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EP2229429A2 - Élimination de cendres liquides et d'alcalis d'un gaz de synthèse - Google Patents

Élimination de cendres liquides et d'alcalis d'un gaz de synthèse

Info

Publication number
EP2229429A2
EP2229429A2 EP08864799A EP08864799A EP2229429A2 EP 2229429 A2 EP2229429 A2 EP 2229429A2 EP 08864799 A EP08864799 A EP 08864799A EP 08864799 A EP08864799 A EP 08864799A EP 2229429 A2 EP2229429 A2 EP 2229429A2
Authority
EP
European Patent Office
Prior art keywords
synthesis gas
oxygen
reactor
gasification
slag
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.)
Withdrawn
Application number
EP08864799A
Other languages
German (de)
English (en)
Inventor
Domenico Pavone
Michael Rieger
Ralf Abraham
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
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 Uhde GmbH filed Critical Uhde GmbH
Publication of EP2229429A2 publication Critical patent/EP2229429A2/fr
Withdrawn legal-status Critical Current

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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • C10K1/20—Purifying combustible gases containing carbon monoxide by treating with solids; Regenerating spent purifying masses
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/025—Processes for making hydrogen or synthesis gas containing a partial oxidation step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/84—Energy production
    • 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
    • C10J2300/0983—Additives
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand

Definitions

  • the invention relates to a process for the production of synthesis gas from a carbonaceous fuel, such as all types of coals, coke, petroleum coke, biomass, but also emulsions, orimulsion, etc.
  • a carbonaceous fuel such as all types of coals, coke, petroleum coke, biomass, but also emulsions, orimulsion, etc.
  • synthesis gas can be directly after the production easy to clean without further cooling down. As a result, the heat energy of the gas can be better utilized.
  • the invention also relates to a device with which this method can be implemented and uses with respect to the getter ceramics used.
  • the synthesis gas is used to recover important chemicals such as ammonia or methanol.
  • the damaging or interfering components contained in the synthesis gas must be removed from the synthesis gas to carry out the necessary process steps.
  • the synthesis gas is often mixed to deliver the high internal energy with a cooler foreign medium. This process is also called quenching process.
  • a foreign medium usually water is used. But can also be used other substances, such as nitrogen or carbon dioxide.
  • the synthesis gas is significantly cooled down.
  • the quenching process is often followed by further process steps requiring further cooling of the synthesis gas. These are, for example, washing processes for removing acid gases.
  • CONFIRM ⁇ ON COPY If the pressure is high, the use of a turbine to obtain kinetic rotational energy is also possible. The kinetic rotational energy of the turbine in turn can be used to generate electricity or to drive plant aggregates. This makes the process for the production of synthesis gas economically favorable. Such a process can be used for the combined production of synthesis gas and electric power.
  • the synthesis gas obtained can be used without a further step of cooling to drive the turbine.
  • the harmful liquid and gaseous constituents of the synthesis gas could be removed without cooling and without changing the state of aggregation. Because liquid droplets and corrosive vapors would lead to erosion and corrosion damage to the turbine blades.
  • US Pat. No. 4,482,358 A describes a process for the production of synthesis gas, which passes the synthesis gas through a cyclone-type pressure vessel in which a solid bed of different size distributions is circulated. When flowing through the solid bed, the entrained solid and slag solids solidify and are discharged from the system. By using a slag breaker, the solids can be crushed and reused. Both the gas and the crushed slag can be passed through heat exchangers that can be used to drive a turbine to generate electricity. Before passing through the pressure vessel, the synthesis gas is subjected to a cooling process with water. The disadvantage of this system is that water must be used to cool the synthesis gas. Another disadvantage is that steam must be generated to drive the turbine. A removal of the metal compounds from the synthesis gas is not described.
  • EP 412 591 B1 describes a process for the separation of alkali and heavy metal compounds from hot gases.
  • the hot gases accumulate as combustion gases during the combustion of fossil fuels and are used to drive a gas turbine with the purpose of power generation.
  • the combustion gases are treated with a sorbent before entering the gas turbine. This is suspended in the stream of hot gases.
  • the state of the suspension is described as the state of a fly-ash cloud or an expanded fluidized bed of the sorbent.
  • the sorbent can be made of SiIi- ciumdioxid, alumina, magnesium aluminates, magnesium aluminosilicates or calcium aluminosilicates exist.
  • the combination of alkali deposition with the production of synthesis gas is not described.
  • a removal of fly ash or the liquefied slag from the hot gas is not described.
  • the object of the invention is therefore to provide methods and devices that liberate the synthesis gas from a gasification process of the entrained liquid slags and alkalis without having to accept a cooling down or relaxing the gas in purchasing.
  • a turbine to generate rotational energy, this should not start any encrustations and should not suffer corrosion or material erosion due to the action of the hot synthesis gas.
  • the object is achieved by a process for the production of synthesis gas by gasification with air or oxygen or oxygen-enriched air and water vapor, wherein
  • a solid or liquid carbonaceous fuel is added to a reactor in which the fuel is reacted with air or oxygen or oxygen-enriched air and with steam at elevated temperature to a synthesis gas consisting essentially of hydrogen, carbon dioxide and carbon monoxide, and
  • the synthesis gas obtained is carried out in any direction from the reactor,
  • these fuels are fed before use of a suitable device for crushing.
  • a suitable device for crushing This can be, for example, a ball mill or a vertical mill. But this can also be a shredder or a milling device.
  • water vapor-containing air is used as the combustion gas, which reacts with the carbon of the fuel predominantly to carbon monoxide and hydrogen.
  • the combustion gas can also be enriched with oxygen.
  • the combustion gas is supplied in particular under elevated pressure.
  • the fuel is preferably pneumatically fed into the gasification reactor. However, it is also possible to feed the fuel through a screw or a conveyor belt in the gasification reactor. If the fuel is added to the reactor in the form of a slurry or emulsion, it may also be pumped into the reactor.
  • the synthesis gas is carried out elsewhere from the reactor. This is preferably done laterally. However, the execution of the synthesis gas can also be carried out on the reactor at any point. Immediately afterwards the separation of the liquid components must take place.
  • the slag separation device is a cyclone-like device in which the hot gas makes a circular movement, so that a large part of the slag contained in the gas is deposited by the centrifugal forces on the walls.
  • the slag separation device contains a packed bed in which the slag is separated from the gas. The bed can be integrated in a cyclone, a corresponding device is described in DE 43 36 100 C1.
  • Further embodiments of the invention relate to the deposition of the vaporous alkalis.
  • the getter ceramic is added to the fuel as a powder, the gettering ceramic in the gasification chamber comes into contact with the resulting synthesis gas, and the removal of the alkalis from the synthesis gas takes place in the gasification chamber.
  • the gettering ceramic comes into contact with the synthesis gas as a bed in a device downstream of the slag separation device and the removal of the alkalis from the synthesis gas takes place in this downstream device.
  • the admixing of the getter materials can also take place after the gasification.
  • An object of the getter materials can be done by spraying or the like.
  • Further embodiments of the invention relate to the process parameters of the gasification.
  • fuel all materials can be used which contain solid carbonaceous materials which are suitable for gasification and reaction with a water vapor and oxygen-containing gas. This is especially fine ground coal with typical particle diameter. Suitable here are all types of coal. For example, crushed hard coal or lignite can be used. However, it is also possible to use comminuted plastics, petroleum coke, biological fuels such as comminuted wood or bitumen or other biomasses. The fuel can also be added in liquid form. These may be, for example, slurries or emulsions of finely divided substances, including orimulsion. Viscous fuels are also suitable in principle. Finally, all substances which can be reacted at elevated temperature to give a synthesis gas which consists essentially of carbon monoxide and hydrogen are suitable.
  • the gasification temperature should be between 800 and 1800 0 C, the pressure of 0.1 to 10 MPa be selected.
  • synthesis gas obtained by the gasification is subjected after slag and alkali deposition of a gas scrubbing to remove acidic gases, such as the removal of sulfur-containing components by chemisorb Schlierenders means.
  • the synthesis gas obtained by the gasification is passed after slag and alkali deposition through a hot gas turbine.
  • the synthesis gas obtained can be used for the synthesis of chemical products, for the production of metals by direct reduction, or for the production of energy in a gas turbine.
  • the invention also includes an apparatus for producing synthesis gas by gasification according to the method described above, comprising a reactor which is suitable for the gasification of carbonaceous fuels at high temperatures, and this reactor comprises a device for supplying air or oxygen or oxygen-enriched air and water vapor, and has a reaction space for the reaction of carbonaceous fuels, with an at least one stage hot gas cyclone is arranged directly downstream of the reactor having a liquid slag draw-off device or a Vorrich- arranged with a bed having a discharge device for liquid slag, or both, the order is selectable.
  • a device with a bed of getter ceramic can be provided directly after the slag separation device and a hot gas turbine can be mounted behind it.
  • the invention also includes the uses of the gettering ceramic.
  • the getter ceramic either silica or silicates or aluminates or alumina or compounds fertilize or mixtures thereof or any compounds of oxide and non-oxide ceramic. Further, it may contain transition metal-containing compounds.
  • the gettering ceramic is formed from aluminosilicates, with kaolin, emathlites, bentonites and montmorillonites being particularly preferred.
  • the getter ceramic is added to the fuel, it is powdery, otherwise it is introduced in the form of a highly porous solid particles in the form of a packed bed in the alkali.
  • the highly porous solid particles may be spheres, calipers, Raschig rings, Pall rings or cylindrical bodies, or any other shapes.
  • the particle diameters are usually between 2 mm and 100 mm and preferably 20 to 40 mm, most preferably 30 mm.
  • FIG. 1 shows in simplified form the process flow of a process according to the invention for the gasification and supply of synthesis gas, which uses the internal energy of the synthesis gas to generate electricity.
  • the fuel 1 is conveyed into the gasification reactor 2 where it is reacted with compressed, oxygen-enriched air 3 and steam 4 into a syngas 5 charged with slag droplets and alkali.
  • the carburetor can be provided with a slag discharge. Additives can be added after the carburetor.
  • the synthesis gas 5 is passed in a cyclone 6, where it is freed from the slag droplets and optionally alkalis.
  • the slag 7 is withdrawn liquid.
  • the thus cleaned hot gas 11 enters the hot gas turbine 12 and is relaxed there.
  • the relaxed and thereby cooled synthesis gas 13 is discharged for further use.
  • the shaft power of the hot gas turbine 12 serves to drive a compressor 14 and a generator 15.
  • the compressor 14 is used for compressing oxygen-enriched air 16. This is fed into the gasification reactor 2
  • reference numeral 1 a fuel with additive for alkalinity removal and by reference numeral 6, a bed or a cyclone with bed to be understood.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Industrial Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne un procédé de fabrication de gaz de synthèse par gazéification avec de l'air ou de l'oxygène ou de l'air enrichi d'oxygène, et de la vapeur d'eau. Sachant: qu'un combustible solide ou liquide contenant du carbone est chargé dans un réacteur, dans lequel le combustible est, avec l'air ou l'oxygène ou l'air enrichi d'oxygène et avec la vapeur d'eau, à une température élevée, transformé en un gaz de synthèse qui est constitué en majeure partie d'hydrogène, de dioxyde de carbone et de monoxyde de carbone; que des gouttelettes de scories minérales sont produites lors de la réaction, qui sont évacuées du réacteur séparément du gaz de synthèse obtenu; que le gaz de synthèse obtenu est évacué du réacteur dans une direction quelconque; que les alcalis sous forme de vapeur contenus dans le gaz de synthèse sont éliminés du gaz de synthèse par mise en contact avec une céramique à effet getter; et que le gaz de synthèse est dirigé sans refroidissement préalable dans un dispositif de séparation de scories, dans lequel sont extraites des gouttelettes de scories sous forme de scories liquides.
EP08864799A 2007-12-22 2008-12-22 Élimination de cendres liquides et d'alcalis d'un gaz de synthèse Withdrawn EP2229429A2 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102007063118 2007-12-22
DE102008013179A DE102008013179A1 (de) 2007-12-22 2008-03-07 Entfernung von Flüssigasche und Alkalien aus einem Synthesegas
PCT/EP2008/010995 WO2009080334A2 (fr) 2007-12-22 2008-12-22 Élimination de cendres liquides et d'alcalis d'un gaz de synthèse

Publications (1)

Publication Number Publication Date
EP2229429A2 true EP2229429A2 (fr) 2010-09-22

Family

ID=40690047

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08864799A Withdrawn EP2229429A2 (fr) 2007-12-22 2008-12-22 Élimination de cendres liquides et d'alcalis d'un gaz de synthèse

Country Status (12)

Country Link
US (1) US20110036013A1 (fr)
EP (1) EP2229429A2 (fr)
CN (1) CN101910376B (fr)
AU (1) AU2008340600B2 (fr)
BR (1) BRPI0821736A2 (fr)
CA (1) CA2709963A1 (fr)
DE (1) DE102008013179A1 (fr)
RU (1) RU2490314C2 (fr)
TW (1) TW200940700A (fr)
UA (1) UA106349C2 (fr)
WO (1) WO2009080334A2 (fr)
ZA (1) ZA201004354B (fr)

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Publication number Priority date Publication date Assignee Title
DE102010006192A1 (de) * 2010-01-29 2011-08-04 Uhde GmbH, 44141 Verfahren zur Biomasse-Vergasung in einer Wirbelschicht
FR2958181B1 (fr) * 2010-04-06 2014-09-05 Inst Francais Du Petrole Procede permettant l'elimination des oxydes alcalins en phase gazeuse
US8691115B2 (en) * 2010-04-29 2014-04-08 Indiana University Research And Technology Corporation System and method for controlling char in biomass reactors
DE102010045537A1 (de) * 2010-09-15 2012-03-15 Uhde Gmbh Verfahren zur Erzeugung von Synthesegas
DE102011114171A1 (de) * 2011-09-19 2013-03-21 Thyssenkrupp Uhde Gmbh Verfahren zur Herstellung von Synthesegas durch Vergasung einer Biomasse in einer Wirbelschicht
DE102017219786A1 (de) * 2017-11-07 2019-05-09 Thyssenkrupp Ag Verfahrenstechnische Anordnung und Verfahren zum Bereitstellen von Alkali-reduziertem Synthesegas sowie Steuerungseinrichtung und Verwendung
DE202022001185U1 (de) 2022-05-18 2022-06-17 Ralf Abraham Vorrichtung zur Alkaliabscheidung bei der Biomassevergasung in Wirbelschichtvergasern
CN115232652A (zh) * 2022-05-30 2022-10-25 浙江石油化工有限公司 一种用燃烧处理碱渣的方法

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US7500997B2 (en) * 2002-02-05 2009-03-10 The Regents Of The University Of California Steam pyrolysis as a process to enhance the hydro-gasification of carbonaceous materials
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US20060108721A1 (en) * 2004-11-19 2006-05-25 Lew Holdings, Llc Single vessel blast furnace and steel making/gasifying apparatus and process
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DE102005043212A1 (de) * 2005-09-09 2007-03-15 Future Energy Gmbh Verfahren und Vorrichtung zur Erzeugung von Synthesegasen durch Partialoxidation von aus aschehaltigen Brennstoffen hergestellten Slurries und Vollquenchung des Rohgases

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Also Published As

Publication number Publication date
CN101910376B (zh) 2017-04-05
CN101910376A (zh) 2010-12-08
AU2008340600A1 (en) 2009-07-02
WO2009080334A2 (fr) 2009-07-02
BRPI0821736A2 (pt) 2015-06-16
CA2709963A1 (fr) 2009-07-02
RU2490314C2 (ru) 2013-08-20
US20110036013A1 (en) 2011-02-17
AU2008340600B2 (en) 2013-07-04
UA106349C2 (ru) 2014-08-26
TW200940700A (en) 2009-10-01
DE102008013179A1 (de) 2009-06-25
ZA201004354B (en) 2011-04-28
WO2009080334A3 (fr) 2010-02-25
RU2010130668A (ru) 2012-01-27

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