Patent US4332670A successfully refreshed from Google Patents.
US4332670A
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Catalytic dewaxing of middle distillates
Assignee: Mobil Oil AS
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Filing: 1981-01-14
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Granted: 1982-06-01
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Expires: 2001-01-14
Abstract
Abstract The fractionation and stripping equipment of a middle distillate catalytic dewaxing unit may be eliminated by integrating the catalytic dewaxing unit with a catalytic cracking unit. The light cycle oil sidestream from the cat cracker fractionator, bypasses the sidestream stripper and serves as the feed to the catalytic dewaxing unit. The dewaxed product is separated into a gasoline fraction which is recycled for fractionation in the cat cracker fractionator and a fuel oil fraction which is recycled to the cat cracker sidestream stripper for removal of light materials to produce a low pour fuel oil meeting product specifications.
Inventors
- 👤 Michael J. Antal
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-06 13:55
CPC Classifications
C; C10; C10G; C10G45/00; C10G45/58; C10G45/60; C10G45/64; C10G2400/00; C10G2400/06
Claims Analysis
Total Claims: 13
Claim 1
Independent Claim
194 words
In a process for reducing the pour point of a middle distillate boiling in the range of about 320° to about 800° F. of the type wherein the middle distillate is catalytically cracked, fractionated and stripped in a catalytic cracking unit and catalytically dewaxed, the improvement which comprises: (a) recovering the middle distillate subsequent to its being catalytically cracked and fractionated but prior to its being stripped in the catalytic cracking unit, (b) contacting the middle distillate of step (a) with a ZSM-5 type crystalline zeolite under hydrodewaxing conditions to produce a hydrodewaxed middle distillate, (c) recovering a first liquid distillate boiling above about 320° F. from the hydrodewaxed middle distillate of step (b) leaving a first gaseous effluent, (d) recovering a second liquid distillate boiling in the gasoline boiling range from the first gaseous effluent leaving a second gaseous effluent comprising hydrogen and light gaseous hydrocarbons, (e) fractionating the second liquid distillate in the fractionator of the catalytic cracking unit to yield a gasoline product, and (f) stripping the first liquid distillate in the middle distillate stripper of the catalytic cracking unit to yield a middle distillate product having a reduced pour point.
Claim 2
Dependent Claim
194 words
In a process for reducing the pour point of a middle distillate boiling in the range of about 320° to about 800° F. of the type wherein the middle distillate is catalytically cracked, fractionated and stripped in a catalytic cracking unit and catalytically dewaxed, the improvement which comprises: (a) recovering the middle distillate subsequent to its being catalytically cracked and fractionated but prior to its being stripped in the catalytic cracking unit, (b) contacting the middle distillate of step (a) with a ZSM-5 type crystalline zeolite under hydrodewaxing conditions to produce a hydrodewaxed middle distillate, (c) recovering a first liquid distillate boiling above about 320° F. from the hydrodewaxed middle distillate of step (b) leaving a first gaseous effluent, (d) recovering a second liquid distillate boiling in the gasoline boiling range from the first gaseous effluent leaving a second gaseous effluent comprising hydrogen and light gaseous hydrocarbons, (e) fractionating the second liquid distillate in the fractionator of the catalytic cracking unit to yield a gasoline product, and (f) stripping the first liquid distillate in the middle distillate stripper of the catalytic cracking unit to yield a middle distillate product having a reduced pour point.
Claim 3
Dependent Claim
29 words
A process according to claim 1 wherein the middle distillate of step (a) is a light cycle oil having a boiling range between about 400° and about 800° F.
Claim 4
Dependent Claim
38 words
A process according to claim 1 wherein step (c) is conducted by cooling the hydrodewaxed middle distillate to a temperature effective to form the first liquid distillate and separating the first liquid distillate from the first gaseous effluent.
Claim 5
Dependent Claim
38 words
A process according to claim 1 wherein step (d) is conducted by cooling the first gaseous effluent to a temperature effective to form the second liquid distillate and separating the second liquid distillate from the second gaseous effluent.
Claim 6
Dependent Claim
15 words
A process according to claim 1 wherein the stripping of step (f) is steam stripping.
Claim 7
Dependent Claim
14 words
A process according to claim 1 wherein the zeolite of step (b) is ZSM-5.
Claim 8
Dependent Claim
14 words
A process according to claim 1 wherein the zeolite of step (b) is ZSM-11.
Claim 9
Dependent Claim
14 words
A process according to claim 1 wherein the zeolite of step (b) is ZSM-21.
Claim 10
Dependent Claim
14 words
A process according to claim 1 wherein the catalytic cracking is fluid catalytic cracking.
Claim 11
Dependent Claim
14 words
A process according to claim 1 wherein the catalytic cracking is thermofor catalytic cracking.
Claim 12
Dependent Claim
16 words
A process according to claim 1 wherein the second gaseous effluent is recycled to step (b).
Claim 13
Dependent Claim
53 words
A process according to claim 1 wherein the hydrodewaxing conditions of step (b) include a temperature of about 500° to about 900° F., a pressure of about 400 to about 800 psig, a LHSV of about 0.1 to about 10.0 and a hydrogen to hydrocarbon mole ratio of about 2:1 to about 10:1.
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) | 1985-05-31 | 1985-11-30 | 1986-06-01 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1989-05-31 | 1989-11-30 | 1990-06-01 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1993-05-31 | 1993-11-30 | 1994-06-01 | $7700.00 | Window Closed / Lapsed |