The invention concerns a process for the preparation of a catalyst for carrying out hydrogenation reactions in hydrotreatment and hydrocracking processes. Said catalyst is prepared from at least one mononuclear precursor based on molybdenum (Mo), in its monomeric or dimeric form, having at least one Mo═O or Mo—OR bond or at least one Mo═S or Mo—SR bond where [R=C.sub.xH.sub.y where x≧1 and (x−1)≦y≦(2x+1) or R=Si(OR′).sub.3 or R=Si(R′).sub.3 where R′=C.sub.x′H.sub.y′ where x′≧1 and (x′−1)≦y′≦(2x′+1)], and optionally from at least one promoter element from group VIII. Said precursors are deposited onto an oxide support which is suitable for the process in which it is used, said catalyst being dried at a temperature of less than 200° C. then advantageously being sulphurized before being deployed in said process.

The invention concerns a process for the preparation of a catalyst for carrying out hydrogenation reactions in hydrotreatment and hydrocracking processes. Said catalyst is prepared from at least one mononuclear precursor based on molybdenum (Mo), in its monomeric or dimeric form, having at least one Mo═O or Mo—OR bond or at least one Mo═S or Mo—SR bond where [R=C.sub.xH.sub.y where x≧1 and (x−1)≦y≦(2x+1) or R=Si(OR′).sub.3 or R=Si(R′).sub.3 where R′=C.sub.x′H.sub.y′ where x′≧1 and (x′−1)≦y′≦(2x′+1)], and optionally from at least one promoter element from group VIII. Said precursors are deposited onto an oxide support which is suitable for the process in which it is used, said catalyst being dried at a temperature of less than 200° C. then advantageously being sulphurized before being deployed in said process.

The invention relates to the use, as a liquid phase heat-transfer medium, of a fluid having a boiling point in the range of from 200° C. to 400° C. and a boiling range below 80° C., said fluid comprising more than 95% by weight isoparaffins and less than 3% by weight of naphthens, a biocarbon content of at least 95% by weight, containing less than 100 ppm by weight aromatics.

A three step method for the conversion of ethanol into fuels that can be utilized as full-performance military jet or diesel fuels. Embodiments of the invention further describe methods for the selective conversion of ethanol to full performance saturated hydrocarbon fuels that are suitable for both jet and diesel propulsion.

A three step method for the conversion of ethanol into fuels that can be utilized as full-performance military jet or diesel fuels. Embodiments of the invention further describe methods for the selective conversion of ethanol to full performance saturated hydrocarbon fuels that are suitable for both jet and diesel propulsion.

A processing facility is provided. The processing facility includes an asphaltenes and metals (AM) removal system configured to process a feed stream to produce a power generation stream, a hydroprocessing feed stream, and an asphaltenes stream. A power generation system is fed by the power generation feed stream. A hydroprocessing system is configured to process the hydroprocessing feed stream to form a gas stream and a liquid stream. A hydrogen production system is configured to produce hydrogen, carbon monoxide and carbon dioxide from the gas feed stream. A carbon dioxide conversion system is configured to produce synthetic hydrocarbons from the carbon dioxide, and a cracking system is configured to process the liquid feed stream.

System and corresponding process for the hydroconversion of heavy oils essentially comprising a reactor, a liquid-vapor separator and a section for stripping conversion products outside the reactor comprising an inlet conduit for the stripping gases located at a point on the conduit providing a connection between the head of the reactor and the liquid-vapor separator inclined, at least from the point of entry, upwards with a gradient of between 2% and 20%, preferably between 3% and 12%, with respect to a horizontal plane. The inlet conduit for the stripping gases is inclined with respect to the axis of the conduit providing a connection between the reactor head and the liquid-vapor separator through an angle of between 20° and 65°, more preferably between 30° and 60°, even more preferably between 40° and 50°. The stripping gas delivered to the connection conduit between the head of the reactor and the separator flows in a downward direction.

System and corresponding process for the hydroconversion of heavy oils essentially comprising a reactor, a liquid-vapor separator and a section for stripping conversion products outside the reactor comprising an inlet conduit for the stripping gases located at a point on the conduit providing a connection between the head of the reactor and the liquid-vapor separator inclined, at least from the point of entry, upwards with a gradient of between 2% and 20%, preferably between 3% and 12%, with respect to a horizontal plane. The inlet conduit for the stripping gases is inclined with respect to the axis of the conduit providing a connection between the reactor head and the liquid-vapor separator through an angle of between 20° and 65°, more preferably between 30° and 60°, even more preferably between 40° and 50°. The stripping gas delivered to the connection conduit between the head of the reactor and the separator flows in a downward direction.

The present disclosure relates to a method that includes a first treating of a first mixture that includes a carboxylic acid having between 2 and 12 carbon atoms, inclusively, to form a second mixture that includes a ketone having between 2 and 25 carbon atoms, inclusively, and a second treating of at least a first portion of the second mixture to form a first product that includes a paraffin having 8 or more carbon atoms.

A catalytic cracking gasoline prehydrogenation method is provided. Thiol etherification and double bond isomerization reactions are carried out on catalytic cracking gasoline through a prehydrogenation reactor. The reaction conditions are as follows: the reaction temperature is between 80° C. and 160° C., the reaction pressure is between 1 MPa and 5 MPa, the liquid-volume hourly space velocity is from 1 to 10 h.sup.−1, and the hydrogen-oil volume ratio is (3-8):1; a prehydrogenation catalyst comprises a carrier and active ingredients, the carrier contains an aluminium oxide composite carrier with a macroporous structure and one or more of ZSM-5, ZSM-11, ZSM-12, ZSM-35, mordenite, amorphous form aluminum silicon, SAPO-11, MCM-22, a Y molecular sieve and a beta molecular sieve, the surface of the carrier is loaded with one or more of the active ingredients cobalt, molybdenum, nickel and tungsten; based on oxides, the content of the active ingredients is between 0.1% and 15.5%.