초록

The present invention is directed to a hydroprocessing catalyst containing at least one catalyst support, one or more metals, optionally one or more molecular sieves, optionally one or more promoters, wherein deposition of at least one of the metals is achieved in the presence of a modifying agent.

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1. A method for hydroprocessing a carbonaceous feedstock, comprising contacting the carbonaceous feedstock with a sulfided hydroprocessing catalyst and hydrogen under hydroprocessing conditions, the hydroprocessing catalyst comprising at least one molecular sieve which is a Y zeolite with a unit cel

1. A method for hydroprocessing a carbonaceous feedstock, comprising contacting the carbonaceous feedstock with a sulfided hydroprocessing catalyst and hydrogen under hydroprocessing conditions, the hydroprocessing catalyst comprising at least one molecular sieve which is a Y zeolite with a unit cell size of between 24.15 Å and 24.45 Å, and at least one metal deposited on an amorphous silica-alumina catalyst support containing SiO2 in an amount of 10 wt. % to 70 wt. % of the dry bulk weight of the carrier as determined by ICP elemental analysis, a BET surface area of between 450 m2/g and 550 m2/g, a total pore volume of between 0.75 mL/g and 1.05 mL/g, and a mean mesopore diameter of between 70 Å and 130 Å, wherein deposition of the metal is achieved in the presence of a modifying agent and with the catalyst support after the deposition subjected to drying for a period of time ranging from 1 to 5 hours and at a temperature sufficient to remove impregnation solution solvent but below the decomposition temperature of the modifying agent, wherein the modifying agent is selected from the group consisting of N,N′-bis(2-aminoethyl)-1,2-ethane-diamine, 2-amino-3-(1H-indol-3-yl)-propanoic acid, benzaldehyde, [[(carboxymethyl)imino]bis(ethylenenitrilo)]-tetra-acetic acid, 1,2-cyclohexanediamine, 2-hydroxybenzoic acid, thiocyanate, thiosulfate, thiourea, pyridine, quinolone, and compounds represented by structures (1) through (4), and condensated forms thereof: wherein:(1) R1, R2 and R3 are independently selected from the group consisting of hydrogen; hydroxyl; methyl; amine; and linear or branched, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 alkenyl groups, C1-C3 hydroxyalkyl groups, C1-C3 alkoxyalkyl groups, C1-C3 amino alkyl groups, C1-C3 oxoalkyl groups, C1-C3 carboxyalkyl groups, C1-C3 aminocarboxyalkyl groups and C1-C3 hydroxycarboxyalkyl groups;(2) R4 through R10 are independently selected from the group consisting of hydrogen; hydroxyl; and linear or branched, substituted or unsubstituted C2-C3 carboxyalkyl groups; and(3) R11 is selected from the group consisting of linear or branched, saturated and unsaturated, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 hydroxyalkyl groups, and C1-C3 oxoalkyl groups. 2. The method of claim 1, wherein the at least one molecular sieve is a Y zeolite having a silica-to-alumina ratio of greater than 10, a micropore volume of from 0.15 mL/g to 0.27 mL/g, a BET surface area of from 700 m2/g to 825 m2/g, and a unit cell size of from 24.15 Å to 24.45 Å. 3. The method of claim 1, wherein the sulfided hydroprocessing catalyst further comprises a Y zeolite having a silica-to-alumina ratio of greater than 10, a micropore volume of from 0.15 mL/g to 0.27 mL/g, a BET surface area of from 700 m2/g to 825 m2/g, and a unit cell size of from 24.15 Å to 24.35 Å, and a low-acidity, highly dealuminated ultrastable Y zeolite having an Alpha value of less than about 5 and Bronsted acidity of from 1 to 40 micro-mole/g. 4. The method of claim 1, wherein the modifying agent is selected from the group consisting of compounds represented by structures (1) through (4), and condensated forms thereof: wherein:(1) R1, R2 and R3 are independently selected from the group consisting of hydrogen; hydroxyl; methyl; amine; and linear or branched, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 alkenyl groups, C1-C3 hydroxyalkyl groups, C1-C3 alkoxyalkyl groups, C1-C3 amino alkyl groups, C1-C3 oxoalkyl groups, C1-C3 carboxyalkyl groups, C1-C3 aminocarboxyalkyl groups and C1-C3 hydroxycarboxyalkyl groups;(2) R4 through R10 are independently selected from the group consisting of hydrogen; hydroxyl; and linear or branched, substituted or unsubstituted C2-C3 carboxyalkyl groups; and(3) R11 is selected from the group consisting of linear or branched, saturated and unsaturated, substituted or unsubstituted C1-C3 alkyl groups, C1-C3 hydroxyalkyl groups, and C1-C3 oxoalkyl groups. 5. The method of claim 1, wherein the modifying agent is selected from the group consisting of N,N′-bis(2-aminoethyl)-1,2-ethane-diamine, 2-amino-3-(1H-indol-3-yl)-propanoic acid, benzaldehyde, [[(carboxymethyl)imino]bis(ethylenenitrilo)]-tetra-acetic acid, 1,2-cyclohexanediamine, 2-hydroxybenzoic acid, thiocyanate, thiosulfate, thiourea, pyridine, and quinolone. 6. The method of claim 1, wherein the modifying agent comprises 2 hydroxyalkyl 1,2,3-propanetricarboxylic. 7. The method of claim 1, wherein the at least one metal is selected from the group consisting of elements from Group 6 and Groups 8 through 10 of the Periodic Table. 8. The method of claim 7, wherein the at least one metal is selected from the group consisting of nickel (Ni), palladium (Pd), platinum (Pt), cobalt (Co), iron (Fe), chromium (Cr), molybdenum (Mo), tungsten (W), and mixtures thereof. 9. The method of claim 7, wherein the at least one metal is at least one metal selected from Group 6 of the Periodic Table and at least one metal selected from Groups 8 through 10 of the periodic table. 10. The method of claim 1, wherein the hydroprocessing conditions comprise a temperature in the range of 175-485° C., hydrogen pressures in the range of 5 to 300 bar, and LHSV in the range of 0.1-30 h−1. 11. The method of claim 10, wherein the carbonaceous feedstock is generated from a gas-to-liquid process. 12. The method of claim 1, wherein the hydroprocessing conditions comprise a reaction temperature between 204-482° C., a pressure between 3.5-34.6 Mpa, a feed rate (LHSV) of 0.5 hr−1 to 20 hr−1 (v/v), and an overall hydrogen consumption of 53.4 to 356 m3 H2 per m3 of liquid hydrocarbon feed.