The present disclosure relates to a reforming catalyst composition comprising a spherical gamma AI.sub.2O.sub.3 support; at least one Group VB metal oxide sheet coated on to the AI.sub.2O.sub.3 support; and at least one active metal and at least one promoter metal impregnated on the AI.sub.2O.sub.3 coated support. The reforming catalyst composition of the present disclosure has improved activity, better selectivity for total aromatics during naphtha reforming and results in less coke formation. The reforming catalyst composition has improved catalyst performance with simultaneous modification of acidic sites as well as metallic sites through metal support interaction. The acid site cracking activity of the catalyst is inhibited because of the use of chloride free alumina support modified with solid acid such as Group VB metal oxide and impregnated with active metals. The present disclosure provides a process for naphtha reforming in the presence of the reforming catalyst composition of the present disclosure to obtain reformates of naphtha.

A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

A fluidized catalytic reactor system cycles from 0.05-5% of catalyst at a time through a rejuvenation unit to be heated in the presence of oxygen to maintain catalyst activity. The use of the rejuvenation unit that may be 2% of the size of the main catalyst regeneration unit allows for reduction in equipment size and in catalyst inventory. The catalyst that is sent to the rejuvenation unit may be spent catalyst but may be partially or fully regenerated catalyst. The rejuvenation unit may be heated by combusting fuel or by hot flue gas.

A process for upgrading a hydrocarbon feed includes contacting the hydrocarbon feed with hydrogen in the presence of a ring opening catalyst in a naphthene conversion unit, the contacting causing naphthenes in the hydrocarbon feed to react to produce a converted effluent comprising isoparaffins and normal paraffins. The process includes separating the converted effluent in a paraffin separation system to produce an isoparaffin-rich stream and an n-paraffin-rich stream. The process includes contacting the isoparaffin-rich stream with hydrogen in the presence of an isomerization catalyst in a reverse isomerization unit, the contacting causing isomerization to produce an isomerate comprising an equilibrium mixture of normal paraffins and isoparaffins. The process include separating the isomerate in the paraffin separation system to produce the isoparaffin-rich stream and the n-paraffin-rich stream, and passing the n-paraffin-rich stream to a steam cracker to produce a cracker effluent comprising olefins.

A process for upgrading a hydrocarbon feed includes contacting the hydrocarbon feed with hydrogen in the presence of a ring opening catalyst in a naphthene conversion unit, the contacting causing naphthenes in the hydrocarbon feed to react to produce a converted effluent comprising isoparaffins and normal paraffins. The process includes separating the converted effluent in a paraffin separation system to produce an isoparaffin-rich stream and an n-paraffin-rich stream. The process includes contacting the isoparaffin-rich stream with hydrogen in the presence of an isomerization catalyst in a reverse isomerization unit, the contacting causing isomerization to produce an isomerate comprising an equilibrium mixture of normal paraffins and isoparaffins. The process include separating the isomerate in the paraffin separation system to produce the isoparaffin-rich stream and the n-paraffin-rich stream, and passing the n-paraffin-rich stream to a steam cracker to produce a cracker effluent comprising olefins.

The invention relates to a catalyst comprising a support, at least one noble metal M, tin, phosphorus and at least one lanthanide group element, the content of phosphorus element being comprised between 0.4 and 1% by weight, and the content of lanthanide group element(s) being less than 1% by weight with respect to the weight of the catalyst. The invention also relates to the process for the preparation of the catalyst and the use thereof in reforming.

The invention relates to a catalyst comprising a support, at least one noble metal M, tin, phosphorus and at least one lanthanide group element, the content of phosphorus element being comprised between 0.4 and 1% by weight, and the content of lanthanide group element(s) being less than 1% by weight with respect to the weight of the catalyst. The invention also relates to the process for the preparation of the catalyst and the use thereof in reforming.

Manage sulfur present as sulfur or a sulfur compound in a hydrocarbon feedstream while effecting dehydrogenation of hydrocarbon(s) (e.g. propane) contained in the hydrocarbon feedstream to its/their corresponding olefin (e.g. propylene where the hydrocarbon is propane) without subjecting the feedstream to desulfurization before it contacts a fluidizable dehydrogenation catalyst that is both a desulfurant and a dehydrogenation catalyst and comprises gallium and platinum on an alumina or alumina-silica catalyst support with optional alkali or alkaline earth metal such as potassium. Contact with such a catalyst yields a desulfurized crude olefin product that corresponds to the hydrocarbon and has a reduced amount of sulfur or sulfur compounds relative to the sulfur or sulfur compounds present in the hydrocarbon feedstream prior to contact with the catalyst.

Manage sulfur present as sulfur or a sulfur compound in a hydrocarbon feedstream while effecting dehydrogenation of hydrocarbon(s) (e.g. propane) contained in the hydrocarbon feedstream to its/their corresponding olefin (e.g. propylene where the hydrocarbon is propane) without subjecting the feedstream to desulfurization before it contacts a fluidizable dehydrogenation catalyst that is both a desulfurant and a dehydrogenation catalyst and comprises gallium and platinum on an alumina or alumina-silica catalyst support with optional alkali or alkaline earth metal such as potassium. Contact with such a catalyst yields a desulfurized crude olefin product that corresponds to the hydrocarbon and has a reduced amount of sulfur or sulfur compounds relative to the sulfur or sulfur compounds present in the hydrocarbon feedstream prior to contact with the catalyst.

A process and system for modifying heterogeneous catalysts by contacting them with chemical compounds to functionalize the surface of the heterogeneous catalyst. A polymetallic catalyst including bimetallic catalyst is functionalized on its surface by employing a precursor of an inorganic compound. The precursor of the inorganic compound is an organometallic compound, and the metal based inorganic compound is aluminum oxide. A process and system for surface modification functionalization of the heterogeneous catalysts at conditions including room temperature and atmospheric pressure.