Institut Francais Du Pe'trole

Societe Francaise Des Produits Pour Catalyse 'procatalyse'

Societe Francaise Des Produits Pour Catalyse

Ste Francaise Des Products Pour Catalyse Pro-catalyse Chez Institut

Ste Francaise Des Produits Pour Catalyse Pro-catalyse Chez Institut

Yves Jacquin

Herve Toulhoat

Jean-Francois Le Page

Alain Billon

Marc Mercier

Jean-Claude Plumail

Jean Cosyns

Germain J Martino

Jean-Pierre Franck

Jean-Paul Euzen

Jean-Pierre Peries

Chan T Dinh

Thierry Dupin

Manuel Gimenez-Coronado

Christian Marcilly

Maurice Born

Christian R Busson

Bernard A Juguin

Philippe Renault

Pierre Giuliani

Jean-Claude Guibet

Hugo Van Landeghem, Deceased

Alain Desvard

Michel Davidson

Dai-Nghia Huynh

Huynh Dai-Nghia

Jean-Francois Josserand

Regis Paulus

Marie-Jose Huron

This invention concerns a method of preparing catalysts and certain catalysts which can be obtained by the method. The method comprises (a) coprecipitating at least a group VIII metal sulfide with at least a group VIB metal sulfide, at a pH maintained at a value of 4.5 to 8; (b) separating the resultant precipitate; (c) drying the precipitate; and (d) calcining the dried precipitate; all the steps being effected under an inert atmosphere. The catalysts have a stoichiometry of 1.2 to 2.2 atoms of sulfur per metal atom, a crystallographic structure of molybdenite for the group VIB metal sulfide(s) and pyrite for the group VIII metal sulfide(s) and characterized by an X-ray diffraction powder pattern having at least two principal peaks a and b of the disulfide of each group VIB metal used (peaks a, b, c, d), and two principal peaks f and j of the disulfide of each group VIII metal used, (peaks e, f, g, h, i, j, k), the height of the principal peak of a group VIII metal monosulfide (1), if it appears being less than 5 times that of the principal peak (f) of the disulfide of the same metal, which are particularly active for all reactions between hydrogen and a mixture of hydrocarbons containing sulfide compounds.

Group VIII and VIB metal sulfide catalysts, their manufacture and their

Supported catalysts which are made by shaping catalyst carrier, with or without catalyst precursors, into balls, calcining the balls at 300.degree.-1000.degree. C., and crushing the calcined balls to particles whose average size is 0.2-0.8 times the average diameter of the balls. When the precursors are not present during the manufacture, they are added thereafter.

Process for the hydrotreatment of hydrocarbon oil employing catalysts

A process for hydrotreating hydrocarbons uses a catalyst which comprises a carrier and at least one catalytic metal selected from vanadium, molybdenum, tungsten, nickel, cobalt and/or iron; this catalyst is in the form of a plurality of juxtaposed agglomerates of acicular platelets, oriented radially to each other. It is prepared from agglomerates of activated alumina subjected to reaction with an acid and a compound providing an anion able to combine with aluminum ions in solution.

Process for hydrotreating metal containing oil fractions using a

Alumina, silica or silica-alumina containing catalysts are manufactured by incorporating at least one active element selected from the metals of the groups V, VI and VIII or their compounds to a carrier, and then drying and activating. The carrier or the catalyst is shaped into extrudates and the latter are crushed to coarse particles.

Crushed catalysts containing alumina, silica or silica-alumina, and

A process for conversion of an asphaltenes-containing heavy oil or heavy oil fraction to lighter fractions comprises 3 steps of: catalytic hydrodemetallation, hydrovisbreaking and catalytic hydrodesulfuration.

Heavy oil process with hydrodemetallation, hydrovisbreaking and

An asphaltene-containing heavy oil or heavy oil fraction is converted to lighter fractions in a process comprising three steps: a hydrovisbreaking, a catalytic hydrodemetallation and catalytic hydrodesulfuration.

Heavy oil process with hydrovisbreaking, hydrodemetallation and

Supported catalysts for use in hydrocarbons hydrotreatments are made by shaping catalyst carrier, with or without catalyst precursors, into balls, calcining the balls at 300.degree.-1000.degree. C., and crushing the calcined balls to particles whose average size is 0.2-0.8 times the average diameter of the balls. When the precursors are not present during the manufacture, they are added thereafter.

Process for manufacturing a supported catalyst for the hydrotreatment of

A catalyst for use in the hydrotreatment of hydrocarbons comprises a carrier and at least one catalytic metal selected from vanadium, molybdenum, tungsten, nickel, cobalt and/or iron; this catalyst is in the form of a plurality of juxtaposed agglomerates of acicular platelets, oriented radially to each other. It is prepared from agglomerates of activated alumina subjected to reaction with an acid and a compound providing an anion able to combine with aluminum ions in solution.

Supported catalyst of increased resistance to poisons, useful for

Catalysts solid particles are supplied to a vertical reactor for the catalytic treatment of fluid charges, at the upper part of said reactor and are progressively withdrawn from the lower part thereof either continuously or periodically through a funnel having the shape of an inverted cone or an inverted pyramid. At least a portion of the charge is introduced at the lower part of the reactor through orifices above the walls of the funnel at a distance thereof from 1 to 500 times the average size of a catalyst particle.

Process and device for withdrawing solid particles and introducing a

Heavy hydrocarbon fractions are made free of asphaltenes and/or resins by extraction with a deasphalting solvent in the presence of ultrasonic radiation.

Process for solvent deasphalting heavy hydrocarbon fractions

Residual oils from steam-cracking or catalytic cracking, oils from coal liquefaction and oils from bituminous sands and shales are converted to gasoline by a process comprising the fractionation of the feed charge to a naphtha and a middle distillate: the naphtha, admixed with a gasoline cut 'E', is hydrotreated and then dehydrogenated to gasoline; the middle distillate is hydrotreated and fractionated to gasoline and a heavier fraction, the heavier fraction is hydrocracked and fractionated, thus producing a gasoline cut which constitutes the above cut 'E'.

Process for manufacturing gasoline with upgrading of hydrocarbon oils

A heavy hydrocarbon charge containing sulfur, asphaltenes and/or resins is hydrotreated in the liquid phase at 250.degree.-500.degree. C. under a pressure of 20-350 bars in the presence of a catalyst previously obtained by reacting an organic compound of a transition metal with an organic aluminum compound, in a hydrocarbon free of asphaltene and resin. The transition metal organic compound is advantageously an iron, nickel, cobalt, molybdenum, tungsten or vanadium acetylacetonate or carboxylate.

Process for the hydrotreatment of heavy hydrocarbons in the presence of

The hydroconversion of a heavy hydrocarbon charge containing asphaltenes and metal, sulfur and nitrogen impurities is performed in the presence of a catalyst comprising:

Process for the catalytic hydroconversion of heavy hydrocarbons in

Catalytic cracking or steam cracking effluents are desulfurized without substantial decrease of their octane number by subdividing said effluent into two fractions of different boiling ranges, the heavier of which is admixed with hydrogen, the resulting mixture being completely vaporized and fed to a hydrodesulfurization zone containing a first bed of selective catalyst formed of cobalt and molybdenum, or cobalt and tungsten, or nickel and molybdenum or nickel and tungsten deposited on a non-acid carrier, and a second bed of conventional hydrodesulfurization catalyst, the effluent from the hydrodesulfurization zone being cooled down and fractionated to separate a hydrocarbon fraction of the gasoline range which is recombined with the lighter fraction of said effluent.

Process for desulfurizing a catalytic cracking or steam cracking effluent

Hydrorefining of a hydrocarbon charge of high metal content with a catalyst containing alumina, a metal from group VI and a metal from the iron group, of a specific surface from 120 to 200 m.sup.2 /g, a total pore volume from 0.8 to 1.2 cc/g and a pore distribution as follows:

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Sevres, France

Yves Jacquin