US4073718A
Expired / Lapsed
US
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Process for the hydroconversion and hydrodesulfurization of heavy feeds and residua
Assignee: ExxonMobil Technology and Engineering Co
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Filing: 1976-10-18
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Granted: 1978-02-14
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Expires: 1996-10-18
Abstract
Abstract A process for the production of low sulfur, low nitrogen fuels at low hydrogen consumption by splitting a feed into two components, a high boiling component, suitably a 1050 DEG F.+ fraction, and a low boiling component, suitably a 1050 DEG F.- fraction, and processing the two different components over two different types of catalysts, at different severities. Suitably, on the one hand, the high boiling component is treated over a large pore metal hydrogenation catalyst at severity sufficient to convert at least 30 percent, preferably at least 50 percent of the feed, based on the weight of the feed, to a 1050 DEG F.- product. The 1050 DEG F.- product from the conversion over the large pore metal hydrogenation catalyst is then blended with the low boiling component split from the original feed, and the blended low boiling material is then treated at low severity over a small pore metal hydrogenation catalyst to hydrodesulfurize and hydrodenitrogenate said low boiling components. The product of the hydrodesulfurization, hydrodenitrogenation reaction constitutes a suitable feed for hydrocracking, or for use as a catalytic cracker feed.
Inventors
- 👤 Glen P. Hamner
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-27 17:59
CPC Classifications
C; C10; C10G; C10G45/00; C10G45/02; C10G45/04; C10G45/06; C10G45/08; B; B01; B01J; B01J23/00; B01J23/70; B01J23/76; B01J23/84; B01J23/85; B01J35/00; B01J35/60; B01J35/61; B01J35/615; B01J35/63; B01J35/633; B01J35/635; B01J35/64; B01J35/647; B01J35/66; B01J35/67
Claims Analysis
Total Claims: 27
Claim 1
Independent Claim
361 words
A process for the hydroconversion and hydrodesulfurization of a sulfur-bearing heavy hydrocarbon feed which comprises splitting said heavy hydrocarbon feed into a high boiling component having a low end boiling point within a range of from about 850° to about 1100° F, and a low boiling component having a high end boiling point within a range of from about 850° to about 1100° F, contacting said high boiling component feed in a first stage, in the presence of added hydrogen, with catalyst comprising a composite of a porous inorganic oxide support and a metal hydrogenation-dehydrogenation component constituted of from about 5 to about 30 percent of a Group VIB metal, or compound thereof, and from about 1 to about 12 percent of a Group VIII metal, or compound thereof, or admixture of said Group VIB and VIII metals or compounds thereof, said catalyst composite comprising greater than 50 percent of its total pore volume of absolute diameter within the range of from about 70A to about 200A, to convert at least about 30 percent by weight of the 1050° F+ hydrocarbons to 1050° F- hydrocarbons, separating hydrogen, light ends and by-product hydrogen sulfide from the effluent, and separating therefrom a product having a high end boiling point ranging from about 850° to about 1100° F, blending said product of high end boiling point with the low boiling component split from the original heavy hydrocarbon feed, and then contacting said blended low boiling material in a second stage with catalyst comprising a composite of a porous inorganic oxide support and a metal hydrogenation-dehydrogenation component constituted of from about 5 to about 30 percent of a Group VIB metal, or compound thereof, and from about 1 to about 12 percent of a Group VIII metal, or admixture of said Group VIB and VIII metals or compounds thereof, said catalyst composite comprising greater than 50 percent of its total pore volume of absolute diameter ranging from about 50A to about 120A, at severity sufficient to desulfurize from about 80 to about 99 percent of the blended low boiling materials, based on the weight of the liquid introduced as feed to said second desulfurization stage.
Claim 2
Dependent Claim
361 words
A process for the hydroconversion and hydrodesulfurization of a sulfur-bearing heavy hydrocarbon feed which comprises splitting said heavy hydrocarbon feed into a high boiling component having a low end boiling point within a range of from about 850° to about 1100° F, and a low boiling component having a high end boiling point within a range of from about 850° to about 1100° F, contacting said high boiling component feed in a first stage, in the presence of added hydrogen, with catalyst comprising a composite of a porous inorganic oxide support and a metal hydrogenation-dehydrogenation component constituted of from about 5 to about 30 percent of a Group VIB metal, or compound thereof, and from about 1 to about 12 percent of a Group VIII metal, or compound thereof, or admixture of said Group VIB and VIII metals or compounds thereof, said catalyst composite comprising greater than 50 percent of its total pore volume of absolute diameter within the range of from about 70A to about 200A, to convert at least about 30 percent by weight of the 1050° F+ hydrocarbons to 1050° F- hydrocarbons, separating hydrogen, light ends and by-product hydrogen sulfide from the effluent, and separating therefrom a product having a high end boiling point ranging from about 850° to about 1100° F, blending said product of high end boiling point with the low boiling component split from the original heavy hydrocarbon feed, and then contacting said blended low boiling material in a second stage with catalyst comprising a composite of a porous inorganic oxide support and a metal hydrogenation-dehydrogenation component constituted of from about 5 to about 30 percent of a Group VIB metal, or compound thereof, and from about 1 to about 12 percent of a Group VIII metal, or admixture of said Group VIB and VIII metals or compounds thereof, said catalyst composite comprising greater than 50 percent of its total pore volume of absolute diameter ranging from about 50A to about 120A, at severity sufficient to desulfurize from about 80 to about 99 percent of the blended low boiling materials, based on the weight of the liquid introduced as feed to said second desulfurization stage.
Claim 3
Dependent Claim
56 words
The process of claim 1 wherein the heavy hydrocarbon feed is split into a high boiling component having a low end boiling point with a range of from about 900° to about 1050° F, and the low boiling component has a high end boiling point within a range of from about 900° to about 1050° F.
Claim 4
Dependent Claim
44 words
The process of claim 1 wherein the heavy hydrocarbon feed is split into a high boiling component having a low end boiling point of about 1050° F, and the low boiling component is one having a high end boiling point of about 1050° F.
Claim 5
Dependent Claim
35 words
The process of claim 1 wherein greater than about 70 percent of the total pore volume of the first stage catalyst is of absolute diameter within the range of from about 70A to about 200A.
Claim 6
Dependent Claim
35 words
The process of claim 1 wherein greater than about 90 percent of the total pore volume of the first stage catalyst is of absolute diameter within the range of from about 70A to about 200A.
Claim 7
Dependent Claim
19 words
The process of claim 1 wherein the Group VIB metal of the first stage catalyst is tungsten or molybdenum.
Claim 8
Dependent Claim
19 words
The process of claim 1 wherein the Group VIII metal of the first stage catalyst is cobalt or nickel.
Claim 9
Dependent Claim
17 words
The process of claim 1 wherein the inorganic oxide support of the first stage catalyst is alumina.
Claim 10
Dependent Claim
20 words
The process of claim 1 wherein the inorganic oxide support of the first stage catalyst is alumina stabilized with silica.
Claim 11
Dependent Claim
38 words
The process of claim 1 wherein the first stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A <3
50-100A <22
100-200A <50
200A+ >25
Pore Volume, cc/g 0.6-2.0
Surface Area, m.sup.2 /g
150-450
______________________________________
Claim 12
Dependent Claim
38 words
The process of claim 1 wherein the first stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A <1
50-100A <14
100-200A >70
200A+ 0
Pore Volume, cc/g 0.6-1.5
Surface Area, m.sup.2 /g
200-400
______________________________________
Claim 13
Dependent Claim
38 words
The process of claim 1 wherein the first stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A 0
50-100A <8
100-200A >90
200A+ 0
Pore Volume, cc/g 0.6-1.0
Surface Area, m.sup.2 /g
250-350
______________________________________
Claim 14
Dependent Claim
32 words
The process of claim 1 wherein, in the first stage, greater than about 50 percent of the 1050° F+ hydrocarbons of the high boiling point component is converted to 1050° F- hydrocarbons.
Claim 15
Dependent Claim
34 words
The process of claim 1 wherein, in the first stage, from about 50 to about 90 percent of the 1050° F+ hydrocarbons of the high boiling point component is converted to 1050° F- hydrocarbons.
Claim 16
Dependent Claim
35 words
The process of claim 1 wherein greater than about 75 percent of the total pore volume of the second stage catalyst is of absolute diameter within the range of from about 50A to about 120A.
Claim 17
Dependent Claim
35 words
The process of claim 15 wherein greater than about 90 percent of the total pore volume of the second stage catalyst is of absolute diameter within the range of from about 50A to about 120A.
Claim 18
Dependent Claim
19 words
The process of claim 16 wherein the Group VIB metal of the second stage catalyst is tungsten or molybdenum.
Claim 19
Dependent Claim
19 words
The process of claim 15 wherein the Group VIII metal of the second stage catalyst is cobalt or nickel.
Claim 20
Dependent Claim
17 words
The process of claim 15 wherein the inorganic oxide support of the second stage catalyst is alumina.
Claim 21
Dependent Claim
20 words
The process of claim 15 wherein the inorganic oxide support of the second stage catalyst is alumina stabilized with silica.
Claim 22
Dependent Claim
38 words
The process of claim 15 wherein the second stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A <30
50-100A >30
100-150A >30
150A+ <10
Pore Volume, cc/g 0.3-0.8
Surface Area, m.sup.2 /g
150-450
______________________________________
Claim 23
Dependent Claim
38 words
The process of claim 15 wherein the second stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A <10
50-100A >40
100-150A >40
150A+ <5
Pore Volume, cc/g 0.4-0.7
Surface Area, m.sup.2 /g
200-400
______________________________________
Claim 24
Dependent Claim
38 words
The process of claim 15 wherein the second stage catalyst is characterized as follows: ______________________________________
Distribution of
Pore Diameter
______________________________________
0-50A <5
50-100A >50
100-150A >35
150A+ <5
Pore Volume, cc/g 0.45-0.6
Surface Area, m.sup.2 /g
250-350
______________________________________
Claim 25
Dependent Claim
96 words
The process of claim 1 wherein the product of the first stage hydroconversion is split into (a) a product having a high end boiling point ranging from about 850° to about 1100° F. which is blended with the low boiling component split from the original heavy hydrocarbon feed, and the blended material hydrodesulfurized in the second hydrodesulfurization stage, and (b) a product having a low end boiling point ranging from about 850° to about 1100° F., and the latter product (b) and the effluent from the second hydrodesulfurization stage are blended to produce a fuel oil.
Claim 26
Dependent Claim
41 words
The process of claim 1 wherein a liquid product is recovered from the second desulfurization stage, and a portion thereof is blended with the high boiling component split from the original heavy hydrocarbon feed and fed into the first hydroconversion stage.
Claim 27
Dependent Claim
43 words
The process of claim 25 wherein from about 25 to about 75 percent of the liquid product from the second hydrodesulfurization stage, based on the total weight of the liquid effluent from said second hydrodesulfurization stage, is blended with said high boiling component.
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USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1981-02-13 | 1981-08-15 | 1982-02-14 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1985-02-13 | 1985-08-15 | 1986-02-14 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1989-02-13 | 1989-08-15 | 1990-02-14 | $7700.00 | Window Closed / Lapsed |