The present invention relates to a method for producing a liquid hydrocarbon fuel comprising a first reaction step and a second reaction step given below: (1) a first reaction step: hydrocracking a raw material oil in the presence of a hydrocracking reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.05 to 0.5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil; and (2) a second reaction step: hydrogenating the cracked solution in the presence of a hydrogenation reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.2 to 5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil. According to the present invention, a desired liquid hydrocarbon fuel can be produced by carrying out a combination of the hydrocracking reaction and the hydrogenation reaction of a raw material oil such as fats and oils in a given composition by feeding a low-pressure hydrogen of nearly a normal pressure.

The present invention relates to a method for producing a liquid hydrocarbon fuel comprising a first reaction step and a second reaction step given below: (1) a first reaction step: hydrocracking a raw material oil in the presence of a hydrocracking reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.05 to 0.5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil; and (2) a second reaction step: hydrogenating the cracked solution in the presence of a hydrogenation reaction catalyst at a feeding pressure of hydrogen of from 0.2 to 0.95 MPa, a liquid hourly space velocity of a liquid volume of the raw material oil of from 0.2 to 5 hr.sup.−1, and a ratio of a flow rate of the hydrogen to a flow rate of the raw material oil of from 100 to 1,000 NL of the hydrogen per 1 L of the raw material oil. According to the present invention, a desired liquid hydrocarbon fuel can be produced by carrying out a combination of the hydrocracking reaction and the hydrogenation reaction of a raw material oil such as fats and oils in a given composition by feeding a low-pressure hydrogen of nearly a normal pressure.

A method for preparing a catalyst with a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, wherein the method involves: a) placing the support in contact with at least one solution containing a nickel precursor; b) placing the support in contact with a solution containing a copper precursor; wherein a) and b) are carried out separately in any order; c) drying the catalyst precursor at the end of a) and b), or b) and a), at a temperature less than 250° C.; and d) supplying the catalyst precursor obtained at the end of c), into a hydrogenation reactor, and carrying out a reduction step by placing the precursor in contact with a reducing gas at a temperature of less than 200° C. and for a period greater than or equal to 5 minutes and less than 2 hours.

A method for preparing a catalyst with a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, wherein the method involves: a) placing the support in contact with at least one solution containing a nickel precursor; b) placing the support in contact with a solution containing a copper precursor; wherein a) and b) are carried out separately in any order; c) drying the catalyst precursor at the end of a) and b), or b) and a), at a temperature less than 250° C.; and d) supplying the catalyst precursor obtained at the end of c), into a hydrogenation reactor, and carrying out a reduction step by placing the precursor in contact with a reducing gas at a temperature of less than 200° C. and for a period greater than or equal to 5 minutes and less than 2 hours.

A process for the selective hydrogenation of polyunsaturated compounds containing at least 2 carbon atoms per molecule, contained in a hydrocarbon feedstock having a final boiling point below or equal to 300 C. in the presence of a catalyst comprising an alumina support and an active phase comprising nickel, said active phase not comprising a metal from Group VIB, said catalyst being prepared by a process comprising at least: i) a step of bringing said support into contact with at least one solution containing at least one nickel precursor; ii) a step of bringing said support into contact with at least one solution containing at least one organic compound comprising at least one carboxylic acid function; iii) a step of drying said impregnated support at a temperature below 250 C.;
steps i) and ii) being carried out separately, in any order.

A process for the selective hydrogenation of polyunsaturated compounds containing at least 2 carbon atoms per molecule, contained in a hydrocarbon feedstock having a final boiling point below or equal to 300 C. in the presence of a catalyst comprising an alumina support and an active phase comprising nickel, said active phase not comprising a metal from Group VIB, said catalyst being prepared by a process comprising at least: i) a step of bringing said support into contact with at least one solution containing at least one nickel precursor; ii) a step of bringing said support into contact with at least one solution containing at least one organic compound comprising at least one carboxylic acid function; iii) a step of drying said impregnated support at a temperature below 250 C.;
steps i) and ii) being carried out separately, in any order.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Producing C5 olefins from steam cracker C5 feeds may include reacting a mixed hydrocarbon stream comprising cyclopentadiene, C5 olefins, and C6+ hydrocarbons in a dimerization reactor where cyclopentadiene is dimerized to dicyclopentadiene. The dimerization reactor effluent may be separated into a fraction comprising the C6+ hydrocarbons and dicyclopentadiene and a second fraction comprising C5 olefins and C5 dienes. The second fraction, a saturated hydrocarbon diluent stream, and hydrogen may be fed to a catalytic distillation reactor system for concurrently separating linear C5 olefins from saturated hydrocarbon diluent, cyclic C5 olefins, and C5 dienes contained in the second fraction and selectively hydrogenating C5 dienes. An overhead distillate including the linear C5 olefins and a bottoms product including cyclic C5 olefins are recovered from the catalytic distillation reactor system. Other aspects of the C5 olefin systems and processes, including catalyst configurations and control schemes, are also described.

Provided are a hydrogenation reaction catalyst and a preparation method therefor, and more particularly, to a hydrogenation reaction catalyst including sulfur as a promoter, thereby selectively hydrogenating an olefin by changing a relative hydrogenation rate of the olefin and an aromatic group during a hydrogenation reaction of an unsaturated hydrocarbon compound containing an aromatic group, and a preparation method therefor.

Preparation of a catalyst comprising an oxide matrix and an active phase comprising nickel: a calcined porous aluminium oxide is prepared; the calcined porous aluminium oxide obtained is kneaded with a solution resulting from mixing one or more solution(s) of at least one nickel precursor and at least one solution of at least one organic compound which has at least one carboxylic acid function, or at least one alcohol function, or at least one ester function, or at least one amine function, or at least one amide function, in order to obtain a paste, wherein the mole ratio of said organic compound to the nickel element is between 0.01 and 5.0 mol/mol; the paste obtained is shaped; the shaped paste obtained is dried at a temperature of less than 250 C. in order to obtain a dried catalyst.