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WO2008095984A2 - Procédé et dispositif de combustion de combustibles solides - Google Patents

Procédé et dispositif de combustion de combustibles solides Download PDF

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Publication number
WO2008095984A2
WO2008095984A2 PCT/EP2008/051507 EP2008051507W WO2008095984A2 WO 2008095984 A2 WO2008095984 A2 WO 2008095984A2 EP 2008051507 W EP2008051507 W EP 2008051507W WO 2008095984 A2 WO2008095984 A2 WO 2008095984A2
Authority
WO
WIPO (PCT)
Prior art keywords
combustion
combustion chamber
zone
solid fuels
dust
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.)
Ceased
Application number
PCT/EP2008/051507
Other languages
German (de)
English (en)
Other versions
WO2008095984A3 (fr
Inventor
Bernd Meyer
Michael Trompelt
Mathias Rieger
Hardy Rauchfuss
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.)
Bergakademie Freiberg
Original Assignee
Bergakademie Freiberg
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 Bergakademie Freiberg filed Critical Bergakademie Freiberg
Publication of WO2008095984A2 publication Critical patent/WO2008095984A2/fr
Publication of WO2008095984A3 publication Critical patent/WO2008095984A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/007—Supplying oxygen or oxygen-enriched air
    • 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
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a method and a device for burning solid fuels with combustion agents containing free oxygen, in particular for an oxyfuel process.
  • the combustion of a carbonaceous fuel produces a nearly pure CO 2 gas.
  • the aim is to convert the chemically combined heat of the fuel (calorific value) completely into sensible heat, which is used in the steam-power process to generate electrical energy.
  • the combustion of the fuel takes place in a dust firing with supply of nitrogen-reduced combustion air (high concentration of oxygen).
  • DE 10 2004 059 360 proposes a "process for burning fossil fuel in power plants operating according to the oxyfuel process", which is characterized in that a known melting chamber furnace is used as the furnace, the furnace being designed in this way and operated at such temperatures that at least a portion of the ash is molten and discharged in this state from the furnace.
  • the theory of partial oxidation known from gasification basically gives the expert no indication as to how to make the complete oxidation of solid fuels under the condition of the extensive to complete conversion of the carbon of the solid fuels to CO 2 .
  • the object of the invention is to achieve a reduction or avoidance of the flue gas recirculation in processes for the combustion of solid fuels with free oxygen-containing combustion agents and thereby plant and operational simplifications and to increase the efficiencies and reduce consumption.
  • the object is achieved by a method for burning solid fuels with free oxygen-containing combustion agents in the dust with dust, in the form of particulate matter and grit laden gases leave the combustion chamber on the top side and predominantly coarse-grained products the combustion chamber as a bottom product on the underside, wherein the combustion chamber the combustion medium necessary for the complete combustion, and characterized in that the combustion chamber is separated into at least one first combustion zone, which is designed as a moving bed, and at least one second combustion zone located above, which formed as a strongly expanded or circulating fluidized bed is that the separation of the combustion chamber by at least one lateral, directed into the middle of the combustion chamber injection of the required for the extensive combustion of the solid fuels second Verb
  • the second combustion agent having an oxygen content> 50 Vo 1 .-% and are injected at a speed of> 10 m / s to 100 m / s, that at the lower end of the first combustion zone required for the virtually complete combustion first Burning in countercurrent be blown, wherein the oxygen content of the gas mixture is
  • the environment extends to a radius around the entry of max. about 1 m. Within this radius, experience has shown that slagging preferably occurs because, due to the high carbon contents, excessive temperature excesses to values above the ash softening temperatures can occur particularly quickly here.
  • the combustion means ie the first and / or the second combustion means may contain, in addition to oxygen, carbon dioxide, water vapor, NH 3 and / or purge gases. These secondary constituents can be oxidized substantially free of pollutants at the temperatures and oxygen concentrations occurring in the process according to the invention (NH 3 , purge). Gases) or used to control the combustion processes (carbon dioxide, water vapor).
  • the combustion process takes place advantageously in a top-cylindrical and bottom-cylindrical or conically narrowing combustion chamber open on both sides.
  • the combustion chamber can also have a square or rectangular flow cross-section.
  • the combustion chamber is subdivided into at least one first combustion zone, whereby it is designed as a moving bed, and into at least one second combustion zone situated above it, this being constructed as a strongly expanded or circulating fluidized bed.
  • the separation of the combustion chamber is effected by at least one lateral, directed into the middle of the combustion chamber injection of the required for the extensive combustion of the solid fuel predominantly free oxygen-containing second combustion agent.
  • the injection angle is 20 ° to 100 °, preferably 45 ° to 90 °.
  • the injection angle .alpha..sub.i is the angle between the injection device (generally its geometric axis) and the inner contour of the combustion chamber seen from the vertex of the angle.
  • the injection of the second combustion agent takes place with a, compared with larger apparatuses, more obtuse injection angle, so that the opposite inner surface of the combustion chamber jacket is not illuminated with free oxygen.
  • the fuels are introduced above the top of the first combustion zone into the combustion chamber, especially into the second combustion zone.
  • the entry is so far above that there is an intensive turbulence and combustion of the fuels with the rising gases of the first and second combustion means.
  • the fuels are introduced at a distance of 1 m to 10 m, more preferably at a distance of 2 m to 5 m, above the upper end of the first combustion zone in the combustion chamber.
  • the supply of solid fuels takes place at an entry angle of 90 ° to 180 °, preferably from 100 ° to 160 °.
  • the entry angle ⁇ 2 is the angle between fuel input (in general its geometric axis) and the inner contour of the combustion chamber seen from the vertex of the angle downwards. An approximately right angle, to the inner contour of the combustion chamber, favors little Appa- rate overall heights.
  • a blunt to elongated angle is advantageous.
  • the supply of the solid fuels may take place at the predetermined distance above the upper end of the first combustion zone at different heights and distributed over the circumference of the combustion chamber jacket.
  • the extensive combustion of the solid fuels takes place in the second combustion zone.
  • the strong fluidization is required to evenly distribute the carbon in the second combustion zone.
  • the uniform distribution is a prerequisite for the formation of so - called hot spot zones in the fluidized bed, in which the ash melts predominantly or completely, and as a consequence, disruptive slagging may occur.
  • the supply of the second combustion means takes place at a high injection rate, since the combustion medium is oxygen predominant fluidizing agent and the oxygen of the second combustion agent is also to reach the center of the combustion chamber of the second combustion zone.
  • the injection rate of the second combustion medium is over 10 m / s for small plants and up to 100 m / s for large plants.
  • the conversion of the carbonaceous solid fuel in the second combustion zone is carried out at temperatures between 750 0 C and 950 0 C, which locally in the areas in which oxygen-containing second combustion agent is injected, higher temperatures may occur, so that, depending on the melting point of the ash the solid fuels may be granulated at least a portion of the ash constituents.
  • These requirements can z. B. be present when burning Rhenish lignite whose ash has a melting point of 1,250 0 C.
  • the first combustion means are used for the most complete possible combustion of the remaining carbonaceous constituents and for the oxidation of the ashes in a first combustion zone, this being designed as a moving bed.
  • the first combustion means may be injected in a plurality of superimposed regions and / or at the lower end of the first combustion zone. If necessary, it is possible to inject first combustion agents of different composition, for example consisting of water, (V vapor, O 2 / CO 2 and VCC vapor mixtures in the individual planes.)
  • first combustion agents for example consisting of water, (V vapor, O 2 / CO 2 and VCC vapor mixtures in the individual planes.)
  • the use of different first combustion agents at different heights in the first combustion zone may occur show that on the one hand a most extensive implementation of carbon-containing residues and possibly also an oxidation of the ash or granules to take place, on the other hand, however, the temperature is kept below the ash melting point and an end product is to be discharged from the first combustion zone, which cooled as far is that it can be handled with the usual means of transport, equipment, etc.
  • the composition and amount of the first combustion agent are adjusted so that the carbon content of the first combustion zones at the lower end of the Verbrennungsr Aumes leaving bottom product is reduced to the values required for landfilling. Furthermore, the final residue, which consists essentially of ash and ash granules, is to be cooled before it leaves the lower end of the first combustion zones of the combustion chamber.
  • the rate at which the carbonaceous ingredients, ashes and ash granules, e.g. B. by means of a screw conveyor, are discharged from the lower end of the first combustion zones of the combustion chamber is essentially determined by the residence time of the solids and dusts in the combustion chamber, which is required at the given conditions, in particular temperatures, to the desired carbon conversion to reach.
  • solid matter and dust circulate in the combustion chamber, or coarse dust is recirculated via the separator into the second combustion zone.
  • the solid fuels introduced into the upper region of the second combustion zone form larger amounts of dust when incinerated, which is only incompletely separated due to the fineness in the separator.
  • the undeclared particulate matter usually significantly ⁇ 1% of the total amount of dust entrained, so it is not returned via the separator, while the coarse dust is recycled through the separator.
  • This separation is particularly beneficial for the method according to the invention.
  • the melting points of the ashes are thus higher, and consequently the risk of malfunctioning sintering, agglomerations or slagging in this particularly sensitive region of high oxygen concentrations is markedly reduced.
  • the inventive method differs from other methods of combustion in the circulating fluidized bed, in which the fuel at the level of the entry of / required for combustion oxygen / air are supplied and fine dust and coarser ash constituents are present side by side and can react with melting point reduction.
  • the grain spectrum of the solid inventory in the second combustion zone shifts to larger grain diameters. This means that the gas flow velocity can be increased while maintaining the same solids discharges, which increases the specific plant performance.
  • the dust-laden gases are discharged from the combustion chamber.
  • the dust entrained with the gases consists essentially of residual coke with a C content of ⁇ 2% by mass.
  • a large part of the dust of the gases is separated as coarse dust and fed into the combustion chamber above the combustion agent introduction of the second combustion agent into the second combustion zone.
  • the feed of the separated coarse dust occurs at a distance of 1 m to 10 m, preferably 2 m to 5 m, above the upper end of the first combustion zones.
  • the return of the separated coarse dust is carried out in an entry angle of 90 ° to 180 °, preferably from 100 ° to 160 °.
  • the entry angle Ct 3 is the angle between coarse dust entry (in general its geometric axis) and the inner contour of the combustion space seen from the vertex of the angle downwards.
  • the erfmdungssiee method ensures that carbon is present with a uniform concentration distribution at a low concentration level in the combustion chamber, mainly with a concentration of ⁇ 5 Ma. -% to even ⁇ 2 Ma. -% in the upper and lower part of the second combustion zone.
  • the bottom of the combustion chamber is preferably designed to be open and free of internals.
  • biomasses including sewage sludge, lignite, coal or anthracite and mixtures thereof may be used for the process according to the invention.
  • a device for burning solid fuels with free-oxygen-containing combustion agents which consists essentially of a coolable pressure-resistant reactor housing with a ash discharge at the foot, a combustion gas outlet at the top of the combustion reactor and in which the combustion chamber is separated into at least a first Combustion zone, which is designed as a moving bed, and in at least one second combustion zone located above it, which is designed as a highly expanded or circulating fluidized bed.
  • the separation of the combustion chamber is carried out by at least one lateral, directed into the middle of the combustion chamber injection device required for the substantial combustion of solid fuels second combustion means.
  • the injection device is designed so that the second combustion agent can be injected with an oxygen content of> 50% by volume and at a rate of> 10 m / s to 100 m / s.
  • the introduction of fuel is arranged so far above the upper end of the first combustion zone that at the level of the entry and its surroundings no hot spot zones are formed in which ash melts predominantly or completely.
  • the injection device consists essentially of a plurality of nozzles uniformly arranged in a plane on the circumference of the device.
  • the injection angle of the nozzles for the second combustion means is 20 ° to 100 °, preferably 45 ° to 90 °.
  • the injection angle ⁇ i is the angle between the injection device (generally its geometric axis) and the inner contour of the combustion chamber seen from the vertex of the angle downwards.
  • the injection of the second combustion agent takes place with a, compared with larger apparatuses, more obtuse injection angle, so that the opposite inner surface of the combustion chamber jacket is not illuminated with free oxygen.
  • the device for injecting the first combustion agent is advantageously designed such that it permits injection in a plurality of superimposed regions and / or at the lower end of the first combustion zone.
  • the fuel entry is advantageously designed as a diagonal tube entry. It is oriented so that the supply of solid fuels in an entry angle of 90 ° to 180 °, preferably from 100 ° to 160 °.
  • the entry angle ⁇ 2 is the angle between fuel input (in general its geometric axis) and the inner contour of the combustion chamber seen from the vertex of the angle downwards. An approximately right angle, to the inner contour of the combustion chamber, favored low apparatus heights. For entry of solid fuels with poor flow behavior, a blunt to elongated angle is advantageous.
  • the fuel entry advantageously consists of several distributed on the circumference of the device in equal or different heights arranged inclined tube entries.
  • the device for returning the dust, mainly coarse Dust is arranged so that it allows the return of dust, especially coarse dust, in an entry angle of 90 ° to 180 °, preferably from 100 ° to 160 °.
  • the entry angle Ct 3 is the angle between coarse dust entry (in general its geometric axis) and the inner contour of the combustion space seen from the vertex of the angle downwards.
  • the incinerator shown in Figure 1 consists of a combustion chamber (1), which is cylindrical at the top and conically constricted at the bottom, but is open on both sides.
  • the inner diameter of the upper cylindrical portion of the reaction space is 8 m.
  • Half the cone angle is 8 °.
  • the combustion chamber (1) is subdivided into a first combustion zone (3), which is designed as a moving bed, and a second combustion zone (2) located above it, this being constructed as a circulating fluidized bed.
  • the height of the combustion chamber (1) is 30 m.
  • the separation of the combustion chamber (1) takes place by a lateral, in the middle of the combustion chamber (1) directed injection of the required for the extensive combustion of the solid fuel predominantly free oxygen second combustion means (4), wherein the second combustion means (4) with a Speed of 20 m / s is injected.
  • the injection angle ⁇ i is 60 °.
  • the supply of the second combustion means (4) is effected by 8 evenly arranged in a nozzle plane nozzles.
  • the second combustion zone (2) As a second combustion agent (4), the second combustion zone (2) a gas mixture of 90 vol .-% oxygen and 10 vol .-% carbon dioxide at a temperature of 200 0 C is supplied.
  • the thermal output of the incinerator is 250 MW (th).
  • a solid fuel (5) comes German dry brown coal with a water content of 12%, a A- scheschmelzddling of 1,250 0 C and a grain size of 0 to 4 mm are used.
  • the amount of dry brown coal used is 45 t / h and is fed to the incinerator at a temperature of 60 ° C.
  • the entry of the dry lignite takes place with the help of Screws and over 2 to 3 symmetrically distributed inclined tubes in the region of the truncated cone-shaped portion of the second combustion zone (2) at a distance (hl) of 5 m above the center of the combustion agent jet.
  • the supply takes place at an entry angle ⁇ 2 of 130 °.
  • the radial speed profile of the second combustion zone (2) shows a design typical of homogeneously fluidized fluidized beds.
  • the axial gas velocity increases slightly in the flow direction. With a combustion chamber diameter of 8 m, this is 5.2 m / s.
  • the conversion of the dry lignite takes place to 90% in the second combustion zone (2) at temperatures between 750 0 C and 950 0 C, which locally in the areas in which oxygen-containing second combustion agent (2) is injected, higher temperatures may occur, so that using the oxygen-containing second combustion means (4) at least locally occurring temperatures exceed the ash melting point of 1250 0 C and it comes to a granulation of about 10% of ash components.
  • first combustion zone (3) At the lower end of the combustion chamber (1) takes place in an open and free of internals designed first combustion zone (3) the ash discharge (7) and the supply of the required for the complete combustion of the carbon amount of first combustion agent (6), consisting of 15 vol .-% oxygen and 85 vol. 1 .-% steam, in countercurrent at a temperature of 200 0 C.
  • the first combustion agent (6) is used for the most complete possible combustion of the remaining carbonaceous constituents and for the oxidation of the ashes in a first combustion zone (3), which is designed as a moving bed. Furthermore, the coarse-grained residue is cooled as a bottom product (7), which consists essentially of ash and ash granules, before it leaves the lower end of the first combustion zone (3) of the combustion chamber (1) trouble-free.
  • the speed with which the solid residues remaining below the moving bed of the first combustion zone (3) moving from top to bottom are discharged by means of a screw conveyor from the lower end of the first combustion zone (3) of the combustion chamber (1) is essentially determined the residence time of the solids and dusts in the combustion chamber (1), which is required at the given conditions, in particular temperatures, to achieve the desired carbon conversion of 100%.
  • the dust-laden combustion gas (8) is discharged.
  • the entrained with the combustion gas dust has a carbon content of usually ⁇ 2 Ma. -% on.
  • a large part of the dust of the combustion gas primarily the coarse dust, is separated and fed to the combustion space (1) above the combustion agent injection of the second combustion agent (4) into the second combustion zone (2 ).
  • the supply of the recirculated dust (11), mainly coarse dust, takes place with a distance (h2) of 3 m above the upper end of the first combustion zone (3).
  • the return of the solid takes place in a entry angle 013 of 130 °.
  • Second combustion zone strongly expanded or circulating fluidized bed

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Combustion Of Fluid Fuel (AREA)

Abstract

L'invention concerne un procédé et un dispositif de combustion de combustibles solides à l'aide d'agents de combustion contenant de l'oxygène libre, en particulier pour un procédé d'oxycombustion. Selon le procédé de combustion de combustibles solides à l'aide d'agents de combustion contenant de l'oxygène libre, des gaz chargés de poussière, sous forme de poussière fine et de poussière grossière, quittent la chambre de combustion par le haut et des produits principalement à gros grains quittent la chambre de combustion par le bas sous forme de produit de queue, les agents de combustion nécessaires à une combustion complète étant amenés à la chambre de combustion. Ledit procédé se caractérise en ce que la chambre de combustion est séparée en au moins une première zone de combustion, conçue sous forme de lit mobile, et au moins une deuxième zone de combustion, située au-dessus de la première et conçue sous forme de lit fluidisé très expansé ou circulant; la séparation de la chambre de combustion est produite par au moins une injection latérale des seconds agents de combustion nécessaires à une combustion importante des combustibles solides en direction du centre de la chambre de combustion, lesquels seconds agents de combustion présentent une teneur en oxygène > 50 % en volume et sont injectés à une vitesse comprise entre 10 m/s et 100m/s; les premiers agents de combustion nécessaires à une combustion pratiquement complète sont injectés à contre-courant à l'extrémité inférieure de la première zone de combustion, la teneur en oxygène du mélange gazeux étant limitée à une valeur < 50 %, de préférence < 21 %, voire < 10 %, et les combustibles solides sont introduits dans la chambre de combustion par l'extrémité supérieure de la première zone de combustion tant qu'aucun point chaud ne se forme au niveau et autour de la matière introduite, point chaud au niveau duquel les cendres fondent entièrement ou en majeure partie.
PCT/EP2008/051507 2007-02-07 2008-02-07 Procédé et dispositif de combustion de combustibles solides Ceased WO2008095984A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007006978.4 2007-02-07
DE102007006978 2007-02-07

Publications (2)

Publication Number Publication Date
WO2008095984A2 true WO2008095984A2 (fr) 2008-08-14
WO2008095984A3 WO2008095984A3 (fr) 2009-01-22

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DE (1) DE102008009132B4 (fr)
WO (1) WO2008095984A2 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014199091A1 (fr) * 2013-06-13 2014-12-18 IFP Energies Nouvelles Procédé et installation de combustion par oxydo-réduction en boucle chimique d'une charge hydrocarbonée solide
US9512999B2 (en) 2008-12-10 2016-12-06 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources High pressure direct contact oxy-fired steam generator
CN115716082A (zh) * 2022-11-17 2023-02-28 陕西省水工环地质调查中心 一种基于土壤修复的生物炭复合材料制备方法

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US5156099A (en) * 1988-08-31 1992-10-20 Ebara Corporation Composite recycling type fluidized bed boiler
DD301982A7 (de) * 1989-08-01 1994-10-06 Enag Energieversorgung Nordthu Vorrichtung zur Waermeerzeugung aus gasfoermigen, fluessigen und festen Brennstoffen
AU1449992A (en) * 1992-03-05 1993-10-05 Technische Universiteit Delft Method and apparatus for combusting a carbonaceous material
EP0722067A3 (fr) * 1995-01-12 1998-02-04 KABUSHIKI KAISHA KOBE SEIKO SHO also known as Kobe Steel Ltd. Dispositif de récupération de chaleur pour lit fluidisé
WO1997048950A1 (fr) * 1996-06-21 1997-12-24 Ebara Corporation Procede et appareil de gazeification de lit fluidise
DE19930071C2 (de) * 1999-06-30 2001-09-27 Wolfgang Krumm Verfahren und Vorrichtung zur Pyrolyse und Vergasung von organischen Stoffen und Stoffgemischen
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DE10029724C2 (de) * 2000-05-31 2003-07-31 Messer Griesheim Gmbh Verfahren zum Blähen von Vermiculit
EP1201731A1 (fr) 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
DE102004059360A1 (de) 2003-12-01 2005-06-23 Technische Universität Dresden Verfahren zur Verbrennung von fossilen Brennstoff in nach dem Oxyfuel-Prozess arbeitenden Kraftwerken

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9512999B2 (en) 2008-12-10 2016-12-06 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources High pressure direct contact oxy-fired steam generator
US9920923B2 (en) 2008-12-10 2018-03-20 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources High pressure direct contact oxy-fired steam generator
WO2014199091A1 (fr) * 2013-06-13 2014-12-18 IFP Energies Nouvelles Procédé et installation de combustion par oxydo-réduction en boucle chimique d'une charge hydrocarbonée solide
FR3007104A1 (fr) * 2013-06-13 2014-12-19 IFP Energies Nouvelles Procede et installation de combustion par oxydo-reduction en boucle chimique d'une charge hydrocarbonee solide
CN105393054A (zh) * 2013-06-13 2016-03-09 Ifp新能源公司 用于固体烃进料的氧化还原化学回路燃烧的方法和设备
US10215400B2 (en) 2013-06-13 2019-02-26 IFP Energies Nouvelles Method and plant for redox chemical looping combustion of a solid hydrocarbon feedstock
CN115716082A (zh) * 2022-11-17 2023-02-28 陕西省水工环地质调查中心 一种基于土壤修复的生物炭复合材料制备方法

Also Published As

Publication number Publication date
DE102008009132B4 (de) 2011-01-27
WO2008095984A3 (fr) 2009-01-22
DE102008009132A1 (de) 2008-08-21

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