US4149965A
Expired / Lapsed
US
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Method for starting-up a naphtha hydrorefining process
Assignee: ExxonMobil Technology and Engineering Co
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Filing: 1978-06-27
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Granted: 1979-04-17
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Expires: 1998-06-27
Abstract
Abstract A naphtha hydrorefining process is initiated by contacting an olefinic naphtha feed at hydrorefining conditions including a pressure below about 200 psig, with hydrogen and a catalyst that has been partially deactivated by treating a fresh or a regenerated catalyst with a substantially non-metals containing hydrocarbonaceous oil in the presence of hydrogen under conditions sufficient to decrease the hydrogenation activity of the catalyst.
Inventors
- 👤 Lloyd A. Pine
- 👤 William E. Winter
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-03 15:27
CPC Classifications
C; C10; C10G; C10G49/00; C10G49/24; C10G2300/00; C10G2300/40; C10G2300/4031
Claims Analysis
Total Claims: 20
Claim 1
Independent Claim
120 words
A method for starting up a naphtha hydrorefining process for removing sulfur contaminants from said naphtha, which comprises: contacting naphtha containing said sulfur contaminants and at least 10 volume percent olefins with a hydrogen-containing gas and with a partially deactivated catalyst under hydrorefining conditions including a pressure ranging from about 60 psig to less than 200 psig, and at a temperature ranging from about 400° to about 800° F., said catalyst having been deactivated by contacting a fresh or a regenerated hydrorefining catalyst having hydrogenation and desulfurization activity with a substantially non-metals containing hydrocarbonaceous oil in the presence of a hydrogen-containing gas under conditions and for a time sufficient to decrease the hydrogenation activity of said fresh or regenerated catalyst.
Claim 2
Independent Claim
120 words
A method for starting up a naphtha hydrorefining process for removing sulfur contaminants from said naphtha, which comprises: contacting naphtha containing said sulfur contaminants and at least 10 volume percent olefins with a hydrogen-containing gas and with a partially deactivated catalyst under hydrorefining conditions including a pressure ranging from about 60 psig to less than 200 psig, and at a temperature ranging from about 400° to about 800° F., said catalyst having been deactivated by contacting a fresh or a regenerated hydrorefining catalyst having hydrogenation and desulfurization activity with a substantially non-metals containing hydrocarbonaceous oil in the presence of a hydrogen-containing gas under conditions and for a time sufficient to decrease the hydrogenation activity of said fresh or regenerated catalyst.
Claim 3
Dependent Claim
19 words
The method of claim 1 wherein said hydrorefining conditions include a pressure of not more than about 195 psig.
Claim 4
Dependent Claim
35 words
The method of claim 1 wherein said conditions for partially deactivating said catalyst comprise a pressure ranging from about 150 to about 2000 psig and a temperature ranging from about 400° to about 800° F.
Claim 5
Dependent Claim
22 words
The method of claim 1 wherein said conditions for partially deactivating said catalyst comprise a pressure of at least about 250 psig.
Claim 6
Dependent Claim
24 words
The method of claim 1 wherein said conditions for partially deactivating said catalyst comprise a pressure ranging from about 250 to about 400 psig.
Claim 7
Dependent Claim
37 words
The method of claim 1 wherein said hydrorefining conditions include a pressure ranging from about 60 to about 100 psig and wherein said partial deactivation conditions comprise a pressure ranging from about 250 to about 400 psig.
Claim 8
Dependent Claim
15 words
The method of claim 1 wherein said naphtha comprises at least 30 volume percent olefins.
Claim 9
Dependent Claim
23 words
The method of claim 1 wherein said naphtha is selected from the group consisting of cracked naphtha, coker naphtha and steam cracked naphtha.
Claim 10
Dependent Claim
26 words
The method of claim 8 wherein said cracked naphtha is a fraction having an atmospheric boiling point ranging from about C 5 to about 330° F.
Claim 11
Dependent Claim
27 words
The method of claim 1 wherein said substantially non-metals containing hydrocarbonaceous oil comprises less than about 80 weight parts per million total metals, calculated as the metal.
Claim 12
Dependent Claim
27 words
The method of claim 1 wherein said substantially non-metals containing hydrocarbonaceous oil comprises less than about 25 weight parts per million total metals, calculated as the metal.
Claim 13
Dependent Claim
31 words
The method of claim 1 wherein said substantially non-metals containing hydrocarbonaceous oil is selected from the group consisting of naphtha, vacuum gas oils, virgin gas oils, thermal and catalytic cycle oils.
Claim 14
Dependent Claim
28 words
The method of claim 1 wherein said fresh or regenerated catalyst comprises at least one Group VIB and one Group VIII non-noble metal component composited with a support.
Claim 15
Dependent Claim
32 words
The method of claim 1 wherein said catalyst comprises a metal, metal oxide and metal sulfide of a Group VIB and of a non-noble metal of a Group VIII on a support.
Claim 16
Dependent Claim
10 words
The method of claim 14 wherein said support is alumina.
Claim 17
Dependent Claim
15 words
The method of claim 15 wherein said alumina additionally comprises a minor amount of silica.
Claim 18
Independent Claim
141 words
A method for starting up a naphtha hydrorefining process for removing sulfur from said naphtha, which comprises: (a) contacting a fresh or regenerated hydrorefining catalyst with a substantially non-metals containing naphtha, said naphtha comprising at least 10 volume percent olefins, and with a hydrogen-containing gas, at a pressure ranging from about 250 to about 400 psig and at a temperature ranging from about 400° to about 800° F. for a time sufficient to decrease the hydrogenation activity of said catalyst, and (b) contacting the resulting partially deactivated catalyst with a hydrogen-containing gas and with a naphtha feed comprising at least 10 volume percent olefins, at hydrorefining conditions, including a pressure of not more than about 195 psig and a temperature ranging from about 400° to about 800° F., and (c) recovering a hydrorefined naphtha comprising less than 100 weight ppm sulfur.
Claim 19
Independent Claim
141 words
A method for starting up a naphtha hydrorefining process for removing sulfur from said naphtha, which comprises: (a) contacting a fresh or regenerated hydrorefining catalyst with a substantially non-metals containing naphtha, said naphtha comprising at least 10 volume percent olefins, and with a hydrogen-containing gas, at a pressure ranging from about 250 to about 400 psig and at a temperature ranging from about 400° to about 800° F. for a time sufficient to decrease the hydrogenation activity of said catalyst, and (b) contacting the resulting partially deactivated catalyst with a hydrogen-containing gas and with a naphtha feed comprising at least 10 volume percent olefins, at hydrorefining conditions, including a pressure of not more than about 195 psig and a temperature ranging from about 400° to about 800° F., and (c) recovering a hydrorefined naphtha comprising less than 100 weight ppm sulfur.
Claim 20
Dependent Claim
24 words
The method of claim 17 wherein the recovered hydrorefined naphtha comprises 85 volume percent of olefins relative to the initial olefins in the feed.
References Cited (Backward Citations)
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1982-04-16 | 1982-10-16 | 1983-04-17 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1986-04-16 | 1986-10-16 | 1987-04-17 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1990-04-16 | 1990-10-16 | 1991-04-17 | $7700.00 | Window Closed / Lapsed |