The present invention relates to the preparation of various types of natural zeolite catalysts from natural zeolites such as clinoptilolite and the method of producing dimethyl ether from methyl alcohol using these natural zeolite catalysts.

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.

This present disclosure relates to processes for methylation of aromatics in an aromatics complex for producing a xylene isomer product. More specifically, the present disclosure relates to a process for producing para-xylene by the selective methylation of toluene and/or benzene in an aromatics complex using mild reaction conditions, namely a combination of low temperatures and elevated pressures using a zeolite with lower number of external acid sites.

There are provided a method for manufacturing a modified aluminosilicate by which a hydroquinone is highly selectively manufactured by reaction of a phenol with hydrogen peroxide, a modified aluminosilicate, and a method for manufacturing an aromatic dihydroxy compound by using the modified aluminosilicate, under industrially advantageous conditions. The method for manufacturing a modified aluminosilicate of the present invention includes a first step of treating an aluminosilicate with an acid, a second step of primarily calcining the treated material obtained in the first step at 550° C. to 850° C., and a third step of contacting the calcined material obtained in the second step with a liquid. containing one or more elements selected from the group consisting of Group 4 elements and. Group 5 elements on. the periodic table, and then drying and secondarily calcining the resultant. The modified aluminosilicate included in the present invention. includes one or more elements selected from the group consisting of Group 4 elements and Group 5 elements on the periodic table, and exhibits an absorbance at 300 nm (A[300]) in an ultraviolet visible spectrum of 1.0 or higher. The method for manufacturing aromatic dihydroxy compounds of the present invention includes a step of reacting a phenol with hydrogen peroxide in the presence of a specific modified. aluminosilicate.

A modified Y-type molecular sieve has a modifying metal content of about 0.5-6.3 wt % calculated on the basis of an oxide of the modifying metal and a sodium content of no more than about 0.5 wt % calculated on the basis of sodium oxide. The modifying metal is magnesium and/or calcium. The modified Y-type molecular sieve has a proportion of non-framework aluminum content to the total aluminum content of no more than about 20%, 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 lattice collapse temperature of not lower than about 1040° C., and a ratio of B acid to L acid in the total acid content of no less than about 2.30.

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 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.