Provided is a conversion process for an organic oil, relating to the field of biomass utilization, energy and chemical industry. The conversion process is carried out in presence of an aqueous slurry and a catalyst selected from the group consisting of an iron oxide compound, a waste agent resulting from use of an iron oxide compound as desulfurizer, and a regeneration product of the waste agent, under a controlled molar ratio of iron element to sulfur element. It is found that free radical condensation polymerization of organic oil during cracking process can be blocked effectively by using carbonylation, and hydrogenation is achieved with active hydrogen produced from the conversion of CO and water. In the conversion process, organic material, especially biomass solid, can be directly converted without dehydration, and water can be additionally added to the biomass liquid or the mineral oil.

A process plant and a process for production of a hydrocarbon suitable for use as jet fuel from a feedstock being a renewable feedstock or an oxygenate feedstock, including combining the feedstock with an amount of a liquid diluent, directing it to contact a material catalytically active in hydrodeoxygenation under hydrotreating conditions to provide a hydrodeoxygenated intermediate product, separating the hydrodeoxygenated intermediate product in at least two fractions; a vapor fraction and a liquid fraction, directing at least an amount of the liquid fraction to contact a material catalytically active in isomerization under isomerization conditions to provide an isomerized intermediate product, directing at least an amount of the isomerized intermediate product and a stream comprising sulfur to provide a hydrocracked intermediate product, and fractionating the hydrocracked intermediate product to provide at least a hydrocarbon suitable for use as jet fuel.

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.sup.−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.

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.sup.−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.

Method for preparing a catalyst comprising a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, comprising the following steps: a step of bringing the support into contact with a solution containing a nickel precursor is carried out; a step of bringing the support into contact with a solution containing a copper precursor is carried out; a step of drying the catalyst precursor at a temperature lower than 250° C. is carried out; the catalyst precursor obtained is supplied to a hydrogenation reactor, and a step of reduction by bringing said precursor into contact with a reducing gas at a temperature lower than 200° C. for a period greater than or equal to 5 minutes and less than 2 hours is carried out.

Method for preparing a catalyst comprising a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, comprising the following steps: a step of bringing the support into contact with a solution containing a nickel precursor is carried out; a step of bringing the support into contact with a solution containing a copper precursor is carried out; a step of drying the catalyst precursor at a temperature lower than 250° C. is carried out; the catalyst precursor obtained is supplied to a hydrogenation reactor, and a step of reduction by bringing said precursor into contact with a reducing gas at a temperature lower than 200° C. for a period greater than or equal to 5 minutes and less than 2 hours is carried out.

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.

The invention is a process for dearomatization and isomerization of a feedstock having less than or equal to 10 ppm by weight of sulphur, the process comprising: Hydrodearomatizing the feedstock at a temperature ranging from 150 to 220° C. and at a pressure ranging from 20 to 150 bars, in order to provide a dearomatized product; Hydroisomerizing the dearomatized product at a temperature ranging from 250 to 320° C. and at a pressure ranging from 40 to 60 bars in the presence of a catalyst based on platinum or palladium, in order to provide an isomerized product; Hydrodearomatizing the isomerized product at a temperature ranging from 150 to 220° C. and at a pressure ranging from 20 to 150 bars, in order to provide an isomerized and dearomatized product.

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.sup.−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.

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.sup.−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.