A process for preparation of a bicyclic fused-ring alkane. In the presence of a bifunctional solid catalyst, one or more cyclitols undergo a CC coupling reaction with itself or each other at a temperature and in a nitrogen gas atmosphere, to produce a bicyclic alkane precursor mixture; then, the nitrogen gas is replaced by hydrogen gas, and the bicyclic alkane precursor mixture is hydrogenated or hydrodeoxygenated at a temperature and under a pressure, to produce the bicyclic fused-ring alkane. The proportion of the bicyclic fused-ring alkane in the product as prepared according to the process is not lower than 80 wt %.

Provided is a production method for indan and hydrindane, including a reaction step of introducing a raw material composition including tetrahydroindene into a continuous reactor including a solid catalyst containing platinum, and bringing the raw material composition into contact with the solid catalyst under the conditions of 150? C. to 350? C. to obtain a reaction product including indan and hydrindane, in which the amount (mol/min) of hydrogen molecules is 5 times or less the amount (mol/min) of tetrahydroindene, and the amount (mol/min) of oxygen molecules is 0.1 times or less the amount (mol/min) of tetrahydroindene.

A process for hydrocracking 2,4-dimethylpentane and/or 2,2,3-trimethylbutane can comprise: contacting a hydrocracking feed stream in the presence of hydrogen with a hydrocracking catalyst, wherein the hydrocracking feed stream comprises at least 0.5 wt % of 2,4-dimethylpentane and/or 2,2,3-trimethylbutane, based upon a total weight of the hydrocracking feed stream; and wherein the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75; preferably the hydrocracking catalyst comprises a medium pore zeolite having a pore size of 5-6 A and a silica to alumina molar ratio of 20-75 and a large pore zeolite having a pore size of 6-8 A and a silica to alumina molar ratio of 10-80, wherein the hydrogenation metal is deposited on the medium pore zeolite and the large pore zeolite.

Disclosed herein is a process for producing para-xylene comprising the steps of: (a) contacting a feedstock comprising toluene with a first catalyst under effective vapor phase toluene disproportionation conditions to disproportionate said toluene and produce a first product comprising benzene, unreacted toluene and greater than equilibrium amounts of para-xylene; and (b) contacting a feedstock comprising C.sub.9+ aromatic hydrocarbons and benzene with a second catalyst in the presence of 0 wt. % or more of hydrogen having a 0 to 10 hydrogen/hydrocarbon molar ratio under effective C.sub.9+ transalkylation conditions to transalkylate said C.sub.9+ aromatic hydrocarbons and produce a second product comprising xylenes.

In an aspect, a method for the aromatization of hydrocarbons comprises contacting a hydrocarbon feedstream with a catalyst; wherein the catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the zeolite further comprises Na; and wherein the catalyst has an Si:Al.sub.2 mole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5, wherein the catalyst has an aluminum content of less than or equal to 0.75 wt % excluding any binder and extrusion aide.

Disclosed herein is a process for preparing a hydrocracking catalyst, comprising (i) combining a zeolite, a binder, water and a hydrogenating metal compound which is a complex or a salt of a hydrogenating metal to obtain a mixture, wherein the zeolite has not been treated with a phosphorus-containing compound and the zeolite has a silica to alumina molar ratio of 5-200; (ii) forming the mixture into a shaped body; and (iii) calcining the shaped body to form the catalyst.

A method for producing hydrocarbons and hydrogen from methane. The method includes packing a catalyst comprising platinum, bismuth and a support material into a reactor; introducing a reactant mixture containing methane into the reactor such that the reactant mixture containing methane is in close contact with the reactant mixture; and heating the reactant mixture containing methane to a temperature for a period of time.

A process for preparing a catalyst composition comprising (a) preparing a carrier comprising (i) mordenite in an amount in the range of from 20 to 80 wt %, based on total weight of carrier, (ii) ZSM-5 type zeolite in an amount in the range of from 10 to 70 wt %, based on total weight of carrier; and (iii) an inorganic binder in an amount in the range of from 10 to 50 wt %, based on total weight of carrier; (b) incorporating in the carrier molybdenum in an amount in the range of from 1 to 10 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 100 to at most 300? C. and (c) incorporating in the molybdenum containing carrier obtained in step (b) platinum in an amount of from 0.005 to 1 wt %, as metal based on total weight of catalyst composition, and subjecting the thus treated carrier to a temperature of from 200 to at most 600? C.; and a process for conversion of alkylaromatic hydrocarbons containing feedstock using a catalyst prepared by said process. Process using the prepared catalyst composition for alkylaromatic hydrocarbon conversion.

A new configuration of ZSM-5 is provided whereby the crystals have a higher average silica to alumina ratio at the edges of each crystallite than in the centre as determined from a narrow slit line scan profile obtained from SEM/EDX or TEM/EDX elemental analysis. Such ZSM-5 crystals are obtained by a preparation process using L-tartaric acid. The new configuration ZSM-5 provides significantly reduced xylene losses in ethylbenzene dealkylation, especially when combined with silica as binder, and one or more hydrogenation metals selected from platinum, tin, lead, silver, copper, and nickel.

In an embodiment, A catalyst comprises a zeolite comprising Si, Al, and Ge in the framework with Pt deposited thereon; wherein the catalyst has an Si:Al.sub.2 mole ratio of greater than or equal to 125, an Si:Ge mole ratio of 40 to 400, and an Na:Al mole ratio of 0.9 to 2.5; wherein the catalyst has an aluminum content of less than or equal to 0.75 wt %; wherein the catalyst is non-acidic.