Hydrocracking with rare earth-containing Y zeolite compositions

Claim 2

A process for hydrocracking a hydrocarbon feedstock to produce a product of lower average boiling point which process comprises contacting said hydrocarbon feedstock with molecular hydrogen under ammonia-deficient hydrocracking conditions in the presence of a catalyst comprising an intimate mixture of a porous refractory oxide component and a type Y crystalline aluminosilicate zeolite containing a rare earth metal and a Group VIII hydrogenation metal, said zeolite having been prepared by a process comprising: (a) cation-exchanging a type Y crystalline aluminosilicate zeolite with rare-earth containing cations; (b) calcining the resultant rare earth-exchanged zeolite in the presence of water vapor at a water vapor partial pressure of a least about 0.2 p.s.i.a.; (c) ion-exchanging the calcine zeolite from step (b) with ammonium ions; and (d) ion-exchanging the ammonium-exchanged zeolite from step (c) with Group VIII metal-containing cations.

Claim 3

A process as defined by claim 1 wherein said Group VIII metal-containing cations comprise noble metal-containing cations.

Claim 4

A process as defined by claim 2 wherein said noble metal-containing cations comprise palladium-containing cations.

Claim 5

A process as defined by claim 1 wherein the ammonium-exchanged zeolite from step (c) is calcined prior to ion-exchanging said ammonium-exchanged zeolite with said Group VIII metal-containing cations.

Claim 6

A process as defined by claim 1 wherein said hydrocracking process is carried out in an essentially ammonia-free environment.

Claim 7

A process as defined by claim 5 wherein said environment is essentially completely ammonia-free.

Claim 8

A process as defined by claim 1 wherein said zeolite in step (a) comprises a sodium Y zeolite.

Claim 9

A process for refining a hydrocarbon feedstock containing organonitrogen and/or organosulfur components comprising: (a) contacting said feedstock with molecular hydrogen under hydrotreating conditions in the presence of a hydrotreating catalyst comprising a Group VIB metal component and a Group VIII metal component such that a substantial proportion of the organonitrogen and/or organosulfur components are converted to ammonia and/or hydrogen sulfide; (b) contacting substantially all of the effluent from step (a) with molecular hydrogen in a first hydrocracking zone in the presence of a hydrocracking catalyst comprising a zeolite and a hydrogenation component to produce a hydrocracking product of substantially lower boiling point; (c) separating said hydrocracking product into a higher boiling fraction and a lower boiling fraction; (d) contacting said higher boiling fraction with molecular hydrogen in a second hydrocracking zone under ammonia-deficient hydrocracking conditions in the presence of a hydrocracking catalyst to convert said higher boiling fraction into lower boiling products, said hydrocracking catalyst having been prepared by a process comprising: (1) cation-exchanging a sodium Y zeolite with rare earth-containing cations such that the resulting zeolite contains at least about 2 percent by weight of rare earth metals, calculated as RE 2 O 3 , but still retains at least some sodium; (2) calcining the resultant rare earth-sodium Y zeolite in the presence of water at a water vapor partial pressure of at least about 0.2 p.s.i.a. so as to effect at least some reduction in the unit cell size of said zeolite, with the resultant unit cell size being between about 24.40 Angstroms and about 24.64 Angstroms; (3) ion-exchanging the calcined zeolite from step (2) with ammonium ions so as to further reduce the sodium content thereof; (4) ion-exchanging the ammonium-exchanged zeolite from step (3) with noble metal-containing cations; and (5) mixing the zeolite from step (4) with a porous, inorganic refractory oxide component and calcining the resultant mixture.

Claim 10

A process for refining a hydrocarbon feedstock containing organonitrogen and/or organosulfur components comprising: (a) contacting said feedstock with molecular hydrogen under hydrotreating conditions in the presence of a hydrotreating catalyst comprising a Group VIB metal component and a Group VIII metal component such that a substantial proportion of the organonitrogen and/or organosulfur components are converted to ammonia and/or hydrogen sulfide; (b) contacting substantially all of the effluent from step (a) with molecular hydrogen in a first hydrocracking zone in the presence of a hydrocracking catalyst comprising a zeolite and a hydrogenation component to produce a hydrocracking product of substantially lower boiling point; (c) separating said hydrocracking product into a higher boiling fraction and a lower boiling fraction; (d) contacting said higher boiling fraction with molecular hydrogen in a second hydrocracking zone under ammonia-deficient hydrocracking conditions in the presence of a hydrocracking catalyst to convert said higher boiling fraction into lower boiling products, said hydrocracking catalyst having been prepared by a process comprising: (1) cation-exchanging a sodium Y zeolite with rare earth-containing cations such that the resulting zeolite contains at least about 2 percent by weight of rare earth metals, calculated as RE 2 O 3 , but still retains at least some sodium; (2) calcining the resultant rare earth-sodium Y zeolite in the presence of water at a water vapor partial pressure of at least about 0.2 p.s.i.a. so as to effect at least some reduction in the unit cell size of said zeolite, with the resultant unit cell size being between about 24.40 Angstroms and about 24.64 Angstroms; (3) ion-exchanging the calcined zeolite from step (2) with ammonium ions so as to further reduce the sodium content thereof; (4) ion-exchanging the ammonium-exchanged zeolite from step (3) with noble metal-containing cations; and (5) mixing the zeolite from step (4) with a porous, inorganic refractory oxide component and calcining the resultant mixture.

Claim 11

A process as defined by claim 8 wherein said noble metal-containing cations comprise platinum or palladium-containing cations.

Claim 12

A process as defined by claim 8 wherein the catalyst in said first hydrocracking zone is the same as the catalyst in said second hydrocracking zone and wherein said catalyst in said second hydrocracking xone is periodically regenerated by the combustion of coke.

Claim 13

A process as defined by claim 1 or 8 wherein said rare earth cation exchange introduces a mixture of rare earth cations into said zeolite, said mixture containing cerium, lanthanum, praseodymium and neodymium cations.

Claim 14

A process as defined by claim 1 wherein said calcination in step (b) is carried out so as to effect at least some reduction in the unit cell size of said zeolite with the resultant unit cell size being between about 24.20 Angstroms and about 24.64 Angstroms.

Claim 15

A process as defined by claim 1 or 8 wherein after said ammonium ion exchange said zeolite is exchanged with noble metal-containing cations, with the resulting zeolite containing at least about 2.0 percent by weight rare earth metals, calculated as RE 2 O 3 , less than about 0.5 weight percent sodium, calculated as Na 2 O, and at least about 0.1 percent by weight of total noble metals, calculated as the metals.

Claim 16

A process as defined by claim 1 wherein said catalyst has been regenerated by the combustion of coke.

Claim 17

A process as defined by claim 1 or 8 wherein said calcination in the presence of water vapor is carried out at a temperature between about 1100° F. and about 1350° F. and at a water vapor partial pressure above about 12 p.s.i.a.

Claim 18

A process as defined by claim 1 or 8 wherein said calcination in the presence of water vapor is carried out at a water partial pressure between about 2 and about 15 p.s.i.a.

Claim 19

A process as defined by claim 1 or 8 wherein said calcination in the presence of water vapor is carried out in the presence of an atmosphere consisting essentially of steam.

Claim 20

A process as defined by claim 7 or 8 wherein said zeolite after said ammonium ion exchange contains less than about 0.5 percent by weight sodium, calculated as Na 2 O.

Claim 21

A process as defined by claim 18 wherein said zeolite after said ammonium ion exchange contains less than about 0.05 percent by weight sodium, calculated as Na 2 O.

Claim 22

A process as defined by claim 7 or 8 wherein said calcination in the presence of water vapor is carried out at a water vapor partial pressure above about 1.0 p.s.i.a.