The present invention provides a process for upgrading a Fischer-Tropsch product by hydrocracking in the presence of a hydrocracking catalyst in a reactor, wherein the process is initiated by a series of steps (i) to (iv). The hydrocracking catalyst is (i) contacted with a hydrogen-containing stream having a feed temperature of from 360° C. to 420° C.; (ii) the feed temperature of the hydrogen-containing stream is reduced to a temperature of from 220° C. to 280° C.; (iii) the catalyst is contacted with a Fischer-Tropsch product stream having a feed temperature of from 220° C. to 280° C., which is co-fed with the hydrogen-containing stream; and (iv) the catalyst is co-fed with a Fischer-Tropsch product stream and hydrogen-containing stream having feed temperatures of from 380° C. and 400° C. for at least four days and wherein the hydrocracking catalyst is not activated by sulfiding.

A process of reforming a diesel feedstock to convert diesel to a gasoline blending component may include desulfurizing and denitrogenizing the diesel feedstock to reduce the sulfur and nitrogen content; and then hydrocracking the diesel feedstock over a metal containing zeolitic catalyst to produce an isomerate fraction. The diesel feedstock may have boiling points ranging from 200 to 360° C.

The present invention is based on the use of a two-step hydrocracking process for the production of naphtha, comprising a step of hydrogenation placed upstream of the second hydrocracking step, the hydrogenation step treating the unconverted liquid fraction separated in the distillation step in the presence of a specific hydrogenation catalyst. Furthermore, the hydrogenation step and a second hydrocracking step are carried out under specific operating conditions and in particular under temperature conditions that are very specific with respect to one another.

A method including subjecting an ultra-stable Y-type zeolite having a low silica-to-alumina molar ratio (SAR), such as in a range of 3 to 6, to acid treatment and heteroatom incorporation contemporaneously to give a framework-modified ultra-stable Y-type zeolite.

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

A process for upgrading vacuum residuum and vacuum gas oil hydrocarbons is disclosed. The process may include: contacting a heavy distillate hydrocarbon fraction and hydrogen with a zeolite selective hydrocracking catalyst in a first ebullated bed hydrocracking reaction zone to convert at least a portion of the vacuum gas oil to lighter hydrocarbons. Contacting a residuum hydrocarbon fraction and hydrogen with a non-zeolite base metal hydroconversion catalyst in a second ebullated bed hydroconversion reaction zone may produce a vapor stream containing unconverted hydrogen, acid gases and volatilized hydrocarbons which may be fed along with the vacuum gas oil in the first ebullated bed hydrocracking zone.

A process for hydrodealkylating a hydrocarbon stream comprising (a) contacting the hydrocarbon stream with a hydroprocessing catalyst in a hydroprocessing reactor in the presence of hydrogen to yield a hydrocarbon product, wherein the hydrocarbon stream contains C.sub.9+ aromatic hydrocarbons; and (b) recovering a treated hydrocarbon stream from the hydrocarbon product, wherein the treated hydrocarbon stream comprises C.sub.9+ aromatic hydrocarbons, wherein an amount of C.sub.9+ aromatic hydrocarbons in the treated hydrocarbon stream is less than an amount of C.sub.9+ aromatic hydrocarbons in the hydrocarbon stream due to hydrodealkylating of at least a portion of C.sub.9+ aromatic hydrocarbons from the hydrocarbon stream during the step (a) of contacting.

A process for hydrodealkylating a hydrocarbon stream comprising (a) contacting the hydrocarbon stream with a hydroprocessing catalyst in a hydroprocessing reactor in the presence of hydrogen to yield a hydrocarbon product, wherein the hydrocarbon stream contains C.sub.9+ aromatic hydrocarbons; and (b) recovering a treated hydrocarbon stream from the hydrocarbon product, wherein the treated hydrocarbon stream comprises C.sub.9+ aromatic hydrocarbons, wherein an amount of C.sub.9+ aromatic hydrocarbons in the treated hydrocarbon stream is less than an amount of C.sub.9+ aromatic hydrocarbons in the hydrocarbon stream due to hydrodealkylating of at least a portion of C.sub.9+ aromatic hydrocarbons from the hydrocarbon stream during the step (a) of contacting.

A process for producing propylene and cumene comprising converting plastics to hydrocarbon liquid and pyrolysis gas in pyrolyzer; feeding hydrocarbon liquid to hydroprocessor to yield hydrocarbon product and first gas stream; introducing hydrocarbon product to second separator to produce first C.sub.6 aromatics and refined product; feeding refined product to steam cracker to produce steam cracker product; introducing steam cracker product to third separator to produce second C.sub.6 aromatics, third propylene stream, second C.sub.2&C.sub.4 unsaturated stream, C.sub.1-4 saturated gas, and balance hydrocarbons product; introducing pyrolysis gas and/or first gas stream to first separator to produce first propylene stream, first C.sub.2&C.sub.4 unsaturated stream, and saturated gas stream; feeding first and/or second C.sub.2&C.sub.4 unsaturated stream to metathesis reactor to produce second propylene stream; feeding first and/or second C.sub.6 aromatics, and first, second, and/or third propylene stream to alkylation unit to produce cumene; and conveying balance hydrocarbons product to pyrolyzer and/or hydroprocessor.

Process for the production of middle distillates from a paraffinic feedstock produced by Fischer-Tropsch synthesis comprising at least one light fraction, known as condensate, and a heavy fraction, known as waxes, in which: the said light fraction is stored in a vessel (B) maintained under an inert atmosphere and in which the temperature inside the vessel is maintained at a value of less than 20 C.; the said heavy fraction is stored in a vessel (C) maintained under an inert atmosphere and in which the temperature inside the vessel is maintained at a value of between 80 and 230 C.