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This invention relates to a process involving hydrocracking of a feedstream in which a converted fraction can exhibit relatively high distillate product yields and maintained or improved distillate fuel properties, while an unconverted fraction can exhibit improved properties particularly useful in

This invention relates to a process involving hydrocracking of a feedstream in which a converted fraction can exhibit relatively high distillate product yields and maintained or improved distillate fuel properties, while an unconverted fraction can exhibit improved properties particularly useful in the lubricant area. In this hydrocracking process, it can be advantageous for the yield of converted/unconverted product for gasoline fuel application to be reduced or minimized, relative to converted distillate fuel and unconverted lubricant. Catalysts and conditions can be chosen to assist in attaining, or to optimize, desirable product yields and/or properties.

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1. A hydrocracking process on a vacuum gasoil feedstream being selective for distillate boiling range converted products and yielding unconverted products useful as lubricants, which process comprises: providing a vacuum gasoil feedstream having a nitrogen content of not greater than about 50 wppm a

1. A hydrocracking process on a vacuum gasoil feedstream being selective for distillate boiling range converted products and yielding unconverted products useful as lubricants, which process comprises: providing a vacuum gasoil feedstream having a nitrogen content of not greater than about 50 wppm and a sulfur content of not greater than about 300 wppm;hydrocracking the vacuum gasoil feedstream in a high-conversion hydrocracking stage with a hydrogen-containing treat gas stream in the presence of a two-stage catalyst system under effective hydrocracking conditions sufficient to attain a conversion level of greater than 55% relative to a conversion temperature of 700° F. (371° C.), so as to form a hydrocracked product; andseparating the hydrocracked product into a converted product and an unconverted product having a higher boiling range than the converted product, the converted product having a yield of material boiling in the range between 350° F. (177° C.) and 700° F. (371° C.) of at least 35 wt %, based on a total weight of the converted product, the converted product having one or more of a cetane number of at least 45, a smoke point of at least 20 mm, and a sulfur content of not greater than 12 wppm, the unconverted product having a viscosity index of at least 105, a pour point of 5° C. or less, and a kinematic viscosity at about 100° C. of at least 1 cSt,wherein the two-stage catalyst system comprises (i) a USY catalyst containing a Group VIII noble metal selected from platinum, palladium, and combinations thereof, the USY catalyst having a unit cell size of less than 24.25 Å and a Si/Al ratio of at least 25, and (ii) a ZSM-48 catalyst containing a Group VIII noble metal selected from platinum, palladium, and combinations thereof. 2. The process of claim 1, wherein the hydrocracking conditions in the high-conversion hydrocracking stage are sufficient to attain a conversion level from about 60% to about 95%. 3. The process of claim 1, wherein the converted product from the high-conversion hydrocracking stage exhibits a cetane number of at least 51 and a sulfur content of not greater than 10 wppm. 4. The process of claim 1, wherein the unconverted product exhibits a viscosity index of 140 or less. 5. The process of claim 1, wherein the unconverted product exhibits a pour point of less than −10° C. and a kinematic viscosity at about 100° C. of at least 2 cSt. 6. The process of claim 1, wherein the two-stage catalyst system of the high-conversion hydrocracking stage consists essentially of a mixture of a USY catalyst loaded with from about 0.1 wt % to about 3.0 wt % platinum, based on the weight of the USY catalyst, and a ZSM-48 catalyst loaded with from about 0.1 wt % to about 3.0 wt % platinum, based on the weight of the ZSM-48 catalyst. 7. The process of claim 1, wherein the vacuum gasoil feedstream has a nitrogen content of not greater than about 20 wppm and a sulfur content of not greater than about 150 wppm. 8. The process of claim 1, wherein the effective hydrocracking conditions of the high-conversion hydrocracking stage comprise a weight average bed temperature from about 550° F. (about 288° C.) to about 800° F. (about 427° C.), a total pressure from about 700 psig (about 4.8 MPag) to about 2000 psig (about 13.8 MPag), an LHSV from about 0.1 hr−1 to about 20 hr−1, and a hydrogen treat gas rate from about 500 scf/bbl (about 85 Nm3/m3) to about 10000 scf/bbl (about 1700 Nm3/m3). 9. The process of claim 2, wherein the converted product exhibits sulfur content of not greater than 8 wppm. 10. The process of claim 9, wherein the unconverted product exhibits a viscosity index of 140 or less. 11. The process of claim 10, wherein the unconverted product exhibits a pour point of less than −10° C. and a kinematic viscosity at about 100° C. of at least 5 cSt. 12. The process of claim 11, wherein the two-stage catalyst system of the high-conversion hydrocracking stage consists essentially of a mixture of a USY catalyst loaded with from about 0.3 wt % to about 1.5 wt % platinum, based on the weight of the USY catalyst, and a ZSM-48 catalyst loaded with from about 0.3 wt % to about 1.5 wt % platinum, based on the weight of the ZSM-48 catalyst. 13. The process of claim 2, wherein the converted product has a yield of material boiling in the range between 350° F. (177° C.) and 700° F. (371° C.) of at least 45 wt %, based on the total weight of the converted product. 14. The process of claim 13, wherein the converted product exhibits sulfur content of not greater than 10 wppm. 15. The process of claim 14, wherein the unconverted product exhibits a viscosity index of 140 or less. 16. The process of claim 15, wherein the unconverted product exhibits a pour point of less than −10° C. and a kinematic viscosity at about 100° C. of at least 5 cSt. 17. The process of claim 16, wherein the two-stage catalyst system of the high-conversion hydrocracking stage consists essentially of a mixture of a USY catalyst loaded with from about 0.3 wt % to about 1.5 wt % platinum, based on the weight of the USY catalyst, and a ZSM-48 catalyst loaded with from about 0.3 wt % to about 1.5 wt % platinum, based on the weight of the ZSM-48 catalyst.