Process for the production of aromatic fuel

Claim 2

A process for the production of high octane gasoline component comprising the sequential steps of: A. Cracking carbometallic petroleum oil characterized by a Conradson Carbon content of at least 1.0 wt% and a metals content of at least 4 ppm Nickel Equivalents by weight in a riser cracking zone at cracking conditions in the presence of fluid cracking catalyst, B. recovering by distillation a light cycle oil fraction boiling in the range of about 216° C. to about 332° C. (about 430° F. to about 630° F.) and containing from about 10 vol. % to about 60 vol. % dual ring unsaturated aromatic hydrocarbons, C. contacting said fraction in the mixed phase in a saturation hydrogenation zone with a nickel-containing hydrogenation catalyst at selective conditions of temperature, pressure, space velocity and hydrogen circulation rate whereby at least 20-80 wt. % of the unsaturated aromatic hydrocarbons add hydrogen molecules to one of the rings to produce a partially saturated bicyclic hydrocarbon fraction, D. subjecting said partially saturated bicyclic hydrocarbon fraction to fluid catalytic cracking in a riser cracking zone at cracking conditions in the presence of with a zeolite fluid cracking catalyst and a metals passivator and in the absence of added hydrogen whereby rate of dehydrogenation is slowed sufficiently so that one ring of the bicyclic hydrocarbon rings cracks yielding monoaromatic hydrocarbons and, E. recovering from said monoaromatic hydrocarbons a gasoline component product characterized by an average octane of at least 91 and a monoaromatic hydrocarbon content in the range of 35 to 55 vol. %.

Claim 3

Process according to claim 1 in which the carbometallic petroleum oil feed to Step A is a reduced crude oil containing at least about 70% by volume of 343° C. (650° F.) plus material said feed being further characterized by a Conradson carbon of at least 1.0 wt.% and a metals content of at least 4 ppm nickel equivalents by weight.

Claim 4

Process according to claim 1 in which the cracking conditions in Step A comprise a temperature in the range of about 482° C. to about 538° F. (about 900° F. to about 1000° F.) a pressure in the range of 10-50 psia and a vapor residence time in the riser of 0.5 to 10 seconds.

Claim 5

Process according to claim 1 in which the cracking effluent from step A is gasoline.

Claim 6

Process according to claim 1 in which the hydrogenation catalyst of step C comprises a support material comprising alumina and a minor proportion of an active component selected from the group consisting of nickel oxide, nickel molybdate and nickel tungstate and mixtures thereof.

Claim 7

Process according to claim 1 in which the hydrogenation conditions of step C include a temperature in the range of 600° F. to 750° F., a pressure in the range of 600 to 1500 PSIA, a space velocity in the range of, 0.5 to 3.0 a hydrogen circulation rate of 1000-4000 cu. ft. per bbl.

Claim 8

Process according to claim 1 in which the fluid catalytic cracking conditions in step D include a temperature in the range of 950° to 1010° F. and a pressure in the range of 15-30 PSIA.

Claim 9

Process according to claim 1 in which the fluid cracking catalyst employed in step D comprises a zeolite supported on matrix and a metals content of 1000 to 3000 PPM nickel equivalents at catalyst equilibrium operating conditions and said catalyst is passivated with said passivator selected from compounds of tin, antimony and mixtures thereof.

Claim 10

Process according to claim 1 in which the gasoline fraction from reduced crude cracking from step A is blended with the gasoline component from FCC step E whereby the total gasoline recovery from the process is in the range of 60 to 70 Vol.% based on the carbometallic oil feed to Step 1.

Claim 11

A process for the production of high octane gasoline component comprising the sequential steps of: A. cracking carbo-metallic petroleum feedstock comprising a reduced crude oil containing at least about 70% by volume of 343° C. (650° F.) plus material said feed being further characterized by a Conradson Carbon of at least 1.0 wt% and a metals content of at least 4 ppm Nickel Equivalents by weight in a riser cracking zone at cracking conditions in the presence of fluid cracking catalyst containing 2000 to 15000 ppm Nickel Equivalents; B. recovering by distillation a light cycle oil fraction boiling in the range of about 216° C. to about 332° C. (about 430° F. to about 630° F.) and containing from about 10 wt% to about 60 vol.% dual ring unsaturated aromatic hydrocarbons, including naphthalenes; C. contacting said fraction in the mixed phase in a saturation hydrogenation zone with a nickel-containing hydrogenation catalyst at selective hydrogenation conditions of temperature, pressure, space velocity and hydrogen circulation rate whereby at least 20-80 wt% of the unsaturated aromatic hydrocarbons add hydrogen molecules to one of the rings to produce a partially saturated bicyclic hydrocarbon fraction, including naphthene-aromatic hydrocarbons; D. subjecting said partially saturated bicyclic hydrocarbon fraction to fluid catalytic cracking in a riser cracking zone at short contact time cracking conditions of less than 0.5 seconds in the presence of zeolite fluid cracking catalyst passivated with a material selected from compounds of tin, antimony and mixtures thereof, in the absence of hydrogen whereby rate of dehydrogenation is slowed sufficiently so that one ring of the bicyclic hydrocarbon rings cracks yielding monoaromatic hydrocarbons, including alkyl aromatics having one to four saturated side chains having from one to four carbon atoms in the side chain; and E. recovering from said monoaromatic hydrocarbons a gasoline component product characterized by an average octane of at least 91 and a monoaromatic hydrocarbon content in the range of 35 to 55 vol.%.

Claim 12

A process for the production of high octane gasoline component comprising the sequential steps of: A. cracking carbo-metallic petroleum feedstock comprising a reduced crude oil containing at least about 70% by volume of 343° C. (650° F.) plus material said feed being further characterized by a Conradson Carbon of at least 1.0 wt% and a metals content of at least 4 ppm Nickel Equivalents by weight in a riser cracking zone at cracking conditions in the presence of fluid cracking catalyst containing 2000 to 15000 ppm Nickel Equivalents; B. recovering by distillation a light cycle oil fraction boiling in the range of about 216° C. to about 332° C. (about 430° F. to about 630° F.) and containing from about 10 wt% to about 60 vol.% dual ring unsaturated aromatic hydrocarbons, including naphthalenes; C. contacting said fraction in the mixed phase in a saturation hydrogenation zone with a nickel-containing hydrogenation catalyst at selective hydrogenation conditions of temperature, pressure, space velocity and hydrogen circulation rate whereby at least 20-80 wt% of the unsaturated aromatic hydrocarbons add hydrogen molecules to one of the rings to produce a partially saturated bicyclic hydrocarbon fraction, including naphthene-aromatic hydrocarbons; D. subjecting said partially saturated bicyclic hydrocarbon fraction to fluid catalytic cracking in a riser cracking zone at short contact time cracking conditions of less than 0.5 seconds in the presence of zeolite fluid cracking catalyst passivated with a material selected from compounds of tin, antimony and mixtures thereof, in the absence of hydrogen whereby rate of dehydrogenation is slowed sufficiently so that one ring of the bicyclic hydrocarbon rings cracks yielding monoaromatic hydrocarbons, including alkyl aromatics having one to four saturated side chains having from one to four carbon atoms in the side chain; and E. recovering from said monoaromatic hydrocarbons a gasoline component product characterized by an average octane of at least 91 and a monoaromatic hydrocarbon content in the range of 35 to 55 vol.%.