EP0073690A1 - Verfahren zur katalytischen Wasserstoffumwandlung von schweren Kohlenwasserstoffen mit einem dispergierten Katalysator und kohleartige Teilchen - Google Patents

Verfahren zur katalytischen Wasserstoffumwandlung von schweren Kohlenwasserstoffen mit einem dispergierten Katalysator und kohleartige Teilchen Download PDF

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Publication number
EP0073690A1
EP0073690A1 EP82401336A EP82401336A EP0073690A1 EP 0073690 A1 EP0073690 A1 EP 0073690A1 EP 82401336 A EP82401336 A EP 82401336A EP 82401336 A EP82401336 A EP 82401336A EP 0073690 A1 EP0073690 A1 EP 0073690A1
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Prior art keywords
cenospheres
weight
nickel
vanadium
hydrogen
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EP82401336A
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English (en)
French (fr)
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EP0073690B1 (de
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Pierre Giuliani
Yves Jacquin
Christian Busson
Jean-François Josserand
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IFP Energies Nouvelles IFPEN
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IFP Energies Nouvelles IFPEN
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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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
    • 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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/10—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles
    • C10G49/12—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 with moving solid particles suspended in the oil, e.g. slurries

Definitions

  • the present invention relates to a process for the catalytic hydroconversion of heavy hydrocarbon feedstocks containing asphaltenes and metallic impurities, sulfur and nitrogen.
  • the catalytic system of the invention leads, under the conditions of hydroconversion, to the transformation of a portion of the heavy products of the feedstock into products with a lower boiling point and significantly lowers the content of impurities by hydrodemetallization, hydrodesulfurization and hydrodenitrification as well as the value of the Conradson carbon residue.
  • cenospheres Another important advantage of the presence of the cenospheres is to allow, at the end of the reaction, easy filtration of the catalyst residues (a) present in the liquid product of the reaction.
  • the fines entrained by the gas, during gasification have an average size of less than 10 microns. They contain the metals from the oil, usually vanadium, iron and nickel, and, in addition, the metallic component of the oil-soluble catalytic metal compound which had been added.
  • U.S. Patent 4,204,943 describes a catalytic hydroconversion process in which the catalyst consists of carbonaceous or fine particles derived therefrom, the diameter of which is less than 10 microns. These particles and fines come from the gasification of coke.
  • US Pat. No. 4,227,995 describes a catalytic hydrodemetallization process in which the catalyst consists of particles of calcined coke or "green coke" having a porosity of less than 0.3 cm3 / g and a specific surface area less than 5 m2 / g, 50 to 80% of the pores having diameters greater than 10 000 hngstrkms (1 pm).
  • US Patent 4,299,685 describes a hydrocracking process for heavy oil, the catalyst of which consists of fly ash; fly ash are particles with a high mineral content and low carbon content; under the electron microscope, they have a smooth appearance. Their porosity is low, of the order of 0.3 to 0.4 cm3 / g.
  • cenospheres make it a very efficient and inexpensive material for transporting insoluble materials and the metals formed during hydroconversion.
  • Their high content of metals (Fe, Ni, V) (approximately 1 to 10% by weight, in total, of these 3 metals) also gives them a catalytic activity of cracking, hydrogenation and demetallation.
  • their roughly spherical shape and their relatively large size ensure their easy removal by filtration without clogging the filters.
  • cenospheres contain, by weight, 0.1 to 2% vanadium (preferably 0.4 to 2%), 0.1 to 5% iron (preferably 0.4 to 2%) and 0 , 2 to 1% of nickel (preferably 0.5 to 1%), these values not being limiting.
  • They also contain carbon, for example 60 to 90% by weight, and sulfur, for example 2 to 10% by weight, as well as common elements such as Na and Ca.
  • the specific surface of the cenospheres can be very variable, most often between 2 and 130 m2 / g, preferably 2 to 20 m2 / g.
  • the average diameter of the cenospheres is usually greater than 10 ⁇ m, for example between 10 and 200 ⁇ m or between 20 and 200 ⁇ m, more particularly between 20 and 60 ⁇ m.
  • Their grain density is usually from 0.3 to 0.8 g / cm3, preferably from 0.4 to 0.6 g / cm3, and their structural density usually from 1.2 to 2.5 g / cm3, from preferably 1.3 to 2.1 g / cm3.
  • Their total pore volume is usually 0.8 to 2.5 cm3 / g, preferably 1.2 to 1.7 cm3 / g.
  • cenospheres Certain initially spherical cenospheres may have been broken and the invention also covers the use of debris from cenospheres.
  • Hydroconversion is a process in which a part of the heavy constituents of the charge is transformed under hydrogen pressure, at high temperature, into products with a lower boiling point.
  • This process is particularly well suited for the heaviest hydrocarbon feedstocks having a Conradson carbon residue of up to 50% by weight.
  • These fillers also have very high contents by weight of asphaltenes (for example up to 40%), sulfur (for example up to 8%) and metals (for example up to 3000 ppm).
  • the catalytic metal compound used in the invention is a finely divided metallic compound preferably originating from a metallic compound soluble in the filler or from an aqueous solution of a metallic salt which is dispersed in the filler or, intermediately , in a hydrocarbon solvent.
  • the metallic constituent of these soluble compounds convertible into a solid dispersed catalyst belongs to groups VB, VI B, VII B and or VIII according to the table published by EH Sargent in 1962.
  • the preferred metals are molybdenum, vanadium, chromium , tungsten, manganese, iron, nickel, cobalt.
  • the preferred compounds are molybdenum naphthenate and molybdenum blue.
  • the amount of the soluble metal compound added to the charge is for example between 10 and 1000 ppm, preferably between 50 and 500 ppm counted by weight of metal relative to the charge.
  • the metal compound can be added either alone or mixed with one or more compounds of different metals.
  • the metallic compound, dissolved in an aqueous solution optionally pre-emulsified with a hydrocarbon can be for example: ammonium or alkali metal heptamolybdate, cobalt nitrate, nickel nitrate, ferrous sulfate or sodium tungstate.
  • the preferred compound is ammonium heptamolybdate either alone or as a mixture with another metallic water-soluble compound.
  • the amount of metallic compound dissolved in the emulsified aqueous solution is between 10 and 1000 ppm, preferably between 50 and 500 ppm counted by weight of metal.
  • the cenospheres most often originate from smoke dedusting installations in large thermal power plants burning heavy industrial fuels, in particular heavy no. 2 fuels.
  • cenospheres are mixed with the filler in the proportion of 0.1 to 5% by weight relative to the latter.
  • the filler containing the cenospheres, the soluble metallic compound or the metallic salt provided by an aqueous solution or emulsion may or may not be subjected to a pretreatment.
  • the purpose of this pretreatment is to transform the metal compound or the metal salt into a finely dispersed solid catalyst comprising from 10 to 1000 ppm, preferably from 50 to 300 ppm by weight of active material counted as elemental metal, based on the weight of filler .
  • the pretreatment is carried out in the presence of hydrogen sulphide alone or in admixture with hydrogen at a temperature between 200 and 450 ° C and under a pressure between 25 and 250 bars. During this pretreatment, some or all of the metals contained in the cenospheres are also transformed into metallic sulphides.
  • the charge mixed with the constituents of the catalytic system is sent to the hydroconversion reactor where the metallic compound or the metallic salt and the metals contained in the cenospheres are transformed into metallic sulfides under the action feed sulfur and / or sulfur compounds formed during the reaction, especially H 2 S.
  • FIG. 3 describes an embodiment of the method given by way of example.
  • the fresh charge, the soluble metallic compound or the emulsion of an aqueous solution of a metallic salt in a hydrocarbon are introduced respectively by lines 1, 2 and 3 into a mixing tank 4.
  • This mixture is pumped, line 5, into a pretreatment reactor 6, where it is brought into contact with hydrogen containing from 2 to 10% of hydrogen sulfide.
  • Hydrogen is a mixture of fresh hydrogen (line 7) and recycled hydrogen (line 8).
  • the hydrogen sulphide is supplied either by recycling (line 8), or by a fresh supply (line 9).
  • the temperature is between 200 and 450 ° C, preferably 350/450 ° C, the pressure between 25 and 250 bars, preferably 100/200 bars, the reaction time between 5 minutes and 4 hours, from preferably 10 minutes to 2 hours.
  • the pretreated product is introduced (line 10) into the hydroconversion reactor 11.
  • the temperature of this reactor is between 380 and 480 ° C, preferably 420 to 460 ° C, the partial pressure of hydrogen between 25 and 250 bars , preferably between 100 and 200 bars, the hydrogen flow rate between 1000 and 5000 liters TPN / liter of charge, preferably between 1000 and 2000 1/1 and the space speed (VVH) defined by the charge volume per hour and per reactor volume between 0.1 and 10, preferably between 0.25 and 5.
  • the effluent which leaves the hydroconversion reactor via line 12 comprises gases and a liquid having solids in suspension. It is introduced into a high pressure separator 13. From this separator leaves a gas (line 14) which contains hydrogen, hydrogen sulfide and light hydrocarbons. Part of this gas is recycled, after treatment to remove the hydrogen sulfide, to the pretreatment reactor or the hydroconversion reactor if there is no pretreatment. The other part is eliminated (28) to maintain the partial pressures of hydrogen and hydrogen sulfide at the fixed level.
  • This fractionation unit can be a simple vacuum evaporator or a vacuum distillation column.
  • the adjustment of the separation between distillate and residue is done to obtain a flowable and pumpable residue under industrial conditions.
  • the residue drawn off through line 17 is mixed in tank 18 with an aromatic solvent with a boiling point of between 100 and 220 ° C., introduced through line 25.
  • This solvent reduces the viscosity and allows a phase to be obtained.
  • which is treated in a separation unit 20, joined at 18 by line 19. In this separation unit, the solids are separated by filtration or centrifugation or decantation.
  • the filtered or centrifuged solids are washed with the same aromatic solvent (line 26), in the separation unit 20, to remove the oily products which coat the sulphides of the catalytic metals, the sulphides of the metals contained in the feed, the cenospheres more or less charged with metals and metal sulfides and insoluble in the aromatic solvent.
  • a fraction of these solids is eliminated via line 21. They can be burned, carbonated or treated in order to recover the metals.
  • the other fraction is recycled to the hydroconversion reactor (line 22), this via the mixing tank 4, the residual aromatic solvent can either be kept or eliminated.
  • the aromatic solvent is withdrawn, which is reinjected into the mixer 18 via line 25, and into the separation unit 20, through line 26, for washing the filtered or centrifuged solids.
  • the hydrotreated residue (line 27), largely free of metals, sulfur, nitrogen and asphaltenes. This residue is either burned, or gasified, or diluted to make a heavy fuel oil No. 2.
  • a 250 ml stainless steel autoclave is used.
  • the gas-liquid contact is ensured by shaking.
  • a test is made with 30 g of filler.
  • the autoclave after loading the soluble molybdenum compound, the cenospheres and the charge, is closed and weighed at atmospheric pressure, scanned with hydrogen and subjected to a hydrogen pressure of 100 bars for one hour to check sealing.
  • the autoclave is first filled with hydrogen sulphide at 10 bars, then it is completed up to 100 bars with hydrogen.
  • the mixture is heated to 380 ° C., left for 1 hour, cooled to room temperature, relaxed, scanned with hydrogen and then the test is repeated as indicated above.
  • the reaction medium is diluted with toluene and filtered.
  • the solids are washed with hot toluene.
  • the two toluene solutions, for filtration and washing, are evaporated at 100 ° C. under 0.025 bar.
  • the hydrocarbons entrained with toluene are analyzed.
  • the evaporation residue constitutes the hydro-converted product.
  • the weight balance must be greater than 95% for a test to be considered valid.
  • the charge containing the soluble metallic compound and the cenospheres is mixed in line with hydrogen containing from 3 to 7% of hydrogen sulfide, then is brought to the reaction temperature through an oven, consisting of five heating elements. It then enters the bottom of a reactor, consisting of a vertical tube.
  • the reactor effluent is cooled to 150 ° C and passed through a high pressure separator. The gas from this separator is recycled after being washed with water. A purge allows the partial pressures of hydrogen and hydrogen sulfide to be adjusted.
  • the hydroconverted product is drawn off at the base of the high pressure separator.
  • the operation is carried out batchwise with 30 g of Safanya asphalt diluted with 35% by volume of diesel oil at 420 ° C. for two hours; initial hydrogen pressure: 100 bars; no pretreatment.
  • Various tests are carried out: test without catalyst, test with cenospheres alone, test with molybdenum naphthenate alone, test with molybdenum naphthenate plus cenospheres.
  • the cenospheres allow the fixation of vanadium, nickel and molybdenum.
  • Molybdenum is not found in the liquid hydroconverted product.
  • Example 2 The tests indicated in this example are carried out under the same conditions as in Example 1. A molybdenum blue in 5.8% solution in a C 7 - Cg alcohol is used as the molybdenum compound.
  • Table III collates the results of these tests. These tests confirm the results obtained with molybdenum naphthenate, namely the presence of cenospheres increases the hydrometallization activity and reduces the weight of insoluble matter.
  • Example 2 The procedure is as in Example 1, but adding to the hydrocarbon feedstock, in addition to cobalt naphthenate and the cenospheres, 0.5% by weight, relative to the feedstock, of cenospheres recovered at the end of the Example 1 and washed with hot toluene.
  • the addition of these recovered cenospheres makes it possible, as shown in Table IV, to reduce the supply of fresh molybdenum naphthenate to 100 ppm, without significant modification of the results.
  • the charge is mixed with molybdenum naphthenate (500 ppm by weight of molybdenum) and 1% by weight of cenospheres, identical to those used in Example 1. It is introduced into the preheating oven at the rate of 1 liter / h , where it is brought to 430 ° C., temperature at which it enters the reaction chamber.
  • molybdenum naphthenate 500 ppm by weight of molybdenum
  • cenospheres identical to those used in Example 1. It is introduced into the preheating oven at the rate of 1 liter / h , where it is brought to 430 ° C., temperature at which it enters the reaction chamber.
  • the total pressure is 150 bars.
  • the recycled hydrogen is introduced online just before the preheater, with an H 2 / Hydrocarbon ratio equal to 1000 liters per liter, the hydrogen being considered at normal temperature and pressure.
  • Hydrogen contains 2 to 3% hydrogen sulfide.
  • the space velocity, charge volume per hour and per reactor volume, is equal to 1.2, which corresponds to a residence time in the reactor of 54 minutes.
  • Table V shows the results obtained after 100 hours of operation under the preceding conditions.
  • Table VI provides the filtration rates for these various products as well as their viscosity at 50 ° C.

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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)
  • Catalysts (AREA)
EP82401336A 1981-08-11 1982-07-16 Verfahren zur katalytischen Wasserstoffumwandlung von schweren Kohlenwasserstoffen mit einem dispergierten Katalysator und kohleartige Teilchen Expired EP0073690B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8115665A FR2511389A1 (fr) 1981-08-11 1981-08-11 Procede d'hydroconversion catalytique d'hydrocarbures lourds en phase liquide et en presence d'un catalyseur disperse et de particules charbonneuses
FR8115665 1981-08-11

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EP0073690A1 true EP0073690A1 (de) 1983-03-09
EP0073690B1 EP0073690B1 (de) 1985-06-19

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US (1) US4431520A (de)
EP (1) EP0073690B1 (de)
JP (1) JPS58108294A (de)
CA (1) CA1191804A (de)
DE (1) DE3264271D1 (de)
FR (1) FR2511389A1 (de)

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EP0096382A2 (de) * 1982-06-05 1983-12-21 VEBA OEL Entwicklungs-Gesellschaft mbH Verfahren zur Hydrierung von Schweröl, Bitumen und dergl.
EP0106221A2 (de) * 1982-10-19 1984-04-25 Rheinische Braunkohlenwerke AG. Verfahren zum Hydrieren von Schwer- und Rückstandsölen und dafür verwendete Katalysatoren
FR2548206A1 (fr) * 1983-06-29 1985-01-04 Inst Francais Du Petrole Procede de formation de melanges de sels metalliques solubles, principalement du vanadium et du nickel, et utilisation des melanges formes comme catalyseurs d'hydrotraitement d'hydrocarbures lourds, en phase liquide
FR2556000A1 (fr) * 1983-12-02 1985-06-07 Asahi Chemical Ind Procede de conversion d'un hydrocarbure lourd en un produit de plus de valeur ou plus leger
GB2159168A (en) * 1984-05-25 1985-11-27 Gulf Research Development Co Process for cracking high metals content feedstocks using a cracking catalyst mixture containing antimony and/or tin
EP0216306A2 (de) * 1985-09-27 1987-04-01 Rheinische Braunkohlenwerke AG. Verbesserte Katalysatoren zur Hydrierung von Schwer- und Rückstandsölen sowie festen kohlenstoffhaltigen Substanzen, ihre Herstellung und Verfahren unter Verwendung derselben
FR2594137A1 (fr) * 1986-02-10 1987-08-14 Inst Francais Du Petrole Procede d'hydrotraitement d'hydrocarbures lourds en phase liquide en presence d'un catalyseur disperse
FR2603598A1 (fr) * 1986-09-10 1988-03-11 Inst Francais Du Petrole Procede d'hydroconversion d'une charge lourde d'hydrocarbures
EP0263522A2 (de) * 1986-10-08 1988-04-13 VEBA OEL Technologie und Automatisierung GmbH Verfahren zur hydrierenden Konversion von Schwer- und Rückstandsölen
EP0271337A2 (de) * 1986-12-12 1988-06-15 Asahi Kasei Kogyo Kabushiki Kaisha Additiv für die Hydroumwandlung eines Schweröls
US4770764A (en) * 1983-03-19 1988-09-13 Asahi Kasei Kogyo Kabushiki Kaisha Process for converting heavy hydrocarbon into more valuable product

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NL8203780A (nl) * 1981-10-16 1983-05-16 Chevron Res Werkwijze voor de hydroverwerking van zware koolwaterstofhoudende olien.
US4592827A (en) * 1983-01-28 1986-06-03 Intevep, S.A. Hydroconversion of heavy crudes with high metal and asphaltene content in the presence of soluble metallic compounds and water
US4518488A (en) * 1983-02-28 1985-05-21 Standard Oil Company (Indiana) Metal-containing active carbon and methods for making and using same
US4863892A (en) * 1983-08-16 1989-09-05 Phillips Petroleum Company Antifoulants comprising tin, antimony and aluminum for thermal cracking processes
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US4637870A (en) * 1985-04-29 1987-01-20 Exxon Research And Engineering Company Hydrocracking with phosphomolybdic acid and phosphoric acid
US4708784A (en) * 1986-10-10 1987-11-24 Phillips Petroleum Company Hydrovisbreaking of oils
US4853110A (en) * 1986-10-31 1989-08-01 Exxon Research And Engineering Company Method for separating arsenic and/or selenium from shale oil
DE3912807A1 (de) * 1989-04-19 1990-11-08 Gfk Kohleverfluessigung Gmbh Katalysator bzw. additiv zur hydrierenden behandlung von schweren erdoelen bzw. schweren erdoelfraktionen sowie verfahren zur gewinnung des katalysators
US5000836A (en) * 1989-09-26 1991-03-19 Betz Laboratories, Inc. Method and composition for retarding coke formation during pyrolytic hydrocarbon processing
US5319119A (en) * 1991-03-15 1994-06-07 Asahi Kasei Kogyo Kabushiki Kaisha Oleophilic molybdenum compound for use in hydroconversion of a hydrocarbon and a method for producing the same
US5951849A (en) * 1996-12-05 1999-09-14 Bp Amoco Corporation Resid hydroprocessing method utilizing a metal-impregnated, carbonaceous particle catalyst
US5954945A (en) * 1997-03-27 1999-09-21 Bp Amoco Corporation Fluid hydrocracking catalyst precursor and method
US5807478A (en) * 1997-05-16 1998-09-15 Exxon Research And Engineering Company Bitumen modification using fly ash derived from bitumen coke
JP3404522B2 (ja) * 1999-10-29 2003-05-12 独立行政法人産業技術総合研究所 重質油の水素化処理方法
US20030234010A1 (en) * 2002-06-25 2003-12-25 Redmond Scott D. Methods and apparatus for converting internal combustion engine (ICE) vehicles to hydrogen fuel
US20040016769A1 (en) * 2002-03-15 2004-01-29 Redmond Scott D. Hydrogen storage, distribution, and recovery system
US7169489B2 (en) * 2002-03-15 2007-01-30 Fuelsell Technologies, Inc. Hydrogen storage, distribution, and recovery system
US7011768B2 (en) * 2002-07-10 2006-03-14 Fuelsell Technologies, Inc. Methods for hydrogen storage using doped alanate compositions
US20040065171A1 (en) * 2002-10-02 2004-04-08 Hearley Andrew K. Soild-state hydrogen storage systems
US7737072B2 (en) * 2004-09-10 2010-06-15 Chevron Usa Inc. Hydroprocessing bulk catalyst and uses thereof
EP1754770B1 (de) * 2005-08-16 2017-01-18 Research Institute of Petroleum Verfahren zur Hydrierung von schweren Kohlenwasserstoffe
JP5566896B2 (ja) * 2007-10-31 2014-08-06 シェブロン ユー．エス．エー． インコーポレイテッド 水素化処理のバルク触媒及びその使用
US8722556B2 (en) * 2007-12-20 2014-05-13 Chevron U.S.A. Inc. Recovery of slurry unsupported catalyst
US7818969B1 (en) 2009-12-18 2010-10-26 Energyield, Llc Enhanced efficiency turbine
US10041004B2 (en) * 2014-11-06 2018-08-07 Uop Llc Processes for producing deashed pitch

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Cited By (20)

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Publication number Priority date Publication date Assignee Title
EP0096382A3 (en) * 1982-06-05 1985-05-08 Veba Oel Entwicklungs-Gesellschaft Mbh Process for the hydrogenation of heavy oils, bitumen and the like
EP0096382A2 (de) * 1982-06-05 1983-12-21 VEBA OEL Entwicklungs-Gesellschaft mbH Verfahren zur Hydrierung von Schweröl, Bitumen und dergl.
EP0106221A2 (de) * 1982-10-19 1984-04-25 Rheinische Braunkohlenwerke AG. Verfahren zum Hydrieren von Schwer- und Rückstandsölen und dafür verwendete Katalysatoren
EP0106221A3 (de) * 1982-10-19 1985-05-15 Rheinische Braunkohlenwerke AG. Verfahren zum Hydrieren von Schwer- und Rückstandsölen und dafür verwendete Katalysatoren
US4770764A (en) * 1983-03-19 1988-09-13 Asahi Kasei Kogyo Kabushiki Kaisha Process for converting heavy hydrocarbon into more valuable product
FR2548206A1 (fr) * 1983-06-29 1985-01-04 Inst Francais Du Petrole Procede de formation de melanges de sels metalliques solubles, principalement du vanadium et du nickel, et utilisation des melanges formes comme catalyseurs d'hydrotraitement d'hydrocarbures lourds, en phase liquide
FR2556000A1 (fr) * 1983-12-02 1985-06-07 Asahi Chemical Ind Procede de conversion d'un hydrocarbure lourd en un produit de plus de valeur ou plus leger
GB2159168A (en) * 1984-05-25 1985-11-27 Gulf Research Development Co Process for cracking high metals content feedstocks using a cracking catalyst mixture containing antimony and/or tin
GB2159168B (en) * 1984-05-25 1989-05-10 Gulf Research Development Co Process for cracking high metals content feedstocks using a cracking catalyst mixture containing antimony and/or tin
EP0216306A2 (de) * 1985-09-27 1987-04-01 Rheinische Braunkohlenwerke AG. Verbesserte Katalysatoren zur Hydrierung von Schwer- und Rückstandsölen sowie festen kohlenstoffhaltigen Substanzen, ihre Herstellung und Verfahren unter Verwendung derselben
EP0216306A3 (de) * 1985-09-27 1987-08-05 Rheinische Braunkohlenwerke AG. Verbesserte Katalysatoren zur Hydrierung von Schwer- und Rückstandsölen sowie festen kohlenstoffhaltigen Substanzen, ihre Herstellung und Verfahren unter Verwendung derselben
EP0235003A1 (de) * 1986-02-10 1987-09-02 Institut Français du Pétrole Verfahren zur Hydrobehandlung von schweren Kohlenwasserstoffen in flüssiger Phase in Gegenwart eines dispergierten Katalysators
FR2594137A1 (fr) * 1986-02-10 1987-08-14 Inst Francais Du Petrole Procede d'hydrotraitement d'hydrocarbures lourds en phase liquide en presence d'un catalyseur disperse
FR2603598A1 (fr) * 1986-09-10 1988-03-11 Inst Francais Du Petrole Procede d'hydroconversion d'une charge lourde d'hydrocarbures
EP0263522A2 (de) * 1986-10-08 1988-04-13 VEBA OEL Technologie und Automatisierung GmbH Verfahren zur hydrierenden Konversion von Schwer- und Rückstandsölen
EP0263522A3 (en) * 1986-10-08 1989-04-12 Intevep S.A. Process for the hydroconversion of heavy and residual oils
EP0516187A2 (de) * 1986-10-08 1992-12-02 VEBA OEL Technologie und Automatisierung GmbH Verfahren zur hydrierenden Konversion von Schwer- und Rückstandsölen
EP0516187A3 (en) * 1986-10-08 1992-12-09 Veba Oel Technologie Gmbh Process for the hydroconversion of heavy and residual oils
EP0271337A2 (de) * 1986-12-12 1988-06-15 Asahi Kasei Kogyo Kabushiki Kaisha Additiv für die Hydroumwandlung eines Schweröls
EP0271337A3 (en) * 1986-12-12 1989-04-12 Asahi Kasei Kogyo Kabushiki Kaisha An additive for the hydroconversion of a heavy hydrocarbon oil

Also Published As

Publication number Publication date
JPS58108294A (ja) 1983-06-28
US4431520A (en) 1984-02-14
FR2511389B1 (de) 1983-11-18
DE3264271D1 (en) 1985-07-25
EP0073690B1 (de) 1985-06-19
FR2511389A1 (fr) 1983-02-18
CA1191804A (fr) 1985-08-13

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