CA2536557A1 - Process of hydrocracking petroleum heavy oil - Google Patents
Process of hydrocracking petroleum heavy oil Download PDFInfo
- Publication number
- CA2536557A1 CA2536557A1 CA 2536557 CA2536557A CA2536557A1 CA 2536557 A1 CA2536557 A1 CA 2536557A1 CA 2536557 CA2536557 CA 2536557 CA 2536557 A CA2536557 A CA 2536557A CA 2536557 A1 CA2536557 A1 CA 2536557A1
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- CA
- Canada
- Prior art keywords
- range
- mpag
- phase stream
- bed reactor
- hydrocracking
- 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
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
There is provided a hydrocracking process of a petroleum heavy oil containing a heavy metal, wherein hydrocracking is carried out in a suspended bed reactor with an iron based catalyst, which process allows selective TI removal without addition of a light solvent.
in such process, (1) a reaction product from the reactor is divided, in a high pressure gas-liquid separator, into a gas phase stream and a liquid phase stream under a pressure which is the same as that of the reactor at a temperature of 200°C to 350 C;
(2) the obtained liquid phase stream is divided, in a low pressure gas-liquid separator, into a gas phase stream and a liquid phase stream under a pressure of normal pressure to 1 MPaG at a temperature of 190° C to 340°C;
(3) the obtained liquid phase stream is supplied to a solid-liquid separator of a gravity settling type so as to settle under a pressure of normal pressure to 1 MPaG at a temperature of 190°C to 340°C, whereby an upper layer in the separator is withdrawn from the separator while a lower layer containing the solid component and an oil component is withdrawn from the separator; and (4) a portion or a whole of the obtained upper layer is recycled to the suspended bed reactor.
in such process, (1) a reaction product from the reactor is divided, in a high pressure gas-liquid separator, into a gas phase stream and a liquid phase stream under a pressure which is the same as that of the reactor at a temperature of 200°C to 350 C;
(2) the obtained liquid phase stream is divided, in a low pressure gas-liquid separator, into a gas phase stream and a liquid phase stream under a pressure of normal pressure to 1 MPaG at a temperature of 190° C to 340°C;
(3) the obtained liquid phase stream is supplied to a solid-liquid separator of a gravity settling type so as to settle under a pressure of normal pressure to 1 MPaG at a temperature of 190°C to 340°C, whereby an upper layer in the separator is withdrawn from the separator while a lower layer containing the solid component and an oil component is withdrawn from the separator; and (4) a portion or a whole of the obtained upper layer is recycled to the suspended bed reactor.
Claims (6)
1. A hydrocracking process of a petroleum heavy oil which contains a heavy metal, wherein for such hydrocracking, a suspended bed reactor is used as a reactor and an iron based catalyst are used as a catalyst, which process comprises:
(1) a high pressure gas-liquid separation step wherein a reaction product from the suspended bed reactor is divided into a gas phase stream and a liquid phase stream containing a solid component in a high pressure gas-liquid separator under the conditions of a pressure which is substantially the same as that of the suspended bed reactor and a temperature in the range between 200°C and 350°C;
(2) a low pressure gas-liquid separation step wherein the liquid phase stream obtained in the high pressure gas-liquid separation step is supplied to a low pressure gas-liquid separator and divided into a gas phase stream and a liquid phase stream containing a solid component under the conditions of a pressure in the range between normal pressure and 1 MPaG and a temperature in the range between 190°C and 340°C;
(3) a solid-liquid separation step wherein the liquid phase stream obtained in the low pressure gas-liquid separation step is supplied to a solid-liquid separator of a gravity settling type (settler) so as to settle a solid component under the conditions of a pressure in the range between normal pressure and 1 MPaG and a temperature in the range between 190°C and 340°C, whereby a stream of an upper layer in the settler is withdrawn from an upper part of the settler while a stream containing the solid component and an oil component is withdrawn from an lower part of the settler; and (4) a recycling step wherein a portion or a whole of the stream from the upper part of the settler obtained in the solid-liquid separation step is recycled to the suspended bed reactor.
(1) a high pressure gas-liquid separation step wherein a reaction product from the suspended bed reactor is divided into a gas phase stream and a liquid phase stream containing a solid component in a high pressure gas-liquid separator under the conditions of a pressure which is substantially the same as that of the suspended bed reactor and a temperature in the range between 200°C and 350°C;
(2) a low pressure gas-liquid separation step wherein the liquid phase stream obtained in the high pressure gas-liquid separation step is supplied to a low pressure gas-liquid separator and divided into a gas phase stream and a liquid phase stream containing a solid component under the conditions of a pressure in the range between normal pressure and 1 MPaG and a temperature in the range between 190°C and 340°C;
(3) a solid-liquid separation step wherein the liquid phase stream obtained in the low pressure gas-liquid separation step is supplied to a solid-liquid separator of a gravity settling type (settler) so as to settle a solid component under the conditions of a pressure in the range between normal pressure and 1 MPaG and a temperature in the range between 190°C and 340°C, whereby a stream of an upper layer in the settler is withdrawn from an upper part of the settler while a stream containing the solid component and an oil component is withdrawn from an lower part of the settler; and (4) a recycling step wherein a portion or a whole of the stream from the upper part of the settler obtained in the solid-liquid separation step is recycled to the suspended bed reactor.
2. The hydrocracking process according to claim 1 wherein reaction conditions of the hydrocracking in the suspended bed reactor are a reaction pressure in the range between 6 MPaG and 14 MPaG, a temperature in the range between 430°C and 450°C, and a reaction time in the range between 30 minutes and 120 minutes.
3. The hydrocracking process according to claim 1 or 2 wherein the iron based catalyst for the hydrocracking is a limonite iron ore catalyst having an average particle diameter of not larger than 2 um which is produced with mechanically pulverized in a petroleum based solvent, and an amount of the catalyst added for the hydrocracking is in the range of 0.3 % by mass and 2 % by mass relative to an amount of the petroleum heavy oil which is supplied to the suspended bed reactor.
4. The hydrocracking process according to any one of claims 1 to 3 wherein the temperature condition of the high pressure gas-liquid separation step is in the range between 250°C and 320°C.
5. The hydrocracking process according to any one of claims 1 to 4 wherein the pressure condition is in the range between 0.3 MPaG and 0.5 MPaG and the temperature condition is in the range between 245°C and 315°C in the low pressure gas-liquid separation step, and the pressure condition is in the range between 0.3 MPaG and 0.5 MPaG
and the temperature condition is in the range between 245°C and 315°C in the solid-liquid separation step.
and the temperature condition is in the range between 245°C and 315°C in the solid-liquid separation step.
6. The hydrocracking process according to any one of claims 1 to 5 wherein an amount of the stream to be recycled to the suspended bed reactor is such that an amount of a heavy oil component having a boiling point of not lower than 525°C in said stream is in the range of 10 by mass and 100 % by mass relative to an amount of the petroleum heavy oil which is supplied to the suspended bed reactor.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JPP2005-059263 | 2005-03-03 | ||
| JP2005059263A JP4523458B2 (en) | 2005-03-03 | 2005-03-03 | Hydrocracking method of heavy petroleum oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2536557A1 true CA2536557A1 (en) | 2006-09-03 |
| CA2536557C CA2536557C (en) | 2011-05-24 |
Family
ID=36955316
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2536557A Expired - Fee Related CA2536557C (en) | 2005-03-03 | 2006-02-14 | Process of hydrocracking petroleum heavy oil |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JP4523458B2 (en) |
| BR (1) | BRPI0601018B1 (en) |
| CA (1) | CA2536557C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7820135B2 (en) | 2008-06-30 | 2010-10-26 | Uop Llc | Catalyst composition with nanometer crystallites for slurry hydrocracking |
| US8025793B2 (en) | 2008-06-30 | 2011-09-27 | Uop Llc | Process for using catalyst with rapid formation of iron sulfide in slurry hydrocracking |
| US8062505B2 (en) | 2008-06-30 | 2011-11-22 | Uop Llc | Process for using iron oxide and alumina catalyst with large particle diameter for slurry hydrocracking |
| EP2404649A1 (en) | 2010-07-06 | 2012-01-11 | Total Raffinage Marketing | Flakes management in hydrocarbon processing units |
| US8123933B2 (en) | 2008-06-30 | 2012-02-28 | Uop Llc | Process for using iron oxide and alumina catalyst for slurry hydrocracking |
| US8128810B2 (en) | 2008-06-30 | 2012-03-06 | Uop Llc | Process for using catalyst with nanometer crystallites in slurry hydrocracking |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4813933B2 (en) * | 2006-03-16 | 2011-11-09 | 株式会社神戸製鋼所 | Hydrocracking method of heavy petroleum oil |
| CN105586088B (en) * | 2014-10-23 | 2017-10-20 | 中国石油化工股份有限公司 | A kind of dry gas lime set processing method |
| JP6725112B6 (en) * | 2016-07-29 | 2020-08-19 | 国立研究開発法人産業技術総合研究所 | Method, apparatus, and program for estimating properties of multi-component solution |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4495060A (en) * | 1982-12-27 | 1985-01-22 | Hri, Inc. | Quenching hydrocarbon effluent from catalytic reactor to avoid precipitation of asphaltene compounds |
| CN1077591C (en) * | 1996-03-15 | 2002-01-09 | 加拿大石油公司 | Hydrotreating of heavy hydrocarbon oils with control of particle size of particulate additives |
| JP3875001B2 (en) * | 1999-07-21 | 2007-01-31 | 株式会社神戸製鋼所 | Hydrocracking method of heavy petroleum oil |
-
2005
- 2005-03-03 JP JP2005059263A patent/JP4523458B2/en not_active Expired - Fee Related
-
2006
- 2006-02-14 CA CA2536557A patent/CA2536557C/en not_active Expired - Fee Related
- 2006-03-03 BR BRPI0601018A patent/BRPI0601018B1/en not_active IP Right Cessation
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7820135B2 (en) | 2008-06-30 | 2010-10-26 | Uop Llc | Catalyst composition with nanometer crystallites for slurry hydrocracking |
| US8025793B2 (en) | 2008-06-30 | 2011-09-27 | Uop Llc | Process for using catalyst with rapid formation of iron sulfide in slurry hydrocracking |
| US8062505B2 (en) | 2008-06-30 | 2011-11-22 | Uop Llc | Process for using iron oxide and alumina catalyst with large particle diameter for slurry hydrocracking |
| US8123933B2 (en) | 2008-06-30 | 2012-02-28 | Uop Llc | Process for using iron oxide and alumina catalyst for slurry hydrocracking |
| US8128810B2 (en) | 2008-06-30 | 2012-03-06 | Uop Llc | Process for using catalyst with nanometer crystallites in slurry hydrocracking |
| US8709966B2 (en) | 2008-06-30 | 2014-04-29 | Uop Llc | Catalyst composition with nanometer crystallites for slurry hydrocracking |
| EP2404649A1 (en) | 2010-07-06 | 2012-01-11 | Total Raffinage Marketing | Flakes management in hydrocarbon processing units |
| WO2012004167A1 (en) | 2010-07-06 | 2012-01-12 | Total Raffinage Marketing | Flakes management in hydrocarbon processing units |
Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0601018B1 (en) | 2016-07-19 |
| JP4523458B2 (en) | 2010-08-11 |
| JP2006241317A (en) | 2006-09-14 |
| CA2536557C (en) | 2011-05-24 |
| BRPI0601018A (en) | 2007-05-08 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20210215 |