CA2370591A1 - Improved process for deasphalting residua by reactive recycle of high boiling material - Google Patents
Improved process for deasphalting residua by reactive recycle of high boiling material Download PDFInfo
- Publication number
- CA2370591A1 CA2370591A1 CA002370591A CA2370591A CA2370591A1 CA 2370591 A1 CA2370591 A1 CA 2370591A1 CA 002370591 A CA002370591 A CA 002370591A CA 2370591 A CA2370591 A CA 2370591A CA 2370591 A1 CA2370591 A1 CA 2370591A1
- Authority
- CA
- Canada
- Prior art keywords
- residence time
- solids
- reaction zone
- fraction
- zone
- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
- C10G9/32—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material according to the "fluidised-bed" technique
-
- 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
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
Abstract
The vaporized fraction is passed via line (11) to soaker drum (2) which is maintained at effective conditions so that the highest boiling materials are condensed out. Typically these conditions will include controlled quenching of vapor fraction just below the dewpoint. A quench stream can also be passed into soaker drum via line (21).
Claims (15)
1. A process for deasphalting an asphalt-containing feedstock in a deasphalting process unit comprised of:
(i) a heating zone wherein solids containing carbonaceous deposits are received from a stripping zone and heated in the presence of a heating gas which may contain oxygen for partial combustion purposes;
(ii) a short vapor residence time reaction zone containing a horizontal moving bed of stirred hot solids recycled from the heating zone and feed, which reaction zone is operated at a temperature from about 450°C to about 700°C and operated under conditions such that the solids residence time and the vapor residence time are independently controlled, which vapor residence time is less than about 5 seconds, and which solids residence is from about 5 to about 60 seconds; and (iii) a stripping zone through which solids having carbonaceous deposits thereon are passed from the reaction zone and wherein lower boiling additional hydrocarbon and volatiles are recovered with a stripping gas;
which process comprises:
(a) feeding the residua feedstock to the short vapor residence time reaction zone wherein it contacts the fluidized and/or stirred hot solids thereby resulting in high Conradson Carbon components and metal-containing components being deposited onto said hot solids, and a vaporized fraction;
(b) separating the vaporized fraction from the solids; and (c) passing the solids to said stripping zone where they are contacted with a stripping gas, thereby removing volatile components therefrom;
(d) passing the stripped solids to a heating zone where they are heated to an effective temperature that will maintain the operating temperature of the reaction zone;
(e) recycling hot solids from the heating zone to the reaction zone where they are contacted with fresh feedstock;
(f) passing the vaporized fraction from step (b) above to a soaker drum where it is quenched to produce a vapor fraction boiling less than about 450-600°C and a high boiling fraction condensate having an initial boiling point in the range of about 450°C to 600°C.
(g) providing sufficient residence time and reactor severity in the soaker drum to permit molecular weight growth reactions to occur;
(h) recycling said high boiling fraction to the short vapor residence time reaction zone; and (i) recovering the vapor fraction having a lower concentration of contaminants from step (h).
(i) a heating zone wherein solids containing carbonaceous deposits are received from a stripping zone and heated in the presence of a heating gas which may contain oxygen for partial combustion purposes;
(ii) a short vapor residence time reaction zone containing a horizontal moving bed of stirred hot solids recycled from the heating zone and feed, which reaction zone is operated at a temperature from about 450°C to about 700°C and operated under conditions such that the solids residence time and the vapor residence time are independently controlled, which vapor residence time is less than about 5 seconds, and which solids residence is from about 5 to about 60 seconds; and (iii) a stripping zone through which solids having carbonaceous deposits thereon are passed from the reaction zone and wherein lower boiling additional hydrocarbon and volatiles are recovered with a stripping gas;
which process comprises:
(a) feeding the residua feedstock to the short vapor residence time reaction zone wherein it contacts the fluidized and/or stirred hot solids thereby resulting in high Conradson Carbon components and metal-containing components being deposited onto said hot solids, and a vaporized fraction;
(b) separating the vaporized fraction from the solids; and (c) passing the solids to said stripping zone where they are contacted with a stripping gas, thereby removing volatile components therefrom;
(d) passing the stripped solids to a heating zone where they are heated to an effective temperature that will maintain the operating temperature of the reaction zone;
(e) recycling hot solids from the heating zone to the reaction zone where they are contacted with fresh feedstock;
(f) passing the vaporized fraction from step (b) above to a soaker drum where it is quenched to produce a vapor fraction boiling less than about 450-600°C and a high boiling fraction condensate having an initial boiling point in the range of about 450°C to 600°C.
(g) providing sufficient residence time and reactor severity in the soaker drum to permit molecular weight growth reactions to occur;
(h) recycling said high boiling fraction to the short vapor residence time reaction zone; and (i) recovering the vapor fraction having a lower concentration of contaminants from step (h).
2. The process of claim 1 wherein the vapor residence time of the short vapor residence time reaction zone is less than about 2 seconds.
3. The process of claim 1 wherein the residua feedstock is selected from the group consisting of vacuum resids, atmospheric resids, heavy and reduced petroleum crude oil; pitch; waste oils; asphalt; bitumen; solvent desphalter residue, and tar sand oil.
4. The process of claim 3 wherein the residua feedstock is a vacuum resid.
5. The process of claim 2 wherein the solids residence time of the short vapor residence time reaction zone is from about 10 to 30 seconds.
6. The process of claim 1 wherein the particles of the short vapor contact time reaction zone are fluidized and/or stirred with the aid of a mechanical means.
7. The process of claim 6 wherein the mechanical means are comprised of a set of horizontally disposed screws within the reactor.
8. The process of claim 1 wherein the soaker drum is operated at a temperature from about 350°C to 520°C and a residence time of about 1 to 60 minutes.
9. The process of claim 8 wherein the soaker drum is operated at a pressure from about 1 to 10 bar.
10. The process of claim 9 wherein the soaker drum is operated at a temperature of about 400° to 450°C and a pressure of about 1 to 3 bar.
11. The process of claim 8 wherein polymerization initiators are added to the soaker drum to increase reaction rates.
12. The process of claim 11 wherein the polymerization initiators are selected from the group consisting of elemental sulfur, peroxides, spent catalyst, coke particles, and air.
13. The process of claim 1 wherein steam, C4 minus, air, or mixtures thereof, is injected into the soaker drum to maintain the solids in slurry suspension and to strip out lower boiling products.
14. The process of claim 1 wherein the soaker drum can be a mechanical mixing device that is operated in plug flow mode and provides self cleaning to minimize coke deposits.
15. The process of claim 1 wherein steam, C4 minus gas, or mixtures thereof, is added to the vaporized fraction from the short residence time reaction zone to reduce its partial pressure and allow condensation of a higher boiling fraction.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US29302999A | 1999-04-16 | 1999-04-16 | |
| US09/293,029 | 1999-04-16 | ||
| PCT/US2000/009607 WO2000063320A1 (en) | 1999-04-16 | 2000-04-11 | Improved process for deasphalting residua by reactive recycle of high boiling material |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2370591A1 true CA2370591A1 (en) | 2000-10-26 |
| CA2370591C CA2370591C (en) | 2011-01-11 |
Family
ID=23127326
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2370591A Expired - Fee Related CA2370591C (en) | 1999-04-16 | 2000-04-11 | Improved process for deasphalting residua by reactive recycle of high boiling material |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP1194498B1 (en) |
| JP (1) | JP4590108B2 (en) |
| CN (1) | CN1347442A (en) |
| AR (1) | AR023503A1 (en) |
| AU (1) | AU771590B2 (en) |
| CA (1) | CA2370591C (en) |
| ES (1) | ES2559272T3 (en) |
| WO (1) | WO2000063320A1 (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020038778A1 (en) | 2000-05-01 | 2002-04-04 | Maa Peter S. | Process for upgrading residua |
| US7033486B2 (en) | 2002-04-01 | 2006-04-25 | Exxonmobil Research And Engineering Company | Residuum conversion process |
| JP5239226B2 (en) * | 2007-06-28 | 2013-07-17 | 株式会社Ｉｈｉ | Heavy fuel reforming method and reformer |
| KR102604852B1 (en) * | 2016-06-14 | 2023-11-21 | 에이씨피 테크놀로지스, 엘엘씨 | Turbulent Mesophase Pitch Processes and Products |
| US10508240B2 (en) | 2017-06-19 | 2019-12-17 | Saudi Arabian Oil Company | Integrated thermal processing for mesophase pitch production, asphaltene removal, and crude oil and residue upgrading |
| US10913901B2 (en) | 2017-09-12 | 2021-02-09 | Saudi Arabian Oil Company | Integrated process for mesophase pitch and petrochemical production |
| JP2021500461A (en) * | 2017-09-12 | 2021-01-07 | サウジ アラビアン オイル カンパニー | Integrated process for mesophase pitch and petrochemicals |
| DE102018213210A1 (en) | 2018-08-07 | 2020-02-13 | Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. | Process for cleaning mineral solids and wood materials, device for this process and its use |
| KR102481197B1 (en) * | 2020-08-13 | 2022-12-27 | 최창균 | Source pitch continuous charging and reformed Precursor pitch continuous discharging device for Pitch Reforming Method |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3334043A (en) * | 1965-09-29 | 1967-08-01 | Sun Oil Co | Neopentane separation of bituminous materials |
| US4054512A (en) * | 1976-10-22 | 1977-10-18 | Exxon Research And Engineering Company | Deasphalting with liquid hydrogen sulfide |
| US4191639A (en) * | 1978-07-31 | 1980-03-04 | Mobil Oil Corporation | Process for deasphalting hydrocarbon oils |
| US4277324A (en) * | 1979-04-13 | 1981-07-07 | Exxon Research & Engineering Co. | Treatment of pitches in carbon artifact manufacture |
| US5714056A (en) * | 1995-07-17 | 1998-02-03 | Exxon Research And Engineering Company | Process for deasphalting residua (HEN9511) |
-
2000
- 2000-04-11 AU AU44542/00A patent/AU771590B2/en not_active Ceased
- 2000-04-11 EP EP00925922.7A patent/EP1194498B1/en not_active Expired - Lifetime
- 2000-04-11 WO PCT/US2000/009607 patent/WO2000063320A1/en active Application Filing
- 2000-04-11 CA CA2370591A patent/CA2370591C/en not_active Expired - Fee Related
- 2000-04-11 ES ES00925922.7T patent/ES2559272T3/en not_active Expired - Lifetime
- 2000-04-11 JP JP2000612401A patent/JP4590108B2/en not_active Expired - Fee Related
- 2000-04-11 CN CN 00806321 patent/CN1347442A/en active Pending
- 2000-04-14 AR ARP000101746 patent/AR023503A1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| CN1347442A (en) | 2002-05-01 |
| AR023503A1 (en) | 2002-09-04 |
| AU4454200A (en) | 2000-11-02 |
| WO2000063320A1 (en) | 2000-10-26 |
| JP2002542375A (en) | 2002-12-10 |
| EP1194498B1 (en) | 2015-11-11 |
| ES2559272T3 (en) | 2016-02-11 |
| EP1194498A4 (en) | 2011-02-16 |
| JP4590108B2 (en) | 2010-12-01 |
| AU771590B2 (en) | 2004-03-25 |
| CA2370591C (en) | 2011-01-11 |
| EP1194498A1 (en) | 2002-04-10 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20150413 |