EP0683218A2 - Procédé de conversion d'une huile résiduelle hydrocarbonée - Google Patents

Procédé de conversion d'une huile résiduelle hydrocarbonée Download PDF

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Publication number
EP0683218A2
EP0683218A2 EP95201314A EP95201314A EP0683218A2 EP 0683218 A2 EP0683218 A2 EP 0683218A2 EP 95201314 A EP95201314 A EP 95201314A EP 95201314 A EP95201314 A EP 95201314A EP 0683218 A2 EP0683218 A2 EP 0683218A2
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EP
European Patent Office
Prior art keywords
dao
hydrocracking
hydrocarbon oil
process according
fraction
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EP95201314A
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German (de)
English (en)
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EP0683218B1 (fr
EP0683218A3 (fr
Inventor
Johan Willem Gosselink
Anneke Van Der Heijden
Tom Huizinga
Hennie P/A Shell Int.Petr.Maatsch.B.V. Schaper
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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Priority to EP19950201314 priority Critical patent/EP0683218B1/fr
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Publication of EP0683218A3 publication Critical patent/EP0683218A3/fr
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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
    • 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

Definitions

  • the present invention relates to a process for the conversion of a residual hydrocarbon oil. More specifically, the present invention relates to a process for the conversion of a residual hydrocarbon oil involving the hydrocracking of upgraded deasphalted oil.
  • residual hydrocarbon oils such as those obtained in the distillation of crude oils at atmospheric or reduced pressure, contain considerable amounts of non-distillable compounds having a high molecular weight.
  • specific examples of such compounds are asphaltenes and metal compounds, in particular vanadium and nickel compounds.
  • demetallisation catalysts are known. They usually consist of oxidic carriers such as alumina, silica or silica-alumina, on which one or more metals or metal compounds having hydrogenation activity are optionally deposited. Metals from Groups VIB and VIII of the Periodic Table of Elements are widely known to be suitable for this purpose. Examples of suitable demetallisation catalysts are disclosed in inter alia U.S. Patents Nos.
  • U.S. Patent No. 4,564,439 discloses a two-stage catalytic hydroconversion process, wherein a heavy hydrocarbonaceous feedstock containing more than 100 parts per million by weight (ppmw) of metallic contaminants is first hydrodemetallised and then hydrocracked. Hydrodemetallisation is carried out by mixing the heavy hydrocarbonaceous feedstock, which might be a deasphalted tar or oil, with up to 10% by weight based on feedstock of solid particles which have sufficient catalytic activity to suppress the adverse coke formation and which induce substantial demetallisation. The resulting slurry, suitably in the form of a dispersion, is subsequently introduced into a first-stage hydrothermal zone, wherein hydrogen is introduced as well.
  • ppmw parts per million by weight
  • the reactant mixture is heated and as a result, demetallisation as well as conversion of hydrocarbons having a boiling point above 1000 °F (538 °C) into lower boiling hydrocarbons occurs.
  • the effluent is then, without substantial reduction of pressure, rapidly passed through a cooling zone into a second-stage hydrocatalytic reaction zone, where hydrogenation and cracking occurs.
  • a major disadvantage of the process according to U.S. Patent No. 4,564,439 is the fact that the contaminated solid particles resulting from the first stage of the process are passed into the hydrocatalytic reaction zone together with the demetallised feedstock. This will usually cause a more rapid and highly unwanted decrease of the activity of the hydrocracking catalyst. Moreover, in said U.S. patent a clear preference for heavy hydrocarbonaceous feedstocks containing very high amounts of metallic contaminants is expressed. Since a deasphalting treatment generally causes a substantial amount of the metallic contaminants present in the feed as high-molecular weight complexes to accumulate in the asphaltic bitumen fraction rather than in the deasphalted oil fraction, the metals content of a deasphalted oil is usually lower than 100 ppmw.
  • the present invention relates to a process for the conversion of a residual hydrocarbon oil, preferably a vacuum hydrocarbon oil residue, comprising the following steps:
  • the residual hydrocarbon oil feed and the flashed distillate fraction(s) used in step (c) may originate from different sources and may be supplied as separate feedstocks. It is, however, preferred that said residual hydrocarbon oil and said flashed distillate fraction(s) used in step (c) are both produced in a vacuum distillation step prior to step (a). Accordingly, in a preferred embodiment of the present invention a hydrocarbon oil, suitably an atmospheric residue, is converted via the subsequent steps of:
  • Vacuum distillation can be carried out by any conventional technique known in the art. Suitable techniques then, include high vacuum distillation using steam ejectors and vacuum flash distillation.
  • the deasphalting of the heavy residual fraction obtained from the vacuum distillation may be carried out in any conventional manner.
  • a well known and suitable deasphalting method is solvent deasphalting, wherein the hydrocarbon feed is treated counter-currently with an extracting medium which is usually a light hydrocarbon solvent containing paraffinic compounds.
  • Commonly applied paraffinic compounds include C3 ⁇ 8 paraffinic hydrocarbons, such as propane, butane, isobutane, pentane, isopentane, hexane or mixtures of two or more of these.
  • C3-C5 paraffinic hydrocarbons most preferably butane, pentane or a mixture thereof, are used as the extracting solvent.
  • the extraction depth increases at increasing number of carbon atoms of the extracting solvent.
  • the higher the extraction depth the larger the amount of hydrocarbons being extracted from the hydrocarbon feed, the smaller and more viscous the asphaltene fraction and the heavier the asphaltenes being present in said asphaltene fraction.
  • a rotating disc contactor or a plate column can be used with the hydrocarbon feed entering at the top and the extracting solvent entering at the bottom.
  • the lighter hydrocarbons which are present in the residual hydrocarbon oil dissolve in the extracting solvent and are withdrawn at the top of the apparatus.
  • the asphaltenes which are insoluble in the extracting solvent are withdrawn at the bottom of the apparatus.
  • deasphalting is carried out at a total extracting solvent to residual hydrocarbon oil ratio of 1.5 to 8 wt/wt, a pressure of from 1 to 50 bar and a temperature of from 160 to 230 °C.
  • Demetallisation of the DAO in accordance with step (b) of the process according to the present invention can be achieved by any well known demetallisation process wherein the hydrocarbon feed to be demetallised is passed at elevated temperature and pressure and in the presence of hydrogen in an upward, downward or radial direction, through one or more vertically disposed reactors containing a fixed or moving bed of demetallisation catalyst particles.
  • Well known demetallisation operations are the bunker flow operation, the fixed bed operation, the fixed bed swing operation and the movable bed operation.
  • suitable demetallisation catalyst usually consist of oxidic carriers such as alumina, silica or silica-alumina, on which one or more Group VIB or Group VIII metals or metal compounds may be deposited.
  • oxidic carriers such as alumina, silica or silica-alumina, on which one or more Group VIB or Group VIII metals or metal compounds may be deposited.
  • Such demetallisation catalysts are commercially available from many catalyst suppliers.
  • Particularly suitable demetallisation catalysts are those having as the active agent one of the combinations nickel/molybdenum (NiMo) or cobalt/molybdenum (CoMo), optionally promoted with phosphorus (P), on an alumina (Al2O3) carrier.
  • catalysts are CoMo/Al2O3, CoMoP/Al2O3 and NiMo/Al2O3 and NiMoP/Al2O3 catalysts. It is well known that the type of catalysts described hereinbefore in practice will also exhibit some upgrading activity in terms of hydrodenitrification and/or hydrodesulphurization, removal of heavy hydrocarbons and conversion of hydrocarbons having a boiling point above 520 °C into lower boiling components. For this reason the DAO leaving the hydrodemetallisation zone is referred to as "upgraded DAO" instead of demetallised DAO.
  • Hydrodemetallisation is usually carried out at a hydrogen partial pressure of 20-250 bar, a temperature of 300-470 °C, preferably 310-440 °C, and a space velocity of 0.1-10 l.l ⁇ 1hr ⁇ 1, preferably 0.2 to 7 l.l ⁇ 1hr ⁇ 1.
  • the blending ratio of the upgraded DAO and the flashed distillate fractions is not particularly critical and is mainly determined by factors such as hydrocracking catalyst choice, viscosity specification of the hydrocracking equipment and desired product distribution in the hydrocarbon effluent.
  • the weight ratio flashed distillates to upgraded DAO is in the range of from 10/90 to 90/10, preferably 25/75 to 75/25 and even more preferably 40/60 to 70/30.
  • the hydrocracking performed in step (c) of the process according to the present invention may be conducted in any way known in the art, provided that at least one of the catalysts used in the hydrocracking zone is acidic. Generally, such process is carried out in the presence of hydrogen and a suitable hydrocracking catalyst at elevated temperature and pressure.
  • Hydrocracking catalysts usually consist of one or more metals from nickel, tungsten, cobalt and molybdenum in elemental, oxidic or sulphidic form on a suitable carrier such as alumina, silica, silica-alumina or a zeolite.
  • a suitable carrier such as alumina, silica, silica-alumina or a zeolite.
  • hydrocracking catalysts which can be suitably applied in the process of the present invention.
  • At least one of the catalysts used in the hydrocracking zone must be acidic, i.e. must contain a silica-alumina and/or zeolitic component.
  • the hydrocracking process can be a single- or multiple-staged process.
  • a stacked bed of a hydrodenitrification/first-stage hydrocracking catalyst on top of a conversion catalyst can suitably be used.
  • Particularly suitable hydrodenitrification/first-stage hydrocracking catalysts are NiMo/Al2O3 and CoMo/Al2O3, optionally promoted with phosphorus and/or fluor.
  • Preferred conversion catalysts are those based on NiW/zeolite or NiW/zeolite/silica-alumina.
  • Common hydrocracking conditions are an operating pressure of 80-250 bar, preferably 100-200 bar, and a temperature of 300-500 °C, preferably 350-475 °C.
  • the hydrodemetallisation of the DAO in step (b) is carried out at a hydrogen partial pressure which is at most 30 bar and suitably less than 20 bar higher than the operating pressure of the hydrocracking in step (c).
  • the hydrogen partial pressure in step (b) is from 0 to about 10 bar higher than the operating pressure in step (c).
  • the operation pressure in the hydrocracking zone is suitably in the range of from 120 to about 200 bar, preferably from 140 to 180 bar.
  • a heavy fraction in the hydrocracking of step (c) can suitably be recycled in order to be subjected to hydrocracking and/or hydrodemetallisation once again.
  • said heavy fraction could also be suitably applied as a feed for a fluidised bed catalytic cracking (FCC) unit or as a feedstock for lubricating oil manufacture.
  • FCC fluidised bed catalytic cracking
  • a combination of these options is possible as well.
  • the asphaltic fraction resulting from the solvent deasphalting treatment in step (a) of the process according to the present invention may be used in several ways. It can for instance be combusted for cogeneration of power and steam. Alternatively, it can be partially combusted for clean fuel gas production, cogeneration of power and steam, hydrogen manufacture or hydrocarbon synthesis. Still another option is application in bitumen, emulsion fuels or solid fuels by means of pelletizing. A preferred option is to subject the asphaltic fraction resulting from the deasphalting treatment in step (a) to partial combustion.
  • Figure 1 depicts a preferred embodiment of the process according to the present invention, wherein the vacuum distillation step has been integrated.
  • Figure 2 depicts a further preferred embodiment of the process according to the present invention.
  • Figure 3 shows how the process according to the present invention can be suitably integrated in a complex hydrocracker refinery line-up.
  • an atmospheric hydrocarbon oil residue (105) is passed into vacuum distillation zone (101), where it is separated in one or more flashed distillate fractions (106) and a vacuum residue fraction (107). At least a part of the flashed distillate fractions (106) is routed to upgraded DAO stream (110).
  • the vacuum residue fraction (107) is deasphalted in deasphalting zone (102), resulting in an asphaltic fraction (109) and a DAO (108) which is subsequently hydrodemetallised in hydrodemetallisation zone (103).
  • the upgraded DAO (110) is blended with at least a part of the flashed distillate fraction(s) (106) and the resulting blendstream is then passed into hydrocracking zone (104), thus producing one or more distillate fractions (111) and optionally a heavy fraction (112).
  • Figure 2 is in fact an extension of Figure 1 in three aspects. Firstly, in that at least a part of the heavy fraction (212) produced in hydrocracking zone (204) is recirculated by routing it to upgraded DAO (210) and blending it therewith prior to being led into hydrocracking zone (204). Secondly, part of the heavy fraction (212) routed to upgraded DAO (210) is routed to DAO (208) and blended therewith in order to be subjected to hydrodemetallisation in hydrodemetallisation zone (203) once again. This option is indicated by a dotted line in figure 2. The third aspect, finally, is also indicated with a dotted line and embodies the option of routing part of the flashed distillate fractions (206) to DAO (208) and blending it therewith. The other reference numbers used in Figure 2 correspond with those used in Figure 1 having the same last two numbers.
  • Figure 3 shows the line-up of a hydrocracker refinery.
  • a crude oil (307) is passed into atmospheric distillation zone (301), where a first separation into one or more distillate fractions (308) and a residual fraction or "long residue” (309).
  • This long residue (309) is further separated in vacuum distillation zone (302) into one or more flashed distillate fractions (310), at least part of which is blended with upgraded DAO (317), and a vacuum residue fraction or "short residue” (311), which is deasphalted in deasphalting zone (303).
  • a part of the flashed distillate fractions (310) is blended with DAO (312).
  • the DAO (312) is passed into hydrodemetallisation zone (304) and the upgraded DAO is led into hydrocracking zone (305).
  • the asphaltic fraction (313) resulting from the deasphalting treatment is passed into gasification zone (306) where it is partially oxidised using oxygen, supplied via stream (314), eventually producing clean fuel gas (315) and hydrogen (316).
  • This hydrogen can for instance be passed into hydrodemetallisation zone (304) and/or hydrocracking zone (305) in order to increase the overall process efficiency.
  • Hydrocracking in hydrocracking zone (305) results in one or more distillate fractions (318) and a heavy fraction (319), which is at least partially recirculated into hydrocracking zone (305) via blending with upgraded DAO (317).
  • a part of the heavy fraction (319) is blended with DAO (312).
  • the invention is further illustrated by the following example.
  • a crude oil feed was subjected to conventional crude distillation; the long residue produced was subjected to conventional vacuum flashing, producing a flashed distillate (FD) and short residue (SR).
  • the SR was subsequently subjected to solvent deasphalting using butane as extracting solvent to produce a DAO at a yield of 70% by weight based on SR.
  • the DAO and FD were coprocessed in an integrated hydro-demetallization/hydrocracking (HDM/HCU) pilot plant for about 5000 hours.
  • the DAO was upgraded in the HDM reactor over a conventional NiMoP/alumina catalyst.
  • Upgraded DAO and FD were subsequently coprocessed in the HCU reactor over a catalyst system including an acidic catalyst, producing hydrowax, gasoil, kerosene, naphtha and gaseous products. Both HDM and HCU reactors were operated at the same pressure.

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  • 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)
EP19950201314 1994-05-19 1995-05-18 Procédé de conversion d'une huile résiduelle hydrocarbonée Expired - Lifetime EP0683218B1 (fr)

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EP19950201314 EP0683218B1 (fr) 1994-05-19 1995-05-18 Procédé de conversion d'une huile résiduelle hydrocarbonée

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Application Number Priority Date Filing Date Title
EP94201423 1994-05-19
EP94201423 1994-05-19
EP19950201314 EP0683218B1 (fr) 1994-05-19 1995-05-18 Procédé de conversion d'une huile résiduelle hydrocarbonée

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EP0683218A2 true EP0683218A2 (fr) 1995-11-22
EP0683218A3 EP0683218A3 (fr) 1996-03-20
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999013024A1 (fr) * 1997-09-11 1999-03-18 Atlantic Richfield Company Utilisation d'un procede de desasphaltage en dissolution pour transformer du petrole brut lourd en distillat ion a partir d'une formation souterraine, a travers un puits de forage
WO2000006670A1 (fr) * 1998-07-29 2000-02-10 Texaco Development Corporation Integration de processus de desasphaltage en dissolution et de gazeification
EP1731588A1 (fr) * 2005-06-08 2006-12-13 Shell Internationale Researchmaatschappij B.V. Procédé de valorisation d'huile brute
WO2008065182A1 (fr) * 2006-12-01 2008-06-05 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'un mélange d'hydrogène et de monoxyde de carbone à partir d'un stock d'alimentation d'hydrocarbure liquide contenant une certaine quantité de cendres
US8052864B2 (en) 2006-12-01 2011-11-08 Shell Oil Company Process to prepare a sweet crude
CN102453545A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 一种渣油轻质化的方法
CN102453541A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 一种处理渣油的联合加工方法
CN101633848B (zh) * 2009-08-31 2012-11-21 中煤能源黑龙江煤化工有限公司 一种中低温煤焦油深加工方法
US8475546B2 (en) 2008-12-04 2013-07-02 Shell Oil Company Reactor for preparing syngas
CN103540358A (zh) * 2012-07-12 2014-01-29 中国石油天然气股份有限公司 渣油转化-芳烃抽提组合工艺
CN113166659A (zh) * 2018-10-22 2021-07-23 沙特阿拉伯石油公司 残油的催化脱金属和气相氧化脱硫

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9051522B2 (en) 2006-12-01 2015-06-09 Shell Oil Company Gasification reactor
US8960651B2 (en) 2008-12-04 2015-02-24 Shell Oil Company Vessel for cooling syngas
CN103059998B (zh) * 2011-10-21 2014-08-20 中国石油化工股份有限公司 一种处理渣油的组合工艺方法

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US3876523A (en) 1973-08-29 1975-04-08 Mobil Oil Corp Catalyst for residua demetalation and desulfurization
US3891541A (en) 1973-08-29 1975-06-24 Mobil Oil Corp Process for demetalizing and desulfurizing residual oil with hydrogen and alumina-supported catalyst
GB1438645A (en) 1972-07-07 1976-06-09 Shell Int Research Hydrocarbon conversion process
DE2638498A1 (de) 1975-08-28 1977-03-03 Mobil Oil Corp Katalysator fuer die hydrierende entfernung von metallen und schwefel, dessen herstellung und dessen verwendung
GB1522629A (en) 1974-09-18 1978-08-23 Shell Int Research Process for the preparation of catalysts
GB1548722A (en) 1975-09-05 1979-07-18 Shell Int Research Process for the conversion of hydrocarbons
NL7901734A (nl) 1978-03-08 1979-09-11 Mobil Oil Corp Katalysator voor het demetalleren en desulfureren van koolwaterstofolieen, alsmede werkwijze voor het demetalleren en desulfureren van koolwaterstofolieen.
GB1560590A (en) 1976-07-08 1980-02-06 Shell Int Research Process for demetallizing hydrocarbon oils
GB1560599A (en) 1976-07-08 1980-02-06 Shell Int Research Process for demetallizing hydrocarbon oils
US4564439A (en) 1984-06-29 1986-01-14 Chevron Research Company Two-stage, close-coupled thermal catalytic hydroconversion process

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FR1423627A (fr) * 1963-04-11 1966-01-07 Inst Francais Du Petrole Procédé de conversion d'hydrocarbures lourds
NL159135B (nl) * 1967-12-27 1979-01-15 Shell Int Research Werkwijze voor de bereiding van lager kokende koolwaterstoffen of fracties, die deze bevatten, uit residuale olien door deze te ontasfalteren en de ontasfalteerde olie te hydrokraken in aanwezigheid van waterstof, die is verkregen door partiele verbranding van de bij de ontasfaltering afgescheiden asfaltenen.
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GB1438645A (en) 1972-07-07 1976-06-09 Shell Int Research Hydrocarbon conversion process
US3876523A (en) 1973-08-29 1975-04-08 Mobil Oil Corp Catalyst for residua demetalation and desulfurization
US3891541A (en) 1973-08-29 1975-06-24 Mobil Oil Corp Process for demetalizing and desulfurizing residual oil with hydrogen and alumina-supported catalyst
GB1522629A (en) 1974-09-18 1978-08-23 Shell Int Research Process for the preparation of catalysts
DE2638498A1 (de) 1975-08-28 1977-03-03 Mobil Oil Corp Katalysator fuer die hydrierende entfernung von metallen und schwefel, dessen herstellung und dessen verwendung
GB1548722A (en) 1975-09-05 1979-07-18 Shell Int Research Process for the conversion of hydrocarbons
GB1560590A (en) 1976-07-08 1980-02-06 Shell Int Research Process for demetallizing hydrocarbon oils
GB1560599A (en) 1976-07-08 1980-02-06 Shell Int Research Process for demetallizing hydrocarbon oils
NL7901734A (nl) 1978-03-08 1979-09-11 Mobil Oil Corp Katalysator voor het demetalleren en desulfureren van koolwaterstofolieen, alsmede werkwijze voor het demetalleren en desulfureren van koolwaterstofolieen.
US4564439A (en) 1984-06-29 1986-01-14 Chevron Research Company Two-stage, close-coupled thermal catalytic hydroconversion process

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999013024A1 (fr) * 1997-09-11 1999-03-18 Atlantic Richfield Company Utilisation d'un procede de desasphaltage en dissolution pour transformer du petrole brut lourd en distillat ion a partir d'une formation souterraine, a travers un puits de forage
WO2000006670A1 (fr) * 1998-07-29 2000-02-10 Texaco Development Corporation Integration de processus de desasphaltage en dissolution et de gazeification
US6241874B1 (en) 1998-07-29 2001-06-05 Texaco Inc. Integration of solvent deasphalting and gasification
EP1731588A1 (fr) * 2005-06-08 2006-12-13 Shell Internationale Researchmaatschappij B.V. Procédé de valorisation d'huile brute
US9487400B2 (en) 2006-11-01 2016-11-08 Shell Oil Company Process to prepare a mixture of hydrogen and carbon monoxide from a liquid hydrocarbon feedstock containing a certain amount of ash
WO2008065182A1 (fr) * 2006-12-01 2008-06-05 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'un mélange d'hydrogène et de monoxyde de carbone à partir d'un stock d'alimentation d'hydrocarbure liquide contenant une certaine quantité de cendres
US8052864B2 (en) 2006-12-01 2011-11-08 Shell Oil Company Process to prepare a sweet crude
US8475546B2 (en) 2008-12-04 2013-07-02 Shell Oil Company Reactor for preparing syngas
CN101633848B (zh) * 2009-08-31 2012-11-21 中煤能源黑龙江煤化工有限公司 一种中低温煤焦油深加工方法
CN102453541A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 一种处理渣油的联合加工方法
CN102453545B (zh) * 2010-10-15 2013-11-06 中国石油化工股份有限公司 一种渣油轻质化的方法
CN102453541B (zh) * 2010-10-15 2013-11-20 中国石油化工股份有限公司 一种处理渣油的联合加工方法
CN102453545A (zh) * 2010-10-15 2012-05-16 中国石油化工股份有限公司 一种渣油轻质化的方法
CN103540358A (zh) * 2012-07-12 2014-01-29 中国石油天然气股份有限公司 渣油转化-芳烃抽提组合工艺
CN113166659A (zh) * 2018-10-22 2021-07-23 沙特阿拉伯石油公司 残油的催化脱金属和气相氧化脱硫

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EP0683218B1 (fr) 2001-04-11
EP0683218A3 (fr) 1996-03-20

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