Patent EA-001677-B1 (EA)
Title: Middle distillate selective hydrocracking process
Inventor: HABIB MOHAMMAD M
IPC: C10G65/10
Filed: 1998-12-03
Abstract: 1. A hydrocracking process comprising contacting a petroleum feedstock and hydrogen at hydrocracking conditions with a first catalyst layer which contains catalyst particles comprising a Y-type zeolite having a unit cell size of greater than about 24.35 Angstroms and contacting the entire effluent from the first catalyst layer at hydrocracking conditions with a second catalyst layer which contains catalyst particles comprising a Y-type zeolite having a unit cell size of less than about 24.30 Angstroms. 2. The hydrocracking process according to claim 1 further comprising recovering a middle distillate product. 3. The hydrocracking process according to claim 1 wherein the catalyst particles in the first catalyst layer comprise a Y-type zeolite having a unit cell size in the range of from about 24.40 Angstroms to about 24.60 Angstroms. 4. The hydrocracking process according to claim 1 wherein the catalyst particles in the second catalyst layer comprise a Y-type zeolite having a unit cell size in the range of from about 24.20 Angstroms to about 24.30 Angstroms. 5. The hydrocracking process according to claim 1 at hydrocracking conditions, including a reaction temperature in the range of from about 250 to about 500 degree C., pressures up to about 300 bar (30 Mpa) and space velocities from about 0.1 to about 10 kg feed per liter of catalyst per hour (kg/1h). 6. The hydrocracking process according to claim 1 wherein the zeolite-containing catalyst particles in the first catalyst layer comprise from about 0.5% to about 10% by weight of Group VIII metal component(s), from about 5% to about 25% by weight of Group VI metal component(s), from 20-75% by weight of a cracking component, and sufficient binder to make up to 100%. 7. The hydrocracking process according to claim 6 wherein the cracking component comprises from about 15% by weight to about 50% by weight of the Y-type zeolite having a unit cell size of greater than about 24.35 Angstroms. 8. The hydrocracking process according to claim 1 wherein the zeolite-containing catalyst particles in the second catalyst layer comprise from about 0.5% to about 10% by weight of Group VIII metal component(s), from about 5% to about 25% by weight of Group VI metal component(s), from 20-75% by weight of a cracking component, and sufficient binder to make up to 100%. 9. The hydrocracking process according to claim 8 wherein the cracking component comprises from about 15% by weight to about 50% by weight of the Y-type zeolite having a unit cell size of less than about 24.30 Angstroms. 10. The hydrocracking process according to claim 1 wherein the first catalyst layer further comprises amorphous catalyst particles, wherein the volumetric ratio of zeolite-containing catalyst particles to amorphous catalyst particles is between about 90/10 and 10/90. 11. The hydrocracking process according to claim 10 wherein the volumetric ratio of zeolite-containing catalyst particles to amorphous catalyst particles is between about 25/75 and 75/25. 12. The hydrocracking process according to claim 1 wherein the second catalyst layer further comprises amorphous catalyst particles, wherein the volumetric ratio of zeolite-containing catalyst particles to amorphous catalyst particles is between about 90/10 and 10/90. 13. The hydrocracking process according to claim 12 wherein the volumetric ratio of zeolite-containing catalyst particles to amorphous catalyst particles is between about 25/75 and 75/25. 14. A hydrocracking process comprising contacting a petroleum feedstock with hydrogen at hydrocracking reaction conditions, including a first reaction temperature, over a first layer catalyst comprising a Y-type zeolite having a unit cell size of greater than about 24.35 Angstroms, and contacting at least a portion of the effluent from the first layer catalyst with hydrogen at hydrocracking reaction conditions, including a second reaction temperature, over a second layer catalyst comprising a Y-type zeolite having a unit cell size of less than about 24.30 Angstroms, wherein the second reaction temperature is at least about 40 degree F (22,24 degree C) higher than the first reaction temperature. 15. The hydrocracking process according to claim 14 wherein the second reaction temperature is at least about 60 degree F (33,36 degree C) higher than the first reaction temperature. 16. A hydrocracking process comprising contacting a sulfur and nitrogen containing petroleum feedstock with hydrogen at hydrocracking conditions, including a reaction temperature in the range of from about 250 to about 500 degree C, pressures up to about 300 bar (30 Mpa) and space velocities from about 0.1 to about 10 hr<-1>, over a first zeolitic catalyst layer comprising a first zeolite catalyst particles which contain a Y-type zeolite having a unit cell size of greater than about 24.35 Angstroms, and contacting the entire effluent from said first zeolitic catalyst layer with hydrogen at hydrocracking conditions over a second zeolitic catalyst layer comprising a second zeolite catalyst particles which contain a Y-type zeolite having a unit cell size of less than about 24.30 Angstroms. 17. The hydrocracking process according to claim 16 wherein the petroleum feedstock contains greater than 100 ppm nitrogen and greater than 0.15 wt % sulfur. 18. A hydrocracking process comprising contacting a petroleum feedstock and hydrogen at hydrocracking conditions with a layered catalyst system contained within a catalytic reaction zone, the feedstock containing greater than about 100 ppm nitrogen and greater than about 0.15 wt % sulfur, the layered catalyst system comprising a first catalyst layer which contains catalyst particles comprising a Y-type zeolite having a unit cell size of greater than about 24.35 Angstroms and a second catalyst layer which contains catalyst particles comprising a Y-type zeolite having a unit cell size of less than about 24.30 Angstroms. 19. The hydrocracking process according to claim 18 comprising: a) contacting the petroleum feedstock at hydrocracking conditions with the first catalyst layer to produce a first effluent stream; b) contacting the entire first effluent stream at hydrocracking conditions with the second catalyst layer to produce a second effluent stream; and  c) separating at least a portion of the second effluent stream to produce a middle distillate product.