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Patent US4090947A successfully refreshed from Google Patents.
US4090947A
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Hydrogen donor diluent cracking process
Assignee: ConocoPhillips Co
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Filing: 1977-08-08
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Granted: 1978-05-23
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Expires: 1997-08-08
Abstract
Abstract A hydrogen donor diluent cracking process for converting hydrogen deficient residual petroleum oils to more valuable distillates. A premium coker gas-oil is utilized as the hydrogen donor diluent.
Inventors
- 👤 Donald P. Satchell, Jr.
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-01 21:47
CPC Classifications
C; C10; C10G; C10G47/00; C10G47/32; C10G47/34
Claims Analysis
Total Claims: 9
Claim 1
Independent Claim
114 words
In a thermal cracking process for converting heavy petroleum residual oil to lighter distillate products in which the thermal cracking of the residual oil takes place in the presence of a hydrogen donor diluent, the improvement wherein the hydrogen donor diluent comprises hydrotreated heavy premium coker gas-oil produced in a premium coking operation utilizing a coke drum pressure of from 10 to 150 psig, a coker furnace transfer line temperature of from 900° to 960° F and a coke drum overhead vapor temperature of from 825° to 900° F and operated at conditions such that the coke produced has a coefficient of thermal expansion of about 5 times 10 -7 /° C or less.
Claim 2
Dependent Claim
114 words
In a thermal cracking process for converting heavy petroleum residual oil to lighter distillate products in which the thermal cracking of the residual oil takes place in the presence of a hydrogen donor diluent, the improvement wherein the hydrogen donor diluent comprises hydrotreated heavy premium coker gas-oil produced in a premium coking operation utilizing a coke drum pressure of from 10 to 150 psig, a coker furnace transfer line temperature of from 900° to 960° F and a coke drum overhead vapor temperature of from 825° to 900° F and operated at conditions such that the coke produced has a coefficient of thermal expansion of about 5 times 10 -7 /° C or less.
Claim 3
Dependent Claim
44 words
The process of claim 1 wherein the products of the thermal cracking process are fractionated, the gas-oil fraction is passed through a hydrotreater in which said fraction is hydrotreated, and the hydrotreated fraction is recycled as hydrogen donor diluent in said thermal cracking process.
Claim 4
Dependent Claim
57 words
The process of claim 1 wherein the products of the thermal cracking process are fractionated, the gas-oil fraction passed to a premium coker unit, heavy premium coker gas-oil from said coker unit is passed to a hydrotreater for hydrogenation thereof, and the hydrogenated premium coker gas-oil is utilized as hydrogen donor diluent in said thermal cracking process.
Claim 5
Dependent Claim
62 words
The process of claim 1 wherein the products of the thermal cracking process are fractionated, a side stream from said fractionation is passed to a premium coker unit, vapors from said premium coker are returned to said fractionator, and a gas-oil fraction from said fractionator is passed to a hydrotreater for hydrogenation and subsequent reuse as hydrogen donor diluent in said process.
Claim 6
Dependent Claim
26 words
The process of claim 1 wherein said hydrogen donor diluent is a heavy premium coker gas-oil having a boiling range of from 650° to 900° F.
Claim 7
Dependent Claim
49 words
The process of claim 1 wherein said hydrogen donor diluent consists essentially of a mixture of: (a) premium coker gas-oil taken directly from a premium coker unit; and (b) a recycled fraction boiling in the gas-oil range and obtained by fractionation of the products from said thermal cracking process.
Claim 8
Dependent Claim
25 words
The process of claim 1 wherein about one volume of diluent is added to each volume of residual oil fed to said thermal cracking process.
Claim 9
Dependent Claim
50 words
The process of claim 1 wherein the heavy premium coker gas-oil is produced in a premium coking operation utilizing a coke drum pressure of from 30 to 70 psig, a transfer line temperature of from 920°945° F and a coke drum overhead vapor temperature of from 840° to 880° F.
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) | 1981-05-22 | 1981-11-21 | 1982-05-23 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1985-05-22 | 1985-11-21 | 1986-05-23 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1989-05-22 | 1989-11-21 | 1990-05-23 | $7700.00 | Window Closed / Lapsed |