CA2397810A1 - Quenching dewaxing reactor with heavy dewaxate recycle - Google Patents
Quenching dewaxing reactor with heavy dewaxate recycle Download PDFInfo
- Publication number
- CA2397810A1 CA2397810A1 CA002397810A CA2397810A CA2397810A1 CA 2397810 A1 CA2397810 A1 CA 2397810A1 CA 002397810 A CA002397810 A CA 002397810A CA 2397810 A CA2397810 A CA 2397810A CA 2397810 A1 CA2397810 A1 CA 2397810A1
- Authority
- CA
- Canada
- Prior art keywords
- process according
- dewaxing
- hydrocarbons
- dewaxate
- waxy
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
- C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
During catalytic dewaxing of paraffinic hydrocarbons, the exothermic catalytic dewaxing reaction is moderated by separating and cooling a heavy dewaxate having an initial boiling point of at least 800 °F+, and recycling it back into the dewaxing zone as quench liquid. The heavy dewaxate reacts very little, if at all, with the hydrogen in the dewaxing zone. This has been found to be particularly useful for dewaxing hydroisomerized, paraffinic Fischer-Tropsch synthesized, hydrocarbons.
Claims (22)
1. A catalytic dewaxing process comprises contacting a waxy, paraffinic hydrocarbon feed with hydrogen, in the presence of a dewaxing catalyst in a catalytic dewaxing zone, at conditions of elevated temperature and pressure effective for the hydrogen to react with said feed and produce a dewaxate of reduced pour point, which includes a heavy fraction, separating and cooling at least a portion of said heavy fraction, and passing it back into said dewaxing zone as a quench liquid for temperature control.
2. A process according to claim 1 wherein said heavy dewaxate fraction has an initial boiling point in the range of from 800-950°F.
3. A process according to claim 2 wherein said waxy feed comprises hydrocarbons having an initial boiling point in the range of 650-750°F.
4. A process according to claim 3 wherein said waxy feed has an end boiling point of at least 1050°F.
5. A process according to claim 4 wherein said waxy feed comprises a hydroisomerate.
6. A process according to claim 5 wherein said dewaxing catalyst comprises at least one catalytic metal component and at least one acidic, microcrystalline aluminosilicate component.
7. A process according to claim 7 wherein said catalytic metal component comprises at least one metal from Group VIII.
8. A process according to claim 7 wherein said metal component comprises a noble metal component.
9. A process according to claim 8 wherein said waxy feed is derived from Fischer-Tropsch synthesized hydrocarbons.
10. A process according to claim 8 wherein said waxy feed is derived from a slack wax or a hydrocrackate which has been treated to remove non-paraffinic hydrocarbons and heteroatom compounds.
11. A process according to claim 10 wherein said waxy feed has been hydroisomerized.
12. A process according to claim 8 wherein said catalyst comprises Pt and H-mordenite.
13. An integrated process for synthesizing a waxy, paraffinic hydrocarbon fraction from a synthesis gas comprising a mixture of H2 and CO, hydroisomerizing said waxy fraction to form a hydroisomerate and catalytically dewaxing said hydroisomerate in a dewaxing zone, to form a dewaxate of reduced pour point which contains a heavy dewaxate fraction, a portion of which is cooled and used as quench liquid in said dewaxing zone, said process comprising:
(a) reacting said mixture of H2 and CO in the presence of a Fischer-Tropsch hydrocarbon synthesis catalyst containing a catalytic cobalt component, at reaction conditions effective to form high purity, paraffinic, waxy hydrocarbons, at least a portion of which are liquid at said reaction conditions;
(b) passing said waxy hydrocarbons it into a hydroisomerization reaction zone;
(c) reacting said waxy hydrocarbons with hydrogen in the presence of a dual functional hydroisomerization catalyst in said hydroisomerization reaction zone to form a hydroisomerate comprising hydrocarbons having an initial boiling point in the range of 650-750°F and an end boiling point of at least 1050°F;
(d) catalytically dewaxing said hydroisomerate in a catalytic dewaxing zone to reduce its pour point, by reacting it with hydrogen at elevated temperature and pressure, in the presence of a catalyst comprising a Group VIII
catalytic metal component and a crystalline aluminosilicate component, to form a dewaxate comprising hydrocarbons having an initial boiling point above and below said 650-750°F range, which includes heavy hydrocarbons having an initial boiling point in the range of 800-950°F;
(e) separating at least a portion of said heavy hydrocarbon dewaxate from the rest of said dewaxate;
(f) cooling at least a portion of said separated heavy hydrocarbon dewaxate to a temperature below that in said catalytic dewaxing zone, and (g) passing said cool dewaxate back into said dewaxing reaction zone as quench liquid.
(a) reacting said mixture of H2 and CO in the presence of a Fischer-Tropsch hydrocarbon synthesis catalyst containing a catalytic cobalt component, at reaction conditions effective to form high purity, paraffinic, waxy hydrocarbons, at least a portion of which are liquid at said reaction conditions;
(b) passing said waxy hydrocarbons it into a hydroisomerization reaction zone;
(c) reacting said waxy hydrocarbons with hydrogen in the presence of a dual functional hydroisomerization catalyst in said hydroisomerization reaction zone to form a hydroisomerate comprising hydrocarbons having an initial boiling point in the range of 650-750°F and an end boiling point of at least 1050°F;
(d) catalytically dewaxing said hydroisomerate in a catalytic dewaxing zone to reduce its pour point, by reacting it with hydrogen at elevated temperature and pressure, in the presence of a catalyst comprising a Group VIII
catalytic metal component and a crystalline aluminosilicate component, to form a dewaxate comprising hydrocarbons having an initial boiling point above and below said 650-750°F range, which includes heavy hydrocarbons having an initial boiling point in the range of 800-950°F;
(e) separating at least a portion of said heavy hydrocarbon dewaxate from the rest of said dewaxate;
(f) cooling at least a portion of said separated heavy hydrocarbon dewaxate to a temperature below that in said catalytic dewaxing zone, and (g) passing said cool dewaxate back into said dewaxing reaction zone as quench liquid.
14. A slurry hydrocarbon synthesis process according to claim 13, wherein said H2 and CO react in a slurry comprising a hydrocarbon slurry liquid, gas bubbles and a particulate hydrocarbon synthesis catalyst and wherein said slurry liquid comprises synthesized hydrocarbons that are liquid at the reaction conditions, and wherein said slurry liquid is withdrawn from said slurry, and passed into said hydroisomerization reaction zone in step (b).
15. A process according to claim 14 wherein said quench liquid reduces the temperature in said dewaxing zone.
16. A process according too claim 15 wherein said waxy synthesized hydrocarbon fraction comprises hydrocarbons having an initial boiling point in said 650-750°F range and an end point of at least 1050°F.
17. A process according to claim 16 wherein said hydroisomerization catalyst comprises a Group VIII non-noble metal catalytic component and an acid support.
18. A process according to claim 17 wherein said dewaxing catalyst comprises a zeolite component and a noble metal component.
19. A process according to claim 18 wherein said dewaxing catalyst comprises Pt and H-mordenite.
20. A process according to claim 18 wherein said hydroisomerization catalyst comprises a cobalt and a molybdenum catalytic metal component and said support comprises alumina-silica having no more than 30 wt. % silica.
21. A process according to claim 14 wherein said slurry liquid comprises 650-750°F- hydrocarbons, at least a portion of which are removed before said liquid is hydroisomerized.
22. A process according to claim 13 wherein said heavy dewaxate fraction has an end boiling point above 1050°F.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US49743900A | 2000-02-03 | 2000-02-03 | |
| US09/497,439 | 2000-02-03 | ||
| PCT/US2001/001703 WO2001057158A1 (en) | 2000-02-03 | 2001-01-18 | Quenching dewaxing reactor with heavy dewaxate recycle |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2397810A1 true CA2397810A1 (en) | 2001-08-09 |
| CA2397810C CA2397810C (en) | 2010-04-27 |
Family
ID=23976875
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2397810A Expired - Fee Related CA2397810C (en) | 2000-02-03 | 2001-01-18 | Quenching dewaxing reactor with heavy dewaxate recycle |
Country Status (13)
| Country | Link |
|---|---|
| EP (1) | EP1254198B1 (en) |
| JP (1) | JP2003522250A (en) |
| AR (1) | AR029033A1 (en) |
| AT (1) | ATE322529T1 (en) |
| AU (1) | AU778654B2 (en) |
| BR (1) | BR0108018A (en) |
| CA (1) | CA2397810C (en) |
| DE (1) | DE60118528T2 (en) |
| DK (1) | DK1254198T3 (en) |
| ES (1) | ES2261375T3 (en) |
| MY (1) | MY137743A (en) |
| NO (1) | NO20023683L (en) |
| WO (1) | WO2001057158A1 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6589415B2 (en) | 2001-04-04 | 2003-07-08 | Chevron U.S.A., Inc. | Liquid or two-phase quenching fluid for multi-bed hydroprocessing reactor |
| US6583186B2 (en) | 2001-04-04 | 2003-06-24 | Chevron U.S.A. Inc. | Method for upgrading Fischer-Tropsch wax using split-feed hydrocracking/hydrotreating |
| US6656342B2 (en) | 2001-04-04 | 2003-12-02 | Chevron U.S.A. Inc. | Graded catalyst bed for split-feed hydrocracking/hydrotreating |
| US20040065584A1 (en) * | 2002-10-08 | 2004-04-08 | Bishop Adeana Richelle | Heavy lube oil from fischer- tropsch wax |
| US10227536B2 (en) * | 2014-12-01 | 2019-03-12 | Uop Llc | Methods for alternating production of distillate fuels and lube basestocks from heavy hydrocarbon feed |
| US10472581B2 (en) * | 2016-06-30 | 2019-11-12 | Uop Llc | Process and apparatus for hydrocracking and hydroisomerizing a hydrocarbon stream |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4681674A (en) * | 1985-11-07 | 1987-07-21 | Mobil Oil Corporation | Fixed bed catalytic reactor system with improved liquid distribution |
| US5246568A (en) * | 1989-06-01 | 1993-09-21 | Mobil Oil Corporation | Catalytic dewaxing process |
| US5885438A (en) * | 1993-02-12 | 1999-03-23 | Mobil Oil Corporation | Wax hydroisomerization process |
| JP3119489B2 (en) * | 1995-12-26 | 2000-12-18 | ジ・エム・ダブリュー・ケロッグ・カンパニー | Integrated hydroprocessing with separation and recycling |
| JPH11189775A (en) * | 1997-12-26 | 1999-07-13 | Japan Energy Corp | Production of low-fluid point oil |
| JP2002503755A (en) * | 1998-02-13 | 2002-02-05 | エクソンモービル リサーチ アンド エンジニアリング カンパニー | Base oil for lubrication excellent in low temperature characteristics and method for producing the same |
-
2001
- 2001-01-18 AT AT01903113T patent/ATE322529T1/en not_active IP Right Cessation
- 2001-01-18 JP JP2001557978A patent/JP2003522250A/en active Pending
- 2001-01-18 BR BR0108018-0A patent/BR0108018A/en not_active Application Discontinuation
- 2001-01-18 AU AU30970/01A patent/AU778654B2/en not_active Ceased
- 2001-01-18 CA CA2397810A patent/CA2397810C/en not_active Expired - Fee Related
- 2001-01-18 WO PCT/US2001/001703 patent/WO2001057158A1/en active IP Right Grant
- 2001-01-18 ES ES01903113T patent/ES2261375T3/en not_active Expired - Lifetime
- 2001-01-18 DE DE60118528T patent/DE60118528T2/en not_active Expired - Lifetime
- 2001-01-18 DK DK01903113T patent/DK1254198T3/en active
- 2001-01-18 EP EP01903113A patent/EP1254198B1/en not_active Expired - Lifetime
- 2001-01-29 AR ARP010100399A patent/AR029033A1/en unknown
- 2001-01-30 MY MYPI20010389A patent/MY137743A/en unknown
-
2002
- 2002-08-02 NO NO20023683A patent/NO20023683L/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| DK1254198T3 (en) | 2006-07-31 |
| ES2261375T3 (en) | 2006-11-16 |
| ATE322529T1 (en) | 2006-04-15 |
| EP1254198A1 (en) | 2002-11-06 |
| BR0108018A (en) | 2002-10-29 |
| AU778654B2 (en) | 2004-12-16 |
| EP1254198B1 (en) | 2006-04-05 |
| DE60118528D1 (en) | 2006-05-18 |
| MY137743A (en) | 2009-03-31 |
| JP2003522250A (en) | 2003-07-22 |
| AU3097001A (en) | 2001-08-14 |
| AR029033A1 (en) | 2003-06-04 |
| DE60118528T2 (en) | 2006-11-02 |
| NO20023683D0 (en) | 2002-08-02 |
| CA2397810C (en) | 2010-04-27 |
| NO20023683L (en) | 2002-09-27 |
| WO2001057158A1 (en) | 2001-08-09 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20130118 |