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WO1997046639A1 - Procede de production de gaz - Google Patents

Procede de production de gaz Download PDF

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Publication number
WO1997046639A1
WO1997046639A1 PCT/EP1997/002485 EP9702485W WO9746639A1 WO 1997046639 A1 WO1997046639 A1 WO 1997046639A1 EP 9702485 W EP9702485 W EP 9702485W WO 9746639 A1 WO9746639 A1 WO 9746639A1
Authority
WO
WIPO (PCT)
Prior art keywords
raw gas
gasification
gas
molten bath
carbon
Prior art date
Application number
PCT/EP1997/002485
Other languages
German (de)
English (en)
Inventor
Adrian Brandl
Volker Kaiser
Ralf Abraham
Werner Baumgartner
Christoph LÜTGE
Ci Liu
Marco Deutsch
Original Assignee
Krupp Uhde 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 Uhde Gmbh filed Critical Krupp Uhde Gmbh
Priority to AU29553/97A priority Critical patent/AU2955397A/en
Publication of WO1997046639A1 publication Critical patent/WO1997046639A1/fr

Links

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
    • C10J3/57—Gasification using molten salts or metals
    • 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
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a process by means of which one or more carbon-containing feedstocks, including waste, by means of partial oxidation in a gasification reactor and an at least gas-side melt pool, gas, metal, sulfur and a base material for the Cement production.
  • Fuel gas or synthesis gas from carbonaceous feedstocks, e.g. From coal, from wood or other biomass, from sewage sludge and / or from waste, these feedstocks are partially oxidized individually or in combination by means of air or oxygen or oxygen-enriched air.
  • Fuel gas is fired under pressure, for example, in the combustion chamber of a gas turbine of a combined cycle power plant.
  • Synthesis gas is used for the production of methanol.
  • the partial oxidation takes place in gasification reactors, from which the gasification residue is drawn off either as a flowable slag or dry as ash.
  • the specialist book "Coal Gasification” [1] explains the form in which the gasification residue occurs in the different types of gasification reactors.
  • the input materials are gasified either in the fixed bed, in the fluidized bed or in the entrained flow. If the gasification takes place in a fixed bed, such as in a rotary grate generator operated at approximately atmospheric pressure or in a rotary grate generator charged to about 30 bar, the gasification residue is obtained as largely unpolluted ash.
  • the gasification residue forms in the fluidized bed granular ash granules which can no longer be fluidized once a certain grain size has been reached and which precipitate out of the fluidized bed as a bottom discharge.
  • Winkler generator operated at approximately atmospheric pressure
  • HW gasifier high-temperature Winkler gasifier
  • the gasification residue is obtained as a liquid slag because of the high gasification temperatures of about 1500 ° to 1900 ° C. that result.
  • page 96 it is reported that in the Koppers-Totzek gasifier, about half of the gasification residue flows downward as liquid slag on the gasifier walls, that it is quenched in a water-filled tank and that it is below the carburetor is withdrawn in granulated form. The other half of the gasification residue is discharged from the Koppers-Totzek gasifier with the crude gas generated as fly ash.
  • the degree of coal conversion is 90-95%, sometimes higher.
  • the coal which is not converted in the entrained-flow gasifier is obtained together with the gasification residue.
  • the granulated slag produced as the bottom discharge in the entrained flow gasifiers also contains combustible components which can be used.
  • the crude gas formed in the gasification reactor is loaded with flyable gasification residue. Flight slag is discharged from the crude gas from the gasification reactor producing slag. Fly ash from the raw gas is discharged from the ash-producing gasification reactor.
  • the flyable gasification residue also contains residues of the unreacted feed.
  • the Winkler gasifier that its fly ash transports 15 to 20% carbon with it.
  • the present invention solves the problems described by a method for the production of gas from at least one carbon-containing feedstock, which in one by means of air or oxygen or oxygen-enriched air
  • the gasification reactor is partially oxidized and this results in primary raw gas and gasification residue; which process is characterized in that the gasification residue is placed in a molten bath, into the melt bath an oxidizer and additives are introduced, with which a secondary raw gas, ceramic slag and alloyed melt is produced from the gasification residue and that in Melting pool formed secondary raw gas is mixed with the primary raw gas.
  • a process for the gasification of waste materials is described in detail in the patent DE 43 39 973.
  • two gasification reactors are interconnected, the first of which is operated as an HTW gasifier in a manner similar to that in the present invention.
  • the ash is ground, which is drawn off from this first carburetor.
  • This ash is mixed together with flying dust, which comes from a dedusting device, and introduced together with additional fuel and gasification agent into a second gasification reactor, which is designed as an entrained flow gasifier of the Shell or Koppers-Totzek type and which, in addition to raw gas, exclusively contains slag Floor extraction produced.
  • the present invention differs fundamentally legend of the technology described in the patent DE 43 39 973.
  • the melt pool used in the present invention leads to a separation of the substances which collectively form slag in entrained-flow gasification into a ceramic phase and a metallic phase.
  • a molten bath is used, as described in the patents US 5,491,279, WO 93/25277, US 4,574,714, US 5,298,233, US 5,443,572, US 5,301,620, US 5,358,549 and in the publication "Molten metal works waste wonders, by Peter Taffe, European Chemical News October 16-22, 1995, pp. 32-33 ".
  • an embodiment of the invention in which, in addition to the gasification residue, at least one lumpy residue is also added to the molten bath in order to generate additional secondary raw gas therefrom.
  • the present invention it is possible to dispense with fine grinding of the granulated slag or ash obtained as the bottom draw of the gasification reactor.
  • the entry into the envisaged weld pool can either be pneumatic, then grinding is advisable. full, or the entry can take place via a lock system, in this case only a refraction of coarse parts is necessary.
  • the present invention has a configuration in which the carbon-containing slag or ash, which is obtained as the bottom discharge of the gasification reactor, is placed in a mixing and conveying device which also carries out a refraction on a predeterminable grain size.
  • This process of thermal / catalytic decomposition in the melt pool can be influenced by adding additives.
  • the present invention therefore provides its own way of adding the additives to the molten bath, namely in such a way that, in addition to the carbon-containing slag or ash, mainly mineral additives are added to the mixing and conveying device, which are used to condition the Melting Ba of serve.
  • these additives consist at least partly of mineralized ashes from other combustion processes. It will e.g. It is also possible to convert ashes containing heavy metals that result from the combustion or partial oxidation of heavy residues from petroleum processing into residues that are easier to deposit.
  • the carbon-containing slag or ash broken in the mixing and conveying device if appropriate also together with the predominantly mineral aggregates introduced into the mixing and conveying device, either pneumatically or via a lock system to bring in the weld pool.
  • Another advantage of the present invention is that, in contrast to the entrained-flow gasification described in the patent DE 43 39 973, no additional fuel has to be provided for the operation of the melt pool.
  • the methane reacts endothermically with oxygen and water vapor to form carbon monoxide and hydrogen, which slightly increases the yield of synthesis gas and thus even generates additional fuel instead of using fuel.
  • methane is additionally introduced into the melt pool as cooling for the input organs.
  • the present invention also has another embodiment in which methane and / or additional steam is added to the melt pool as cooling when the melt bath temperature is to be reduced.
  • the electric heater is used only during the starting phase.
  • the gasification parameters for example the pressure-charged fluidized-bed gasification, are set such that a sufficiently large proportion of carbon remains in the extracted ash of the pressure-charged fluidized-bed reactor, so that an electrical heater only required in exceptional cases.
  • the present invention is therefore designed such that the hot secondary raw gas is fed from the melt bath to a water wash, where it cools down and where the gaseous salt and metal compounds are washed out.
  • the present invention provides for the use of a fluidized bed cooler, as described in US Pat. No. 4,936,872.
  • the vaporous, salt-like or metallic compounds are condensed or desublimated on the grains of the cooled fluidized bed material and are thus recovered.
  • the present invention is also designed in such a way that the hot secondary raw gas is passed from the melt pool into a fluidized bed cooler in which the thermal energy of the hot secondary raw gas is used for steam generation and where the gaseous gases are used Condense or desublimate salt and metal compounds on the grains of the fluidized bed material and the fluidized bed material loaded in this way is drawn off.
  • the fluidized-bed particles loaded in this way are expediently continuously removed from the fluidized bed and returned to the molten bath.
  • the entry in the weld pool can be done in the same way as previously described for ashes: either pneumatically as dust, which requires grinding, or via a lock system together with the other substances which are added to the molten bath.
  • the use of the molten bath also allows the production of a slag which is used as a cement base material. This is due on the one hand to the fact that the composition can be adjusted by adding additives to the molten bath and, on the other hand, to the fact that the heavy metals are absorbed by the metallic phase and can therefore only be found to a very small extent in the ceramic slag, which represents a further advantage of the invention. It is also possible through a suitable mixing ratio of the additives to influence the melting temperature of the liquid, ceramic phase.
  • the substances calcium oxide (CaO), aluminum oxide (Al 2 0 3 ) and silicon dioxide (Si0 2 ) come into consideration as additives.
  • the operating temperature of the melting bath can be selected so that a low-melting eutectic is formed in the ceramic phase.
  • base metals such as vanadium are also to be incorporated into noble metals that form the metallic phase of the molten pool, such as iron, the temperature of the molten pool must be raised accordingly, the relationship is described in Ullmann's Encyclopedia of Industrial Chemistry, 4. , revised and expanded edition, 1975, Weinheim, volume 10, p. 330, is shown in detail. In this case, the choice of a higher melting eutectic is recommended.
  • the present invention therefore provides in one of its embodiments that the molten bath has a liquid, ceramic phase and at least one liquid, metallic phase in which the starting materials are thermally and catalytically decomposed.
  • the present invention has a configuration in which a base material for cement production is made from the ceramic, liquid phase of the molten bath is obtained which contains the mineral additives and the mineral components of the carbonaceous feedstocks.
  • a fluidized bed cooler is used to cool the hot secondary raw gas generated in the melt pool, it is advisable to also select the fluidized bed material in the above-mentioned suitable mixing ratio, since this is also added to the melt pool and to form the liquid, contributes to the ceramic phase.
  • the sensible heat carried by the primary raw gas is devalued in a thermodynamic sense.
  • the hot primary raw gas has recently been passed through filters fitted with ceramic filter cartridges.
  • the major portion of the dust loading of the primary raw gas can thus be separated from it. All- However, with this hot gas dedusting, the hot primary raw gas must first be cooled to a temperature at which the filter candle material is still stable.
  • the fly ash in the hot gas filter must also be disposed of.
  • configurations were created with which the carbon content of the fly ash is particularly advantageously fed to recycling in a simple manner.
  • the waste heat of the primary raw gas generated in the gasification reactor is used for steam generation, the primary raw gas being cooled to a temperature which permits subsequent hot gas dedusting.
  • the flying dust separated from the cooled primary raw gas by means of hot gas dedusting is also added to the mixing and conveying device, into which the ashes from the bottom vent of the gasification reactor and possibly the mineral additives are also added.
  • the flying dust from the primary raw gas is transferred to the melt pool in order to convert the carbon content of the flying dust into additional secondary raw gas there.
  • An alternative embodiment of the present invention fertilizer provides that the cooled primary raw gas is fed to a hot gas dedusting system and that the dust separated there is introduced directly into the melting bath through an injection pipe.
  • FIG 1 and 2 show two process flow diagrams, in which the process according to the invention is described by way of example.
  • the carbon-containing feed 1 and the oxygen-containing feed gas 2 are placed in a pressure-charged fluidized bed reactor 3 and converted to synthesis gas 4 and carbon-containing ash 10.
  • the synthesis gas 4 is cooled in a steam generator 5, the cooled synthesis gas 6 is dedusted in a hot gas filter 7.
  • the carbon-containing dust 8, the carbon-containing ash 10 and the additives 11 are placed in a mixing and conveying device which preferably consists of a cooling screw and is capable of crushing coarse pieces.
  • the mixed ash 12, together with the lumpy residues 13 and the oxygen-containing feed gas 15, is introduced into the molten bath 16 by means of entry elements which are cooled with the methane / water vapor mixture 14.
  • FIG. 2 shows that the hot synthesis gas 19 is passed into a fluidized bed cooler 26, where the condensable or desublimable, harmful gas components are separated and the synthesis gas is cooled.
  • fresh fluidized bed material 27 is fed in and loaded fluidized bed material 28 is drawn off.
  • the loaded fluidized bed material 28 is fed into the mixing and conveying device 9 and from there it is passed into the melt pool 16 in the mixed ash 12.
  • the cleaned and cooled synthetic gas 23 is combined with the dedusted synthesis gas 24 from the hot gas filter 7 and fed as a mixed synthetic gas 25 for further processing and use.
  • a calculated mass balance for FIG. 2 serves to further explain the method: -

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé de production de gaz à partir d'au moins un matériau de départ renfermant du carbone, qui est partiellement oxydé au moyen d'air ou d'oxygène ou d'air enrichi en oxygène dans un réacteur de gazéification. L'invention vise à transformer en gaz la plus grande quantité possible de carbone résiduel présent également dans les cendres. A cet effet, le résidu de gazéification est introduit dans un bain de fusion dans lequel on ajoute un oxydant et des additifs, afin de produire, à partir du résidu de gazéification, un gaz brut secondaire, des scories céramiques et une matière fondue alliée, ledit gaz brut secondaire formé dans le bain de fusion étant mélangé au gaz brut primaire.
PCT/EP1997/002485 1996-06-01 1997-05-15 Procede de production de gaz WO1997046639A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU29553/97A AU2955397A (en) 1996-06-01 1997-05-15 Gas generation process

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19622152A DE19622152A1 (de) 1996-06-01 1996-06-01 Verfahren zur Erzeugung von Gas
DE19622152.8 1996-06-01

Publications (1)

Publication Number Publication Date
WO1997046639A1 true WO1997046639A1 (fr) 1997-12-11

Family

ID=7795961

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1997/002485 WO1997046639A1 (fr) 1996-06-01 1997-05-15 Procede de production de gaz

Country Status (5)

Country Link
AU (1) AU2955397A (fr)
DE (1) DE19622152A1 (fr)
ID (1) ID18179A (fr)
WO (1) WO1997046639A1 (fr)
ZA (1) ZA974765B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108264938A (zh) * 2018-01-15 2018-07-10 江西蓝天路之友环卫设备科技有限公司 一种城镇生活垃圾处理工艺

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2034003A1 (fr) * 2007-09-07 2009-03-11 ReSeTec Patents Geneva S.A. i.o. Procédé et appareil de production de gaz de synthèse à partir des déchets
SG155092A1 (en) * 2008-02-29 2009-09-30 Gueh How Kiap Hydrocarbon synthesis and production onboard a marine system using varied feedstock
SG155093A1 (en) * 2008-02-29 2009-09-30 Gueh How Kiap Hydrocarbon synthesis and production onboard a marine system using varied feedstock
SG155095A1 (en) * 2008-02-29 2009-09-30 Gueh How Kiap Hydrocarbon synthesis and production onboard a marine system using varied feedstock

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2286873A1 (fr) * 1974-10-05 1976-04-30 Otto & Co Gmbh Dr C Procede pour debarrasser des gaz de vapeurs et d'aerosols et installation pour la realisation du procede
FR2546178A1 (fr) * 1983-05-20 1984-11-23 Gagneraud Pere Fils Entreprise Procede de desulfuration des gaz a l'aide de bains mineraux fondus lors de la gazeification de produits carbones
GB2140453A (en) * 1982-03-22 1984-11-28 Midrex Corp Method of generating a reducing gas
DE3530240A1 (de) * 1984-11-07 1986-05-22 Voest-Alpine Ag, Linz Verfahren zum schmelzen von zumindest teilweise reduziertem eisenerz, vorrichtung zur durchfuehrung dieses verfahrens sowie verwendung der reaktionsgase und gichtgase einer derartigen vorrichtung
DE3529740C1 (en) * 1985-08-20 1987-01-08 Greul Artur Richard Process and equipment for gasifying carbonaceous wastes, if appropriate with addition of toxic and highly toxic wastes, to give synthesis gas
US4682985A (en) * 1983-04-21 1987-07-28 Rockwell International Corporation Gasification of black liquor
DE3633511A1 (de) * 1986-10-02 1988-04-14 Kloeckner Humboldt Deutz Ag Verfahren und anlage zum vergasen von kohlenstofftraegern, insbesondere kohle
EP0301213A2 (fr) * 1987-07-28 1989-02-01 Uhde GmbH Procédé et appareil pour refroidir des gaz bruts provenant d'une oxydation partielle d'un matériau carboné

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3434004C2 (de) * 1984-09-15 1987-03-26 Dornier System Gmbh, 7990 Friedrichshafen Verfahren und Vorrichtung zur Müllvergasung

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2286873A1 (fr) * 1974-10-05 1976-04-30 Otto & Co Gmbh Dr C Procede pour debarrasser des gaz de vapeurs et d'aerosols et installation pour la realisation du procede
GB2140453A (en) * 1982-03-22 1984-11-28 Midrex Corp Method of generating a reducing gas
US4682985A (en) * 1983-04-21 1987-07-28 Rockwell International Corporation Gasification of black liquor
FR2546178A1 (fr) * 1983-05-20 1984-11-23 Gagneraud Pere Fils Entreprise Procede de desulfuration des gaz a l'aide de bains mineraux fondus lors de la gazeification de produits carbones
DE3530240A1 (de) * 1984-11-07 1986-05-22 Voest-Alpine Ag, Linz Verfahren zum schmelzen von zumindest teilweise reduziertem eisenerz, vorrichtung zur durchfuehrung dieses verfahrens sowie verwendung der reaktionsgase und gichtgase einer derartigen vorrichtung
DE3529740C1 (en) * 1985-08-20 1987-01-08 Greul Artur Richard Process and equipment for gasifying carbonaceous wastes, if appropriate with addition of toxic and highly toxic wastes, to give synthesis gas
DE3633511A1 (de) * 1986-10-02 1988-04-14 Kloeckner Humboldt Deutz Ag Verfahren und anlage zum vergasen von kohlenstofftraegern, insbesondere kohle
EP0301213A2 (fr) * 1987-07-28 1989-02-01 Uhde GmbH Procédé et appareil pour refroidir des gaz bruts provenant d'une oxydation partielle d'un matériau carboné

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108264938A (zh) * 2018-01-15 2018-07-10 江西蓝天路之友环卫设备科技有限公司 一种城镇生活垃圾处理工艺

Also Published As

Publication number Publication date
ZA974765B (en) 1998-11-30
ID18179A (id) 1998-03-12
DE19622152A1 (de) 1997-12-04
AU2955397A (en) 1998-01-05

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