Process for upgrading heavy hydrocarbonaceous oils

Claim 2

A process for the upgrading of viscous hydrocarbonaceous oils comprising: (a) fractionally distilling said hydrocarbonaceous oil to produce at least one fraction boiling below a temperature from substantially 300° C. to substantially 570° C. and a residuum boiling above said temperature, without significantly cracking said hydrocarbonaceous oil, (b) contacting said residuum with a liquid hydrogen donor material stream at hydrocracking conditions to produce a hydrocracked stream, (c) separating said hydrocracked stream into a gaseous stream and a liquid hydrocracked stream, (d) fractionally distilling said liquid hydrocracked stream to separate, from lower and higher boiling fractions, a hydrogen donor precursor stream boiling above a temperature from substantially 180° C. to substantially 200° C. and below a temperature from substantially 330° C. to substantially 350° C., (e) catalytically reacting said hydrogen donor precursor stream with a hydrogen-rich gaseous stream to produce a hydrogenated donor material, and (f) recycling at least part of said hydrogenated hydrogen donor material as the material which constitutes the entire liquid hydrogen donor material stream to contact said residuum in step (b) noted above.

Claim 3

A process as claimed in claim 1 in which the heavy viscous hydrocarbonaceous oil is heavy crude oil or oil sands bitumen.

Claim 4

A process as claimed in claim 1 in which the hydrocarbonaceous oil is initially distilled under atmospheric pressure to remove volatile material and then distilled under reduced pressure to leave a residuum with an initial boiling point in the range from 450° C. to 570° C.

Claim 5

A process as claimed in claim 1 in which the residuum is mixed with said recycled liquid hydrogen donor material stream in a weight ratio of from 0.5:1 to 4:1 under hydrocracking conditions.

Claim 6

A process as claimed in claim 1 in which said hydrocracking conditions include temperature in the range from substantially 350° C. to substantially 500° C., pressure in the range from substantially 2 MPa to substantially 7 MPa and liquid space velocity from substantially 0.5 h -1 to substantially 10.0 h -1 .

Claim 7

A process as claimed in claim 5 in which the temperature is between 400° C. to 460° C., the pressure is between 2.5 MPa and 6 MPa, and the space velocity is between 0.8 h -1 and 7.0 h -1 .

Claim 8

A process as claimed in claim 1 in which the gaseous stream separated from the hydrocracked stream is desulphurized then reacted with steam in a steam reforming operation to form the hydrogen-rich gaseous stream for reaction with said hydrogen donor precursor stream.

Claim 9

A process as claimed in claim 1 in which the hydrogen donor precursor stream is a fraction distilled from the liquid hydrocracked stream and boils from substantially 200° C. to substantially 330° C.

Claim 10

A process as claimed in claim 1 in which the hydrogenated hydrogen donor material from step (e) is fractionally distilled to separate therefrom material boiling below substantially 220° C. and material boiling above substantially 295° C., before being recycled to step (b).

Claim 11

A process as claimed in claim 1 in which fractions distilled from the residuum are combined with the fractions of the liquid hydrocracked stream other than the hydrogen donor precursor stream to form an upgraded oil of lower viscosity and specific gravity than the original hydrocarbonaceous oil.

Claim 12

A process as claimed in claim 1 in which at least one fraction distilled from the residuum is individually combined with the corresponding boiling range fraction distilled from the liquid hydrocracked stream, and the resulting material is catalytically hydrogenated.

Claim 13

In a process for the upgrading of heavy, viscous hydrocarbonaceous oils comprising fractionally distilling said hydrocarbonaceous oil to produce at least one distilled fraction and a residuum without substantially cracking said hydrocarbonaceous oil, contacting said residuum with a liquid hydrogen donor material stream to produce a hydrocracked stream and separating said hydrocracked stream into a gaseous stream and a liquid hydrocracked stream, the improvement comprising: (a) fractionally distilling said liquid hydrocracked stream to separate from higher and lower boiling fractions a hydrogen donor precursor stream boiling above a temperature from substantially 180° C. to substantially 200° C. and below a temperature from substantially 330° C. to substantially 350° C., (b) catalytically reacting said hydrogen donor precursor stream with a hydrogen-rich gaseous stream to produce a hydrogenated hydrogen donor material, and (c) recycling at least part of said hydrogenated hydrogen donor material as the material which constitutes the entire length hydrogen donor material stream to contact said residuum.

Claim 14

In a process for the upgrading of heavy, viscous hydrocarbonaceous oils comprising fractionally distilling said hydrocarbonaceous oil to produce at least one distilled fraction and a residuum without substantially cracking said hydrocarbonaceous oil, contacting said residuum with a liquid hydrogen donor material stream to produce a hydrocracked stream and separating said hydrocracked stream into a gaseous stream and a liquid hydrocracked stream, the improvement comprising: (a) fractionally distilling said liquid hydrocracked stream to separate from higher and lower boiling fractions a hydrogen donor precursor stream boiling above a temperature from substantially 180° C. to substantially 200° C. and below a temperature from substantially 330° C. to substantially 350° C., (b) catalytically reacting said hydrogen donor precursor stream with a hydrogen-rich gaseous stream to produce a hydrogenated hydrogen donor material, and (c) recycling at least part of said hydrogenated hydrogen donor material as the material which constitutes the entire length hydrogen donor material stream to contact said residuum.

Claim 15

In a process for the upgrading of heavy, viscous hydrocarbonaceous oils comprising fractionally distilling said hydrocarbonaceous oil to produce at least one distilled fraction and a residuum without substantially cracking said hydrocarbonaceous oil, contacting said residuum with a liquid hydrogen donor material stream to produce a hydrocracked stream and separating said hydrocracked stream into a gaseous stream and a liquid hydrocracked stream, the improvement comprising: (a) fractionally distilling said liquid hydrocracked stream to separate from higher and lower boiling fractions a hydrogen donor precursor stream boiling above a temperature from substantially 180° C. to substantially 200° C. and below a temperature from substantially 330° C. to substantially 350° C., (b) catalytically reacting said hydrogen donor precursor stream with a hydrogen-rich gaseous stream to produce a hydrogenated hydrogen donor material, (c) fractionally distilling said hydrogenated hydrogen donor material to separate from higher and lower boiling fractions an optimized hydrogenated hydrogen donor material boiling above a temperature of substantially 220° C. and below a temperature of substantially 295° C., and (d) recycling said optimized hydrogenated hydrogen donor material as the material which constitutes the entire liquid hydrogen donor material stream to contact said residuum.

Claim 16

In a process for the upgrading of heavy, viscous hydrocarbonaceous oils comprising fractionally distilling said hydrocarbonaceous oil to produce at least one distilled fraction and a residuum without substantially cracking said hydrocarbonaceous oil, contacting said residuum with a liquid hydrogen donor material stream to produce a hydrocracked stream and separating said hydrocracked stream into a gaseous stream and a liquid hydrocracked stream, the improvement comprising: (a) fractionally distilling said liquid hydrocracked stream to separate from higher and lower boiling fractions a hydrogen donor precursor stream boiling above a temperature from substantially 180° C. to substantially 200° C. and below a temperature from substantially 330° C. to substantially 350° C., (b) catalytically reacting said hydrogen donor precursor stream with a hydrogen-rich gaseous stream to produce a hydrogenated hydrogen donor material, (c) fractionally distilling said hydrogenated hydrogen donor material to separate from higher and lower boiling fractions an optimized hydrogenated hydrogen donor material boiling above a temperature of substantially 220° C. and below a temperature of substantially 295° C., and (d) recycling said optimized hydrogenated hydrogen donor material as the material which constitutes the entire liquid hydrogen donor material stream to contact said residuum.