Hydrocracking catalyst
Process for preparing a hydrocracking catalyst carrier which process comprises subjecting a carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10 to calcination at a temperature of from 700 to 900° C., hydrocracking catalyst carrier comprising amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, the infrared spectrum of which catalyst has a peak at 3690 cm −1 , substantially reduced peaks at 3630 cm −1 and 3565 cm −1 and no peak at 3600 cm −1 , hydrocracking catalyst carrier comprising an amorphous binder and zeolite Y having a silica to alumina molar ratio of at least 10, which catalyst has an acidity as measured by exchange with perdeuterated benzene of at most 20 micromole/gram, hydrocracking catalyst derived from such carrier and hydrocracking process with the help of such catalyst.
1. A hydrocracking process for converting a hydrocarbon feedstock into lower boiling materials, wherein said process comprises:
contacting said hydrocarbon feedstock and hydrogen at an elevated temperature in the range of from 250 to 500° C. and an elevated pressure in the range of from 3×10 6 to 3×10 7 Pa with a hydrocracking catalyst within a hydrocracking reaction vessel having a reactor inlet and a reactor outlet, wherein said hydrocracking catalyst comprises, a Group VIII metal; a Group VIB metal; and a carrier, wherein said carrier comprises an amorphous binder in an amount in the range of from 30% wt to 98% wt based on the total weight of said carrier, a zeolite Y, having a silica-to-alumina molar ratio of at least 10, in an amount in the range of from 2% to 70% wt based on the total weight of said carrier, and a second zeolite component that is either zeolite beta or ZSM-5 in an amount up to 20% wt based on the total weight of said carrier, and wherein the infrared spectrum of said carrier has peaks at 3690 cm −1 , 3630 cm −1 , and 3565 cm −1 , and no peak at 3600 cm −1 .
2. A process as recited in claim 1 , wherein said hydrocracking catalyst contains from 2 to 40 parts by weight of the Group VIB metal and from 0.05 to 10 parts by weight of the Group VIII metal, calculated as metal per 100 parts by weight of the hydrocracking catalyst.
3. A process as recited in claim 1 , wherein said amorphous binder is selected from the group consisting of alumina, silica, silica-alumina and mixtures thereof.
4. A process as recited in claim 1 , wherein said amorphous binder is silica-alumina containing silica in an amount in the range of from 25% to 95% by weight as calculated on the total carrier.
5. A process as recited in claim 1 , wherein said Group VIII metal is either nickel or cobalt, and said Group VIB metal is either molybdenum or tungsten.
6. A process as recited in claim 1 , wherein said hydrocracking catalyst contains from 2 to 40 parts by weight of the Group VIB metal and from 0.05 to 10 parts by weight of the Group VIII metal, calculated as metal per 100 parts by weight of the hydrocracking catalyst.
7. A process as recited in claim 1 , wherein said second zeolite component is zeolite beta present in said carrier in an amount in the range of from 0.5 to 10% wt, based on the total carrier.
8. A process as recited in claim 1 , wherein said hydrocarbon feedstock comprises hydrocarbons having a boiling point of at least 330° C.
9. A process as recited in claim 1 , wherein the hydrocarbon feedstock and hydrogen at the reactor inlet are such that there is a hydrogen partial pressure at said reactor inlet is in the range of from 3×10 6 to 2.9×10 7 Pa.
10. A process as recited in claim 1 , wherein said hydrocarbon feedstock and hydrogen are such that there is a space velocity is in the range of from 0.1 to 10 kg of said hydrocarbon feedstock per liter of said hydrocracking catalyst per hour.