Catalyst and process for the hydrogenitrogenation and hydrocracking of high-nitrogen feeds

Claim 2

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream containing a substantial amount of nitrogen compounds, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal, a crystalline molecular sieve zeolite selected from the group consisting of ZSM crystalline aluminosilicate and AMS crystalline metallosilicate and containing exchangeable cations, and a porous refractory inorganic oxide, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof, said stream being selected from the group consisting of petroleum hydrocarbon distillates, liquids derived from coal, liquids derived from tar sands, and whole shale oil or any fraction of shale oil.

Claim 3

The process of claim 1, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate of hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 4

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream containing a substantial amount of nitrogen compounds, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of a refractory inorganic oxide support material, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof, said stream being selected from the group consisting of petroleum hydrocarbon distillates, liquids derived from coal, liquids derived from tar sands, and whole shale oil or any fraction of shale oil.

Claim 5

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream containing a substantial amount of nitrogen compounds, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of a refractory inorganic oxide support material, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof, said stream being selected from the group consisting of petroleum hydrocarbon distillates, liquids derived from coal, liquids derived from tar sands, and whole shale oil or any fraction of shale oil.

Claim 6

The process of claim 3, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 7

The process of claim 3, wherein said refractory inorganic oxide support material is an alumina, said metal of Group VIII is present in an amount within the range of about 0.5 wt% to about 10 wt%, calculated as the oxide of the metal, said molybdenum is present in an amount within the range of about 5 wt% to about 25 wt%, calculated as MoO 3 , and said chromium is present in an amount within the range of about 3 wt% to about 15 wt%, calculated as Cr 2 O 3 , each amount being based upon the weight of said catalyst, and said molecular sieve zeolite is present in an amount within the range of about 5 wt% to about 90 wt%, based upon the weight of said support.

Claim 8

The process of claim 5, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 9

The process of claim 5, wherein said Group VIII metal of said catalyst is cobalt or nickel and said crystalline molecular sieve zeolite of said catalyst is an AMS-1B crystalline borosilicate.

Claim 10

The process of claim 7, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 11

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream comprising whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal, a crystalline molecular sieve zeolite selected from the group consisting of ZSM crystalline aluminosilicate and AMS crystalline metallosilicate and containing exchangeable cations, and a porous refractory inorganic oxide, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof.

Claim 12

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream comprising whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal, a crystalline molecular sieve zeolite selected from the group consisting of ZSM crystalline aluminosilicate and AMS crystalline metallosilicate and containing exchangeable cations, and a porous refractory inorganic oxide, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof.

Claim 13

The process of claim 9, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 14

The process of claim 9, wherein said crystalline molecular sieve zeolite of said catalyst is an AMS crystalline metallosilicate.

Claim 15

The process of claim 11, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 16

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream comprising whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of a high-surface area refractory inorganic oxide support material, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof.

Claim 17

A process for the hydrodenitrogenation and hydrocracking of a hydrocarbon stream comprising whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of a high-surface area refractory inorganic oxide support material, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof.

Claim 18

The process of claim 13, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 19

A process for the hydrodenitrogenation and hydrocracking of a whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under dehydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of an alumina, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof, said metal of Group VIII being present in an amount within the range of about 0.5 wt% to about 10 wt%, calculated as the oxide of the metal, said molybdenum being present in an amount within the range of about 5 wt% to about 25 wt%, calculated as MoO 3 , and said chromium being present in an amount within the range of about 3 wt% to about 15 wt%, calculated as Cr 2 O 3 , each amount being based upon the weight of said catalyst, and said molecular sieve zeolite being present in an amount within the range of about 5 wt% to about 90 wt%, based upon the weight of said support.

Claim 20

A process for the hydrodenitrogenation and hydrocracking of a whole shale oil or any fraction thereof to produce jet fuel components, which process comprises contacting said stream in a reaction zone under dehydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a ZSM-5 crystalline aluminosilicate and an AMS-1B crystalline borosilicate suspended in and distributed throughout a matrix of an alumina, the metals of said hydrogenation component being present in the elemental form as oxides, as sulfides, or mixtures thereof, said metal of Group VIII being present in an amount within the range of about 0.5 wt% to about 10 wt%, calculated as the oxide of the metal, said molybdenum being present in an amount within the range of about 5 wt% to about 25 wt%, calculated as MoO 3 , and said chromium being present in an amount within the range of about 3 wt% to about 15 wt%, calculated as Cr 2 O 3 , each amount being based upon the weight of said catalyst, and said molecular sieve zeolite being present in an amount within the range of about 5 wt% to about 90 wt%, based upon the weight of said support.

Claim 21

The process of claim 15, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 22

The process of claim 15, wherein said conditions comprise a temperature within the range of about 740° F. (393° C.) to about 790° F. (416° C.), a hydrogen partial pressure within the range of about 1,600 psi (11,024 kPa) to about 2,000 psi (13,780 kPa), an LHSV within the range of about 0.3 volume of hydrocarbon per hour per volume of catalyst to about 2 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 6,000 SCFB (1,079 m 3 /m 3 ) to about 14,000 SCFB (2,517 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 10 moles of hydrogen per mole of hydrocarbon to about 30 moles of hydrogen per mole of hydrocarbon.

Claim 23

The process of claim 15, wherein said metal of Group VIII of said catalyst is cobalt or nickel.

Claim 24

The process of claim 18, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 25

The process of claim 18, wherein said crystalline molecular sieve zeolite of said catalyst is a ZSM-5 crystalline aluminosilicate.

Claim 26

The process of claim 20, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 27

The process of claim 18, wherein said crystalline molecular sieve zeolite of said catalyst is an AMS-1B crystalline borosilicate.

Claim 28

The process of claim 22, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 29

A process for the hydrodenitrogenation and hydrocracking of a petroleum hydrocarbon distillate containing a substantial amount of nitrogen compounds to produce motor fuel components, heater oil components, and a hydrocarbon stream that is a suitable feedstock for a catalytic cracking unit, said distillate comprising heavy vacuum gas oils, light virgin gas oils, heavy coker gas oils, full-range gas oils, or mixtures thereof, which process comprises contacting said distillate in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a HAMS-1B crystalline borosilicate and a HZSM-5 crystalline aluminosilicate suspended in and distributed throughout a matrix of a catalytically active alumina, the metals of said hydrogenation component being present in the elemental form, as oxides, as sulfides, or mixtures thereof, said metal of Group VIII being present in an amount within the range of about 0.5 wt% to about 10 wt%, calculated as the oxide of the metal, said molybdenum being present in an amount within the range of about 5 wt% to about 25 wt%, calculated as MoO 3 , and said chromium being present in an amount within the range of about 3 wt% to about 15wt%, calculated as Cr 2 O 3 , each amount being based upon the weight of said catalyst, and said molecular sieve zeolite being present in an amount within the range of about 5 wt% to about 90 wt%, based upon the weight of said support.

Claim 30

A process for the hydrodenitrogenation and hydrocracking of a petroleum hydrocarbon distillate containing a substantial amount of nitrogen compounds to produce motor fuel components, heater oil components, and a hydrocarbon stream that is a suitable feedstock for a catalytic cracking unit, said distillate comprising heavy vacuum gas oils, light virgin gas oils, heavy coker gas oils, full-range gas oils, or mixtures thereof, which process comprises contacting said distillate in a reaction zone under hydrodenitrogenation and hydrocracking conditions and in the presence of hydrogen with a catalyst comprising a hydrogenation component comprising chromium, molybdenum, and at least one Group VIII metal deposed upon a support comprising a crystalline molecular sieve zeolite selected from the group consisting of a HAMS-1B crystalline borosilicate and a HZSM-5 crystalline aluminosilicate suspended in and distributed throughout a matrix of a catalytically active alumina, the metals of said hydrogenation component being present in the elemental form, as oxides, as sulfides, or mixtures thereof, said metal of Group VIII being present in an amount within the range of about 0.5 wt% to about 10 wt%, calculated as the oxide of the metal, said molybdenum being present in an amount within the range of about 5 wt% to about 25 wt%, calculated as MoO 3 , and said chromium being present in an amount within the range of about 3 wt% to about 15wt%, calculated as Cr 2 O 3 , each amount being based upon the weight of said catalyst, and said molecular sieve zeolite being present in an amount within the range of about 5 wt% to about 90 wt%, based upon the weight of said support.

Claim 31

The process of claim 24, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 32

The process of claim 24, wherein said conditions comprise a temperature within the range of about 740° F. (393° C.) to about 790° F. (416° C.), a hydrogen partial pressure within the range of about 1,600 psi (11,024 kPa) to about 2,000 psi (13,780 kPa), an LHSV within the range of about 0.3 volume of hydrocarbon per hour per volume of catalyst to about 2 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 6,000 SCFB (1,079 m 3 /m 3 ) to about 14,000 SCFB (2,517 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 10 moles of hydrogen per mole of hydrocarbon to about 30 moles of hydrogen per mole of hydrocarbon.

Claim 33

The process of claims 24, wherein said Group VIII metal of said catalyst is nickel.

Claim 34

The process of claim 27, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), and LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 35

The process of claims 24, wherein said Group VIII metal of said catalyst is cobalt.

Claim 36

The process of claim 29, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate of hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 37

The process of claim 24, wherein said crystalline molecular sieve zeolite is a HAMS-1B crystalline borosilicate.

Claim 38

The process of claim 31, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.

Claim 39

The process of claim 31, wherein said distillate is a heavy vacuum gas oil.

Claim 40

The process of claim 33, wherein said conditions comprise a temperature within the range of about 740° F. (393° C.) to about 790° F. (416° C.), a hydrogen partial pressure within the range of about 1,600 psi (11,024 kPa) to about 2,000 psi (13,780 kPa), an LHSV within the range of about 0.3 volume of hydrocarbon per hour per volume of catalyst to about 2 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 6,000 SCFB (1,079 m 3 /m 3 ) to about 14,000 SCFB (2,517 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 10 moles of hydrogen per mole of hydrocarbon to about 30 moles of hydrogen per mole of hydrocarbon.

Claim 41

The process of claim 24, wherein said crystalline molecular sieve zeolite is an HZSM-5 crystalline aluminosilicate.

Claim 42

The process of claim 35, wherein said distillate is a heavy vacuum gas oil.

Claim 43

The process of claim 36, wherein said conditions comprise a temperature within the range of about 700° F. (371° C.) to about 800° F. (427° C.), a pressure within the range of about 1,000 psi (6,890 kPa) to about 2,500 psi (17,225 kPa), an LHSV within the range of about 0.1 volume of hydrocarbon per hour per volume of catalyst to about 5 volumes of hydrocarbon per hour per volume of catalyst, a hydrogen addition rate or hydrogen recycle rate within the range of about 2,000 SCFB (359 m 3 /m 3 ) to about 20,000 SCFB (3,596 m 3 /m 3 ), and a hydrogen-to-hydrocarbon molar ratio within the range of about 3 moles of hydrogen per mole of hydrocarbon to about 60 moles of hydrogen per mole of hydrocarbon.