Process for the production of ultra high octane gasoline, and other fuels from aromatic hydrocrackates

Claim 2

A process for the production of high octane gasoline, or high octane gasoline blending components from a sulfur and nitrogen-containing feed composition boiling with a range of from about 400° F. to about 750° F. and constituted of fused multi-ring aromatic hydrocarbons, containing two, and three or more rings in the molecule, inclusive of naphthalenes, which comprises hydrogenating over a hydrogenating catalyst at hydrogenation conditions in a hydrogenation zone, the whole feed at conditions sufficient to remove sulfur and nitrogen and saturate one ring of the two-ring molecular species, inclusive of naphthalenes, but insufficient to saturate the second ring of said molecular species, of the fused two-ring aromatic hydrocarbons components of said mixture of hydrocarbons, hydrocracking over a hydrocracking catalyst at hydrocracking conditions in a first hydrocracking zone, the previously hydrogenated product, as a feed, to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule and produce lower molecular weight lower boiling components, separating the liquid product of said first hydrocracking zone into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons boiling within a range of from about 400° F. to about 600° F., and (ii) a blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule boiling within a range of from about 600° F. to about 750° F., then contacting and reacting in a reaction zone said blend rich in fused two-ring aromatic hydrocarbons as defined in (i), supra, with hydrogen, over a catalyst comprised of elements iron and one or more alkali or alkaline-earth metals components at a temperature ranging from about 437° F. (225° C.) to about 806° F. (430° C.), and hydrogen partial pressure ranging to about 1000 psig to selectively hydrogenate and crack said previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight, higher octane components suitable per se as gasoline or gasoline blending components, and contacting and reacting in a second hydrocracking zone said blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule over a hydrocracking catalyst at hydrocracking conditions to crack the fused multi-ring aromatic hydrocarbon components and produce lower molecular weight lower boiling components suitable as gasoline, or gasoline blending components.

Claim 3

The process of claim 1 wherein the hydrogenation conducted in said first reaction zone is carried out by reaction of the 400/750° F. feed over a Group VIB or Group VIII metal catalyst at temperature ranging from about 550° F. to about 800° F., pressure ranging from about 200 psig to about 2000 psig, flow rate ranging from about 0.1 V/V/Hr. to about 10 V/V/Hr. and hydrogen rate of from about 500 SCF/B to about 10,000 SCF/B to saturate one ring of said fused two-ring aromatic hydrocarbons and produce a product which is employed as a feed and reacted over the iron catalyst.

Claim 4

The process of claim 2 wherein the hydrogenation catalyst of said first reaction zone is comprised of molybdenum, tungsten, cobalt, nickel, nickel-molybdenum, cobalt-molybdenum, or the like, supported on alumina, and the hydrogenation reaction is conducted at temperatures ranging from about 600° F. to about 750° F., at pressures ranging from about 500 psig to about 1500 psig, flow rate ranging from about 0.5 V/V/Hr. to about 2.0 V/V/Hr., and at hydrogen rates ranging from about 1000 SCF/B to about 5000 SCF/B.

Claim 5

The process of claim 1 wherein the product of the hydrogenation reaction, as a feed, is hydrocracked in said first hydrocracking zone over a zeolite catalyst which contains a metal hydrogenation component, at temperatures ranging from about 450° F. to about 850° F., pressures ranging from about 500 psig to about 4000 psig, space velocities ranging from about 0.2 LHSV to about 20 LHSV and a hydrogen circulation rate ranging from about 2000 SCF/B to about 20,000 SCF/B.

Claim 6

The process of claim 1 wherein the hydrocracking temperature ranges from about 500° F. to about 775° F., pressure of from about 1000 psig to about 3000 psig, space velocity of from about 0.5 LHSV to about 10 LHSV, and hydrogen circulation rate of from about 2000 SCF/B to about 10,000 SCF/B.

Claim 7

The process of claim 1 wherein the separated 400° F./500° F. fraction rich in fused two-ring aromatic hydrocarbons is contacted and reacted with the iron catalyst at temperatures ranging from about 482° F. to about 742° F., and at pressures ranging from about 100 psi to about 600 psig.

Claim 8

The process of claim 1 wherein the separated 400° F./600° F. fraction rich in fused two-ring aromatic hydrocarbons is contacted and reacted with the iron catalyst at hydrogen pressures ranging from about 100 psig to about 450 psig, and in the presence of naphthalenes in concentration ranging up to about 5 percent, based on the weight of the feed.

Claim 9

The process of claim 7 wherein the hydrogen pressure ranges from about 250 psig to about 350 psig, and the concentration of the naphthalenes ranges up to about 3 percent.

Claim 10

The process of claim 1 wherein the separated 400° F./600° F. fraction rich in fused two-ring aromatic hydrocarbons is contacted and reacted with the iron catalyst at hydrogen pressures ranging from about 500 psig to about 100 psig, and in the presence of naphthalenes in concentration ranging from about 5 percent to about 25 percent, based on the weight of the feed.

Claim 11

The process of claim 9 wherein the hydrogen pressure ranges from about 500 psig to about 650 psig, and the concentration of naphthalenes ranges from about 10 percent to about 20 percent.

Claim 12

The process of claim 1 wherein the product of the reaction over the iron catalyst is separately fractionated to recover an ultra high octane gasoline, or gasoline blending component.

Claim 13

The process of claim 1 wherein the iron catalyst with which the 400° F./600° F. fraction rich in fused two-ring aromatic hydrocarbons is contacted and reacted as a feed is characterized as (i) a bulk iron catalyst which contains at least 50 percent elemental iron, based on the weight of the catalyst, and the catalyst is modified with one or more alkali or alkaline-earth metals, or (ii) an iron catalyst wherein the iron is dispersed upon an inorganic oxide support, the catalyst containing at least about 0.1 percent iron, based on the total weight of the catalyst, the supported metallic component containing at least 50 percent iron, exclusive of the support component, or components, of the catalyst, and the iron is modified with one or more alkali or alkaline-earth metals.

Claim 14

The process of claim 12 wherein the iron catalyst with which the feed and hydrogen are contacted at reaction conditions, when a bulk iron catalyst, is one which contains at least 70 percent to about 98 percent elemental iron.

Claim 15

The process of claim 13 wherein the catalyst with which the feed and hydrogen are contacted at reaction conditions is modified with one or more alkali or alkaline-earth metals in concentrations ranging from about 0.01 percent to about 10 percent, and aluminum in concentration ranging from about 0.01 percent to about 20 percent.

Claim 16

The process of claim 1 wherein the iron catalyst with which the hydrogenated product is contacted and reacted as a feed, with hydrogen, is a fused iron catalyst.

Claim 17

The process of claim 1 wherein the iron catalyst with which the hydrogenated product contacted and reacted as a feed, with hydrogen, is a supported iron catalyst which contains from about 70 percent to about 98 percent iron, exclusive of the support component, or components.

Claim 18

The process of claim 16 wherein the supported iron catalyst is modified with one or more alkali or alkaline-earth metals in concentration ranging from about 0.01 percent to about 10 percent, and aluminum in concentration ranging from about 0.01 percent to about 20 percent.

Claim 19

The process of claim 1 wherein the separated 600° F./760° F. fraction rich in fused three-ring aromatic hydrocarbons is hydrocracked in said second hydrocrackzone over a zeolite catalyst which contains a metal hydrogenation component, at temperatures ranging from about 450° F. to about 850° F., pressures ranging from about 500 psig to about 4000 psig, space velocities ranging from about 0.2 LHSV to about 20 LHSV and a hydrogen circulation rate ranging from about 2000 SCF/B to about 20,000 SCF/B.

Claim 20

The process of claim 18 wherein the hydrocracking temperature ranges from about 500° F. to about 775° F., pressure of from about 1000 psig to about 3000 psig, space velocity of from about 0.5 LHSV to about 10 LHSV, and hydrogen circulation rate of from about 2000 SCF/B to about 10,000 SCF/B.

Claim 21

A process for the production of high octane gasoline, high octane blending components, diesel fuel and diesel fuel blending components from a sulfur and nitrogen-containing feed composition boiling within a range of from about 400° F. to about 750° F. and constituted of fused multi-ring aromatic hydrocarbons containing two, and three or more rings in the molecule, inclusive of naphthalenes, which comprises hydrogenating over a hydrogenating catalyst at hydrogenation conditions in a first hydrogenation zone, the whole feed at conditions sufficient to remove sulfur and nitrogen and saturate one ring of the two ring molecular species, inclusive of naphthalenes, but insufficient to saturate the second ring of said molecular species, of the fused two-ring aromatic hydrocarbons components of said mixture of hydrocarbons, hydrocracking over a hydrocracking catalyst at hydrocracking conditions in a hydrocracking zone, the previously hydrogenated product, as a feed, to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule and produce lower molecular weight lower boiling components, separating the liquid product of said first hydrocracking zone into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons boiling within a range of from about 400° F. to about 600° F., and (ii) a blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule boiling within a range of from about 600° F. to bout 750° F., then contacting and reacting in a reaction zone said blend rich in fused two-ring aromatic hydrocarbons as defined in (1), supra, with hydrogen, over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components at a temperature ranging from about 437° F. (225° C.) to about 806° F. (430° C.), and hydrogen partial pressure ranging to about 1000 psig to selectively hydrogenate and crack said previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight, higher octane components suitable per se as gasoline or gasoline blending components, and contacting and reacting in a second hydrogenation zone said blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule over a hydrogenation catalyst at hydrogenation conditions to hydrogenate the fused multi-ring aromatic hydrocarbon components and produce components suitable as diesel, or diesel blending components.

Claim 22

A process for the production of high octane gasoline, high octane blending components, diesel fuel and diesel fuel blending components from a sulfur and nitrogen-containing feed composition boiling within a range of from about 400° F. to about 750° F. and constituted of fused multi-ring aromatic hydrocarbons containing two, and three or more rings in the molecule, inclusive of naphthalenes, which comprises hydrogenating over a hydrogenating catalyst at hydrogenation conditions in a first hydrogenation zone, the whole feed at conditions sufficient to remove sulfur and nitrogen and saturate one ring of the two ring molecular species, inclusive of naphthalenes, but insufficient to saturate the second ring of said molecular species, of the fused two-ring aromatic hydrocarbons components of said mixture of hydrocarbons, hydrocracking over a hydrocracking catalyst at hydrocracking conditions in a hydrocracking zone, the previously hydrogenated product, as a feed, to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule and produce lower molecular weight lower boiling components, separating the liquid product of said first hydrocracking zone into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons boiling within a range of from about 400° F. to about 600° F., and (ii) a blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule boiling within a range of from about 600° F. to bout 750° F., then contacting and reacting in a reaction zone said blend rich in fused two-ring aromatic hydrocarbons as defined in (1), supra, with hydrogen, over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components at a temperature ranging from about 437° F. (225° C.) to about 806° F. (430° C.), and hydrogen partial pressure ranging to about 1000 psig to selectively hydrogenate and crack said previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight, higher octane components suitable per se as gasoline or gasoline blending components, and contacting and reacting in a second hydrogenation zone said blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule over a hydrogenation catalyst at hydrogenation conditions to hydrogenate the fused multi-ring aromatic hydrocarbon components and produce components suitable as diesel, or diesel blending components.

Claim 23

The process of claim 20 wherein the hydrogenation conducted in said second hydrogenation zone is carried out by reaction of the 600/750° F. feed fraction over a Group VIB or Group VIII metal catalyst at temperature ranging from about 550° F. to about 800° F., pressure ranging from about 200 psig to about 2000 psig, flow rate ranging from about 0.1 V/V/Hr. to about 10 V/V/Hr., and hydrogen rate of from about 500 SCF/B to about 10,000 SCF/B.

Claim 24

The process of claim 21 wherein the hydrogenation catalyst of said first reaction zone is comprised of molybdenum, tungsten, cobalt, nickel, nickel-molybdenum, cobalt-molybdenum, or the like, supported on aluminia, and the hydrogenation reaction is conducted at temperatures ranging from about 600° F. to about 750° F., at pressures from about 500 psig to about 1500 psig, flow rate ranging from about 0.5 V/V/Hr. to about 20 V/V/Hr., and at hydrogen rates ranging from about 1000 SCF/B to about 500 SCF/B.

Claim 25

A process for the production of high octane gasoline, high octane blending components, diesel fuel and diesel fuel blending components from a sulfur and nitrogen-containing feed composition boiling within a range of from about 400° F. to about 750° F. and constituted of fused multi-ring aromatic hydrocarbons containing two, and three or more rings in the molecule, inclusive of naphthalenes, which comprises hydrogenating over a hydrogenating catalyst at hydrogenation conditions in a first hydrogenation zone, the whole feed at conditions sufficient to remove sulfur and nitrogen and saturate one ring of the two ring molecular species, inclusive of naphthalenes, but insufficient to saturate the second ring of said molecular species, of the fused two-ring aromatic hydrocarbons components of said mixture of hydrocarbons, hydrocracking over a hydrocracking catalyst at hydrocracking conditions in a hydrocracking zone, the previously hydrogenated product, as a feed, to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule and produce lower molecular weight lower boiling components, separating the liquid product of said first hydrocracking zone into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons boiling within a range of from about 400° F. to about 500° F., and (ii) a blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule boiling within a range of from about 600° F. to about 750° F., then contacting and reacting in a reaction zone said blend rich in fused two-ring aromatic hydrocarbons as defined in (i), supra, with hydrogen, over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components at a temperature ranging from about 437° F. (225° C.) to about 806° F. (430° C.), and hydrogen partial pressure ranging to about 1000 psig to selectively hydrogenate and crack said previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight, higher octane components suitable per se as gasoline or gasoline blending components, and contacting and reacting over a catalystic cracking catalyst at catalytic cracking conditions said blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule to crack said multi-ring hydrocarbons to produce lower molecular weight hydrocarbons suitable as gasoline, or gasoline blending components.

Claim 26

A process for the production of high octane gasoline, high octane blending components, diesel fuel and diesel fuel blending components from a sulfur and nitrogen-containing feed composition boiling within a range of from about 400° F. to about 750° F. and constituted of fused multi-ring aromatic hydrocarbons containing two, and three or more rings in the molecule, inclusive of naphthalenes, which comprises hydrogenating over a hydrogenating catalyst at hydrogenation conditions in a first hydrogenation zone, the whole feed at conditions sufficient to remove sulfur and nitrogen and saturate one ring of the two ring molecular species, inclusive of naphthalenes, but insufficient to saturate the second ring of said molecular species, of the fused two-ring aromatic hydrocarbons components of said mixture of hydrocarbons, hydrocracking over a hydrocracking catalyst at hydrocracking conditions in a hydrocracking zone, the previously hydrogenated product, as a feed, to crack fused multi-ring aromatic hydrocarbons containing three or more rings to the molecule and produce lower molecular weight lower boiling components, separating the liquid product of said first hydrocracking zone into blends which include (i) a blend rich in fused two-ring aromatic hydrocarbons boiling within a range of from about 400° F. to about 500° F., and (ii) a blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule boiling within a range of from about 600° F. to about 750° F., then contacting and reacting in a reaction zone said blend rich in fused two-ring aromatic hydrocarbons as defined in (i), supra, with hydrogen, over a catalyst comprised of elemental iron and one or more alkali or alkaline-earth metals components at a temperature ranging from about 437° F. (225° C.) to about 806° F. (430° C.), and hydrogen partial pressure ranging to about 1000 psig to selectively hydrogenate and crack said previously hydrogenated fused two-ring aromatic hydrocarbons to produce lower molecular weight, higher octane components suitable per se as gasoline or gasoline blending components, and contacting and reacting over a catalystic cracking catalyst at catalytic cracking conditions said blend rich in fused multi-ring hydrocarbons containing three or more rings to the molecule to crack said multi-ring hydrocarbons to produce lower molecular weight hydrocarbons suitable as gasoline, or gasoline blending components.