WO1993018341A1 - Procede et appareil de combustion d'un materiau carbone - Google Patents

Procede et appareil de combustion d'un materiau carbone Download PDF

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Publication number
WO1993018341A1
WO1993018341A1 PCT/NL1992/000043 NL9200043W WO9318341A1 WO 1993018341 A1 WO1993018341 A1 WO 1993018341A1 NL 9200043 W NL9200043 W NL 9200043W WO 9318341 A1 WO9318341 A1 WO 9318341A1
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WO
WIPO (PCT)
Prior art keywords
stage
reaction chamber
sulphur
fluidised
capture agent
Prior art date
Application number
PCT/NL1992/000043
Other languages
English (en)
Inventor
Marek Andrzej WÓJTOWICZ
Jacob Adriaan Moulijn
Original Assignee
Technische Universiteit Delft
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 Technische Universiteit Delft filed Critical Technische Universiteit Delft
Priority to PCT/NL1992/000043 priority Critical patent/WO1993018341A1/fr
Priority to AU14499/92A priority patent/AU1449992A/en
Publication of WO1993018341A1 publication Critical patent/WO1993018341A1/fr

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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
    • F23C10/02—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
    • 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 
    • F23C6/00—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion
    • F23C6/04—Combustion apparatus characterised by the combination of two or more combustion chambers or combustion zones, e.g. for staged combustion in series connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire
    • 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 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/101—Combustion in two or more stages with controlled oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/501—Fluidised bed furnace with external recirculation of entrained bed material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/503—Fluidised bed furnace with two or more fluidised beds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/10—Nitrogen; Compounds thereof
    • F23J2215/101—Nitrous oxide (N2O)
    • 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 present invention concerns a method for combusting a carbonaceous material in a two-stage process, comprising the steps of: in a first stage, combusting or gasifying said carbonaceous material under substoichio etric oxygen conditions; in a second stage, combusting at least part of the products formed in said first stage under excess stoichiometric oxygen conditions; and introducing a sulphur- capture agent into said process-
  • a method is known in practice. Combustion takes place at a temperature of about 700-1200 °C, the pressure being substantially atmospheric or elevated.
  • Carbonaceous materials such as coal may be burnt by contacting with oxygen-containing gas or they may be gasified by contact with an oxidising agent such as steam, carbon dioxide, air, or a mixture thereof, for instance in a fluidised-bed combustor (FBC) .
  • FBC fluidised-bed combustor
  • this term is used for the sake of simplicity, and that the teachings of this invention extend to other carbonaceous materials, such as different types and grades of coal, oil shale, petroleum coke, peat, (municipal) solid waste, refuse-derived fuel, refinery and sewage plant sludges, liquid wastes and solid biomass material.
  • air is often used to denote any suitable oxidising gas.
  • a carbonaceous material contains nitrogen and sulphur, the combustion products of these elements providing environmental problems.
  • the nitrogen-containing products of combustion are mainly nitric oxide (NO) and nitrogen dioxide (NO 2 ) , often referred to as NOx, nitrous oxide (N 2 O) and molecular nitrogen (N 2 ).
  • staged combustion In staged combustion, two zones are set up in series and the amount of air needed to combust a certain amount of carbonaceous material is divided into two streams. The first zone operates under fuel-rich conditions, with only a fraction of the total amount of air injected.
  • N2O was not recognised as an environmental pollutant. Its role in global warming phenomena was unknown and emissions of N2O were not monitored. Recent studies, however, show unequivocally that substantial reduction in NOx emission from FBC, due to both relatively low combustion temperature (800 - 1000 * C) and staging, is accompanied by increased N 2 O levels. Combustion of fossil fuels is believed to be a major source of anthropogenic N 2 O and legislation limiting its emissions is expected to be passed in many ⁇ countries within a few years.
  • Sulphur-containing products of combustion or gasification are mainly sulphur dioxide (SO 2 ) , sulphur trioxide (SO 3 ) , hydrogen sulphide (H 2 S) and carbonyl sulphide (COS) . These gases are all considered pollutants and thus are environmentally unacceptable.
  • SO 2 sulphur dioxide
  • SO 3 sulphur trioxide
  • H 2 S hydrogen sulphide
  • COS carbonyl sulphide
  • a sulphur-capture.agent is mixed with the fuel in the first stage in order to form a solid sulphur-containing product to be subsequently removed.
  • sulphur-capture agent CaC ⁇ 3 is mixed with the fuel, usually in the form of limestone or dolomite.
  • limestone limestone
  • limestone limestone
  • (s) is used to indicate a solid and (g) is used to indicate a gas.
  • CaS ⁇ 4 calcium sulphate
  • CaS calcium sulphide
  • a drawback of this known method is that the removal and subsequent disposal of sorbent need to be done with care. Further, in this known method sulphur-capture is not efficient because of the reducing conditions that prevail in the first stage.
  • a further drawback of said known method is associated with the effect limestone has upon selectivity of fuel-bound nitrogen conversion to NO and N 2 O.
  • the volatiles comprise such nitrogen-containing species as N 2 , ammonia (NH 3 ) and hydrogen cyanide (HCN) .
  • N 2 nitrogen-containing species
  • NH 3 ammonia
  • HCN hydrogen cyanide
  • Each of the latter two species is known to be an NO and N 2 O gas-phase precursor, with NH 3 producing mainly NO and HCN producing mainly N 2 O.
  • limestone addition to an FBC results in an over-all decrease in N 2 O. emission, accompanied by an increase in NOx emission (see e.g.
  • said sulphur-capture agent is introduced' in the second stage.
  • the first advantage of the method according to the invention is related to the capture of sulphur.
  • calcium sulphide decomposes to form CaO and SO2, which subsequently react to yield calcium sulphate according to reaction (2) .
  • calcium sulphate is a neutral, environmentally acceptable solid by-product.
  • sulphur retention by limestone is iproved by its taking place under oxidising conditions.
  • a second advantage of the method according to the invention is related to the production of environmentally acceptable nitrogen-containing by-products.
  • CaO and CaS0 4 have a strong catalytic activity towards decomposition of N 2 O into N 2 and O 2 .
  • the effects of staging are improved: in the reducing atmosphere of the first stage, coal-bound nitrogen is, in the absence of limestone, converted primarily into N 2 O and 2 ; in the oxidising atmosphere of the second stage, N 2 O is decomposed into N 2 and O 2 under the catalytic action of CaO and CaSO- t , thus resulting in a "clean" nitrogen product.
  • a method and apparatus for combusting carbonaceous materials which have a high combustion efficiency, low emissions of NOx, N 2 O, SO 2 , SO 3 and hydrocarbons, and which yield calcium sulphate as a safe, stable and disposable solid by-product.
  • figure 1 schematically illustrates a first embodiment of a two-stage combustor according to this invention
  • figure 2 schematically illustrates a second embodiment of a two-stage combustor according to this invention.
  • a two-stage fluidised-bed combustor 1 comprises a first-stage bubbling fluidised bed 2 and a second- stage circulating fluidised bed 3.
  • the first stage 2 operates under fuel-rich, substoichiometric conditions and is fluidised by a stream of gas introduced to the system through the gas inlet 5.
  • This gas will be subsequently referred to as primary air, although, in principle, any suitable gaseous oxidising agent can be used.
  • Another stream of oxidising gas is introduced through a second gas inlet 6 into the second stage 3 of the combustor 1, and this stream will be referred to as secondary air.
  • the second stage 3 operates under excess oxygen conditions to facilitate complete combustion.
  • Oxygen supplied with the primary air usually constitutes about 40 - 70 % of the total amount used in the combustor 1, but this value may be different depending on a particular application.
  • the temperature of the first-stage combustion may be between 700 and 1200 * C, a value typical for an atmospheric fluidised-bed combustor (AFBC) .
  • AFBC atmospheric fluidised-bed combustor
  • the temperature in the second stage is similar, or even somewhat higher, due to the high oxygen concentration in this part of the system and due to highly turbulent combustion.
  • the process of the present invention is suitable for both atmospheric and high-pressure applications, depending on particular application, type of carbonaceous material used, etc.
  • Any carbonaceous materials that are appropriate for fluidised-bed combustion can be used in the process of this invention, such as different types and grades of coal, oil shale, petroleum coke, peat, (municipal) solid waste, refuse- derived fuel, refinery and sewage plant sludges, liquid wastes and solid biomass material.
  • Coal is a preferred fuel and will be referred to in the detailed description of the preferred embodiment, without limiting the process of the present invention with respect to carbonaceous feed material.
  • Coal is fed into the combustor 1 through a coal inlet port 4, and any suitable coal feeding device (not shown for the sake of simplicity) can be used to this end.
  • Coal is usually crushed to a particle size below 5 mm and, in general, no other coal pretreatment is required.
  • the amount of oxygen introduced into the first stage 2 constitutes only a fraction of the total oxygen needed for complete combustion, preferably 40 - 70 %, as mentioned before.
  • most coal-bound nitrogen is converted to molecular nitrogen (N 2 ) and nitrous oxide (N 2 O) , the production of NOx thus being minimised.
  • the sulphur-containing combustion products at this stage are mainly SO 2 , H 2 S and COS, in proportions depending on particular operating conditions.
  • the whole inventory of all these species is subsequently transferred to the second stage 3.
  • Small particles of coal are also .entrained in the stream of gas leaving the first stage 2, and they undergo further combustion in the oxidising atmosphere of the second stage 3.
  • particles of a sulphur- capture agent preferably limestone or dolomite, are introduced, preferably having a particle size in the submillimeter range. These particles may be introduced separately, but preferably they are introduced together with the secondary air, as illustrated in fig.1.
  • the limestone particles are stored in a bunker 7. The limestone particles are dispersed in the stream of secondary air 6 and the resulting mixture enters the second combustion stage 3.
  • the second combustion stage 3 may operate either as a typical circulating fluidised-bed combustor (CFBC) , with limestone and secondary air introduced together or separately, or as a cyclonic CFBC, with limestone and secondary air introduced together through at least one, but preferably through a plurality of tangentially disposed inlet ports, as illustrated schematically in fig. 1, in quantities sufficient to generate a highly turbulent swirl.
  • CFBC circulating fluidised-bed combustor
  • High heat- and mass-transfer coefficients can be achieved in this zone, which facilitates heat recovery, efficient combustion, sulphur capture as well as solid-catalysed NOx and N 2 O reduction to N 2 .
  • Sulphur removal takes place essentially only in the second stage, i.e. under oxidising conditions, which makes it possible to obviate difficulties associated with sulphur capture in a reducing environment.
  • the limestone is ground preferably to submillimeter particle size to improve sulphur removal efficiency.
  • the molar calcium-to-sulphur ratio typically used in FBC varies between 1 and 5. In combustors built according to the present invention, relatively low values of this ratio are possible (e.g. 1.5 - 2.5) due to small limestone particle size and high turbulence in the CFBC.
  • flue gas is directed to a stack, as indicated at 10, whereas solids are recycled to the bottom of the second combustion stage 2, as indicated at 9.
  • Fly ash and spent sorbent are removed from the system using any suitable method, which may be a known per se method, as indicated at 11. Similarly, a conventional method may be used to withdraw ash 12 from the bubbling fluidised bed.
  • the gas velocity in the second combustion stage 3 is ⁇ preferably substantially higher than in the bottom part of the combustor 1, in order to prevent transfer of solids (such as sand or other inert material particles that constitute a circulating fluidised bed of the second zone, or the particles of a sulphur-capture agent introduced with the secondary air) from the second stage 3 to the first stage 2.
  • solids such as sand or other inert material particles that constitute a circulating fluidised bed of the second zone, or the particles of a sulphur-capture agent introduced with the secondary air
  • a relatively narrow passageway between said first reaction chamber 2 and said second reaction chamber 3 is provided.
  • a grid 14, preferably a perforated plate may be provided between said first reaction chamber 2 and said second reaction chamber 3.
  • the apparatus and method of the invention can be used for coal gasification by steam, carbon dioxide, air, mixture thereof, or by any other suitable gasifying agent, realised in the first, i_e. bubbling, fluidised bed, followed by combustion of the generated gases and char in the second stage operating as a CFBC as described before.
  • gasification can be considered an extreme case of oxygen- starved combustion, and that any conventional gasifying agent, • such as steam or carbon dioxide, can be employed.
  • said fine particles of limestone or dolomite may be introduced via a separate entrance port.
  • Another modification may involve the use of other catalysts or sorbents, in addition to or instead of a sulphur-capture agent.
  • the role of such additives may be, for instance, enhancement of NOx and 2O reduction to molecular nitrogen.
  • the active agent for sulphur-capture as described is CaO.
  • any precursor of CaO such as Ca(OH)2 or CaC03, the latter being preferred because it is relative cheap and easily and abundantly obtainable.
  • FIG. 2 Another preferred embodiment 20 of the invention is presented in fig. 2.
  • This combustor 20 differs from the above- described combustor 1 in the relative position of the first and second combustion stages 2 and 3. As shown in fig. 2, the stages 2, 3 are separated by a weir 21, over which material processed in stage 2 is transferred to the oxygen-rich stage 3.
  • this configuration requires an additional ash disposal conduit 12a, as well as an additional fluidising gas inlet 5a, this configuration has an advantage over the embodiment shown in fig. 1 in the relative ease with which clearance between both stages 2 and 3 can be controlled by changing the height of weir 21.
  • the gas inlet 5a can be considered as a secondary air inlet, with the gas inlet 6 being considered as optional.
  • the element of swirl in the circulated fluidised bed is an optional feature of the system.
  • the degree of entrainment of coal particles into the upper, circulating fluidised-bed region can be controlled by varying the coal feed rate into the reactor and/or the inlet flow rate of the gas.
  • first combustion stage 2 is described as being a bubbling stage and the second combustion stage 3 is described as being a circulating stage
  • other combinations of combustion types are also possible, such as bubbling-bubbling, circulating-circulating, or circulating- bubbling.
  • Moving beds are also conceivable.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)

Abstract

L'invention concerne un procédé et un appareil de combustion de matériaux carbonés selon un processus à deux étages. Dans une première chambre de réaction (2) fonctionnant dans des conditions riches en combustible sous un régime de fluidisation bouillonnante, le combustible subit une combustion primaire ou gazéification. Un gaz oxydant (5) est envoyé dans la première chambre de réaction à une vitesse suffisante pour maintenir la fluidisation. Les produits de combustion quittent la première chambre de réaction et rentrent dans une seconde chambre de réaction (3), fonctionnant dans des conditions riches en oxygène comme un brûleur à lit fluidisé circulant. Un second courant de gaz oxydant (6) est envoyé dans la seconde chambre, de préférence tangentiellement de manière à générer un tourbillonnement turbulent. Des particules d'un agent de capture de soufre, de préférence le calcaire, sont envoyées dans la seconde chambre, de préférence avec le second courant de gaz. Dans un deuxième étage, le charbon et les gaz combustibles générés dans le premier étage, sont brûlés. Le soufre lié avec le combustible est retiré et converti avantageusement en sulfate de calcium, pendant que l'azote lié avec le combustible est converti avantageusement en azote gazeux.
PCT/NL1992/000043 1992-03-05 1992-03-05 Procede et appareil de combustion d'un materiau carbone WO1993018341A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/NL1992/000043 WO1993018341A1 (fr) 1992-03-05 1992-03-05 Procede et appareil de combustion d'un materiau carbone
AU14499/92A AU1449992A (en) 1992-03-05 1992-03-05 Method and apparatus for combusting a carbonaceous material

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/NL1992/000043 WO1993018341A1 (fr) 1992-03-05 1992-03-05 Procede et appareil de combustion d'un materiau carbone

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Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL9301828A (nl) * 1993-10-21 1995-05-16 Univ Delft Tech Werkwijze en inrichting voor het verbranden van vaste brandstof.
WO1996021824A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede de traitement thermique de dechets
EP0685688A3 (fr) * 1994-05-30 1997-02-05 Ishikawajima Harima Heavy Ind Procédé et appareil de combustion.
EP0851173A3 (fr) * 1996-12-30 1999-07-28 Combustion Engineering, Inc. Procédé de contrÔle d'oxyde nitrique dans un générateur de vapeur à lit fluidisé circulant
WO2008095984A2 (fr) * 2007-02-07 2008-08-14 Technische Universität Bergakademie Freiberg Procédé et dispositif de combustion de combustibles solides
WO2008112345A1 (fr) * 2007-03-13 2008-09-18 Alstom Technology Ltd Appareil secondaire de sollicitation de flux d'air et procédé pour faire circuler des systèmes de chaudière à lit fluidifié
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
US8580152B2 (en) 2010-04-13 2013-11-12 Ineos Usa Llc Methods for gasification of carbonaceous materials
US8585789B2 (en) 2010-04-13 2013-11-19 Ineos Usa Llc Methods for gasification of carbonaceous materials
US8999021B2 (en) 2010-04-13 2015-04-07 Ineos Usa Llc Methods for gasification of carbonaceous materials
CN105698163A (zh) * 2016-01-27 2016-06-22 华北电力大学 一种固体燃料循环流化床富氧燃烧装置及方法
CN105861104A (zh) * 2015-01-21 2016-08-17 宋文奇 通过形成复合型钠化合物解决高钠煤燃烧时沾污的方法

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WO1981001873A1 (fr) * 1979-12-26 1981-07-09 Battelle Development Corp Reduction de nox dans des chambres de combustion a lits fluidises multi solides
EP0082673A2 (fr) * 1981-12-17 1983-06-29 YORK-SHIPLEY, Inc. Réacteur à lit fluidifié à action rapide et procédé de l'opération dudit réacteur
GB2159432A (en) * 1984-06-01 1985-12-04 Ahlstroem Oy Fluidised combustion of fuel
WO1987001790A1 (fr) * 1985-09-20 1987-03-26 Oy Tampella Ab Procede pour diminuer les emissions d'oxydes d'azote et d'oxydes de soufre lors du brulage de combustibles contenant de l'azote et du soufre
EP0247798A2 (fr) * 1986-05-29 1987-12-02 Donlee Technologies Inc. Réacteur à lit fluidisé et procédé d'opération d'un tel réacteur
EP0308300A1 (fr) * 1987-09-14 1989-03-22 Babcock-Entreprise Procédé de combustion en lit fluidisé et installation pour la mise en oeuvre de ce procédé

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1981001873A1 (fr) * 1979-12-26 1981-07-09 Battelle Development Corp Reduction de nox dans des chambres de combustion a lits fluidises multi solides
EP0082673A2 (fr) * 1981-12-17 1983-06-29 YORK-SHIPLEY, Inc. Réacteur à lit fluidifié à action rapide et procédé de l'opération dudit réacteur
GB2159432A (en) * 1984-06-01 1985-12-04 Ahlstroem Oy Fluidised combustion of fuel
WO1987001790A1 (fr) * 1985-09-20 1987-03-26 Oy Tampella Ab Procede pour diminuer les emissions d'oxydes d'azote et d'oxydes de soufre lors du brulage de combustibles contenant de l'azote et du soufre
EP0247798A2 (fr) * 1986-05-29 1987-12-02 Donlee Technologies Inc. Réacteur à lit fluidisé et procédé d'opération d'un tel réacteur
EP0308300A1 (fr) * 1987-09-14 1989-03-22 Babcock-Entreprise Procédé de combustion en lit fluidisé et installation pour la mise en oeuvre de ce procédé

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PATENT ABSTRACTS OF JAPAN vol. 3, no. 29 (M-51)10 March 1979 *

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
NL9301828A (nl) * 1993-10-21 1995-05-16 Univ Delft Tech Werkwijze en inrichting voor het verbranden van vaste brandstof.
EP0685688A3 (fr) * 1994-05-30 1997-02-05 Ishikawajima Harima Heavy Ind Procédé et appareil de combustion.
US5662049A (en) * 1994-05-30 1997-09-02 Ishikawajima-Harima Jukogyo Kabushiki Kaisha Combustion method and apparatus
WO1996021824A1 (fr) * 1995-01-10 1996-07-18 Von Roll Umwelttechnik Ag Procede de traitement thermique de dechets
CH690790A5 (de) * 1995-01-10 2001-01-15 Von Roll Umwelttechnik Ag Verfahren zur thermischen Behandlung von Abfallmaterial.
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