EP0403087A1 - Conversion increase of vacuum residuums - Google Patents
Conversion increase of vacuum residuums Download PDFInfo
- Publication number
- EP0403087A1 EP0403087A1 EP90305447A EP90305447A EP0403087A1 EP 0403087 A1 EP0403087 A1 EP 0403087A1 EP 90305447 A EP90305447 A EP 90305447A EP 90305447 A EP90305447 A EP 90305447A EP 0403087 A1 EP0403087 A1 EP 0403087A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- vacuum residuum
- bottoms
- cosolvent
- unconverted
- 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.)
- Withdrawn
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/049—The hydrotreatment being a hydrocracking
Definitions
- This invention relates to a process for the conversion of vacuum residua in a hydrocracking operation. More particularly, it relates to the treatment of unconverted vacuum residua to remove the most undesired asphaltenic materials therefrom in order to increase the conversion of the vacuum residue virgin feed.
- a problem with obtaining a good or better conversion is the amount of asphaltenes or asphaltenic materials which are deficient in hydrogen and have a high trace metals content.
- the effective conversion of the remaining 1000°F material, as well as the original vacuum residum chargestock may be significantly enhanced.
- U.S. Patent Re. 32,265 discloses a hydrogenation process using at least one fluidized catalytic stage and a recycle material of heavy hydrogenated effluent.
- the heavy effluent material is cooled to a temperature within 350-600°F to separate toluene and heptane insoluble coke precursors prior to recycle. This separation may be enhanced by the use of centrifugation, filtration or a bed of particulate material, e.g., calcined coke.
- U.S. Patent 4,411,768 discloses a higher conversion in a process for upgrading high boiling hydrocarbon materials to valuable lower boiling hydrocarbon materials in an ebullated catalytic bed wherein recycle is recovered from the upgraded product and at least 25 percent by volume of the recycle is comprised of the 950°F plus components of the product.
- the liquid recycle is cooled to a temperature of 350°F to 700°F to separate coke precursors from the liquid recycle on a bed of particulate solids prior to recycling it back to the hydrogenation zone.
- U.S. Patent 4,305,814 discloses an energy efficient process for separating a hydrocarbonaceous material into various fractions employing solvents at elevated temperatures and pressures.
- the solvent composition comprises at least one member selected from the group of paraffinic hydrocarbons containing from 3 through 9 carbon atoms, mono-olfin hydrocarbons containing from 4 through 8 carbon atoms, aromatic hydrocarbons having a normal boiling point temperature below about 350°F and alcohols containing from 3 through 9 carbon atoms.
- the particular amount of asphaltenes or sediment that should be removed to obtain a deasphalted oil that has excellent recycle properties is not disclosed.
- U.S. Patent 4,502,944 discloses a method of separating a process material comprising oils, resins and asphaltenes into at least three fractions. Method employs light organic solvents (paraffinic hydrocarbons preferably having between 3 and 8 carbon atoms in a solvent/process material ratio of at least about 3:1) under elevated temperature and pressure conditions. As in U.S. Patent 4,305,814, the particular amount of asphaltenes or sediment that should be removed to obtain a deasphalted oil that has excellent recycle properties is not disclosed.
- U.S. Patent 3,412,010 discloses that the conversion of a vacuum residuum in a hydrocracker is improved by recycling the 680-975°F cut and the 975° plus residue back to the reactor. No mention of removing coke precursors or asphaltenes in the recycle streams is provided.
- U.S. Patent 3,905,892 discloses a process for hydrocracking vacuum residuum wherein the 975°F plus product may be recycled after removing the asphaltenes. The latter is partially oxidized to yield hydrogen for providing make-up hydrogen for the hydrocracking reactor. The effect of deasphalting conditions on product yields when the deasphalted oil is recycled is not disclosed.
- U.S. Patent 4,457,830 discloses the use of inorganic acids for precipitating and decomposing preasphaltenes and coprecipitating solids. The effect of deasphalting conditions on product yields when the deasphalted oil is recycled is not disclosed.
- the present invention provides an improvement in a method for conversion of a vacuum residuum feed in a hydrocracking operation which comprises upgrading the vacuum residuum feed, recovering and separating distillates from the remaining vacuum residuum feed and recycling unconverted vacuum residuum bottoms to the upgrading zone.
- the improvement comprises deasphalting the unconverted asphaltene- containing unconverted vacuum residuum bottoms in the recycle stream by treating said unconverted vacuum residuum bottoms in an extraction zone with a cosolvent under ambient conditions to a related temperature (and sufficient pressure wherein the recycle stream and cosolvent are maintained in a liquid state), whereby the most undesirable hydrogen deficient asphaltenes are selectively removed from the unconverted vacuum residuum bottoms to increase the overall conversion of the vacuum residuum feed.
- the present invention for improving the conversion of a virgin vacuum residuum into a useful product suggests the treatment of the unconverted vacuum bottoms after separating it from the cracked reaction distillate product in the reactor effluent. Then the treated vacuum bottoms, less the most undesirable hydrogen deficient asphaltenes and a majority of the trace metals, is recycled back to the reaction zone to be converted to additional quantities of the desired distillate products, i.e. naphtha, diesel fuel and vacuum gas oil.
- the latter stream is used to make additional naphtha and diesel fuel by using it as a charge stock component for a fluidized catalytic cracking unit.
- the improvement provided by the present invention is the treatment of the unconverted vacuum bottoms with a cosolvent to selectively remove most of the undesirable hydrogen deficient asphaltenes from the vacuum bottoms prior to their being recycled to the reactor, i.e., reaction zone, for further hydrocracking.
- the amount of the most undesirable hydrogen deficient asphaltenes to be selectively removed ranges from about 10 percent to about 20 percent.
- the amount of cosolvent used is defined as the volume ratio of cosolvent to unconverted vacuum bottoms and ranges from about 1:1 to about 40:1.
- the aromatics being benzene and toluene.
- a sample of the untreated unconverted vacuum bottoms and various deasphalted oils from the same unconverted vacuum bottoms sample were processed in a continuous stirred tank reactor (CSTR) at a catalyst space velocity of 0.13 bbl/lb/day at successive temperatures of 795, 805 and 815°F over an Mo/A1203 catalyst that mimics the steady-state activity of a commercial NiMo/A1203.
- the CSTR pressure was held at 2,250 psig with hydrogen and an H2 treatment rate of 7,000 SCF/bbl.
- n-heptane deasphalted vacuum bottoms sample provides a much improved recycle stream for a residuum hydrocracking process designed to upgrade 1000°F and above boiling point components. Not only is the allowable conversion increased at a given temperature but, essentially, no sediment is formed. The latter is very important for reducing catalyst poisoning and minimizing plugging problems on account of sediment formation and deposition in flow control valves, heat exchangers and separation vessels downstream from the reaction zone.
- deasphalting the vacuum bottoms recycle stream with n-heptane versus the other solvents allows the reactor temperature to be increased by at least 10°F to further improve hydrocracking conversion without causing additional sediment.
- Deasphalting vacuum bottoms with toluene shows a negligible improvement in the overall conversion of the 1000°F plus boiling point components compared with the untreated vacuum bottoms and essentially no improvement in reducing sediment formation as measured by Soxhlet extractions with toluene.
- the cyclohexane deasphalted vacuum bottoms provides an intermediate valued recycle stream in that the conversion is significantly improved over the untreated or toluene deasphalted vacuum bottoms but sediment begins to form in the reactor effluent as the reactor temperature is raised to provide a better overall conversion of the components boiling above 1000°F.
- n-heptane deasphalted vacuum bottoms improves conversion without causing any additional sediment
- the n-pentane deasphalted vacuum bottoms would do as well but there would be the additional amount of asphaltenes to be disposed of. Consequently, it is proposed that deasphalting with n-heptane provides a standard for determining how much of the asphaltene phase should be removed for a given vacuum bottoms stream if a mixed solvent comprising paraffins and naphthenes with some aromatics is being used.
- Another reason for not removing more of the sediment than necessary is to avoid removing the lighter asphaltenes containing a higher proportion of hydrogen and less carbon since the number of condensed aromatics is less.
- the lighter asphaltenes crack more easily and thereby help to improve the overall conversion of the 1000°F plus boiling point components.
Abstract
The conversion of a vacuum residuum feed in a hydrocracking operation comprising hydrocracking said feed vacuum residuum in a hydrocracking zone, recovering and separating distillates from the hydrocracking zone, and recycling a stream of unconverted vacuum residuum bottoms to the hydrocracking zone, can be increased by deasphalting unconverted vacuum residuum bottoms in the recycle stream by treatment in an extraction zone with a cosolvent (e.g. n-heptane) at ambient or elevated temperature, and a pressure sufficient to maintain the cosolvent in the liquid state. The most undesirable sediments are selectively removed from said unconverted vacuum residuum bottoms to increase the conversion of said vacuum residuum feed.
Description
- This invention relates to a process for the conversion of vacuum residua in a hydrocracking operation. More particularly, it relates to the treatment of unconverted vacuum residua to remove the most undesired asphaltenic materials therefrom in order to increase the conversion of the vacuum residue virgin feed.
- In converting heavy vacuum residua, e.g., in a hydrocracking operation, a problem with obtaining a good or better conversion is the amount of asphaltenes or asphaltenic materials which are deficient in hydrogen and have a high trace metals content. In selectively removing a major portion of the more hydrogen deficient asphaltenes from the unconverted 1000°F plus material, the effective conversion of the remaining 1000°F material, as well as the original vacuum residum chargestock, may be significantly enhanced.
- Thus, it is an object of the present invention to provide a means of treating the unconverted vacuum bottoms to obtain the optimum conversion of virgin vacuum residuum.
- U.S. Patent Re. 32,265 discloses a hydrogenation process using at least one fluidized catalytic stage and a recycle material of heavy hydrogenated effluent. The heavy effluent material is cooled to a temperature within 350-600°F to separate toluene and heptane insoluble coke precursors prior to recycle. This separation may be enhanced by the use of centrifugation, filtration or a bed of particulate material, e.g., calcined coke.
- U.S. Patent 4,411,768 discloses a higher conversion in a process for upgrading high boiling hydrocarbon materials to valuable lower boiling hydrocarbon materials in an ebullated catalytic bed wherein recycle is recovered from the upgraded product and at least 25 percent by volume of the recycle is comprised of the 950°F plus components of the product. The liquid recycle is cooled to a temperature of 350°F to 700°F to separate coke precursors from the liquid recycle on a bed of particulate solids prior to recycling it back to the hydrogenation zone.
- U.S. Patent 4,305,814 discloses discloses an energy efficient process for separating a hydrocarbonaceous material into various fractions employing solvents at elevated temperatures and pressures. The solvent composition comprises at least one member selected from the group of paraffinic hydrocarbons containing from 3 through 9 carbon atoms, mono-olfin hydrocarbons containing from 4 through 8 carbon atoms, aromatic hydrocarbons having a normal boiling point temperature below about 350°F and alcohols containing from 3 through 9 carbon atoms. The particular amount of asphaltenes or sediment that should be removed to obtain a deasphalted oil that has excellent recycle properties is not disclosed.
- U.S. Patent 4,502,944 discloses a method of separating a process material comprising oils, resins and asphaltenes into at least three fractions. Method employs light organic solvents (paraffinic hydrocarbons preferably having between 3 and 8 carbon atoms in a solvent/process material ratio of at least about 3:1) under elevated temperature and pressure conditions. As in U.S. Patent 4,305,814, the particular amount of asphaltenes or sediment that should be removed to obtain a deasphalted oil that has excellent recycle properties is not disclosed.
- U.S. Patent 3,412,010 discloses that the conversion of a vacuum residuum in a hydrocracker is improved by recycling the 680-975°F cut and the 975° plus residue back to the reactor. No mention of removing coke precursors or asphaltenes in the recycle streams is provided.
- U.S. Patent 3,905,892 discloses a process for hydrocracking vacuum residuum wherein the 975°F plus product may be recycled after removing the asphaltenes. The latter is partially oxidized to yield hydrogen for providing make-up hydrogen for the hydrocracking reactor. The effect of deasphalting conditions on product yields when the deasphalted oil is recycled is not disclosed.
- U.S. Patent 4,457,830 discloses the use of inorganic acids for precipitating and decomposing preasphaltenes and coprecipitating solids. The effect of deasphalting conditions on product yields when the deasphalted oil is recycled is not disclosed.
- The present invention provides an improvement in a method for conversion of a vacuum residuum feed in a hydrocracking operation which comprises upgrading the vacuum residuum feed, recovering and separating distillates from the remaining vacuum residuum feed and recycling unconverted vacuum residuum bottoms to the upgrading zone. The improvement comprises deasphalting the unconverted asphaltene- containing unconverted vacuum residuum bottoms in the recycle stream by treating said unconverted vacuum residuum bottoms in an extraction zone with a cosolvent under ambient conditions to a related temperature (and sufficient pressure wherein the recycle stream and cosolvent are maintained in a liquid state), whereby the most undesirable hydrogen deficient asphaltenes are selectively removed from the unconverted vacuum residuum bottoms to increase the overall conversion of the vacuum residuum feed.
- The present invention for improving the conversion of a virgin vacuum residuum into a useful product suggests the treatment of the unconverted vacuum bottoms after separating it from the cracked reaction distillate product in the reactor effluent. Then the treated vacuum bottoms, less the most undesirable hydrogen deficient asphaltenes and a majority of the trace metals, is recycled back to the reaction zone to be converted to additional quantities of the desired distillate products, i.e. naphtha, diesel fuel and vacuum gas oil. The latter stream is used to make additional naphtha and diesel fuel by using it as a charge stock component for a fluidized catalytic cracking unit.
- In the overall process of converting a vacuum residuum feed into the desired distillates, the improvement provided by the present invention is the treatment of the unconverted vacuum bottoms with a cosolvent to selectively remove most of the undesirable hydrogen deficient asphaltenes from the vacuum bottoms prior to their being recycled to the reactor, i.e., reaction zone, for further hydrocracking.
- As a result of the cosolvent treatment, the amount of the most undesirable hydrogen deficient asphaltenes to be selectively removed ranges from about 10 percent to about 20 percent.
- In treating the unconverted vacuum bottoms with a cosolvent, the amount of cosolvent used is defined as the volume ratio of cosolvent to unconverted vacuum bottoms and ranges from about 1:1 to about 40:1.
- The cosolvents that may be used according to the present invention include individual solvents such as n-pentane or n-heptane or (C₅-C₇) paraffines or a mixture of (C₅-C₆) naphthenes and (C₆-C₇) aromatics. The aromatics being benzene and toluene.
- To illustrate the advantage of deasphalting with n-heptane, a sample of the untreated unconverted vacuum bottoms and various deasphalted oils from the same unconverted vacuum bottoms sample were processed in a continuous stirred tank reactor (CSTR) at a catalyst space velocity of 0.13 bbl/lb/day at successive temperatures of 795, 805 and 815°F over an Mo/A1203 catalyst that mimics the steady-state activity of a commercial NiMo/A1₂0₃. The CSTR pressure was held at 2,250 psig with hydrogen and an H2 treatment rate of 7,000 SCF/bbl. Processing the untreated and unconverted vacuum bottoms and samples of the same unconverted vacuum bottoms individually deasphalted with toluene, cyclohexane and n-heptane gave the following results:
TABLE I PERFORMANCE INDICATORS* SAMPLE TEMPERATURE (°F) CALCULATED OVERALL CONVERSION 1000°F PLUS BOILING POINT MATERIAL (wt.%) Presence of Sediments Toluene Insolubles (wt.%) Untreated and unconverted vacuum bottoms 795 33 yes 0.6 805 38 yes 1.2 815 47 yes 1.3 Unconverted vacuum bottoms after toluene insolubles 795 39 yes n.a. 805 42 yes 1.3 815 50 yes 1.3 Unconverted vacuum bottoms after removing cyclohexane insolubles 795 41 none 0.3 805 49 none 0.5 815 58 yes 0.8 825 62 yes 0.7 Unconverted vacuum bottoms after removing n-hexane insolubles 795 52 none 0.0 805 56 none 0.0 815 65 none 0.0 825 73 none n.a. * Presence of sediment detected visually through a low power microscope at the end of each sample period (key samples confirmed by taking slide photographs at 600 magnification). Toluene insolubles in total liquid product were measured by Soxhlet extractions. - The above results show that the n-heptane deasphalted vacuum bottoms sample provides a much improved recycle stream for a residuum hydrocracking process designed to upgrade 1000°F and above boiling point components. Not only is the allowable conversion increased at a given temperature but, essentially, no sediment is formed. The latter is very important for reducing catalyst poisoning and minimizing plugging problems on account of sediment formation and deposition in flow control valves, heat exchangers and separation vessels downstream from the reaction zone. In addition, deasphalting the vacuum bottoms recycle stream with n-heptane versus the other solvents allows the reactor temperature to be increased by at least 10°F to further improve hydrocracking conversion without causing additional sediment.
- Deasphalting vacuum bottoms with toluene shows a negligible improvement in the overall conversion of the 1000°F plus boiling point components compared with the untreated vacuum bottoms and essentially no improvement in reducing sediment formation as measured by Soxhlet extractions with toluene. The cyclohexane deasphalted vacuum bottoms, on the other hand, provides an intermediate valued recycle stream in that the conversion is significantly improved over the untreated or toluene deasphalted vacuum bottoms but sediment begins to form in the reactor effluent as the reactor temperature is raised to provide a better overall conversion of the components boiling above 1000°F.
- It is of interest to note the relative amounts of sediment removed from the particular vacuum bottoms sample (VB) with solvents selected from each of the three basic hydrocarbon types at solvent/VB dosages of 20/1 at ambient conditions:
Sediment, wt.% Toluene < 0.5 Cyclohexane 6 - 7 n-Heptane 15 - 16 - It is well known in the art that the lighter the n-paraffin used for deasphalting the more sediment (comprising asphaltenes, other carbonaceous material and trace metals) will be removed from vacuum or atmospheric residuum. For instance, deasphalting the same vacuum bottoms sample with n-pentane removed 20-22 wt.% sediment. The object is to remove as little sediment as possible and still improve the overall conversion of 1000°F plus material while producing no more sediment.
- Certainly if the n-heptane deasphalted vacuum bottoms improves conversion without causing any additional sediment, the n-pentane deasphalted vacuum bottoms would do as well but there would be the additional amount of asphaltenes to be disposed of. Consequently, it is proposed that deasphalting with n-heptane provides a standard for determining how much of the asphaltene phase should be removed for a given vacuum bottoms stream if a mixed solvent comprising paraffins and naphthenes with some aromatics is being used.
- Another reason for not removing more of the sediment than necessary is to avoid removing the lighter asphaltenes containing a higher proportion of hydrogen and less carbon since the number of condensed aromatics is less. The lighter asphaltenes crack more easily and thereby help to improve the overall conversion of the 1000°F plus boiling point components. Some of the key analytical indicators for the deasphalted vacuum bottom (VB) samples are summarized in Table II:
TABLE II Micro Carbon Test, wt.% Hydrogen/Carbon Weight Ratio Trace Metal Analyses, ppm Nickel Vanadium Untreated VB 22.5 0.1140 28 38 Toluene DAVB 22.3 0.1156 29 28 Cyclohexane DAVB 18.1 0.1211 13 14 n-Heptane DAVB 12.3 0.1341 < 5 2.4 n-Pentane DAVB 10.4 - < 5 2 - In Table III below, samples of untreated and n-heptane deasphalted vacuum bottoms were blended with virgin vacuum residue and processed in a CSTR, as described in the first illustration, to better stimulate a commercial application. The blends were made up of one part untreated VB (or n-heptane DAVB) and two parts by weight of virgin vacuum residue. The results show that as the hydrocracking reactor severity was increased by raising the temperature to 815°F the n-heptane DAVB allowed the conversion of 1000°F plus material to be increased without producing any additional sediment. Moreover, by deasphalting the same vacuum bottoms sample with n-heptane the reactor temperature could be raised at least another 10°F to obtain additional conversion without producing any additional sediment formation.
TABLE III Sample Temperature °F Calculated Overall Conversion of 1000°F Plus Boiling Point Material (wt.%) Presence of Sediment Untreated VB with Virgin VR 795 52 none 805 55 yes 815 65 yes n-Heptane Deasph. VB recycle with Virgin VR 795 51 none 805 55 none 815 66 none 825 70 none
Claims (10)
1. A method for increasing the conversion of a vacuum residuum feed in a hydrocracking operation which comprises hydrocracking said feed vacuum residuum in a hydrocracking zone, recovering and separating distillates from the hydrocracking zone, and recycling a stream of unconverted vacuum residuum bottoms to the hydrocracking zone characterized by deasphalting unconverted vacuum residuum bottoms in the recycle stream by treatment in an extraction zone with a cosolvent at ambient or an elevated temperature, and a pressure sufficient to maintain the cosolvent in the liquid state, whereby the most undesirable sediments are selectively removed from said unconverted vacuum residuum bottoms to increase the conversion of said vacuum residuum feed.
2. A method according to Claim 1 characterized in that said cosolvent is n-heptane.
3. A method according to Claim 2 characterized in that the volume ratio of n-heptane to unconverted vacuum residuum bottoms is from 1:1 to 40:1.
4. A method according to Claim 1 characterized in that the cosolvent is a mixture of hydrocarbons selected from (C₅-C₇) paraffins, (C₅-C₆) naphthenes and (C₆-C₇) aromatics.
5. A method according to Claim 4 characterized in that the paraffins are n-pentane, n-hexane and n-heptane and the aromatics are toluene and benzene.
6. A method according to any one of Claims 1 to 5 characterized in that the unconverted vacuum residuum bottoms are treated with the cosolvent at a temperature from ambient to 700°F (371°C).
7. A method according to Claim 6 characterized in that the temperature is from 150 to 650°F (65.5 to 343°C).
8. A method according to any one of Claims 1 to 7 characterized in that the pressure is 1 to 60 atmospheres (0.10 to 6.08 MPa).
9. A method according to Claim 8 characterized in that the pressure is from 1 to 40 atmospheres (0.10 to 4.05 MPa).
10. A method according to any one of Claims 1 to 9 characterized in that the amount of the most undesirable hydrogen deficient asphaltenes selectively removed is from 10 to 20 percent.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US36429789A | 1989-06-12 | 1989-06-12 | |
US364297 | 1989-06-12 |
Publications (1)
Publication Number | Publication Date |
---|---|
EP0403087A1 true EP0403087A1 (en) | 1990-12-19 |
Family
ID=23433885
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP90305447A Withdrawn EP0403087A1 (en) | 1989-06-12 | 1990-05-18 | Conversion increase of vacuum residuums |
Country Status (3)
Country | Link |
---|---|
EP (1) | EP0403087A1 (en) |
JP (1) | JPH0374491A (en) |
CA (1) | CA2010774A1 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2906813A1 (en) * | 2006-10-06 | 2008-04-11 | Inst Francais Du Petrole | Heavy petroleum feed e.g. vacuum residue, hydroconverting method for producing petrol, involves de-asphalting vacuum residue to obtain de-asphalted oil, and recycling totality of oil by hydroconversion |
WO2010151300A1 (en) * | 2009-06-23 | 2010-12-29 | Lummus Technology Inc. | Multistage resid hydrocracking |
WO2016057362A1 (en) * | 2014-10-07 | 2016-04-14 | Shell Oil Company | A hydrocracking process integrated with solvent deasphalting to reduce heavy polycyclic aromatic buildup in heavy oil hydrocracker ecycle stream |
US9777226B2 (en) | 2014-09-08 | 2017-10-03 | Uop Llc | Methods and systems for slurry hydrocracking with reduced feed bypass |
WO2021025893A1 (en) * | 2019-08-02 | 2021-02-11 | Saudi Arabian Oil Company | Hydrocracking process and system including separation of heavy poly nuclear aromatics from recycle by extraction |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107966347B (en) * | 2016-10-20 | 2020-07-24 | 中国石油化工股份有限公司 | Extract liquid for soluble matters of waterproof coiled material and application thereof |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3905892A (en) * | 1972-03-01 | 1975-09-16 | Cities Service Res & Dev Co | Process for reduction of high sulfur residue |
EP0216448A1 (en) * | 1985-06-28 | 1987-04-01 | Gulf Canada Resources Limited | Process for improving the yield of distillables in hydrogen donor diluent cracking |
-
1990
- 1990-02-23 CA CA 2010774 patent/CA2010774A1/en not_active Abandoned
- 1990-05-18 EP EP90305447A patent/EP0403087A1/en not_active Withdrawn
- 1990-06-12 JP JP15175690A patent/JPH0374491A/en active Pending
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3905892A (en) * | 1972-03-01 | 1975-09-16 | Cities Service Res & Dev Co | Process for reduction of high sulfur residue |
EP0216448A1 (en) * | 1985-06-28 | 1987-04-01 | Gulf Canada Resources Limited | Process for improving the yield of distillables in hydrogen donor diluent cracking |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2906813A1 (en) * | 2006-10-06 | 2008-04-11 | Inst Francais Du Petrole | Heavy petroleum feed e.g. vacuum residue, hydroconverting method for producing petrol, involves de-asphalting vacuum residue to obtain de-asphalted oil, and recycling totality of oil by hydroconversion |
WO2010151300A1 (en) * | 2009-06-23 | 2010-12-29 | Lummus Technology Inc. | Multistage resid hydrocracking |
US8287720B2 (en) | 2009-06-23 | 2012-10-16 | Lummus Technology Inc. | Multistage resid hydrocracking |
EP2562235A1 (en) * | 2009-06-23 | 2013-02-27 | Lummus Technology Inc. | Multistage resid hydrocracking |
RU2495911C2 (en) * | 2009-06-23 | 2013-10-20 | Ламмус Текнолоджи Инк. | Multistage hydrocracking of refining residues |
US9441174B2 (en) | 2009-06-23 | 2016-09-13 | Lummus Technology Inc. | Multistage resid hydrocracking |
US9777226B2 (en) | 2014-09-08 | 2017-10-03 | Uop Llc | Methods and systems for slurry hydrocracking with reduced feed bypass |
WO2016057362A1 (en) * | 2014-10-07 | 2016-04-14 | Shell Oil Company | A hydrocracking process integrated with solvent deasphalting to reduce heavy polycyclic aromatic buildup in heavy oil hydrocracker ecycle stream |
US10479947B2 (en) | 2014-10-07 | 2019-11-19 | Shell Oil Company | Hydrocracking process integrated with solvent deasphalting to reduce heavy polycyclic aromatic buildup in heavy oil hydrocracker recycle stream |
WO2021025893A1 (en) * | 2019-08-02 | 2021-02-11 | Saudi Arabian Oil Company | Hydrocracking process and system including separation of heavy poly nuclear aromatics from recycle by extraction |
US11180701B2 (en) | 2019-08-02 | 2021-11-23 | Saudi Arabian Oil Company | Hydrocracking process and system including separation of heavy poly nuclear aromatics from recycle by extraction |
Also Published As
Publication number | Publication date |
---|---|
CA2010774A1 (en) | 1990-12-12 |
JPH0374491A (en) | 1991-03-29 |
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