Hydrocracking catalyst
View Patent ↗Process of preparing a hydrocracking catalyst carrier comprising amorphous binder and zeolite Y, which process comprises subjecting zeolite Y having a silica to alumina molar ratio of at least 10 to calcination at a temperature of from 700 to 1000° 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 micro-mole/gram, hydrocracking catalyst derived from such carrier and hydrocracking process with the help of such catalyst.
1. A process of preparing a hydrocracking catalyst carrier for use in the preparation of a hydrocracking catalyst having enhanced gas oil selectivity, wherein said hydrocracking catalyst carrier comprises an amorphous binder and zeolite Y, wherein said process comprises: calcining zeolite Y, having a silica to alumina molar ratio of at least 10, in the absence of added steam at a temperature in the range of from 700° C. to 1000° C. followed by mixing the obtained zeolite Y with said amorphous binder, comprising silica-alumina containing silica in an amount in the range of from 25 to 95% by weight as calculated on the carrier alone, and an acidic aqueous solution in amount so as to provide a mixture having a pH in the range of from 4.4 to 5.7 and an LOI in the range of from 50 to 65% such that said hydrocracking catalyst carrier has a monomodal pore size distribution, wherein at least 50% of the total pore volume is present in pores having a diameter in the range of from 4 to 50 nm; extruding said mixture to give an extrudate; and calcining said extrudate at a temperature of from 700 to 1000° C.
2. A process according to claim 1 , in which process zeolite beta is also included in the mixing step and the mixture.
3. A process according to claim 2 , in which process the hydrocracking catalyst carrier comprises of from 2 to 70% wt of zeolite and of from 98 to 30% wt of amorphous binder.
4. A process according to claim 3 , in which process the calcining step is carried out during a time of from 20 minutes to 5 hours.
5. A process according to claim 4 , wherein the pore volume present in said pores of said hydrocracking catalyst carrier is at least 0.4 ml/g, all as measured by mercury intrusion porosimetry.
6. A process according to claim 5 , in which before calcination the zeolite Y has a bulk silica to alumina molar ratio above 12, a unit cell size in the range of from 24.10 to 24.40 Angstrom, and a surface area of at least 850 m 2 /g.
7. A process according to claim 1 , which process the hydrocracking catalyst carrier comprises of from 2 to 70% wt of zeolite and of from 90 to 30% wt of amorphous binder.
8. A process according to claim 7 , in which process the calcination is carried out during a time of from 20 minutes to 5 hours.
9. A process according to claim 8 , in which process the hydrocracking catalyst carrier has a monomodal pore size distribution, wherein at least 50% of the total pore volume is present in pores having a diameter in the range of from 4 to 50 nm, and wherein the pore volume present in said pores is at least 0.04 ml/g, all as measured by mercury intrusion porosimetry.
10. A process according to claim 9 , in which process the hydrocracking catalyst carrier is prepared by shaping the mixture with added zeolite beta, wherein the mixture has a loss of ignition (LOT) in the range of from 55 to 65%.
11. A process according to claim 10 , in which process, before the calcination the zeolite Y has a bulk silica to alumina molar ratio above 12, a unit cell size in the range of 24.10 to 24.40 Angstrom, and a surface area of at least 850 m 2 /g.