EP0257260B2 - Verfahren zur hydrierenden Behandlung von mit Chlorbiphenylen kontaminierten Mineralölen - Google Patents

Verfahren zur hydrierenden Behandlung von mit Chlorbiphenylen kontaminierten Mineralölen Download PDF

Info

Publication number
EP0257260B2
EP0257260B2 EP87109958A EP87109958A EP0257260B2 EP 0257260 B2 EP0257260 B2 EP 0257260B2 EP 87109958 A EP87109958 A EP 87109958A EP 87109958 A EP87109958 A EP 87109958A EP 0257260 B2 EP0257260 B2 EP 0257260B2
Authority
EP
European Patent Office
Prior art keywords
weight
process according
oil
hydrogenation
phase
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.)
Expired - Lifetime
Application number
EP87109958A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0257260A1 (de
EP0257260B1 (de
Inventor
Werner Dr. Döhler
Rolf Dr. Holighaus
Klaus Dr. Niemann
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
Original Assignee
Veba Oel Technologie und Automatisierung GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=6304975&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0257260(B2) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Veba Oel Technologie und Automatisierung GmbH filed Critical Veba Oel Technologie und Automatisierung GmbH
Priority to AT87109958T priority Critical patent/ATE68099T1/de
Publication of EP0257260A1 publication Critical patent/EP0257260A1/de
Application granted granted Critical
Publication of EP0257260B1 publication Critical patent/EP0257260B1/de
Publication of EP0257260B2 publication Critical patent/EP0257260B2/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D3/00—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances
    • A62D3/30—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents
    • A62D3/37—Processes for making harmful chemical substances harmless or less harmful, by effecting a chemical change in the substances by reacting with chemical agents by reduction, e.g. hydrogenation
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
    • A—HUMAN NECESSITIES
    • A62—LIFE-SAVING; FIRE-FIGHTING
    • A62D—CHEMICAL MEANS FOR EXTINGUISHING FIRES OR FOR COMBATING OR PROTECTING AGAINST HARMFUL CHEMICAL AGENTS; CHEMICAL MATERIALS FOR USE IN BREATHING APPARATUS
    • A62D2101/00—Harmful chemical substances made harmless, or less harmful, by effecting chemical change
    • A62D2101/20—Organic substances
    • A62D2101/22—Organic substances containing halogen
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C10G2300/1007—Used oils
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S210/00—Liquid purification or separation
    • Y10S210/902—Materials removed
    • Y10S210/908—Organic
    • Y10S210/909—Aromatic compound, e.g. pcb, phenol

Definitions

  • the invention relates to a process for the hydrogenating treatment of mineral oils contaminated with multiply chlorinated biphenyls (PCBs), and to distillation residues of such mineral oils.
  • PCBs multiply chlorinated biphenyls
  • PCB-containing liquids or PCB-containing liquids mixed with oil residues after their use are to be regarded as hazardous waste, which must be recorded, properly handled and disposed of or safely disposed of.
  • thermal incineration processes therefore require extensive precautions to control and possibly treat the resulting exhaust gases and, if necessary, also to treat and landfill any solid residues that may occur. Still, thermal combustion processes are the most developed and widely used. The rest of the processes are only partially developed on a laboratory scale or on a semi-industrial scale.
  • EP-0 178 001 A describes a further process for working up by refining and / or eliminating halogen, nitrogen and / or sulfur-containing compounds which are difficult to biodegrade in hydrocarbon feed streams.
  • the feed stream is first passed together with hydrogen gas over a pre-column filled with an absorbent and then over a fixed bed contact preferably made of nickel or cobalt plus molybdenum on a support.
  • the object of the invention is to provide a further process which can be used on an industrial scale for working up PCB-containing waste oils.
  • This process enables multi-chlorinated biphenyls to be broken down to values of up to 1 ppm and below.
  • the mineral base oils contained as the main component can be reused without being lost, for example, by incineration or other mining processes.
  • this object is achieved in that the above-mentioned feed hydrogen pressurization under the typical conditions of a sump phase hydrogenation or a combined sump / gas phase hydrogenation at hydrogen pressures of 20 to 325 bar. Temperatures from 250 to 500 ° C and gas-oil ratios of 100 to 3000 Nm 3 t are subjected to, wherein 0.5 to 5 wt .-% of a hollow surface-containing suspended solid are used in the bottom phase hydrogenation.
  • This method is particularly suitable for waste oils containing PCB or with drilling oils, cutting oils, transformer oils, hydraulic oils and the like. Work up mixed used oils in a sump or combined sump / gas phase hydrogenation.
  • the feed oils are preferably used as such or in a mixture with residual oils, heavy oils or finely ground coal in the bottom phase hydrogenation, with the use of coal providing a step for preparing the mixture of finely ground coal and the oil components. It is advantageous to add 30 to 95% by weight, preferably 50 to 95% by weight of residual oil or heavy oil to the bottoms hydrogenation.
  • additive a finely divided carbon-containing surface-rich suspended material
  • the feed mixture then goes through a compression stage and is charged with hydrogen-containing cycle gas and fresh hydrogen.
  • heat exchangers in which heat is exchanged with product streams to heat the feed mixture, the mixture passes through a so-called preheater and enters the bottom phase reactor from below. They are generally vertical tubular reactors without internals.
  • the hydrogenation reaction takes place at elevated pressure, at hydrogen pressures between 20 and 325 bar, and at elevated temperature, between 250 and 500 ° C and at gas-oil ratios of 100 to 3,000 Nm 3 / t, with the gas is the hydrogen-containing hydrogenation gas.
  • the desired degree of conversion and the required limit for the degradation of the chlorobiphenyls determine the flow rate of the feed products. Typical values are 0.4 to 1.0 t / m 3 h.
  • the reaction products are expediently passed over a hot separator operated at reaction pressure and at a temperature which is preferably 20 to 50 ° C. lower than the reaction temperature.
  • the uncondensed hydrocarbons are removed overhead and the bottom products containing residues at the bottom.
  • Distillable heavy oil components can be separated in a downstream stripper and can be further processed by combining with the top product of the hot separator.
  • the residue behind the stripper can be used to generate hydrogen or energy.
  • a gas phase hydrogenation for further processing of the uncondensed reaction products, which have been drawn off at the top of the hot separator, can be directly coupled to the previously described bottom phase hydrogenation without reheating or depressurization.
  • the further hydrogenation, stabilization and removal in the gas phase hydrogenation, for example of heteroatoms such as sulfur or nitrogen, to obtain feedstocks with reformer feed specification or middle distillate takes place on fixed bed catalysts using commercially available catalysts.
  • the product streams After passing through the gas phase hydrogenation, the product streams are condensed and cooled by intensive heat exchange and separated into a liquid phase and a gas phase in a high-pressure cold separator. After the liquid phase has been let down, it is usually fed to a stabilizing column in order to remove the C 4 products and to obtain a stabilized syncrude.
  • the gaseous products pass through a gas scrubber to remove, among other things, H 2 S and NH 3 .
  • Part of the purified hydrogen-rich gas is recycled as cycle gas into the bottom phase hydrogenation.
  • the separation is then carried out in an atmospheric distillation, depending on the determination of the boiling cuts in naphtha, middle distillate and vacuum gas oil. If coal and feed oil are used together, the ratio is preferably 1:20 to 1: 1, in particular 1: 5 to 4: 5.
  • a cold separator stage with subsequent expansion and separation of the liquid products into an aqueous phase and a mineral oil-containing phase and atmospheric distillation of the oil-containing phase can also directly follow the bottom phase hydrogenation.
  • the suspended lignite coke from shaft and hearth furnaces, lignite coarse, soot from the gasification of heavy oil, hard coal are additives.
  • Lignite or hydrogenation residues and activated coke, petroleum coke and dusts from the Winkler gasification and high-temperature Winkler gasification of coal, ie materials with a large inner surface and with a pore structure for demetallization and deasphalting and for taking up coke precursors when carrying out the phase-phase hydrogenation are suitable .
  • Red masses, Bavarian masses, iron oxides and electrostatic filter dust and cyclone dust from metal / ore processing can also be used with advantage.
  • the proportion of these additives is preferably 0.5 to 5% by weight and, if carbon-containing additives are used, these can be mixed with salts of metals from subgroups 1 to 8 and 4.
  • Main group of the periodic system of the elements preferably iron, cobalt, nickel, vanadium, molybdenum, for example Fe (II) sulfate.
  • Alkaline earth compounds can also be used to neutralize the hydrogen halide and form water-soluble salts.
  • the sodium compounds for example sodium sulfide, are preferred.
  • a used motor oil with 1 100 ppm polychlorobiphenyl (PCB) is contacted in a continuous hydrogenation system at 430 ° C and a pressure of 280 bar with 1500 Nm 3 t hydrogen.
  • PCB polychlorobiphenyl
  • 1% by weight of Fe-containing (Fe 2 O 3 ) dust from iron ore processing and 0.2% by weight of Na 2 S are added to the oil.
  • the PCBs are broken down below the analytical detection limit of 1 ppm, while the waste oil undergoes a shift in the boiling point according to the following tables.
  • Waste oil Raffinate IBP start of boiling
  • ° C 256 98 ⁇ 100 ° C% by weight - - 100 - 300 ° C% by weight 2nd 24th 300 - 500 ° C% by weight 76 70 > 500 ° C% by weight 22 5
  • FBP end of boiling point
  • the lubricating oil fraction in the raffinate (Frakt. 300 -500 ° C) has a viscosity index of 120, it is therefore a base oil component for the production of a quality motor oil.
  • the proposed process is therefore much more economical than the thermal combustion process for waste oils containing PCBs, which is also carried out on an industrial scale, and it also avoids the problems associated with combustion of the formation of non-harmless secondary products of the combustion of chlorinated hydrocarbons or Oils containing chlorobiphenyls.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Business, Economics & Management (AREA)
  • Emergency Management (AREA)
  • Toxicology (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fire-Extinguishing Compositions (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Processing Of Solid Wastes (AREA)
EP87109958A 1986-07-11 1987-07-10 Verfahren zur hydrierenden Behandlung von mit Chlorbiphenylen kontaminierten Mineralölen Expired - Lifetime EP0257260B2 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87109958T ATE68099T1 (de) 1986-07-11 1987-07-10 Verfahren zur hydrierenden behandlung von mit chlorbiphenylen u. dgl. kontaminierten mineraloelen.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19863623430 DE3623430A1 (de) 1986-07-11 1986-07-11 Verfahren zur hydrierenden behandlung von mit chlorbiphenylen u. dgl. kontaminierten mineraloelen
DE3623430 1986-07-11

Publications (3)

Publication Number Publication Date
EP0257260A1 EP0257260A1 (de) 1988-03-02
EP0257260B1 EP0257260B1 (de) 1991-10-09
EP0257260B2 true EP0257260B2 (de) 1996-08-07

Family

ID=6304975

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87109958A Expired - Lifetime EP0257260B2 (de) 1986-07-11 1987-07-10 Verfahren zur hydrierenden Behandlung von mit Chlorbiphenylen kontaminierten Mineralölen

Country Status (8)

Country Link
US (1) US4810365A (enrdf_load_stackoverflow)
EP (1) EP0257260B2 (enrdf_load_stackoverflow)
JP (1) JP2544391B2 (enrdf_load_stackoverflow)
AT (1) ATE68099T1 (enrdf_load_stackoverflow)
CA (1) CA1297063C (enrdf_load_stackoverflow)
DE (2) DE3623430A1 (enrdf_load_stackoverflow)
ES (1) ES2025597T5 (enrdf_load_stackoverflow)
GR (2) GR3002876T3 (enrdf_load_stackoverflow)

Families Citing this family (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3723607A1 (de) * 1987-07-17 1989-01-26 Ruhrkohle Ag Verfahren zum hydrierenden aufarbeiten von altoelen
DE3839799A1 (de) * 1988-11-25 1990-07-05 Rwe Entsorgung Ag Verfahren zur aufarbeitung kontaminierter oele
EP0371201A1 (de) * 1988-12-01 1990-06-06 Ruhrkohle Aktiengesellschaft Verfahren zur Hydrierung von Organochlorverbindungen und Neutralisation des anfallenden Chlorwasserstoffs sowie Neutralisationsmittel für aus Organochlorverbindungen anfallenden Clorwasserstoff
DE3932927A1 (de) * 1989-10-03 1991-04-18 Hansjoerg Prof Dr Sinn Verfahren zur entfernung von organohalogenverbindungen aus kohlenwasserstoffgemischen, insbesondere aus pyrolyseprodukten in gasphase
US5051030A (en) * 1990-06-05 1991-09-24 Roy F. Weston, Inc. Chemical detoxification process for treatment of soils contaminated with halogenated organic compounds
US5316663A (en) * 1992-01-13 1994-05-31 Uop Process for the treatment of halogenated hydrocarbons
FR2687684A1 (fr) * 1992-02-24 1993-08-27 Font Pierre Amelioration des traitements des huiles usagees et autres.
WO1994014731A1 (en) * 1992-12-23 1994-07-07 Commonwealth Scientific And Industrial Research Organisation Destruction of halide containing organics and solvent purification
US5397459A (en) * 1993-09-10 1995-03-14 Exxon Research & Engineering Co. Process to produce lube oil basestock by low severity hydrotreating of used industrial circulating oils
US5951852A (en) * 1993-12-23 1999-09-14 Commonwealth Scientific And Industrial Research Organisation Et Al. Destruction of halide containing organics and solvent purification
CN1123268A (zh) * 1994-11-21 1996-05-29 陶氏化学公司 卤化烃的处理方法
US5849172A (en) * 1997-06-25 1998-12-15 Asarco Incorporated Copper solvent extraction and electrowinning process
IT1292420B1 (it) * 1997-06-26 1999-02-08 Enel Spa Processo per rimuovere policlorobifenili da olii minerali
DE19742266A1 (de) * 1997-09-25 1999-05-06 Ludger Dr Steinmann Aufwertung von Chemie- und Energierohstoffen durch Reaktion mit geringwertigen Rohstoffen
US7444305B2 (en) * 2001-02-15 2008-10-28 Mass Connections, Inc. Methods of coordinating products and service demonstrations
JP3758537B2 (ja) 2001-07-23 2006-03-22 豊田合成株式会社 Ｉｉｉ族窒化物系化合物半導体の製造方法
US7745369B2 (en) * 2003-12-19 2010-06-29 Shell Oil Company Method and catalyst for producing a crude product with minimal hydrogen uptake
US20050133406A1 (en) * 2003-12-19 2005-06-23 Wellington Scott L. Systems and methods of producing a crude product
US7674368B2 (en) * 2003-12-19 2010-03-09 Shell Oil Company Systems, methods, and catalysts for producing a crude product
US20070000810A1 (en) * 2003-12-19 2007-01-04 Bhan Opinder K Method for producing a crude product with reduced tan
US20070012595A1 (en) * 2003-12-19 2007-01-18 Brownscombe Thomas F Methods for producing a total product in the presence of sulfur
US20070000808A1 (en) * 2003-12-19 2007-01-04 Bhan Opinder K Method and catalyst for producing a crude product having selected properties
US20060289340A1 (en) * 2003-12-19 2006-12-28 Brownscombe Thomas F Methods for producing a total product in the presence of sulfur
TW200602591A (en) * 2004-07-08 2006-01-16 hong-yang Chen Gas supply device by gasifying burnable liquid
TWI415930B (zh) * 2005-04-06 2013-11-21 Shell Int Research 減少液態含烴原料總酸值（ｔａｎ）的方法
CN101166810A (zh) * 2005-04-11 2008-04-23 国际壳牌研究有限公司 生产原油产品的系统、方法和催化剂
JP2008536001A (ja) * 2005-04-11 2008-09-04 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 窒素含有量の少ない原油生成物の製造方法及び触媒
WO2006110556A1 (en) * 2005-04-11 2006-10-19 Shell International Research Maatschappij B.V. Method and catalyst for producing a crude product having a reduced nitroge content
BRPI0610670B1 (pt) 2005-04-11 2016-01-19 Shell Int Research método para produzir um produto bruto, catalisador para produzir um produto bruto, e, método para fabricar um catalisador
WO2007149917A1 (en) * 2006-06-22 2007-12-27 Shell Oil Company Methods for producing a total product with selective hydrocarbon production
CA2655581A1 (en) * 2006-06-22 2007-12-27 Shell Internationale Research Maatschappij B.V. Methods for producing a crude product from selected feed
CA2655600A1 (en) * 2006-06-22 2007-12-27 Shell Internationale Research Maatschappij B.V. Method for producing a crude product with a long-life catalyst
US20080085225A1 (en) * 2006-10-06 2008-04-10 Bhan Opinder K Systems for treating a hydrocarbon feed
JP5070169B2 (ja) * 2008-09-18 2012-11-07 Ｊｘ日鉱日石エネルギー株式会社 炭化水素油の製造方法
WO2025051086A1 (en) 2023-09-04 2025-03-13 Basf Se Recycling method and recycled products

Family Cites Families (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE474915A (enrdf_load_stackoverflow) * 1941-12-26
US2377546A (en) * 1943-08-30 1945-06-05 Phillips Petroleum Co Process for treating hydrocarbon containing organically combined fluorine
US2412220A (en) * 1944-01-03 1946-12-10 Phillips Petroleum Co Treatment of fluorine-containing hydrocarbon mixtures
US2409372A (en) * 1944-01-03 1946-10-15 Phillips Petroleum Co Removal of organic fluorine
US2413871A (en) * 1945-07-24 1947-01-07 Phillips Petroleum Co Process of removing organically combined chlorine from hydrocarbons
US2535735A (en) * 1945-10-23 1950-12-26 Phillips Petroleum Co Method of removing aluminum halides in hydrocarbon conversion processes
US2917456A (en) * 1956-12-13 1959-12-15 American Cyanamid Co Process for hydrodesulfurizing crude oil in the presence of coke
NL300450A (enrdf_load_stackoverflow) * 1962-11-16
US3355376A (en) * 1965-11-15 1967-11-28 Consolidation Coal Co Hydrocracking of polynuclear hydrocarbons
US3595931A (en) * 1968-05-28 1971-07-27 Gulf Research Development Co Hydrogenolysis of aromatic halides
US3855347A (en) * 1972-09-15 1974-12-17 Badger Co Process for hydrogenating halogenated hydrocarbons
US3935295A (en) * 1973-01-23 1976-01-27 Catalysts And Chemicals, Inc. Process for removing chlorine-containing compounds from hydrocarbon streams
US3925193A (en) * 1974-10-10 1975-12-09 Phillips Petroleum Co Removal of fluorides from catalytic reactor feed
CA1156449A (en) * 1979-11-30 1983-11-08 Oscar L. Norman Method of destruction of polychlorinated biphenyls
DE3004968A1 (de) * 1980-02-11 1981-08-20 Sante M Cundari Material zur waermeerzeugung, dessen herstellung und verwendung
US4351978A (en) * 1980-07-21 1982-09-28 Osaka Prefectural Government Method for the disposal of polychlorinated biphenyls
NL8402837A (nl) * 1984-09-14 1986-04-01 Kinetics Technology Werkwijze voor het zuiveren en/of onschadelijk maken van een door halogeen-, stikstof- en/of zwavel (verbindingen) verontreinigde vloeibare koolwaterstofstroom.
US4601817A (en) * 1984-09-21 1986-07-22 Globus Alfred R Treatment of hazardous materials
US4623448A (en) * 1985-03-12 1986-11-18 Moreco Energy, Inc. Removing halogenated polyphenyl materials from used oil products
US4599472A (en) * 1985-06-27 1986-07-08 Phillips Petroleum Company Purification of iodine-containing mixtures and compositions useful therefor
US4719007A (en) * 1986-10-30 1988-01-12 Uop Inc. Process for hydrotreating a hydrocarbonaceous charge stock
JPH101847A (ja) * 1996-06-12 1998-01-06 Tsudakoma Corp ウォータジェットルームの切り換え弁の動作安定化方法

Also Published As

Publication number Publication date
JPS6323989A (ja) 1988-02-01
EP0257260A1 (de) 1988-03-02
ATE68099T1 (de) 1991-10-15
ES2025597T3 (es) 1992-04-01
JP2544391B2 (ja) 1996-10-16
GR3002876T3 (en) 1993-01-25
US4810365A (en) 1989-03-07
DE3623430C2 (enrdf_load_stackoverflow) 1989-02-23
DE3623430A1 (de) 1988-01-28
DE3773586D1 (de) 1991-11-14
EP0257260B1 (de) 1991-10-09
ES2025597T5 (es) 1996-11-01
GR3021219T3 (en) 1997-01-31
CA1297063C (en) 1992-03-10

Similar Documents

Publication Publication Date Title
EP0257260B2 (de) Verfahren zur hydrierenden Behandlung von mit Chlorbiphenylen kontaminierten Mineralölen
DE69100303T2 (de) Verfahren für die gleichzeitige Behandlung von zwei gefährlichen Chargen.
DE68926747T2 (de) Gleichzeitige Hydrodehalogenierung von zwei halogenierte organische Verbindungen enthaltenden Strömen
DE69914145T2 (de) Integrierte Wasserstoffbehandlung und Hydrocrackverfahren
EP0377606B1 (de) Verfahren zur reinigung und regenerierung von altölen
DE102019133911B4 (de) Verfahren zur Co-Verarbeitung
DE2215665C3 (de) Verfahren zum Herstellen von Benzin und raffinierten flüssigen Kohlenwasserstoffen
DD268477A5 (de) Verfahren zur hydrierenden konversion von schwer- und rueckstandsoelen
DE69121573T2 (de) Hydrierende Konversion eines Abfalleinsatzstoffes aus hochreaktiven organischen Verbindungen
DE2850540C2 (de) Verfahren zur Aufbereitung von Altöl
DE3437374A1 (de) Verfahren zur rueckgewinnung von wasserstoff
EP0372276B1 (de) Verfahren zur Aufarbeitung kontaminierter Öle
EP0314992A2 (de) Verfahren zur hydrierenden Konversion von Schwer- und Rückstandsölen, Alt- und Abfallölen in Mischung mit Klärschlämmen
EP0299149A2 (de) Verfahren zum hydrierenden Aufbereiten von Altölen
DE69419703T2 (de) Verfahren zur Gewinnung von verwendbaren Materialien durch Cracken von Kunststoffen
EP0330757B1 (de) Verfahren zur Aufarbeitung von Abfallstoffen u. dgl. durch Schwelung und anschliessende Weiterverarbeitung des Schwelöls
DE3033259A1 (de) Verfahren zur loesungsmittelraffination von kohle
DE3875314T2 (de) Verfahren zum hydrieren von temperaturempfindlichen abfall-kohlenwasserstoffmaterialien.
EP0230543A1 (de) Verfahren zur Aufarbeitung von Altöl
DE3229898A1 (de) Verfahren zur hydrobehandlung eines kohlenwasserstoffhaltigen materials
DE2821159C2 (de) Verfahren zur Herstellung von im wesentlichen aschefreiem Schmieröl
DE1212662B (de) Verfahren zum Entfernen metallischer und stickstoffhaltiger Verunreinigungen aus Kohlenwasserstoffoelen
DE2259959C3 (de) Verfahren zur Herstellung von Heizölen durch Asphaltenabtrennung und zweistufige katalytische hydrierende Entschwefelung
DE3329222A1 (de) Verfahren zur kohleverfluessigung mit einem aktivierten zinksulfidkatalysator
DE68909587T2 (de) Behandlung eines temperaturempfindlichen Kohlenwasserstoffeinsatzes.

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19870718

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE ES FR GB GR IT LI LU NL SE

17Q First examination report despatched

Effective date: 19890807

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: VEBA OEL TECHNOLOGIE GMBH

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE ES FR GB GR IT LI LU NL SE

REF Corresponds to:

Ref document number: 68099

Country of ref document: AT

Date of ref document: 19911015

Kind code of ref document: T

REF Corresponds to:

Ref document number: 3773586

Country of ref document: DE

Date of ref document: 19911114

ET Fr: translation filed
ITF It: translation for a ep patent filed
GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2025597

Country of ref document: ES

Kind code of ref document: T5

PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

26 Opposition filed

Opponent name: RWE ENTSORGUNG AKTIENGESELLSCHAFT

Effective date: 19920429

NLR1 Nl: opposition has been filed with the epo

Opponent name: RWE ENTSORGUNG AG.

REG Reference to a national code

Ref country code: GR

Ref legal event code: FG4A

Free format text: 3002876

RAP2 Party data changed (patent owner data changed or rights of a patent transferred)

Owner name: VEBA OEL TECHNOLOGIE UND AUTOMATISIERUNG GMBH

NLT2 Nl: modifications (of names), taken from the european patent patent bulletin

Owner name: VEBA OEL TECHNOLOGIE UND AUTOMATISIERUNG GMBH TE G

EPTA Lu: last paid annual fee
EAL Se: european patent in force in sweden

Ref document number: 87109958.6

PLAB Opposition data, opponent's data or that of the opponent's representative modified

Free format text: ORIGINAL CODE: 0009299OPPO

R26 Opposition filed (corrected)

Opponent name: RWE ENTSORGUNG AKTIENGESELLSCHAFT

Effective date: 19920429

NLR1 Nl: opposition has been filed with the epo

Opponent name: RWE ENTSORGUNG AKTIENGESELLSCHAFT

PLAW Interlocutory decision in opposition

Free format text: ORIGINAL CODE: EPIDOS IDOP

PUAH Patent maintained in amended form

Free format text: ORIGINAL CODE: 0009272

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: PATENT MAINTAINED AS AMENDED

27A Patent maintained in amended form

Effective date: 19960807

AK Designated contracting states

Kind code of ref document: B2

Designated state(s): AT BE CH DE ES FR GB GR IT LI LU NL SE

ET3 Fr: translation filed ** decision concerning opposition
GBTA Gb: translation of amended ep patent filed (gb section 77(6)(b)/1977)

Effective date: 19960807

REG Reference to a national code

Ref country code: CH

Ref legal event code: AEN

Free format text: AUFRECHTERHALTUNG DES PATENTES IN GEAENDERTER FORM

NLR2 Nl: decision of opposition
NLR3 Nl: receipt of modified translations in the netherlands language after an opposition procedure
NLT1 Nl: modifications of names registered in virtue of documents presented to the patent office pursuant to art. 16 a, paragraph 1

Owner name: VEBA OEL TECHNOLOGIE UND AUTOMATISIERUNG GMBH

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GR

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19961002

ITF It: translation for a ep patent filed
REG Reference to a national code

Ref country code: ES

Ref legal event code: DC2A

Kind code of ref document: T5

Effective date: 19960925

REG Reference to a national code

Ref country code: GR

Ref legal event code: FG4A

Free format text: 3021219

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 19990702

Year of fee payment: 13

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GR

Payment date: 20000426

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 20000508

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 20000614

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20000703

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20000706

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: LU

Payment date: 20000710

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20000728

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20000731

Year of fee payment: 14

Ref country code: DE

Payment date: 20000731

Year of fee payment: 14

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 20000928

Year of fee payment: 14

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010710

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010710

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010710

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010711

Ref country code: ES

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010711

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010731

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010731

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010731

BERE Be: lapsed

Owner name: VEBA OEL TECHNOLOGIE UND AUTOMATISIERUNG G.M.B.H.

Effective date: 20010731

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020201

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20010710

EUG Se: european patent has lapsed

Ref document number: 87109958.6

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020329

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee

Effective date: 20020201

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020501

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20020810

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20050710