A modified Y-type molecular sieve having a calcium content of about 0.3-4 wt % calculated on the basis of calcium oxide, a rare earth content of about 2-7 wt % calculated on the basis of rare earth oxide, and a sodium content of no more than about 0.5 wt % calculated on the basis of sodium oxide. The modified Y-type molecular sieve has a total pore volume of about 0.33-0.39 ml/g, a proportion of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 10-25%, a lattice constant of about 2.440-2.455 nm, a proportion of non-framework aluminum content to the total aluminum content of no more than about 20%, a lattice collapse temperature of not lower than about 1050° C., and a ratio of B acid to L acid in the total acid content of no less than about 2.30.

The invention relates to a molecular sieve modification method and a catalytic cracking catalyst containing a molecular sieve. The method comprises: mixing a solution containing an ion of a Group MB metal in the periodic table, an organic complexing agent, and/or a dispersant and a precipitation agent, and stirring the same to form a suspension containing a precipitant of a Group IIIB element; and mixing the resulting precipitant and a molecular sieve slurry, stirring the same to obtain a mixed slurry containing the precipitant of the Group MB element and a molecular sieve, and performing spray drying and optional calcination, to obtain a modified molecular sieve. The catalyst comprises, as calculated based on the catalyst mass being 100%, 10-55% of a modified molecular sieve (on a dry basis), 10-80% of clay (on a dry basis), 0-40% of an inorganic oxide (on an oxide basis), and 5-40% of a binding agent (on an oxide basis). The catalyst has good activity stability and heavy metal contamination resistance.

A bottoms cracking catalyst composition, comprising: about 30 to about 60 wt % alumina; greater than 0 to about 10 wt % of a dopant, measured as the oxide; about 2 to about 20 wt % reactive silica; about 3 to about 20 wt % of a component comprising peptizable boehmite, colloidal silica, aluminum chlorohydrol, or a combination of any two or more thereof; and about 10 to about 50 wt % of kaolin.

Bimetallic catalysts for the hydrodeoxygenation (HDO) conversion of lignin into useful hydrocarbons are provided. The catalysts are bifunctional bimetallic ruthenium catalysts Ru-M/X.sup.+Y comprising a metal M such as iron (Fe), nickel (Ni), copper (Cu) or zinc (Zn), zeolite Y and cation X.sup.+ (e.g. H.sup.+) associated with zeolite Y.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

Process scheme configurations are disclosed that enable deep hydrogenation of middle distillates. The hydrogenated middle distillates are processed in a steam cracker for conversion into light olefins. Feeds to the deep hydrogenation zone include diesel range streams from a diesel hydrotreating zone, a gas oil hydroprocessing zone, and/or a vacuum residue hydrocracking zone. The deep hydrogenation zone operates under conditions effective to reduce aromatic content in a diesel range feedstream from a range of about 10-40 wt % or greater, to a hydrogenated distillate range intermediate product having an aromatic content of less than about 5-0.5 wt %.

A process is provided for improving cold flow properties of distillates, the process comprises the step of contacting a hydrocarbon feedstock with a framework-substituted ultra-stable Y (USY)-type zeolite in which a portion of aluminum atoms constituting a zeolite framework thereof is substituted with zirconium atoms and/or titanium and/or hafnium atoms, thereby producing a dewaxed distillate product.

A modified Y-type molecular sieve has a rare earth content of about 4-11% by weight on the basis of rare earth oxide, a sodium content of no more than about 0.7% by weight on the basis of sodium oxide, a zinc content of about 0.5-5% by weight on the basis of zinc oxide, a phosphorus content of about 0.05-10% by weight on the basis of phosphorus pentoxide, a framework silica-alumina ratio of about 7-14 calculated on the basis of SiO.sub.2/Al.sub.2O.sub.3 molar ratio, a percentage of non-framework aluminum content to the total aluminum content of no more than about 20%, and a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 15-30%. The modified Y-type molecular sieve has a high crystallinity, a structure comprising secondary pores, and a high thermal and hydrothermal stability.