EP0064089A1 - Dispositif pour la gazéification sous pression de poussier de charbon - Google Patents

Dispositif pour la gazéification sous pression de poussier de charbon Download PDF

Info

Publication number
EP0064089A1
EP0064089A1 EP81103343A EP81103343A EP0064089A1 EP 0064089 A1 EP0064089 A1 EP 0064089A1 EP 81103343 A EP81103343 A EP 81103343A EP 81103343 A EP81103343 A EP 81103343A EP 0064089 A1 EP0064089 A1 EP 0064089A1
Authority
EP
European Patent Office
Prior art keywords
coal dust
reactor
pressure gasification
gasification
oxygen
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.)
Granted
Application number
EP81103343A
Other languages
German (de)
English (en)
Other versions
EP0064089B1 (fr
Inventor
Jürgen Dipl.-Ing. Seipenbusch
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.)
RAG AG
Original Assignee
Ruhrkohle AG
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
Application filed by Ruhrkohle AG filed Critical Ruhrkohle AG
Priority to EP81103343A priority Critical patent/EP0064089B1/fr
Priority to AT81103343T priority patent/ATE10645T1/de
Publication of EP0064089A1 publication Critical patent/EP0064089A1/fr
Application granted granted Critical
Publication of EP0064089B1 publication Critical patent/EP0064089B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam

Definitions

  • the invention relates to a method for coal dust pressure gasification, in which coal dust and / or a coal dust / liquid mixture is blown into a reactor and gasified in the presence of oxygen and water vapor to form a CO and H 2 -containing gas.
  • Gasification in the slag bath is known.
  • the coal dust with the gasification agent is blown obliquely from above onto a molten slag.
  • the solid particles which are specifically lighter than the slag, are deposited on the surface of the bath and float on the surface until only the molten ash portion remains.
  • the slag is drawn down over an overflow of the bath. The gas leaves the reactor upwards.
  • the very long residence time of the solid ensures almost complete carbon conversion. Lower degrees of fineness of the carbon carrier are sufficient for this and an exactly constant dosage is not necessary.
  • the reactor temperature is to be set so that the flow behavior of the slag allows turbulent movement of the slag bath.
  • the gasification takes place in a flight dust cloud, which is created by blowing the very fine-grained gasification agent into a reactor.
  • the reactor can be operated without special installations.
  • the flow guidance is determined by the burner with which the gasification agent is blown in and the reactor geometry. Due to the relatively short residence time of a few seconds, a high reactor temperature is required to achieve high carbon conversions. A complete carbon conversion is sometimes not economical considering the overall energy balance of the process.
  • the simple structure of the reactor ensures trouble-free operation, but in order to achieve constant operating conditions, an absolutely constant use of coal and gasification agent is required. To reduce the necessary dwell time of the solid particles, a very fine grinding of the coal is also imperative.
  • the present invention has for its object to improve the carbon conversion in coal dust gasification while maintaining or increasing the economy.
  • the invention is based on the fact that the residence time of the solid should be independent of the residence time of the gas, as is the case in the slag bath generator.
  • the simple operation of the entrained-flow gasifier should be retained as far as possible.
  • this is achieved in that the coal dust for generating and maintaining a slag film on the reactor wall is directed as far as possible to the reactor wall.
  • the outer circumference immediately melts Coal dust particles are brought into the liquid state on the reactor wall so that a slag film is formed in a short time.
  • the slag film runs downwards when the reactor is standing vertically and is maintained by subsequent coal dust particles.
  • the slag film runs at a relatively low speed in accordance with its toughness, which depends on the composition of the slag and the temperature. It gives the solid particles adhering to the slag film a residence time which is many times greater than that in the flight cloud under reaction conditions.
  • Such extensive separation of the carbon particles from the gas stream can be achieved in various ways. Tangential blowing of the coal dust into a preferably cylindrical reaction space is considered. This creates a rotating gas stream, and the coal dust particles in the gas stream are thrown against the reactor wall due to the acting centrifugal forces.
  • Another possibility of bringing the carbon particles to the reactor wall consists in blowing the coal dust particles exially into the interior of the reactor, the fuel being moved against the reactor wall in a semi-conically widening jet as a result of a conical burner mouthpiece arranged centrally in the burner outlet opening.
  • the carbon dust particles are then separated at the line of incidence of this cone on the reactor wall and can be reinforced by constricting the reaction space at the outlet end.
  • baffles serve to redirect the gas flow in the reactor. This creates the greatest possible solids separation on the chicanes.
  • the baffles can be designed, for example, as slag grids arranged centrally in the reactor.
  • a burner 1 turns a rotationally symmetrical reactor space 2 into a solid carbon carrier, e.g. Coal dust, supplied in dry or suspended form.
  • a solid carbon carrier e.g. Coal dust
  • the necessary gasification agent e.g. Oxygen and water vapor, in the reactor interior 2.
  • the reactor interior is surrounded by a refractory lining 3, which, as shown in FIG. 1, is only cooled by the heat given off by a steel jacket 4, or else has forced cooling (not shown) inside the steel jacket 4.
  • the oxygen portion of the gasification agent converts with the combustible portions of the gas atmosphere in the reactor interior 2 in a flame.
  • the coal dust is brought to the reaction temperature by absorbing heat from the environment, the average temperature of which is above the slag pour point, that is, depending on the type of coal, above approximately 1350 ° C.
  • the coal dust is introduced in the form e.g. a coal-water suspension, the suspension drops produced on the burner 1 by atomization are still dried before they are heated to the reaction temperature.
  • the temperature difference between the coal particles and the surrounding gas atmosphere is large, so that the heat flow necessary for the gasification reactions is ensured.
  • the temperature difference becomes smaller because the surrounding gas atmosphere cools down in accordance with the heat consumption of the reaction.
  • the carbon conversion rates per unit of time become lower and lower the further the reaction progresses, since the partial pressure reduction in the gasification agent also has the same effect.
  • a built-in flow guiding device 5 has the effect that some of the coal dust particles settle directly on the surface of this flow guiding device and the remaining coal dust particles are separated on the refractory lining 3 by sharp deflection of the gas flow.
  • a built-in flow guiding device 5 has the effect that some of the coal dust particles settle directly on the surface of this flow guiding device and the remaining coal dust particles are separated on the refractory lining 3 by sharp deflection of the gas flow.
  • the flow guide device 5 is designed here in the form of a round table.
  • the table top consists of several spirally wound, pinned tubes 6, which are clad with a refractory mass.
  • a cooling medium flows through the tubes 6, which enters at 7 and exits at 8.
  • the total of four feed and discharge pipes 9, 10 are also pinned and clad with a refractory mass. They also serve as a supporting structure for the table top.
  • the resulting slag film runs on the wall of the reactor neck 11 and arrives in a water bath (not shown), where the slag is granulated and discharged via a lock device.
  • the gas generated also leaves the reactor through the reactor neck 11 and is subsequently cleaned or fed to any use.
  • the slag film reactor according to the invention according to FIG. 2 is particularly suitable for the gasification of coal dust which is introduced into the reactor as a coal-water suspension.
  • the coal dust runs in the area of highest temperature p items within the gasification reactor, namely in the region of the combustion gas with the oxygen, the drying and heating, during the gasification reaction takes place in the coldest part of the reactor.
  • the gasification reaction in the high-temperature region of the reactor is brought about with the advantage of a particularly intensive reaction, while the drying and heating of the carbon particles takes place at low but sufficient temperatures.
  • FIG. 2 with FIG. 1 have the same designations.
  • a pumpable coal-water suspension enters burner 1 through burner 1.
  • pressure atomization of the suspension takes place. This atomization is possibly carried out by additional atomizing medium, e.g. Steam, supported.
  • the suspension drops are first dried and preheated by heat transfer from the backflow of hot gas from the gasification zone before they reach the actual reaction zone at the highest temperature.
  • the reaction zone is located in the lower reactor area, in which a flow control device 12 similar to the flow control device 5 is located.
  • the flow guide device 12 is designed in the same way as the flow guide device 5 in the form of a round, centrally arranged table which is provided with tubes 6 and is held by the feed lines 9 and discharge lines 10.
  • a line 14 for oxygen or air is passed through one of the supply lines 9.
  • the line 14 is connected via a connecting piece 13 to an air or oxygen supply line and leads to a nozzle 15 at the other end.
  • the nozzle 15 protrudes centrally through the flow guide device 12 into the reactor interior 2. It has a cap 18 to prevent clogging by slag particles protected.
  • the line 14 is cooled by the cooling medium flowing into the tubes 6.
  • the oxygen entering the reactor interior 2 through the nozzle 15 reacts in a flame with combustible gas formed in the reactor and with dried and preheated coal dust. This results in a particularly high and advantageous reaction temperature in the area of the flow control device 12 in the lower reactor part.
  • the remaining reaction sequences are the same as those described in the description of FIG. 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
EP81103343A 1981-05-04 1981-05-04 Dispositif pour la gazéification sous pression de poussier de charbon Expired EP0064089B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP81103343A EP0064089B1 (fr) 1981-05-04 1981-05-04 Dispositif pour la gazéification sous pression de poussier de charbon
AT81103343T ATE10645T1 (de) 1981-05-04 1981-05-04 Vorrichtung zur kohlenstaub-druckvergasung.

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP81103343A EP0064089B1 (fr) 1981-05-04 1981-05-04 Dispositif pour la gazéification sous pression de poussier de charbon

Publications (2)

Publication Number Publication Date
EP0064089A1 true EP0064089A1 (fr) 1982-11-10
EP0064089B1 EP0064089B1 (fr) 1984-12-05

Family

ID=8187696

Family Applications (1)

Application Number Title Priority Date Filing Date
EP81103343A Expired EP0064089B1 (fr) 1981-05-04 1981-05-04 Dispositif pour la gazéification sous pression de poussier de charbon

Country Status (2)

Country Link
EP (1) EP0064089B1 (fr)
AT (1) ATE10645T1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0372658A3 (en) * 1988-12-05 1990-09-12 Shell Internationale Research Maatschappij B.V. Constant volume tubular reactor
CN107033972A (zh) * 2017-05-09 2017-08-11 哈尔滨工业大学 一种带有吹扫气保护的干煤粉气流床气化炉烧嘴

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE885766C (de) * 1942-01-18 1953-08-06 Koppers Gmbh Heinrich Einrichtung zur Vergasung staubfoermiger oder feinkoerniger Brennstoffe
US2681852A (en) * 1948-05-28 1954-06-22 Texas Co Method for partial combustion of carbonaceous materials
FR1207478A (fr) * 1958-06-20 1960-02-17 Sumitomo Chemical Co Procédé de gazéification de charbon pulvérisé
DE1091268B (de) * 1953-09-29 1960-10-20 Texaco Development Corp Einrichtung zur Erzeugung eines Brenngases durch Vergasen eines festen feinzerteilten Brennstoffes
FR1314303A (fr) * 1962-02-09 1963-01-04 Koppers Gmbh Heinrich Procédé et dispositif pour la gazéification de poussier de charbon en suspension
DE1250046B (fr) * 1967-09-14
US3607156A (en) * 1968-12-26 1971-09-21 Texaco Inc Hydrogen and carbon monoxide from slurries of solid carboniferous fuels
DE2044310A1 (en) * 1970-09-08 1972-03-16 Texaco Development Corp., New York, N.Y. (V.StA.) Synthesis gas prodn
DE2411086A1 (de) * 1974-03-08 1975-09-18 Koppers Gmbh Heinrich Verfahren und vorrichtung zur verbesserung des kohlenstoff-vergasungsgrades bei der vergasung von kohlenstaub in der schwebe
US3988123A (en) * 1975-08-15 1976-10-26 The United States Of America As Represented By The United States Energy Research And Development Administration Gasification of carbonaceous solids
FR2369502A1 (fr) * 1976-11-01 1978-05-26 Inex Resources Inc Procede et appareil de combustion de matieres carbonees solides

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1250046B (fr) * 1967-09-14
DE885766C (de) * 1942-01-18 1953-08-06 Koppers Gmbh Heinrich Einrichtung zur Vergasung staubfoermiger oder feinkoerniger Brennstoffe
US2681852A (en) * 1948-05-28 1954-06-22 Texas Co Method for partial combustion of carbonaceous materials
DE1091268B (de) * 1953-09-29 1960-10-20 Texaco Development Corp Einrichtung zur Erzeugung eines Brenngases durch Vergasen eines festen feinzerteilten Brennstoffes
FR1207478A (fr) * 1958-06-20 1960-02-17 Sumitomo Chemical Co Procédé de gazéification de charbon pulvérisé
FR1314303A (fr) * 1962-02-09 1963-01-04 Koppers Gmbh Heinrich Procédé et dispositif pour la gazéification de poussier de charbon en suspension
US3607156A (en) * 1968-12-26 1971-09-21 Texaco Inc Hydrogen and carbon monoxide from slurries of solid carboniferous fuels
DE2044310A1 (en) * 1970-09-08 1972-03-16 Texaco Development Corp., New York, N.Y. (V.StA.) Synthesis gas prodn
DE2411086A1 (de) * 1974-03-08 1975-09-18 Koppers Gmbh Heinrich Verfahren und vorrichtung zur verbesserung des kohlenstoff-vergasungsgrades bei der vergasung von kohlenstaub in der schwebe
US3988123A (en) * 1975-08-15 1976-10-26 The United States Of America As Represented By The United States Energy Research And Development Administration Gasification of carbonaceous solids
FR2369502A1 (fr) * 1976-11-01 1978-05-26 Inex Resources Inc Procede et appareil de combustion de matieres carbonees solides

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0372658A3 (en) * 1988-12-05 1990-09-12 Shell Internationale Research Maatschappij B.V. Constant volume tubular reactor
CN107033972A (zh) * 2017-05-09 2017-08-11 哈尔滨工业大学 一种带有吹扫气保护的干煤粉气流床气化炉烧嘴

Also Published As

Publication number Publication date
ATE10645T1 (de) 1984-12-15
EP0064089B1 (fr) 1984-12-05

Similar Documents

Publication Publication Date Title
DE102011088628B4 (de) Verfahren und Vorrichtung zur Flugstromvergasung fester Brennstoffe unter Druck
EP1027407B1 (fr) Procede et dispositif de production de gaz de combustion, de gaz de synthese et de gaz de reduction a partir de combustibles solides
EP0095103B1 (fr) Procédé et appareil pour la production de gaz de synthèse par oxydation partielle de suspensions de charbon dans l'eau
DE2952434C2 (de) Verfahren und Vorrichtung zum Vergasen von festem, feinverteiltem, kohlenstoffhaltigem Brennstoff in einem Schmelzbad, sowie Aufblaselanze hierfür
DE3019937C2 (fr)
DE112015000112B4 (de) Vergasungsvorrichtung für Kohlepulver mit mehrstufiger Zuführung von Vergasungsmittel und starker Verwirbelung sowie entsprechendes Vergasungsverfahren
EP0180249B1 (fr) Méthode de fonctionnement d'un brûleur
DE69627475T2 (de) Brenner zur teiloxidation mit versenktem mundstück und mit einer druckgaszufuhr
DE2710154C2 (de) Unter Druck und hoher Temperatur arbeitender Gaserzeuger
DE68902784T2 (de) Auswechselbarer quenchgas-injektionsring.
EP0177090A2 (fr) Dispositif de production de suspensions solides/gaz inflammables
DE2918859A1 (de) Anlage zum entgasen und/oder vergasen von kohle
DE3741181C2 (fr)
DE19806823C2 (de) Vorrichtung und Verfahren zur Verbrennung vanadiumhaltiger Brennstoffe
DE3628866A1 (de) Reaktor zur kohlenstaubvergasung
DE3537758C2 (fr)
EP0064089A1 (fr) Dispositif pour la gazéification sous pression de poussier de charbon
US3057708A (en) Method for the thermal processing of carbon-containing gas by direct heat exchange with another gas
EP0533733B1 (fr) Procede permettant la combustion partielle de liqueurs epuisees de cellulose
DE3837586A1 (de) Vergasungsbrenner fuer eine anlage fuer die vergasung von festen brennstoffen
DE3017229A1 (de) Kohlestaub-druckvergasung
DE1040734B (de) Verfahren und Vorrichtung zur Verbrennung oder Vergasung von Brennstoffen
DE2751911A1 (de) Verfahren und vorrichtung fuer die vergasung von kohlenstaub
DE2736493A1 (de) Verfahren und vorrichtung zum verbrennen von kohle
AT219633B (de) Verfahren und Vorrichtungen zur Verhüttung von Eisenerzen in der Wirbelschmelzkammer-Feuerung eines Dampferzeugers

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: 19811203

AK Designated contracting states

Designated state(s): AT BE CH FR GB IT LU NL SE

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

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

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 FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;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: 19841205

REF Corresponds to:

Ref document number: 10645

Country of ref document: AT

Date of ref document: 19841215

Kind code of ref document: T

ET Fr: translation filed
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: 19850531

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

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

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19900328

Year of fee payment: 10

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

Ref country code: GB

Payment date: 19900420

Year of fee payment: 10

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

Ref country code: LU

Payment date: 19900430

Year of fee payment: 10

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

Ref country code: FR

Payment date: 19900509

Year of fee payment: 10

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

Ref country code: AT

Payment date: 19900522

Year of fee payment: 10

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

Ref country code: NL

Payment date: 19900531

Year of fee payment: 10

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

Ref country code: BE

Payment date: 19900607

Year of fee payment: 10

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

Ref country code: GB

Effective date: 19910504

Ref country code: AT

Effective date: 19910504

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

Ref country code: LI

Effective date: 19910531

Ref country code: CH

Effective date: 19910531

Ref country code: BE

Effective date: 19910531

BERE Be: lapsed

Owner name: RUHRKOHLE A.G.

Effective date: 19910531

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

Ref country code: NL

Effective date: 19911201

GBPC Gb: european patent ceased through non-payment of renewal fee
NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19920131

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

EAL Se: european patent in force in sweden

Ref document number: 81103343.0

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

Ref country code: SE

Payment date: 19950428

Year of fee payment: 15

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

Ref country code: SE

Effective date: 19960505

EUG Se: european patent has lapsed

Ref document number: 81103343.0