초록 ▼

The invention concerns a catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight

The invention concerns a catalyst comprising a calcined oxide matrix which is mainly alumina and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix which is mainly alumina, the nickel content being in the range 5% to 65% by weight of said element with respect to the total mass of catalyst, said active phase not comprising metal from group VIB, the nickel particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 8 nm to 25 nm, a median macropore diameter of more than 300 nm, a mesopore volume, measured by mercury porosimetry, of 0.30 mL/g or more and a total pore volume, measured by mercury porosimetry, of 0.34 mL/g or more. The invention also concerns the process for the preparation of said catalyst, and its use in a hydrogenation process.

대표청구항 ▼

1. A catalyst comprising a calcined oxide matrix having alumina content of at least 90% by weight with respect to the total weight of the matrix and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix a nickel content of 5% to 65%

1. A catalyst comprising a calcined oxide matrix having alumina content of at least 90% by weight with respect to the total weight of the matrix and an active phase comprising nickel, said active phase being at least partially co-mixed within said calcined oxide matrix a nickel content of 5% to 65% by weight with respect to the total mass of catalyst, said active phase not comprising metal from group VIB, the nickel in the form of particles having a diameter of less than 15 nm, said catalyst having a median mesopore diameter in the range 8 nm to 25 nm, a median macropore diameter of 390 to 800 nm, a mesopore volume, measured by mercury porosimetry, of 0.30 mL/g or more, a total pore volume, measured by mercury porosimetry, of 0.34 mL/g or more, and a macropore volume of 20% to 35% of the total pore volume, and wherein the active phase is entirely co-mixed with the calcined oxide matrix. 2. The catalyst as claimed in claim 1, in which the nickel content is in the range 10% to 34% by weight of said element with respect to the total mass of catalyst. 3. The catalyst as claimed in claim 1, having no micropores. 4. The catalyst as claimed in claim 1, in which the nickel particles have a diameter in the range 1.5 to 12 nm. 5. The catalyst as claimed in claim 1, in which a portion of the active phase is impregnated onto the calcined oxide matrix. 6. A process for the preparation of a catalyst as claimed in claim 1, comprising: a) dissolving an acidic aluminium precursor that is aluminium sulphate, aluminium chloride or aluminium nitrate in water, at a temperature of 20° C. to 90° C., at a pH of 0.5 to 5, for a period of 2 to 60 minutes,b) adjusting the pH by adding at least one basic precursor that is sodium aluminate, potassium aluminate, ammonia, sodium hydroxide or potassium hydroxide to the suspension obtained in a), at a temperature of 20° C. to 90° C., and a pH of 7 to 10, for a period of 5 to 30 minutes,c) co-precipitation of the suspension obtained from b) by adding to the suspension at least one basic precursor that is sodium aluminate, potassium aluminate, ammonia, sodium hydroxide or potassium hydroxide and at least one acidic precursor that is aluminium sulphate, aluminium chloride, aluminium nitrate, sulphuric acid, hydrochloric acid or nitric acid, at least one of the basic or acidic precursors comprising aluminium, the relative flow rate of the acidic and basic precursors being selected in a manner so as to obtain a pH of the reaction medium of 7 to 10 and the flow rate of the acidic and basic precursors containing aluminium being adjusted in a manner so as to obtain a final concentration of alumina in the suspension of 10 to 38 g/L,d) filtration of the suspension obtained from the co-precipitation c) in order to obtain an alumina gel,e) drying said alumina gel obtained in d) in order to obtain a powder,f) heat treatment of the powder obtained from e) at a temperature of 500° C. to 1000° C., in the optional presence of a stream of air containing up to 60% by volume of water, for a period of 2 to 10 hours, in order to obtain a calcined porous aluminium oxide,g) mixing the calcined porous aluminium oxide obtained from f) with a solution comprising at least one nickel precursor in order to obtain a paste,h) shaping the paste obtained,i) drying the shaped paste at a temperature of 15° C. to less than 250° C., in order to obtain a dried catalyst,j) optionally, a heat treatment of the dried catalyst at a temperature of 250° C. to 1000° C. in the optional presence of water. 7. The process as claimed in claim 6, in which at least one reduction treatment k) is carried out in the presence of a reducing gas after i) or j) in order to obtain a catalyst comprising nickel which is at least partially in the metallic form. 8. The process as claimed in claim 7, in which a passivation 1) using a sulphur-containing or oxygen-containing compound or CO2 is carried out before or after the reduction treatment k). 9. The process as claimed in claim 6, in which the concentration of alumina in the suspension of alumina gel obtained in c) is 13 to 35 g/L. 10. The process as claimed in claim 6, in which the acidic precursor of a) and c) is aluminium sulphate, aluminium chloride or aluminium nitrate, and in which the basic precursor of a) and c) is sodium aluminate or potassium aluminate. 11. A hydrogenation process, in which the catalyst as claimed in claim 1 is brought into contact, in the presence of hydrogen, with a feed of hydrocarbons containing polyunsaturated molecules and/or aromatic molecules in a manner such as to obtain an at least partially hydrogenated effluent. 12. The hydrogenation process as claimed in claim 11, in which a selective hydrogenation is carried out at a temperature of 0° C. to 500° C., at a pressure of 0.1 to 20 MPa, at a molar ratio of hydrogen/(polyunsaturated compounds to be hydrogenated) of 0.1 to 10 and at an hourly space velocity of 0.1 to 200 h−1 for a liquid feed, of 100 to 15000 h−1 for a gaseous feed, of a hydrocarbon feed containing polyunsaturated compounds containing at least 2 carbon atoms per molecule and having a final boiling point of 250° C. or less. 13. The hydrogenation process as claimed in claim 11, in which a hydrogenation of aromatics is carried out at a temperature of 30° C. to 350° C., at a pressure of 0.1 to 20 MPa, at a molar ratio of hydrogen/(aromatic compounds to be hydrogenated) of 0.1 to 10 and at an hourly space velocity of 0.05 to 50 h−1 of a feed of hydrocarbons containing aromatic compounds and having a final boiling point of 650° C. or less.