EP0516187A2 - Procédé d'hydroconversion d'huiles lourdes et résiduelles - Google Patents

Procédé d'hydroconversion d'huiles lourdes et résiduelles Download PDF

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Publication number
EP0516187A2
EP0516187A2 EP19920112758 EP92112758A EP0516187A2 EP 0516187 A2 EP0516187 A2 EP 0516187A2 EP 19920112758 EP19920112758 EP 19920112758 EP 92112758 A EP92112758 A EP 92112758A EP 0516187 A2 EP0516187 A2 EP 0516187A2
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EP
European Patent Office
Prior art keywords
catalyst
additive
weight
grain fraction
particle size
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Application number
EP19920112758
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German (de)
English (en)
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EP0516187A3 (en
EP0516187B1 (fr
Inventor
Klaus Kretschmar
Ludwig Dr. Merz
Klaus Dr. Niemann
José Quinta Yole Guitian
Julio Edif.La Villa Krasuk
Franzo Dr. Quinta Mimie Maruffo
Klaus Kurzeja
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Veba Oel Technologie und Automatisierung GmbH
Intevep SA
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Veba Oel Technologie und Automatisierung GmbH
Intevep SA
Petroleos de Venezuela SA
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Publication of EP0516187A3 publication Critical patent/EP0516187A3/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0041—Working-up used lubricants to recover useful products ; Cleaning by thermal processes by hydrogenation processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C1/00—Working-up tar
    • C10C1/20—Refining by chemical means inorganic or organic compounds
    • C10C1/205—Refining by chemical means inorganic or organic compounds refining in the presence of hydrogen
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
    • C10G47/26—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries

Definitions

  • the invention relates to a method for the hydrogenative conversion of heavy and residual oils, waste and waste oils, tar sands and the like.
  • heavy metals V + Ni
  • asphaltenes of 2 wt .-% or more
  • Conradson coal of 5 wt .-% or more and a density of less than 20 ° API, which with a catalyst or additive or a mixture thereof from the group consisting of red mud, Fe2O3, iron ores, hard coal, brown coal, hard coal coke, brown coal coke, preferably impregnated with heavy metal salts, activated carbon, carbon blacks from the gasification of solid or liquid fuels, cokes from hydrogenation or distillation residues are contacted with Hydrogen at a hydrogen partial pressure between 50 and 300 bar, a temperature between 300 and 500 ° C, a throughput between 0.1 to 5 t / m3h, a gas / liquid ratio between 100 and 10,000 Nm3 / t, gas velocities
  • the feedstocks are characterized by a high metal, sulfur and asphalt content as well as a high tendency to form coke.
  • the invention relates in particular to a catalytic process for converting hydrocarbon-containing feedstocks such as Orinoco Belt Crudes, Maracaibo Lake Crudes, tar sands from Athabasca and Canada crude oils such as Cold Lake in the sump phase in the presence of hydrogen.
  • the feedstocks have a sulfur content between 2 and 6%, a metal content (vanadium and nickel) of 200 to 1400 ppm and more, a density of less than 20 ° API, a coking residue of more than 2% and a residue content of more than 40% .-% (500 ° C+).
  • hydrocracking conditions pressure, temperature, gas / oil ratio etc.
  • tendency to coke a catalyst or
  • Additive such as activated coke from hard coal or lignite, soot, red mud, ferric oxide, blast furnace dust, ash from the gasification process of the aforementioned crude oils, natural, inorganic minerals containing iron such as laterite and limonite, in an amount of 0.5 to 15% by weight. % Based on the liquid or liquid and solid use added to the hydrogenation process.
  • the American patent US 4,396,495 describes a process for the conversion of hydrocarbon-containing dark oils in suspension reactors using finely divided metal catalysts, such as vanadium sulfide, with a particle size of 0.1 to 2000 ⁇ m, preferably 0.1 to 100 ⁇ m.
  • a silicone based anti-foaming agent is also added to to reduce foam formation in the hydrocracking zone, where the reaction takes place at 510 ° C., 204 bar and a catalyst concentration of 0.1 to 10% by weight.
  • This method cannot be used at temperatures above 430 ° C because the silicones decompose and lose their activity. The silicon remains in the low-boiling fraction and leads to difficulties in the upstream process.
  • Canadian Patent CA 1,117,887 describes a hydrocracking process for converting heavy oil into lighter hydrocarbons under high pressure and high temperature.
  • the heavy oil is mixed with a finely divided brown coal additive with a grain size of less than 149 ⁇ m, which is loaded with at least one metal from element group IVa or VIII of the periodic table.
  • US Pat. No. 4,591,426 also describes a hydroconversion process for heavy feedstocks with a metal content of at least 200 ppm at temperatures above 400 ° C. and a total hydrogen pressure of 1022 bar using a natural inorganic material such as laterite or limonite.
  • the invention has for its object to avoid excessive foam formation in a method of the type mentioned.
  • Another object of the invention is the improved utilization of the reaction zone or the hydrogenation reaction.
  • the amount of liquid in the hydrocracking zone of the reactor initially increases for a given gas velocity when larger particles are used.
  • the present invention enables improved utilization of the reaction zone by using two metering streams of the catalyst or additive with two different particle size distributions.
  • One embodiment of the present invention discloses a conversion process for heavy crude oils with a density of less than 20 ° API, more than 200 ppm metal content and more than 5% by weight Conradson coal in the presence of hydrogen and a catalyst or additive in a bottom phase reactor, in which an upward three-phase flow is formed.
  • the catalyst can comprise metals from element group Va, VIa or VIIIa of the periodic table, with or without porous support, on which metals also contained in the crude oil are deposited.
  • the present invention discloses that for very high conversion rates (90% and more) of fractions boiling above 500 ° C at moderately high flow rates (0.5t / m3h or more), a considerable proportion of small particles (below 50 microns) is needed , since this brings significant advantages for the hydrogenation capacity of the catalyst system.
  • thermodynamic, fluid dynamic and kinetic relationships in the bottom phase hydrogenation with the addition of additives or catalysts in a bottom-flow tube reactor have not yet been completely clarified, it is assumed that the coarse grain fraction limits the foam formation or the gas residence time and that the amount of liquid is limited to Cost of the gas portion within the reactor, which is reflected by the differential pressure across the reactor height as well expresses the conversion rate and the preheating temperature. This phenomenon is noticeable at gas velocities in the reactor of more than 3 cm / s, temperatures of more than 250 ° C and pressures between 50 and 300 bar.
  • the corresponding catalyst mixture which is formed from additives of two different particle size distributions, can also be prepared beforehand in another separate apparatus, in order then to be brought into contact with the oil insert via a single metering system.
  • a remarkable aspect of the present invention is that two separate particle size distributions of the catalyst or the additive are used, both fractions being able to consist of the same or different materials.
  • the present invention discloses a method for treating heavy oils of various origins, such as petroleum, shale oil, tar sand, etc. These heavy oils have a high metal and asphaltene content and a high tendency to form coke. High metal concentrations (vanadium and nickel) of over 200 ppm, asphaltene contents over 2% by weight, Conradson coal values over 5% and more than 50% by weight residue fraction (500 ° C+) are typical.
  • the invention is concerned with a hydroconversion process in which the use of heavy oil in the presence of hydrogen with a catalyst or additive, such as activated coke, lignite, red mud, iron III oxide, blast furnace dust, ash from the gasification process of heavy oil, natural inorganic iron-containing mineral such as limonite or laterite, which in an amount of 0, 5 to 15 wt .-% is added in relation to the liquid content, is contacted.
  • a catalyst or additive such as activated coke, lignite, red mud, iron III oxide, blast furnace dust, ash from the gasification process of heavy oil, natural inorganic iron-containing mineral such as limonite or laterite, which in an amount of 0, 5 to 15 wt .-% is added in relation to the liquid content, is contacted.
  • a metering system for adding the highly active fine grain fraction, which has a grain size of less than 100 ⁇ m, preferably less than 50 ⁇ m.
  • the coarse grain fraction which influences the fluid dynamic behavior of the liquid phase reaction system and increases the liquid filling in the reactor, is entered via the second metering system, this fraction being characterized by a grain size between 100 and 2000 ⁇ m, preferably 150 and 1000 ⁇ m.
  • the proportion of the coarse grain fraction is between 5 and 80% by weight, preferably between 10 and 30% by weight, of the total amount of catalyst or additive.
  • a special embodiment of the invention is characterized in that the coarse grain fraction contains a proportion of 0.0 to 70% by weight, preferably less than 50% by weight, of fine particles with a particle size of at most 100 ⁇ m.
  • the proportion of the coarse grain fraction is 20% by weight or more, based on the total amount of the catalyst or additive used.
  • a further preferred embodiment is characterized in that the proportion of the coarse grain fraction is 20% by weight and in the subsequent operating period is at least 5% by weight of the amount of catalyst or additive.
  • the coarse grain fraction is added only when starting up or discontinuously in the course of the operating period.
  • a method in which the fine grain fraction used as the additive and the coarse grain fraction do not consist of the same material is particularly advantageous.
  • the following combinations are preferred: Fine grain fraction Coarse grain fraction Red mud Coal soot ground brown coal ground brown coal ground brown coal natural materials containing iron Bituminous coal or ground brown coal natural inorganic materials containing iron natural inorganic materials containing iron natural inorganic materials containing iron Hard coal or petroleum coke natural inorganic materials containing iron Soot from gasification processes
  • FIG. 1 shows the hydroconversion process according to the invention with subsequent distillation and hydrosulfurization in a flow diagram.
  • FIG. 2 shows a double logarithmic plot of the cumulative weight fractions over the logarithm of the particle sizes of samples A and B according to Tables 1 and 2.
  • FIG. 3 shows a corresponding application as in FIG. 2 for two samples which belong to a normal distribution, and for mixtures of these samples.
  • Figure 4 shows the effect of the proportion of the coarse grain fraction on the differential pressure over the reactor height of the first reactor.
  • the fine-grain fraction is introduced via line 1 with a grain size of less than 100 ⁇ m, preferably less than 50 ⁇ m, from the storage vessel 2 discontinuously via valve 3 into a weighing container 4, from which the desired catalyst is fed via a continuous screw conveyor 5 or the amount of additive is fed via line 6 to the mixing container 13.
  • the concentration of fine catalyst particles in the mixing container is set to 0.5 to 6% by weight, preferably to 0.5 to 3% by weight.
  • the coarse grain fraction of the single-use catalyst or additive which according to the invention has grain sizes of 100 to 2000 ⁇ m, preferably has 150 to 1000 microns supplied.
  • the coarse grain fraction is provided via line 7 in the storage vessel 8 and fed discontinuously to the weighing container 10 via valve 9.
  • the desired amount of coarse grain fraction is introduced into the mixing container 13 via a continuous screw conveyor 11 and mixed with the heavy oil and fine grain fraction fed via line 16, so that a concentration of coarse catalyst particles based on the heavy oil of 0.5 to 13%, preferably 0 , 5 to 6% is set.
  • the invention is not limited to the illustrated embodiment with the two dosing systems described.
  • the different grain fractions of the catalyst can also be supplied in other ways.
  • the heavy oil and the two grain fractions of the catalyst or additive are fed from the mixing container 13 via line 14 to a high-pressure pump 15 and via line 15 'to the heat exchangers 49 and 50, in which this material flow is preheated using the heat of reaction of the reaction products.
  • the fresh hydrogen is fed via line 61, the hydrogen-containing cycle gas via line 59 to the cycle gas preheater 63, where the gas is heated to 200 to 500 ° C. and is fed to the heater 18 together with the preheated feed stream from line 50 ′.
  • the reactor system consists of one or at least two reactors connected in series. To be favoured three reactors connected in series.
  • the reactors 20, 24 and 27 are vertical tubular reactors with or without internals, which are operated with the flow direction from bottom to top. Here the conversion takes place at temperatures between 400 and 490 ° C, preferably 430 and 480 ° C, a hydrogen partial pressure between 50 and 300 bar and a circulating gas volume of 100 Nm3 / t to 10000 Nm3 / t.
  • a quasi-isothermal mode of operation of the reactors is possible by supplying cold gas via lines 21, 23 and 26.
  • downstream hot separators which are operated at approximately the same temperature level as the reactors, the unconverted portion of the heavy and residual oils used as well as the solids is separated from the gaseous reaction products under process conditions.
  • the bottom product of the hot separator is expanded in a multi-stage flash unit.
  • the top product of the hot separators, the flash distillates and any crude oil distillate fractions to be processed are combined and fed to the downstream gas phase reactors. Hydrotreating or mild hydrocracking is carried out on a catalytic fixed bed under trickle flow conditions under the same total pressure as in the sump phase.
  • the gaseous reaction products (C1 to C4 gases, H2S, NH3) are largely separated from the process gas, the remaining hydrogen is recycled as recycle gas.
  • two or three separate and independent metering systems are required in order to add the fine grain fraction with a grain size of less than 100 ⁇ m by one metering system and the coarse grain fraction with a grain size between 100 and 2000 ⁇ m by another metering system.
  • the proportion of the coarse grain fraction in the total amount of catalyst is 5 to 80%, preferably 10 to 30%, the total amount of catalyst or additive is between 0.5 and 15% by weight, based on the heavy crude oil used.
  • the amount of liquid in the reactor can be optimized so that the conversion of the heavy crude oil in the reaction system increases while the preheating temperature is reduced, thereby reducing the investment and operating costs of the preheater system.
  • the process according to the invention has particular advantages in the event that the gas velocity in the Reactor under reaction conditions is greater than 3 cm / s based on the reactor cross section, which is normally true for gas velocities in industrial reactors.
  • the same additive or catalyst material is added as fine grain and as coarse grain fraction.
  • additives of different compositions for the fine and coarse grain fraction e.g. B. Fe2O3 as a fine grain fraction with a particle size with an upper limit of 30 microns and for the coarse grain fraction activated coke from lignite with a lower grain size of 100 microns.
  • the two catalyst fractions do not necessarily have to be fed to the catalyst-oil mixing container 13 (FIG. 1) via two separate metering systems. but can also be mixed beforehand and added directly as a catalyst mixture.
  • the only decisive factor is the use of two different particle size distributions of the catalyst or additive from the same or different chemical species. The use of these two catalyst fractions leads to the unexpected result described in the invention.
  • Tables 1 and 2 show the cumulative weight distributions of samples A and B (coarse-grain and fine-grain fractions), which are each produced by a special grinding process.
  • the present invention also allows closed-circuit grinding, in which the ground product is separated and the coarse material in the Grinding device is returned.
  • This customary procedure is not the same as mixing separate catalyst streams of different grain sizes, but aims to achieve a certain yield with a given sieve size.
  • FIG. 3 shows mixtures of samples A and B - sample C (50% A and 50% B, table 3), sample D (30% A and 70% B, table 4), sample E (10% A and 90% B, Table 5), - and it can be seen that the mixtures cannot be represented by straight lines like the pure samples, but result in curves.
  • (% By weight) % by weight rough +% By weight fine
  • the amount of catalyst can be minimized if the minimum amount of coarse grain fraction required to avoid foam formation is used.
  • the double catalyst metering system gives greater flexibility to reduce the total amount of catalyst.
  • the coarse catalyst can be replaced by the fine-grain fraction under operating conditions when the foam formation has been brought under control. Since the latter reduces coke formation, this in turn enables a reduction in the amount of fine-grain fraction to be added, so that a minimization of the total amount added to the reactor system is made possible.
  • a preferred mode of operation is therefore the supply of the fine-grain and coarse-grain fractions through two separate metering systems.
  • This invention can also be used for the hydrogenation of mixtures of heavy, residual and waste oils with ground lignite and / or hard coal, the oil / coal weight ratio preferably being between 5: 1 and 1: 1.
  • the coal can be used as a coarse grain fraction with a corresponding proportion of a grain size of 100 ⁇ m and more.
  • the hydrocracking product is fed via line 28 into the first hot separator 29 in order to separate the gas / vapor phase from the heavier liquid products which contain unconverted residues, catalyst and additive.
  • the temperature of the hot separators 29 and 33 is regulated in a range from 300 to 450 ° C. by supplying quench gas via lines 32 and 34, which is fed in at the bottom.
  • the second hot separator 33 mainly serves as a scraper for the gas phase reactors 40 and 46.
  • the top product of the second hot separator 33 is combined via line 36, the flash distillate 77 as well as the crude oil distillate 36 ', which is produced elsewhere, and the gas phase reactors 40 and 46 at the same total pressure and approximately the same or fed to a somewhat reduced temperature as in the bottom phase reactor.
  • the operating conditions of these reactors are according to the invention for the pressure between 50 and 300 bar, for the temperature between 300 and 450 ° C and for the gas / liquid ratio between 50 and 10000 Nm3 / t.
  • Hydrotreating or mild is carried out in this conventional reactor Hydrocracking at fixed bed reaction zones under trickle flow conditions using a conventional hydrodesulfurization catalyst or a mild hydrocracking catalyst from groups VIa or VIIIa of the periodic table on an alumina support.
  • the product is fed via line 47 to intensive cooling and condensation (49, 50).
  • the heat of reaction is used to preheat the fresh insert.
  • the gas / liquid mixture is fed to the high-pressure cold separator 52 via line 51.
  • the liquid product is relaxed and can then be fed to the standard refinery technology.
  • the gaseous reaction product After passing through the cold separator 52, the gaseous reaction product is separated as much as possible from the process gas which is discharged via line 56. The remaining hydrogen is fed to the compressor 58 via line 57 and returned to the process via line 59.
  • the bottom product of the hot separators 29 and 33 is fed via lines 32 and 34 to a multi-stage flash unit 65 and 72, decompressed and the residue of the used catalysts or additives is removed for workup, for example by carbonization, gasification or solids separation, via line 73 in order to be used again later can.
  • a vertical bubble column reactor without internals the temperature of which is controlled via the outlet temperature of a preheater system and via a cold gas quench system, is charged with a specific throughput of 1.5 t / m3h with vacuum residue from a conventional residual oil of Venezuelan origin at a hydrogen partial pressure of 190 bar, whereby 2000 Nm3 of hydrogen can be used per ton of residue.
  • the gas velocity is 6 cm / s. 2% by weight of lignite coke with a sharp upper grain limit at 90 ⁇ m are added to the feed product.
  • a temperature in the reactor of 455 ° C. is reached at a preheater outlet temperature of 447 ° C.
  • the differential pressure across the reactor height is about 100 mbar. A residue conversion of approximately 45% is achieved under these conditions.
  • the system was then operated with two different dosing systems.
  • the total amount of catalyst was again 2% by weight.
  • the differential pressure increased from 100 mbar to approximately 300 mbar, while the preheater outlet temperature decreased from 447 ° C to 438 ° C.
  • the conversion rate (RU) of the residue rose from 45 to 62%.
  • H middle Temperature ° C Conversion% A 100% by weight 30 ⁇ m 0.5 461 90 B 75% by weight 30 ⁇ m 0.5 455 90 25% by weight 90-130 ⁇ m C. like B 0.75 455 78 D like B 0.75 461 90
  • the differential pressure can be influenced when using two separate and independent metering systems according to this invention can ( Figure 4); an increase or decrease depends on the amount of the coarse grain fraction used (50/200 ⁇ m with 70%> 100 ⁇ m).
  • the differential pressure is completely stable despite full filling of the reactor.
  • the differential pressure increases at a rate of 5 mbar / h . If the addition of the coarse-grain fraction is stopped and replaced by an additional 2% by weight of fine-grain fraction, so that the total amount of catalyst is still 4%, the differential pressure drops at a rate of 7 mbar / h. This test was carried out at a total pressure of 140 bar, a gas / liquid ratio of 1500 Nm3 / t and a gas velocity of 6 cm / s.
  • a natural mineral Fe2O3-containing catalyst with a grain size of less than 20 ⁇ m is fed to the reactor through one of two installed metering systems.
  • a coarse grain fraction with a grain size of less than 300 ⁇ m and a 50% proportion of particles with a grain size of less than 100 ⁇ m is supplied by the second metering system.
  • the total amount of catalyst was 3.1% based on the feed.
  • the insert consisted of Morichal vacuum residue.
  • the total pressure in this test was 170 bar with a hydrogen partial pressure of 130 bar.
  • the gas velocity in the reactor system was 7.8 cm / s.
  • the fine grain fraction (1.1% by weight based on the feed) with a grain size of less than 20 ⁇ m and the coarse grain fraction (2% by weight based on the use) with a grain size of less than 300 ⁇ m and a proportion of 50% by weight % with a grain size of less than 100 ⁇ m was fed to the reactor in two separate metering systems. Under these operating conditions the conversion rate was 92%, the asphaltene conversion 90% and the coke production 1.2% (test 1, table 8).
  • the amount of fine grain fraction (below 30 ⁇ m) is reduced to 0.6% by weight and the amount of coarse grain fraction (below 300 ⁇ m) with 50% by weight below 100 ⁇ m is reduced to 2.5% by weight. % is increased while maintaining a total catalyst quantity of 3.1% by weight, the crude oil conversion is of the same order of magnitude, namely 92%. However, the asphaltene conversion drops to 65%, while the coke formation increases to 2.5%, which leads to considerable problems when working up in the hot separator (Test 2, Table 8).
  • a 92% residue conversion and a 90% asphaltene conversion can also be achieved when the coarse grain fraction increases to 2.5% by weight if the total amount of catalyst increases by 0.5% by weight to a total of 3.6% by weight (Test 3, Table 8).

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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  • Lubricants (AREA)
EP92112758A 1986-10-08 1987-10-08 Procédé d'hydroconversion d'huiles lourdes et résiduelles Expired - Lifetime EP0516187B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19863634275 DE3634275A1 (de) 1986-10-08 1986-10-08 Verfahren zur hydrierenden konversion von schwer- und rueckstandsoelen
DE3634275 1986-10-08
EP87114725A EP0263522B1 (fr) 1986-10-08 1987-10-08 Procédé d'hydroconversion d'huiles lourdes et résiduelles

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EP87114725A Division-Into EP0263522B1 (fr) 1986-10-08 1987-10-08 Procédé d'hydroconversion d'huiles lourdes et résiduelles
EP87114725.2 Division 1987-10-08

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EP0516187A2 true EP0516187A2 (fr) 1992-12-02
EP0516187A3 EP0516187A3 (en) 1992-12-09
EP0516187B1 EP0516187B1 (fr) 1995-09-20

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EP87114725A Expired - Lifetime EP0263522B1 (fr) 1986-10-08 1987-10-08 Procédé d'hydroconversion d'huiles lourdes et résiduelles
EP92112758A Expired - Lifetime EP0516187B1 (fr) 1986-10-08 1987-10-08 Procédé d'hydroconversion d'huiles lourdes et résiduelles

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US (1) US4851107A (fr)
EP (2) EP0263522B1 (fr)
JP (1) JPH0696710B2 (fr)
AT (1) ATE128174T1 (fr)
CA (1) CA1302332C (fr)
DE (3) DE3634275A1 (fr)
ES (2) ES2043629T3 (fr)
NO (1) NO171219C (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2753112A1 (fr) * 1996-09-06 1998-03-13 Us Energy Procede pour produire des catalyseurs a partir de charbon
US9688934B2 (en) 2007-11-23 2017-06-27 Bixby Energy Systems, Inc. Process for and processor of natural gas and activated carbon together with blower

Families Citing this family (46)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5166118A (en) * 1986-10-08 1992-11-24 Veba Oel Technologie Gmbh Catalyst for the hydrogenation of hydrocarbon material
DE3737370C1 (de) * 1987-11-04 1989-05-18 Veba Oel Entwicklungs Gmbh Verfahren zur hydrierenden Konversion von Schwer- und Rueckstandsoelen,Alt- und Abfalloelen in Mischung mit Klaerschlaemmen
DE3806365C1 (fr) * 1988-02-27 1989-07-20 Veba Oel Entwicklungs-Gesellschaft Mbh, 4650 Gelsenkirchen, De
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US5755955A (en) * 1995-12-21 1998-05-26 Petro-Canada Hydrocracking of heavy hydrocarbon oils with conversion facilitated by control of polar aromatics
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ES2043629T3 (es) 1994-01-01
EP0263522A3 (en) 1989-04-12
JPS63146989A (ja) 1988-06-18
NO874205L (no) 1988-04-11
CA1302332C (fr) 1992-06-02
EP0516187A3 (en) 1992-12-09
JPH0696710B2 (ja) 1994-11-30
ES2078610T3 (es) 1995-12-16
US4851107A (en) 1989-07-25
EP0263522B1 (fr) 1993-09-15
EP0263522A2 (fr) 1988-04-13
NO171219C (no) 1993-02-10
NO874205D0 (no) 1987-10-07
ATE128174T1 (de) 1995-10-15
DE3634275A1 (de) 1988-04-28
EP0516187B1 (fr) 1995-09-20
DE3751534D1 (de) 1995-10-26
DE3787434D1 (de) 1993-10-21
NO171219B (no) 1992-11-02

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