type structure; and (f) water; and (2) crystallizing the mixture obtained in step (1).

A high-purity artificial zeolite is industrially mass produced by carrying out osmosis treatment of fly ash in an alkaline aqueous solution, subsequently carrying out the osmosis treatment again with an acidic aqueous solution of pH 1.0 or less obtained by adding acid to the osmotic aqueous solution of fly ash, then performing solid-liquid separation while water wash and dewatering in a centrifuge, thereby synthesizing a starting composition, and performing hydrothermal reaction treatment to this starting composition.

A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P.sub.0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P.sub.0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.

A molecular sieve has a silica/alumina molar ratio of 100-300, and has a mesopore structure. One closed hysteresis loop appears in the range of P/P.sub.0=0.4-0.99 in the low temperature nitrogen gas adsorption-desorption curve, and the starting location of the closed hysteresis loop is in the range of P/P.sub.0=0.4-0.7. The catalyst formed from the molecular sieve as a solid acid not only has a good capacity of isomerization to reduce the freezing point, but also can produce a high yield of the product with a lower pour point. The process for preparing the catalyst involves steps including crystallization, filtration, calcination, and hydrothermal treatment.