EP0416242A1 - Installation pour la production d'un gaz à partir de solides carbonifères finement divisés - Google Patents

Installation pour la production d'un gaz à partir de solides carbonifères finement divisés Download PDF

Info

Publication number
EP0416242A1
EP0416242A1 EP90113136A EP90113136A EP0416242A1 EP 0416242 A1 EP0416242 A1 EP 0416242A1 EP 90113136 A EP90113136 A EP 90113136A EP 90113136 A EP90113136 A EP 90113136A EP 0416242 A1 EP0416242 A1 EP 0416242A1
Authority
EP
European Patent Office
Prior art keywords
product gas
cooling
reactor
gasification
reaction zone
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
EP90113136A
Other languages
German (de)
English (en)
Other versions
EP0416242B1 (fr
Inventor
Michael Lang
Gerhard Wilmer
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.)
Krupp Koppers GmbH
Original Assignee
Krupp Koppers 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
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Publication of EP0416242A1 publication Critical patent/EP0416242A1/fr
Application granted granted Critical
Publication of EP0416242B1 publication Critical patent/EP0416242B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime 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
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only

Definitions

  • the invention relates to a plant for the production of a product gas from a finely divided carbon carrier, in particular from fine-grained to dusty coal, by pressure gasification, - with a vertical reactor with gasification part and radiation cooling boiler, which flows through the reactor from bottom to top, a vertical convection cooling apparatus, which is flowed from top to bottom, and a cooled connecting line between the head of the reactor and the head of the convection cooling apparatus, the reactor having a shaft formed from pipes, a lower liquid slag outlet and an upper, retracted connecting section for the connecting line and for cooling the product gas until sufficiently entrained liquid entrained slag particles are set up, the convection cooling apparatus being equipped with a lower outlet for the product gas and for entrained slag particles, and Pierre i furthermore, the gasification part of the reactor has a lower primary reaction zone and an upper secondary reaction zone.
  • the reaction mainly leads to CO2 and H2 O.
  • a water gas reaction takes place, which leads to the product gas consisting essentially of CO2 and H2.
  • the product gas is obtained as raw product gas and is then cleaned. It is used, for example, as a synthesis gas for the production of hydrocarbons, as a heating gas, in particular for gas turbines, or as a reducing gas for metallurgical purposes.
  • the product gas stream leaves the gasification section at a temperature in the range from 1300 ° C. to 1700 ° C.
  • the aim in this area is a temperature of the product gas at approximately 1400 ° C.
  • the overall height ratios are so balanced in relation to the so-called slag split that the product gas does not entail fine-particle slag and the slag mainly runs off liquid from the gasification part.
  • the overall height of the gasification part is set up in such a way that a sufficiently high gasification efficiency is achieved and the product gas does not entrain fine-particle carbon carriers that are not gassed. If the height of the gasification part were to be reduced in the known systems, the slag split and the gasification efficiency would be adversely affected. The product gas would entrain too much slag and, to a disruptive degree, non-gassed fine carbon carriers.
  • the invention has for its object to provide a system of the intended purpose described above and the basic structure specified at the outset, the gasification part of which is characterized by a considerable reduction in the overall height, without interfering impairment of the gasification efficiency and the slag split, without enlarging the cross section of the gasification part .
  • the invention teaches that the gasification part, at least in the region of the secondary reaction zone, has radial bulkheads which are cooled with water and leave a central region free, and that the surface of the bulkheads is provided with pins and is coated with a refractory material.
  • the invention achieves a reduction in the overall height of the gasification part without increasing the cross-section, in that, in deviation from the prevailing building theory, the bulkheads set up as indicated are at least guided into the gasification part.
  • the thermodynamic relationships, in particular the reaction sequence are not significantly disturbed by the cooled bulkheads arranged in the gasification part, although in the gasification part with its significantly reduced overall height, the product gas formed is cooled down to a temperature in the range from 1300 ° C. to 1700 ° C. , preferably to a temperature of about 1400 ° C. This is due on the one hand to the fact that the bulkheads leave a central flow area free.
  • the bulkheads in the gasification part are coated with refractory material in the manner described.
  • the liquid slag that runs off the bulkheads is deposited on these bulkheads.
  • the radiation interaction with the components to be formed depends on the surface temperature of the slag that runs off, which is considerably higher than the temperature of the bulkhead walls or even the cooling pipes in the bulkheads. Otherwise, the radial bulkheads define chambers between them.
  • the spacing of the bulkheads can be chosen such that the cooling influence of the bulkheads on the desired reactions is relatively small even in the center of these chambers between the radial bulkheads, so that the radiation efficiency is not adversely affected.
  • the bulkheads with their leading edges and their coated surfaces increase the slag discharge so that, despite the reduced overall height of the gasification part, the slag split is not impaired, even if the flow rate is relatively high.
  • the secondary reaction zone is drawn into a lower section of the radiation cooling boiler and this section of the radiation cooling boiler also has cooled radial bulkheads which leave a central area free and provided with pins and with a refractory Material are coated.
  • the radial bulkheads from the gasification are also used Part lead to the upper part of the radiation cooling boiler and only with a coating of a refractory material in the area of the secondary reaction zone in the gasification part or in the lower part of the radiation cooling boiler.
  • the overall height of the gasification part can be reduced by half and by more than half. Based on the radiation cooling part, the design can be made such that the gasification part has a height that is approximately a factor of 0.5 to 0.4 less than the height of the radiation cooling part. If you compare the height of the secondary reaction zone in the plant according to the invention with a secondary reaction zone which is of classic design without bulkheads, the height of the embodiment according to the invention is 0.2 to 0.8 times smaller. Operation with significantly improved efficiency and reduced energy losses is possible if the following further measures are implemented in combination with the measures described.
  • the reactor has a shaft, which is designed with respect to the disturbance of the product gas as a constant-speed flow channel, into which the cooled bulkheads protrude radially and that of devices for the supply of third parties Coolant is free, and that the constant-velocity flow channel is designed as a radiation cooler with respect to the cooling of the product gas so that the entrained slag is sufficiently solidified solely by the radiation cooling.
  • a foreign coolant is not introduced means that a quench device is not provided in the radiation cooling boiler.
  • the constant-velocity flow channel has a cross section which decreases in the flow direction in accordance with the cooling-related volume reduction of the product gas.
  • the constant-speed flow channel begins in the gasification section immediately above the combustion chambers of the gasification burners.
  • the constant-speed flow channel can also be designed as a flow channel with a cylindrical cross section and as a radiation cooler for cooling the product gas down to about 1300 ° C to 1000 ° C upon entry into the connecting line, a drawn connecting part for the connecting line and / or a quenching device for the introduction of external coolants is then arranged and a subsequent section of the connecting line is set up as a direct cooling section and is designed for cooling the product gas to about 1000 ° C. to 700 ° C.
  • the flow rate of the product gas can be within wide limits in the equipotential flow channel, e.g. B. vary from 0.2 to 20 m / sec.
  • the constant speed flow channel is preferably for a flow speed of the product gas of less than 1 m / sec. set up.
  • the system shown in the figures is used to generate a product gas from a finely divided carbon carrier.
  • a finely divided carbon carrier In particular from fine-grained to dust-like coal or a similar fuel, by means of pressure gasification.
  • Belong to the basic structure a vertical reactor with gasification part 1 and radiation cooling boiler 2, which is flowed through from bottom to top, a vertical convection cooling apparatus 3, which is flowed through from top to bottom and a cooled connecting line 4 between the head of the reactor 1, 2 and the head of the convection cooling apparatus 3.
  • the arrangement is such that the reactor 1, 2 is a substantially circular circular section formed from tubes 5 Has shaft 6, a lower liquid slag outlet 7 and an upper retracted connector 3 for the connecting line 4.
  • the burners 9 are arranged in the lower region of the gasification part 1.
  • the reactor 1, 2 is set up to cool the product gas until sufficient solidified entrained slag particles.
  • the convection cooling apparatus 3 is equipped with a lower vent 10 for the product gas and for entrained slag particles.
  • the gasification part 1 of the reactor has a lower primary reaction zone 11 and an upper secondary reaction zone 12.
  • the secondary reaction zone 12 is drawn into a lower section of the radiation cooling boiler 2 and that this section of the radiation cooling boiler also has guided radial bulkheads 13 which leave a central area 14 free and which are provided with pins 15 provided and coated with a refractory material 16.
  • the radial bulkheads 13 are also in the embodiment from the Ver Gasing part 1 out into the upper part of the radiation cooling boiler 2, but only in the area of the secondary reaction zone 12 in the gasification part 1 or in the hatched area 17 of the radiation cooling boiler 2 with the pins 15 and a coating of a refractory material 16.
  • the reactor has a shaft 20 which is designed as a constant-speed flow channel with respect to the flow of the product gas. He is free from facilities for the direct supply of external coolants.
  • the constant-speed flow channel 20 is designed as a radiation cooler with respect to the cooling of the product gas and is designed such that the entrained slag particles are sufficiently solidified solely by the radiation cooling.
  • the constant-speed flow channel 20 is designed as a flow channel which is cylindrical in cross section and is designed as a radiation cooler for cooling the product gas down to approximately 1300 ° C. to 1000 ° C. upon entry into the connecting line 4.
  • a quench device 21 for the direct introduction of external coolants can be seen in the area of the connecting section 8 drawn in in the form of a nozzle for the connecting line 4 and / or in connection thereafter.
  • the connecting line 4 set up as a direct cooling section and designed for cooling the product gas to about 1000 ° C to 7000 ° C.
  • the constant-speed flow channel 20 has a cross section that decreases in the flow direction in accordance with the cooling-related volume reduction of the product gas.
  • the constant-speed flow channel 20 begins immediately above the burners 9, which can otherwise be seen in particular in FIG. 2, which represents a section in the direction AB through the object of FIG. 1. Otherwise, a steam superheater 22 is provided in the exemplary embodiment; it is located in the upper part of the convection cooling apparatus 3. Knock-out cleaning devices 23 are indicated in FIG. 1, which act on the outside of the shaft that forms the constant-speed flow channel 20. However, they can also be recognized by the convection cooling apparatus 3.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP90113136A 1989-09-07 1990-07-10 Installation pour la production d'un gaz à partir de solides carbonifères finement divisés Expired - Lifetime EP0416242B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3929766 1989-09-07
DE3929766A DE3929766A1 (de) 1989-09-07 1989-09-07 Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger

Publications (2)

Publication Number Publication Date
EP0416242A1 true EP0416242A1 (fr) 1991-03-13
EP0416242B1 EP0416242B1 (fr) 1992-12-02

Family

ID=6388842

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90113136A Expired - Lifetime EP0416242B1 (fr) 1989-09-07 1990-07-10 Installation pour la production d'un gaz à partir de solides carbonifères finement divisés

Country Status (10)

Country Link
EP (1) EP0416242B1 (fr)
CN (1) CN1024678C (fr)
CS (1) CS9004315A3 (fr)
DD (1) DD297661A5 (fr)
DE (2) DE3929766A1 (fr)
DK (1) DK0416242T3 (fr)
ES (1) ES2036871T3 (fr)
PL (1) PL164182B1 (fr)
TR (1) TR26096A (fr)
ZA (1) ZA905420B (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0722999A1 (fr) * 1995-01-20 1996-07-24 Shell Internationale Researchmaatschappij B.V. Appareil pour refroidir des gaz chauds chargés de solides
EP0845522A3 (fr) * 1996-11-29 1999-01-27 MAN Gutehoffnungshütte Aktiengesellschaft Echangeur de chaleur pour le gaz de synthèse
US8083815B2 (en) 2008-12-22 2011-12-27 Shell Oil Company Process to prepare methanol and/or dimethylether
US8308983B2 (en) 2008-10-08 2012-11-13 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
WO2013032537A1 (fr) * 2011-04-06 2013-03-07 Ineos Bio Sa Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée
US8685119B2 (en) 2005-05-02 2014-04-01 Shell Oil Company Method and system for producing synthesis gas, gasification reactor, and gasification system
DE102005041931B4 (de) * 2005-09-03 2018-07-05 Siemens Aktiengesellschaft Vorrichtung zur Erzeugung von Synthesegasen durch Partialoxidation von aschehaltigen Brennstoffen unter erhöhtem Druck mit Teilquenchung des Rohgases und Abhitzegewinnung
CN109340782A (zh) * 2018-11-27 2019-02-15 湖北金炉节能股份有限公司 一种固体污泥废料焚烧炉

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4123377A1 (de) * 1991-07-15 1993-01-21 Neumann Siegmar Vorrichtung und verfahren zur reinigung von abgasen bei verbrennungsanlagen mit sortierung der schadstoffe
DE4307462C2 (de) * 1993-03-10 2002-10-17 Krupp Koppers Gmbh Einrichtung für die Vergasung feinkörniger bis staubförmiger Brennstoffe und Verfahren zu deren Betrieb
US9051522B2 (en) 2006-12-01 2015-06-09 Shell Oil Company Gasification reactor
CN101328434B (zh) * 2008-07-17 2011-06-22 中国科学技术大学 一种干煤粉气流床气化炉
US8960651B2 (en) 2008-12-04 2015-02-24 Shell Oil Company Vessel for cooling syngas
JP5818704B2 (ja) 2012-01-25 2015-11-18 三菱日立パワーシステムズ株式会社 ガス化炉、ガス化発電プラント
CN102851081B (zh) * 2012-09-28 2014-12-31 中国船舶重工集团公司第七一一研究所 一种用水分级激冷的水煤浆或干煤粉气化装置
CN105670708A (zh) * 2016-03-22 2016-06-15 胡志阳 一种合成气冷却的设备和方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4610697A (en) * 1984-12-19 1986-09-09 Combustion Engineering, Inc. Coal gasification system with product gas recycle to pressure containment chamber
DE3725424C1 (de) * 1987-07-31 1988-07-21 Steinmueller Gmbh L & C Strahlungskuehler fuer die Abkuehlung von mit Staub beladenen Gasen
DE3844613A1 (de) * 1988-07-16 1990-01-18 Krupp Koppers Gmbh Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger
EP0351563A1 (fr) * 1988-07-16 1990-01-24 Krupp Koppers GmbH Appareillage pour la production de gaz à partir de solides carbonifères finement divisés

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4610697A (en) * 1984-12-19 1986-09-09 Combustion Engineering, Inc. Coal gasification system with product gas recycle to pressure containment chamber
DE3725424C1 (de) * 1987-07-31 1988-07-21 Steinmueller Gmbh L & C Strahlungskuehler fuer die Abkuehlung von mit Staub beladenen Gasen
DE3844613A1 (de) * 1988-07-16 1990-01-18 Krupp Koppers Gmbh Anlage fuer die erzeugung eines produktgases aus einem feinteiligen kohlenstofftraeger
EP0351563A1 (fr) * 1988-07-16 1990-01-24 Krupp Koppers GmbH Appareillage pour la production de gaz à partir de solides carbonifères finement divisés

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0722999A1 (fr) * 1995-01-20 1996-07-24 Shell Internationale Researchmaatschappij B.V. Appareil pour refroidir des gaz chauds chargés de solides
EP0845522A3 (fr) * 1996-11-29 1999-01-27 MAN Gutehoffnungshütte Aktiengesellschaft Echangeur de chaleur pour le gaz de synthèse
US6051195A (en) * 1996-11-29 2000-04-18 Man Gutehoffnungshutte Aktiengesellschaft Synthesis gas heat exchanger unit
US8685119B2 (en) 2005-05-02 2014-04-01 Shell Oil Company Method and system for producing synthesis gas, gasification reactor, and gasification system
DE102005041931B4 (de) * 2005-09-03 2018-07-05 Siemens Aktiengesellschaft Vorrichtung zur Erzeugung von Synthesegasen durch Partialoxidation von aschehaltigen Brennstoffen unter erhöhtem Druck mit Teilquenchung des Rohgases und Abhitzegewinnung
US8308983B2 (en) 2008-10-08 2012-11-13 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
US8470291B2 (en) 2008-10-08 2013-06-25 Shell Oil Company Process to prepare a gas mixture of hydrogen and carbon monoxide
US8083815B2 (en) 2008-12-22 2011-12-27 Shell Oil Company Process to prepare methanol and/or dimethylether
US9045706B2 (en) 2011-04-06 2015-06-02 Ineos Bio Sa Method of operation of process to produce syngas from carbonaceous material
EP3301143A1 (fr) * 2011-04-06 2018-04-04 Ineos Bio SA Système de refroidisseur de gaz de synthèse et procédé de fonctionnement
EA029848B1 (ru) * 2011-04-06 2018-05-31 Инеос Био Са Способ осуществления процесса получения синтез-газа из углеродсодержащего материала
WO2013032537A1 (fr) * 2011-04-06 2013-03-07 Ineos Bio Sa Processus de fonctionnement de procédé de production de gaz de synthèse à partir de matière carbonée
EP3556828A1 (fr) * 2011-04-06 2019-10-23 Jupeng Bio (HK) Limited Système de refroidisseur de gaz de synthèse et procédé de fonctionnement
CN109340782A (zh) * 2018-11-27 2019-02-15 湖北金炉节能股份有限公司 一种固体污泥废料焚烧炉
CN109340782B (zh) * 2018-11-27 2024-04-16 湖北金炉节能股份有限公司 一种固体污泥废料焚烧炉

Also Published As

Publication number Publication date
ZA905420B (en) 1991-04-24
ES2036871T3 (es) 1993-06-01
DK0416242T3 (da) 1993-02-22
PL164182B1 (pl) 1994-06-30
DE3929766A1 (de) 1991-03-14
CS275487B2 (en) 1992-02-19
CN1024678C (zh) 1994-05-25
DD297661A5 (de) 1992-01-16
DE59000540D1 (de) 1993-01-14
TR26096A (tr) 1994-12-15
EP0416242B1 (fr) 1992-12-02
CS9004315A3 (en) 1992-02-19
CN1050039A (zh) 1991-03-20
PL286686A1 (en) 1991-08-26

Similar Documents

Publication Publication Date Title
EP0416242B1 (fr) Installation pour la production d'un gaz à partir de solides carbonifères finement divisés
DE102006059149B4 (de) Flugstromreaktor zur Vergasung fester und flüssiger Energieträger
DE2624302A1 (de) Verfahren zur durchfuehrung exothermer prozesse
DE102012005450B4 (de) Verfahren und Vorrichtung zur Entgasung von flüssigem Schwefel
DE102007042543A1 (de) Verfahren und Vorrichtung zur Behandlung von beladenem Heißgas
EP0616022B1 (fr) Procédé pour la gazéification sous pression de combustibles finement divisés
DE2918859A1 (de) Anlage zum entgasen und/oder vergasen von kohle
DE102008012732A1 (de) Vergasungsvorrichtung mit Schlackeabzug
DE2520584A1 (de) Verfahren und vorrichtung zur entschwefelung bei der kohlevergasung
DE3100767A1 (de) "verfahren und anlage zum reduzieren eines eisenoxidmaterials in einer wirbelschicht"
DE3606108A1 (de) Verfahren und einrichtung zur herstellung eines hauptsaechlich co + h(pfeil abwaerts)2(pfeil abwaerts) enthaltenden gases durch thermisches reformen von gasfoermigem kohlenwasserstoff
DD273430A5 (de) Verfahren und Einrichtung zur Beschickung von Flachglas
EP1390316A1 (fr) Installation et procede de production de clinker de ciment
DE2757410A1 (de) Verfahren und vorrichtung zur erzeugung von metallpulver
DE2520883A1 (de) Verfahren und vorrichtung zur kontinuierlichen vergasung von kohle in einem eisenbadreaktor
DD265051A3 (de) Vorrichtung zur verteilung eines feststoffbeladenen gases in einer waschfluessigkeit
EP0367966A1 (fr) Brûleur pour la gazéification des combustibles solides à grains fins ou pulvérulents
DE2837416C3 (de) Vorrichtung zur Weiterverarbeitung von Kohleentgasungsrohgas
DE1175224B (de) Vorrichtung zur Erzeugung von Acetylen und AEthylen durch thermische Spaltung von Kohlen-wasserstoffen mittels eines im elektrischen Licht-bogen erhitzten gasfoermigen Waermetraegers
DE2947128A1 (de) Verfahren zur kontinuierlichen erzeugung eines hochtemperatur-reduktionsgases
DE3639343A1 (de) Verfahren und anlage zur pyrometallurgischen verhuettung von feinverteilten materialien
EP2809751B1 (fr) Dispositif et procédé de gazéification de combustibles poussiéreux, solides et carbonés en lit entraîné
DE68905681T2 (de) Methode zur umaenderung der schmutzstoffe in einem rohen hochtemperatur-hochdruck-synthesegasstrom.
DE202016006668U1 (de) Vorrichtung zur Kühlung und Reinigung eines Feststoffe enthaltenden Heißgasstromes
EP0053802A1 (fr) Procédé et dispositif pour protéger les tuyères et le garnissage d'un récipient pour l'affinage d'un bain métallique

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: 19901128

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE DK ES GB NL

17Q First examination report despatched

Effective date: 19920409

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE DK ES GB NL

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)

Effective date: 19921215

REF Corresponds to:

Ref document number: 59000540

Country of ref document: DE

Date of ref document: 19930114

REG Reference to a national code

Ref country code: DK

Ref legal event code: T3

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2036871

Country of ref document: ES

Kind code of ref document: T3

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: GB

Payment date: 19980612

Year of fee payment: 9

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

Ref country code: DK

Payment date: 19980625

Year of fee payment: 9

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

Ref country code: NL

Payment date: 19980629

Year of fee payment: 9

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

Ref country code: DE

Payment date: 19980630

Year of fee payment: 9

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

Ref country code: ES

Payment date: 19980716

Year of fee payment: 9

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

Ref country code: GB

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

Effective date: 19990710

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

Ref country code: ES

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

Effective date: 19990711

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

Ref country code: DK

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

Effective date: 19990802

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: 20000201

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

Effective date: 19990710

REG Reference to a national code

Ref country code: DK

Ref legal event code: EBP

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

Effective date: 20000201

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: 20000503

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20000810