Patent US4542247A successfully refreshed from Google Patents.
US4542247A
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Conversion of LPG hydrocarbons to distillate fuels or lubes using integration of LPG dehydrogenation and MOGDL
Assignee: Mobil Oil AS
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Filing: 1984-09-14
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Granted: 1985-09-17
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Expires: 2004-09-14
Abstract
Abstract Disclosed is a method and apparatus for producing distillate and/or lubes which employ integrating catalytic (or thermal) dehydrogenation of paraffins with MOGDL. The process feeds the product from a low temperature propane and/or butane dehydrogenation zone into a first catalytic reactor zone, which operates at low pressure and contains zeolite oligomerization catalysts, where the low molecular weight olefins are reacted to primarily gasoline range materials. These gasoline range materials can then be pressurized to the pressure required for reacting to distillate in a second catalytic reactor zone operating at high pressure and containing a zeolite oligomerization catalyst. The distillate is subsequently sent to a hydrotreating unit and product separation zone to form lubes and other finished products.
Inventors
- 👤 Clarence D. Chang
- 👤 Joe E. Penick
- 👤 Richard F. Socha
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-11-03 21:00
CPC Classifications
C; C10; C10G; C10G50/00; C10G50/02
Claims Analysis
Total Claims: 12
Claim 1
Independent Claim
221 words
A method for converting olefins by catalytic oligomerization to produce distillates and lubes which comprise the steps of: (a) passing a paraffinic feed stream into a dehydrogenation zone at conditions of pressure and temperature which favor conversion of paraffins to an olefin rich effluent stream comprising at least one of the group consisting of propylene and butylene; (b) contacting said olefin rich effluent stream in a first catalytic reactor zone with a crystalline zeolite oligomerization catalyst at conditions of pressure and temperature which favor conversion of olefins to a first reactor effluent stream rich in olefinic gasoline; (c) separating said first reactor effluent stream in a first separation zone to form a C 5 + rich stream and a C 4 - rich stream; (d) passing said C 5 + rich stream to a second catalytic reactor zone; (e) contacting said C 5 + rich stream in said second catalytic reactor zone with a crystalline zeolite oligomerization catalyst at temperature and pressure conditions which favor production of a second reactor effluent stream which is rich in distillate; (f) separating the second reactor effluent stream in a second separation zone to recover a olefinic gasoline stream and a distillate stream; and (g) contacting said distillate stream with hydrogen in a hydrotreating unit to produce a hydrotreated distillate stream comprising lube range hydrocarbons.
Claim 2
Independent Claim
221 words
A method for converting olefins by catalytic oligomerization to produce distillates and lubes which comprise the steps of: (a) passing a paraffinic feed stream into a dehydrogenation zone at conditions of pressure and temperature which favor conversion of paraffins to an olefin rich effluent stream comprising at least one of the group consisting of propylene and butylene; (b) contacting said olefin rich effluent stream in a first catalytic reactor zone with a crystalline zeolite oligomerization catalyst at conditions of pressure and temperature which favor conversion of olefins to a first reactor effluent stream rich in olefinic gasoline; (c) separating said first reactor effluent stream in a first separation zone to form a C 5 + rich stream and a C 4 - rich stream; (d) passing said C 5 + rich stream to a second catalytic reactor zone; (e) contacting said C 5 + rich stream in said second catalytic reactor zone with a crystalline zeolite oligomerization catalyst at temperature and pressure conditions which favor production of a second reactor effluent stream which is rich in distillate; (f) separating the second reactor effluent stream in a second separation zone to recover a olefinic gasoline stream and a distillate stream; and (g) contacting said distillate stream with hydrogen in a hydrotreating unit to produce a hydrotreated distillate stream comprising lube range hydrocarbons.
Claim 3
Dependent Claim
25 words
The method of claim 1, further comprising the step of passing said hydrotreated distillate stream to a product separation zone to recover a lubes stream.
Claim 4
Dependent Claim
28 words
The method of claim 1, comprising recycling a portion of said C 4 - rich stream to the dehydrogenation zone as a recycle C 4 - rich stream.
Claim 5
Dependent Claim
26 words
The method of claim 1, wherein each of the catalyst reactor zones comprises a fixed bed downflow pressurized reactor having a porous bed of zeolite catalyst.
Claim 6
Dependent Claim
33 words
The method of claim 1, wherein the first catalytic reactor zone is maintained at a pressure of 10-1000 psia and a temperature of 400°-800° F., and at a space velocity of 0.2-4 WHSV.
Claim 7
Dependent Claim
32 words
The method of claim 5, wherein the first catalytic reactor zone is maintained at a pressure of 10-40 psia, a temperature of 450°-600° F., and at a space velocity of 0.5-1.5 WHSV.
Claim 8
Dependent Claim
33 words
The method of claim 1, wherein the second catalytic reactor zone is maintained at a pressure of 100-3000 psig at a temperature of 350°-600° F. and a space velocity of about 0.1-5 WHSV.
Claim 9
Dependent Claim
19 words
The method of claim 7, wherein the second catalytic reactor zone is maintained at a pressure of 800-2000 psig.
Claim 10
Dependent Claim
30 words
The method of claim 1, wherein the first and second catalytic reactor zones contain at least one catalyst from the group consisting of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35 and ZSM-38.
Claim 11
Dependent Claim
14 words
The method of claim 1, wherein said dehydrogenation zone is a catalytic dehydrogenation zone.
Claim 12
Dependent Claim
14 words
The method of claim 1, wherein said dehydrogenation zone is a thermal dehydrogenation zone.
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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) | 1988-09-16 | 1989-03-18 | 1989-09-17 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1992-09-16 | 1993-03-18 | 1993-09-17 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1996-09-16 | 1997-03-18 | 1997-09-17 | $7700.00 | Window Closed / Lapsed |