Abstract: The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

Abstract: 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 downstream of the second hydrocracking step, the hydrogenation step treating the effluent resulting from the second hydrocracking step in the presence of a specific hydrogenation catalyst. Furthermore, the hydrogenation step and the second hydrocracking step are performed under specific operating conditions and in particular under quite specific temperature conditions.

Abstract: The present invention is based on the use of a two-step hydrocracking process 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 second hydrocracking step are carried out under specific operating conditions and in particular under very specific temperature conditions.

Abstract: Catalyst comprising a nickel-based active phase and an alumina support, characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises between 40% and 80% by weight of nickel element relative to the total weight of nickel contained in the catalyst; the size of the nickel particles in the catalyst is less than 7 nm.

Abstract: Catalyst comprising a nickel-based active phase and an alumina support, characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises between 40% and 80% by weight of nickel element relative to the total weight of nickel contained in the catalyst.

Abstract: Hydrogenation of at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point below or equal to 650° C., at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) molar ratio between 0.1 and 10 and at an hourly space velocity HSV of between 0.05 and 50 h?1, in the presence of a catalyst comprising an alumina support and an active phase comprising nickel, prepared by i) contacting the support with a solution containing a nickel precursor; ii) bringing the support into contact with a solution containing an organic compound comprising a carboxylic acid, or alcohol, or ester, or amide function; iii) drying the impregnated support at a temperature below 250° C.; i) and ii) being carried out separately, in any order, or at the same time.

Abstract: Catalyst comprising nickel and copper, in a proportion of 1% to 50% by weight of nickel element relative to the total weight of the catalyst, in a proportion of 0.5% to 15% by weight of copper element relative to the total weight of the catalyst, and an alumina support, said catalyst being characterized in that: the mole ratio between nickel and copper is between 0.5 and 5 mol/mol; at least one portion of the nickel and copper is in the form of a nickel-copper alloy; the nickel content in the nickel-copper alloy is between 0.5% and 15% by weight of nickel element relative to the total weight of the catalyst, the size of the nickel particles in the catalyst is less than 7 nm.

Abstract: Nickel and copper catalyst, and an alumina support: nickel distributed both in the core of and on a crust at the periphery of the support, crust thickness being 2% to 15% of catalyst diameter; nickel density ratio between the crust and the core greater than 3; crust contains more than 25% by weight of nickel element relative to total weight of nickel in the catalyst; mole ratio between nickel and copper is 0.5 to 5, at least one portion of nickel and copper is a nickel-copper alloy; nickel content in the nickel-copper alloy is 0.5% to 15% by weight of nickel element relative to total weight of the catalyst; size of the nickel particles in the catalyst is less than 7 nm.

Abstract: Catalyst comprising nickel and sulfur on an alumina support, said catalyst being characterized in that: the nickel is distributed both on a crust at the periphery of the support, and in the core of the support, the thickness of said crust being between 2% and 15% of the diameter of the catalyst; the nickel density ratio between the crust and the core is strictly greater than 3; said crust comprises more than 25% by weight of nickel element relative to the total weight of nickel contained in the catalyst, the size of the nickel particles in the catalyst, measured in oxide form, is between 7 and 25 nm.

Abstract: Process for hydrogenating at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point of less than or equal to 650° C., said process being performed in the gas phase or in the liquid phase at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) mole ratio of between 0.1 and 10 and at an hourly space velocity (HSV) of between 0.05 and 50 h?1, in the presence of a catalyst comprising an active phase comprising nickel, said active phase not comprising any group VIB metal, and a support comprising an amorphous mesoporous alumina having a connectivity (Z) of greater than 2.7, the connectivity being determined from the nitrogen adsorption/desorption isotherms.

Abstract: The invention describes a process for the capture of organometallic impurities in a hydrocarbon feedstock of gasoline type containing olefins and sulfur, in which a capture body is brought into contact with the feedstock to be treated and a stream of hydrogen, said capture body comprises an active phase based on nickel oxide particles with a size of less than or equal to 15 nm, said active phase not comprising other metal elements of Group VIb or Group VIII, which are deposited on a porous support chosen from the group consisting of aluminas, silica, silicas/aluminas, or also titanium or magnesium oxides, used alone or as a mixture with alumina or silica/alumina.

Abstract: The present invention is based on the use of a two-step hydrocracking process 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 second hydrocracking step are carried out under specific operating conditions and in particular under very specific temperature conditions.

Abstract: The invention relates to the implementation of a multi-stage hydrocracking process comprising a hydrogenation stage located downstream of the second hydrocracking stage, said hydrogenation stage treating the effluent produced in the second hydrocracking stage, in the presence of a specific hydrogenation catalyst. In addition, the hydrogenation and second hydrocracking stages are implemented under specific operating conditions and particularly under very specific temperature conditions.

Abstract: 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 downstream of the second hydrocracking step, the hydrogenation step treating the effluent resulting from the second hydrocracking step in the presence of a specific hydrogenation catalyst. Furthermore, the hydrogenation step and the second hydrocracking step are performed under specific operating conditions and in particular under quite specific temperature conditions.

Abstract: The present invention relates to a hydrogenolysis process wherein a hydrocarbon-based feedstock comprising aromatic compounds having at least 8 carbon atoms is treated by means of a hydrogen feed and in the presence of a catalyst, in order to convert C2+ alkyl chains of said aromatic compounds into methyl groups and to produce a hydrogenolysis effluent enriched in methyl-substituted aromatic compounds, wherein the catalyst comprises a support, comprising at least one refractory oxide, and an active phase comprising nickel and molybdenum, wherein: the nickel content being between 0.1 and 25% by weight relative to the total weight of the catalyst; the molybdenum content being between 0.1 and 20% by weight relative to the total weight of the catalyst; and the catalyst comprising a molar ratio of molybdenum to nickel of between 0.2 and 0.9. The present invention also relates to said catalyst and to the process for preparing said catalyst.

Abstract: The invention relates to a selective hydrogenolysis method for treating a feed rich in aromatic compounds having more than 8 carbon atoms, comprising transforming at least one alkyl group with at least two carbon atoms (ethyl, propyl, butyl, isopropyl, etc.) attached to a benzene ring into at least one methyl group. The invention also relates to the integration of the hydrogenolysis unit into an aromatic complex.

Abstract: A process for the hydrogenation of a polyunsaturated compound contained in a hydrocarbon feedstock in the presence of a catalyst comprising a porous support and an active phase comprising a group VIII metal, said catalyst being prepared according to the following steps: a) an organic compound containing oxygen and/or nitrogen, but not comprising sulfur, is added to the porous support; b) said porous support is brought into contact with a solution containing a salt of a precursor of the active phase; c) the porous support obtained at the end of step b) is dried; characterized in that step a) is carried out before or after steps b) and c) and is carried out by bringing together said porous support and said organic compound under conditions of temperature, pressure and duration such that a fraction of said organic compound is transferred in the gaseous state to the porous support.

Abstract: The invention describes a process for the capture of organometallic impurities in a hydrocarbon feedstock of gasoline type containing olefins and sulfur, in which a capture body is brought into contact with the feedstock to be treated and a stream of hydrogen, said capture body comprises an active phase based on nickel oxide particles with a size of less than or equal to 15 nm, said active phase not comprising other metal elements of Group VIb or Group VIII, which are deposited on a porous support chosen from the group consisting of aluminas, silica, silicas/aluminas, or also titanium or magnesium oxides, used alone or as a mixture with alumina or silica/alumina.

Abstract: 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.

Abstract: Process for hydrogenating at least one aromatic or polyaromatic compound contained in a hydrocarbon feedstock having a final boiling point of less than or equal to 650° C., said process being performed in the gas phase or in the liquid phase at a temperature of between 30 and 350° C., at a pressure of between 0.1 and 20 MPa, at a hydrogen/(aromatic compounds to be hydrogenated) mole ratio of between 0.1 and 10 and at an hourly space velocity (HSV) of between 0.05 and 50 h?1, in the presence of a catalyst comprising an active phase comprising nickel, said active phase not comprising any group VIB metal, and a support comprising an amorphous mesoporous alumina having a connectivity (Z) of greater than 2.7, the connectivity being determined from the nitrogen adsorption/desorption isotherms.