CA2402126A1 - Production of low sulfur/low aromatics distillates - Google Patents
Production of low sulfur/low aromatics distillates Download PDFInfo
- Publication number
- CA2402126A1 CA2402126A1 CA002402126A CA2402126A CA2402126A1 CA 2402126 A1 CA2402126 A1 CA 2402126A1 CA 002402126 A CA002402126 A CA 002402126A CA 2402126 A CA2402126 A CA 2402126A CA 2402126 A1 CA2402126 A1 CA 2402126A1
- Authority
- CA
- Canada
- Prior art keywords
- stage
- hydrodesulfurization
- stream
- reaction
- product stream
- 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
- C10G65/08—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 hydrogenation of the aromatic hydrocarbons
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- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4081—Recycling aspects
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
A process for producing distillate boiling range streams that are low in both sulfur and aromatics. A distillate feedstock is treated in a first hydrodesulfurization stage in the presence of a hydrogen-containing treat gas and a hydrodesulfurization catalyst, thereby resulting in partial desulfurization of the stream. The partially desulfurized distillate stream is then treated in a second hydrodesulfurization stage, also in the presence of a hydrogen-containing treat gas and a hydrodesulfurization catalyst. The hydrogen-containing treat gas is cascaded from the next downstream reaction stage, which is an aromatics hydrogenation stage.
Claims (26)
1. A multi-stage process for hydrodesulfurizing and hydrogenating a distillate feedstock having a sulfur content greater than about 3,000 wppm, which process comprises:
a) reacting said feedstream in a first hydrodesulfurization stage in the presence of a hydrogen-containing treat gas, said first hydrotreating stage containing one or more reaction zones, each reaction zone operated at hydrodesulfurizing conditions and in the presence of a hydrodesulfurization catalyst, thereby resulting in a liquid product stream having a sulfur content less than about 3,000 wppm;
b) passing the liquid product stream to a first separation zone wherein a vapor phase product stream and a liquid phase product stream are produced;
c) passing the liquid phase product stream to a second hydrodesulfurization stage;
d) reacting said liquid phase product stream in said second hydrodesulfurization stage in the presence of a hydrogen-containing treat gas cascaded from, or partially cascaded from, the next downstream stage herein, said second hydrodesulfurization stage containing one or more reaction zones operated at hydrodesulfurization conditions wherein each reaction zone contains a bed of hydrotreating catalyst, thereby resulting in a liquid product stream having less than about 100 wppm sulfur;
e) passing the liquid product stream from said second hydrodesulfurization stage to a second separation zone wherein a vapor phase stream and a liquid phase stream are produced;
f) collecting said vapor phase stream;
g) passing said liquid phase stream from step e) to an aromatics hydrogenation stage; and h) reacting said liquid phase stream in said aromatics hydrogenation stage in the presence of a hydrogen-containing treat gas, said hydrogenation stage containing one or more reaction zones operated at aromatics hydrogenation conditions wherein each reaction zone contains a bed of aromatics hydrogenation catalyst, thereby resulting in a liquid product stream having substantially reduced levels of sulfur and aromatics, and a hydrogen-containing product stream that is cascaded to an upstream hydrodesulfurization stage.
a) reacting said feedstream in a first hydrodesulfurization stage in the presence of a hydrogen-containing treat gas, said first hydrotreating stage containing one or more reaction zones, each reaction zone operated at hydrodesulfurizing conditions and in the presence of a hydrodesulfurization catalyst, thereby resulting in a liquid product stream having a sulfur content less than about 3,000 wppm;
b) passing the liquid product stream to a first separation zone wherein a vapor phase product stream and a liquid phase product stream are produced;
c) passing the liquid phase product stream to a second hydrodesulfurization stage;
d) reacting said liquid phase product stream in said second hydrodesulfurization stage in the presence of a hydrogen-containing treat gas cascaded from, or partially cascaded from, the next downstream stage herein, said second hydrodesulfurization stage containing one or more reaction zones operated at hydrodesulfurization conditions wherein each reaction zone contains a bed of hydrotreating catalyst, thereby resulting in a liquid product stream having less than about 100 wppm sulfur;
e) passing the liquid product stream from said second hydrodesulfurization stage to a second separation zone wherein a vapor phase stream and a liquid phase stream are produced;
f) collecting said vapor phase stream;
g) passing said liquid phase stream from step e) to an aromatics hydrogenation stage; and h) reacting said liquid phase stream in said aromatics hydrogenation stage in the presence of a hydrogen-containing treat gas, said hydrogenation stage containing one or more reaction zones operated at aromatics hydrogenation conditions wherein each reaction zone contains a bed of aromatics hydrogenation catalyst, thereby resulting in a liquid product stream having substantially reduced levels of sulfur and aromatics, and a hydrogen-containing product stream that is cascaded to an upstream hydrodesulfurization stage.
2. The process of claim 1 wherein step d) is performed so that the liquid product stream contains less than about 50 wppm sulfur.
3. The process of claim 2 wherein step d) is performed so that the liquid product stream contains less than about 25 wppm sulfur.
4. The process of claim 1 wherein the catalyst of said first and second hydrodesulfurization stages are selected from catalysts comprised of at least one Group VI and at least one Group VIII metal on an inorganic refractory support.
5. The process of claim 4 wherein the Group VI metal is selected from Mo and W and the Group VIII metal is selected from Ni and Co.
6. The process of claim 1 wherein at least a portion of the vapor phase stream from said first separation stage is recycled to said first hydrodesulfurization stage.
7. The process of claim 1 wherein at least a portion of the vapor phase stream from said second separation stage is recycled to said first hydrodesulfurization stage.
8. The process of claim 1 wherein the rate of introduction of hydrogen portion of the treat gas in the second reaction stage is less than or equal to 3 times the chemical hydrogen consumption in said second reaction stage.
9. The process of claim 8 wherein the rate of introduction of treat gas in the second reaction stage is less than or equal to 2 times the chemical hydrogen consumption in said second reaction stage.
10. The process of claim 1 wherein said second hydrodesulfurization stage contains two or more reaction zones operated at different temperatures, wherein at least one of said reaction zones is operated at least about 25°C
lower in temperature than the other reaction zone or zones.
lower in temperature than the other reaction zone or zones.
11. The process of claim 10 wherein said second hydrodesulfurization stage contains two or more different reaction zones wherein at least one of said reaction zones is operated at least about 50°C lower in temperature than the other reaction zone or zones.
12. The process of claim 10 wherein the last downstream reaction zone of said second hydrodesulfurization stage, with respect to the flow of feedstock, is the lower temperature zone.
13. The process of claim 1 wherein said hydrogenation stage contains two or more reaction zones operated at different temperature wherein at least one of said reaction zones is operated at least about 25°C lower in temperature than the other reaction zone or zones.
14. The process of claim 13 wherein said hydrogenation stage contains two or more different reaction zones wherein at least one of said reaction zones is operated at least about 50°C lower in temperature than the other reaction zone or zones.
15. The process of claim 13 wherein the last downstream reaction zone with respect to the flow of feedstock is the lower temperature reaction zone.
16. The process of claim 1 wherein the hydrogen-containing treat gas and said liquid phase stream of said aromatics hydrogenation stage flow countercurrent to each other.
17. The process of claim 16 wherein said liquid phase stream of step e), prior to being passed to said aromatics hydrogenation stage, is passed to a stripping stage wherein it is contacted with countercurrent flowing hydrogena containing treat gas in the substantial absence of catalyst.
18. The process of claim 1 wherein the Vapor phase stream from the second hydrodesulfurization reaction stage is cooled and the resulting condensed liquid stream is separated from the remaining uncondensed stream, and a portion of the condensed liquid stream is combined with the liquid feed to the aromatics hydrogenation stage.
19. The process of claim 1 wherein the aromatics hydrogenation catalyst is selected from those comprised of a noble metal on an inorganic refractory support.
20. The process of claim 19 wherein the noble metal is selected from Pt and Pd.
21. The process of claim 20 wherein the support is alumina.
22. The process of claim 20 wherein the support is a zeolitic material.
23. A distillate fuel product produced by the process of claim 1.
24. The process of claim 1, further comprising combining the liquid product stream of step (h) with at least one of (i) one or more lubricity aid, (ii) one or more viscosity modifier, (iii) one or more antioxidant, (iv) one or more cetane improver, (v) one or more dispersant, (vi) one or more cold flow improver, (vii) one or more metals deactivator, (viii) one or more corrosion inhibitor, (ix) one or more detergent, and (x) one or more distillate or upgraded distillate.
25. A distillate fuel product produced by the process of claim 24.
26. The process of claim 1 wherein the treat gas provided to the aromatics hydrogenation stage is a once-through treat gas.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US09/553,374 | 2000-04-20 | ||
| US09/553,374 US6824673B1 (en) | 1998-12-08 | 2000-04-20 | Production of low sulfur/low aromatics distillates |
| PCT/US2001/012517 WO2001081507A1 (en) | 2000-04-20 | 2001-04-17 | Production of low sulfur/low aromatics distillates |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2402126A1 true CA2402126A1 (en) | 2001-11-01 |
| CA2402126C CA2402126C (en) | 2010-06-22 |
Family
ID=24209164
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2402126A Expired - Lifetime CA2402126C (en) | 2000-04-20 | 2001-04-17 | Production of low sulfur/low aromatics distillates |
Country Status (6)
| Country | Link |
|---|---|
| EP (1) | EP1409612A4 (en) |
| JP (1) | JP4856837B2 (en) |
| AU (2) | AU5165801A (en) |
| CA (1) | CA2402126C (en) |
| NO (1) | NO20025017L (en) |
| WO (1) | WO2001081507A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020148757A1 (en) * | 2001-02-08 | 2002-10-17 | Huff George A. | Hydrotreating of components for refinery blending of transportation fuels |
| JP2007100013A (en) * | 2005-10-07 | 2007-04-19 | Petroleum Energy Center | Method for hydrorefining of gas oil |
| US20140174988A1 (en) * | 2012-12-21 | 2014-06-26 | Exxonmobil Research And Engineering Company | Hydroprocessing configuration for low sulfur diesel |
| SA121430164B1 (en) * | 2020-09-21 | 2024-01-18 | انديان اويل كوربوريشن ليمتد | A Process and a System for Production of Multiple Grade De-Aromatized Solvents from Hydroc |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8910711D0 (en) * | 1989-05-10 | 1989-06-28 | Davy Mckee London | Process |
| JP2519191B2 (en) * | 1990-04-10 | 1996-07-31 | 触媒化成工業株式会社 | Kerosene oil hydrotreating method |
| US5114562A (en) * | 1990-08-03 | 1992-05-19 | Uop | Two-stage hydrodesulfurization and hydrogenation process for distillate hydrocarbons |
| FR2757532B1 (en) * | 1996-12-20 | 1999-02-19 | Inst Francais Du Petrole | PROCESS FOR THE CONVERSION OF A GAS CUT TO PRODUCE FUEL WITH A HIGH INDEX OF CETANE, DESAROMATISED AND DESULPHURIZED |
| US5720872A (en) * | 1996-12-31 | 1998-02-24 | Exxon Research And Engineering Company | Multi-stage hydroprocessing with multi-stage stripping in a single stripper vessel |
| US6103104A (en) * | 1998-05-07 | 2000-08-15 | Exxon Research And Engineering Company | Multi-stage hydroprocessing of middle distillates to avoid color bodies |
-
2001
- 2001-04-17 CA CA2402126A patent/CA2402126C/en not_active Expired - Lifetime
- 2001-04-17 WO PCT/US2001/012517 patent/WO2001081507A1/en active Application Filing
- 2001-04-17 JP JP2001578581A patent/JP4856837B2/en not_active Expired - Fee Related
- 2001-04-17 EP EP01925060A patent/EP1409612A4/en not_active Withdrawn
- 2001-04-17 AU AU5165801A patent/AU5165801A/en active Pending
- 2001-04-17 AU AU2001251658A patent/AU2001251658B2/en not_active Expired
-
2002
- 2002-10-18 NO NO20025017A patent/NO20025017L/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| AU2001251658B2 (en) | 2006-03-02 |
| NO20025017D0 (en) | 2002-10-18 |
| NO20025017L (en) | 2002-12-18 |
| CA2402126C (en) | 2010-06-22 |
| JP2003531275A (en) | 2003-10-21 |
| JP4856837B2 (en) | 2012-01-18 |
| EP1409612A1 (en) | 2004-04-21 |
| AU5165801A (en) | 2001-11-07 |
| EP1409612A4 (en) | 2004-06-16 |
| WO2001081507A1 (en) | 2001-11-01 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKEX | Expiry |
Effective date: 20210419 |