EP2340395A1 - Système de combustion oxygaz pratiquement dépourvu ou dépourvu d'oxygène excédentaire - Google Patents

Système de combustion oxygaz pratiquement dépourvu ou dépourvu d'oxygène excédentaire

Info

Publication number
EP2340395A1
EP2340395A1 EP09792976A EP09792976A EP2340395A1 EP 2340395 A1 EP2340395 A1 EP 2340395A1 EP 09792976 A EP09792976 A EP 09792976A EP 09792976 A EP09792976 A EP 09792976A EP 2340395 A1 EP2340395 A1 EP 2340395A1
Authority
EP
European Patent Office
Prior art keywords
reactor
oxygen
secondary reactor
stoichiometric ratio
combustion
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Withdrawn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
EP09792976A
Other languages
German (de)
English (en)
Inventor
Mark Daniel D'agostini
Jeffrey William Kloosterman
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.)
Air Products and Chemicals Inc
Original Assignee
Air Products and Chemicals Inc
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 Air Products and Chemicals Inc filed Critical Air Products and Chemicals Inc
Publication of EP2340395A1 publication Critical patent/EP2340395A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • 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
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/50—Control or safety arrangements
    • 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
    • F23G2207/00—Control
    • F23G2207/10—Arrangement of sensing devices
    • F23G2207/103—Arrangement of sensing devices for oxygen
    • 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 disclosure is directed to an oxy/fuel combustion system and method.
  • the present disclosure is directed to an oxygen- enriched solid fuel combustion system and method.
  • This disclosure provides a device and method for burning solid fuel, such as coal, with oxygen and recycled flue gas in a multi-stage combustion process.
  • a combustion system includes a primary reactor arranged and disposed to receive a solid fuel and a first oxygen stream and deliver a first substantially gaseous product and a substantially solid or molten product, a secondary reactor in fluid communication with the primary reactor, and a furnace in fluid communication with the secondary reactor.
  • the secondary reactor is disposed to receive a second oxygen stream thereby converting the first substantially gaseous product from being oxygen deficient upon entering the secondary reactor to oxygen rich upon exiting the secondary reactor.
  • a method of operating a combustion system includes providing a primary reactor arranged and disposed to receive a solid fuel and a first oxygen stream and deliver a first substantially gaseous product and a substantially solid or molten product, providing a secondary reactor in fluid communication with the primary reactor, providing a furnace in fluid communication with the secondary reactor, and determining a stoichiometric ratio selected from the group consisting of the stoichiometric ratio of the primary reactor, the stoichiometric ratio of the secondary reactor, the stoichiometric ratio of the furnace, and combinations thereof.
  • the secondary reactor is disposed to receive a second oxygen - A -
  • An advantage of the present disclosure is the ability to achieve substantially complete combustion of coal with a reduced amount of O 2 .
  • Another advantage of the present disclosure is the ability to produce a product gas with high CO 2 purity.
  • Yet another advantage of the present disclosure is the ability to remove fly ash and other contaminants resulting in reduced fouling.
  • FIG. 1 illustrates a graphic representation of the effect of the stoichiometric ratio on flue gas CO 2 in oxygen-enriched coal combustion.
  • FIG. 2 illustrates a diagrammatic representation of an exemplary embodiment of a combustion system according to the disclosure.
  • FIG. 3 illustrates a diagrammatic representation of a portion of a combustion system according to an embodiment of the disclosure.
  • FIG. 4 illustrates a diagrammatic representation of a portion of a combustion system according to another embodiment of the disclosure.
  • FIG. 5 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 6 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 7 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 8 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 9 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 10 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 11 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 12 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 13 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 14 illustrates a diagrammatic representation of a portion of a combustion system according to still another embodiment of the disclosure.
  • FIG. 15 illustrates a diagrammatic representation of an alternate exemplary embodiment of a combustion system according to the disclosure.
  • FIG. 16 illustrates a diagrammatic representation of an alternate exemplary embodiment of a combustion system according to the disclosure.
  • solid fuel and grammatical variations thereof refers to any solid fuel suitable for combustion purposes.
  • the disclosure may be used with many types of carbon-containing solid fuels, including but not limited to: anthracite, bituminous, sub-bituminous, and lignite coals; tar; bitumen; petroleum coke; paper mill sludge solids and sewage sludge solids; wood; peat; grass; and combinations and mixtures of all of those fuels.
  • oxygen and grammatical variations thereof refers to an oxidizer having an O 2 concentration greater than that of atmospheric or ambient conditions.
  • combustion fluid and grammatical variations thereof refers to a fluid formed from and/or mixed with the products of combustion, which may be utilized for convective heat transfer. The term is not limited to the products of combustion and may include fluids mixed with or otherwise traveling through at least a portion of combustion system.
  • flue gas Although not so limited, one such example is flue gas.
  • cycled flue gas and grammatical variations thereof refers to combustion fluid exiting the system that is recirculated to any portion of the system.
  • flue gas recycle and grammatical variations thereof refers to a configuration permitting the combustion fluid to be recirculated.
  • Figure 1 illustrates a graphic representation of the effect of the stoichiometric ratio on flue gas CO 2 during the combustion of coal with oxygen; hereinafter referred to as oxygen fired coal or oxygen fired fuel combustion.
  • oxygen fired coal or oxygen fired fuel combustion In the context of air fired fuel combustion, operation with a relatively high stoichiometric ratio results in relatively high stack sensible enthalpy losses and fan power requirements, the latter being typically only a fraction of a percent of gross power generation of the steam turbine.
  • the penalty of relatively high stoichiometric ratio operation during oxygen fired fuel combustion is much greater. This is principally due to higher power requirements for compression within the Air Separation Unit (ASU), as well as the need for higher capacity ASU equipment, leading to higher capital costs.
  • ASU compressor power is typically several percent of gross generation, rather than the fraction of a percent for fan power in air fired fuel systems.
  • Emissions of CO and unbumed carbon are known to increase substantially as the stoichiometric ratio is lowered beneath about 1.2, leading to poor thermal efficiency, a higher propensity for fouling, potentially hazardous conditions within the plant and a higher collection burden on downstream particulate control equipment.
  • Known systems do not provide means for generating electric power in oxygen fired coal boilers with simultaneously low stoichiometric ratio and high thermal efficiency.
  • Figure 1 illustrates the variation of CO 2 purity and balance of inert gases, principally O 2 , SO 2 and N 2 formed from fuel nitrogen, with stoichiometric ratio for oxygen fired fuel combustion of a typical low sulfur ( ⁇ 1 wt %) coal.
  • lowering the stoichiometric ratio from about 1.2 to about 1.05 reduces the concentration of inerts from about 18% to about 6% and increases the CO 2 concentration from about 81.5% to about 94%. Note that all concentrations are presented on a dry basis.
  • Methods of combustion according to the present disclosure provide low excess oxygen and serve as a method for reducing the size of, or potentially eliminating, CO 2 purification equipment.
  • both the size/extent of purification equipment and the respective operating costs may be lower due to the smaller volume of gases to be removed.
  • the reduction or removal of this equipment may lead to significant savings, particularly in relation to flue gas compression required for efficient CO 2 transport, for example to an external pipeline, where pressures of 1000 psia or greater, depending upon end use, may be required.
  • the combustion system operates at stoichiometric ratios of about 1.05 or less.
  • Known coal combustion systems typically operate at a stoichiometric ratio of about 1.2 or greater.
  • Operation of a solid fuel combustion system of a stoichiometric ratio of less than about 1.05 results in additional features being desired for efficient combustion system operation. For example, it is desirable to provide additional residence time between the solid fuel and oxidizer to facilitate complete evolution of fuel carbon into a gaseous phase. It is also desirable to provide oxygen instead of air as an oxidizer in order to attain sufficiently high temperature within the primary reactor to melt ash constituent of the solid fuel, and to increase the combustion reaction rates throughout the system.
  • FIG. 2 illustrates a diagrammatic representation of an exemplary embodiment of a combustion system according to the disclosure. Specifically, Figure 2 illustrates an embodiment of an oxygen fired coal combustion system 202 required to facilitate efficient, low-excess O 2 operation.
  • oxygen fired coal combustion system 202 includes a primary reactor 204, a secondary reactor 206, and a furnace 208 (which includes, but is not limited to a combustion chamber).
  • Primary reactor 204 is in fluid communication with secondary reactor 206.
  • Secondary reactor 206 is in fluid communication with primary reactor 204 and furnace 208.
  • Furnace 208 is in fluid communication with secondary reactor 206.
  • primary reactor 204 may be a slagging combustor/gasifier such as, for example, a slagging cyclone.
  • the type of reactor is selected to provide the ability to achieve relatively long solid particle residence times and withstand high gas temperatures, thus promoting efficient gasification and/or combustion of the feed coal with little or no carbon residue.
  • Residual solid material 212 which includes ash, may be removed as a viscous slag and delivered into the boiler where it is captured in the bottom of furnace 208, thus minimizing the concentration of particulate in flue gas.
  • Residual solid material 203 may be integral, as illustrated in the embodiment of Figure 2. Alternatively, slag collection may be separate from furnace 208 as illustrated in the embodiment of Figure 16.
  • primary reactor 204 may be a slagging cyclone which is operated with less than the stoichiometric amount of oxygen required for complete combustion of the fuel. That is, the stoichiometric ratio of the fuel and oxidant introduced into the primary reactor is less than 1.0. More preferably it is less than 0.95, and still more preferably it is the range of 0.3 to 0.95, wherein the lower limit is sufficiently high to ensure that the slag can be maintained in a molten state and the higher limit is dictated by the preference, for control purposes, to maintain at least a minimal amount of oxygen that must be added outside the primary reactor to complete the low excess oxygen combustion process.
  • Suitable arrangements of slagging combustor/gasifiers include, for example, the arrangement disclosed in US Patent No. 5,291 ,841 , and US Patent No. 5,052,312, which are both incorporated herein by reference in their entirety, while not intending to be limiting.
  • primary reactor 204 is arranged and disposed to receive fuel 210 and oxygen 205.
  • Fuel 210 may be crushed or pulverized fuel in a proportion dictated by the need to attain a specific temperature for primary reactor 204.
  • the fuel may also be conveyed by a small amount of a transport fluid.
  • the transport fluid may be air, CO 2 , N 2 , liquid or gaseous H 2 O, recycled flue gas, or combinations thereof.
  • the desired temperature of primary reactor 204 may be determined based upon the slag melting temperature, and monitored using commercially available instrumentation for temperature measurement. These temperatures permit conversion of essentially all of a solid carbon fuel into a gaseous phase.
  • Primary reactor 204 is arranged and disposed to permit a residual solid material 212 to be expelled from it (i.e. slag). Generally, residual solid material 212 is in a molten state and is essentially free of residual carbon. Primary reactor 204 is arranged and disposed to permit a partially combusted gaseous product 216 to be expelled from it into secondary reactor 206. In one embodiment, residual solid material 212 is expelled separate from partially combusted gaseous product 216 expelled from primary reactor 204.
  • oxygen fired coal combustion system 202 includes a recirculator 218 arranged and disposed to permit a recycled flue gas 214 to be transported from a recirculator 218 to primary reactor 204.
  • recycled flue gas 214 is injected into primary reactor 204 with a stream of primary oxygen 207 and crushed or pulverized fuel in a proportion dictated by the preference to maintain a predetermined temperature in primary reactor 204 in excess of residential solid material 212 temperature and convert essentially all of the solid carbon into a gaseous phase.
  • Other process constraints such as moderation of boiler radiant heat flux and final steam temperatures may also contribute to the selection of primary reactor 204 operating conditions.
  • embodiments of the present disclosure also include streams of tertiary oxygen 225 and quaternary oxygen 227.
  • embodiments include additional streams of recycled flue gas 215, 219.
  • secondary reactor 206 may be arranged and disposed to receive recycled flue gas 214 from recirculator 218 thereby adding it to partially combusted gaseous product 216.
  • secondary reactor 206 includes an inner stream comprised of partially combusted gaseous product 216 expelled from primary reactor 204. Partially combusted gaseous product 216 may also include trace amounts of fully or partially combusted particulates.
  • secondary reactor 206 may further include at least one stream of secondary oxygen 224 (see also Figure 2) bounding partially combusted gaseous product 216 as it enters secondary reactor 206.
  • Reactants introduced into secondary reactor 206 in this manner afford several advantages. Primarily, the configuration of secondary reactor 206 allows for control of the extent of reaction and the momentum of the reacting gases. This control or operation is exerted principally through the relative amounts of fuel and oxygen present within secondary reactor 206, the manner in which reactants are introduced into secondary reactor 206, and the size of secondary reactor 206.
  • the manner of mixing illustrated in Figure 3 has two principal advantages. First, arranging the stream of secondary oxygen 224 around partially combusted gaseous product 216 entering from primary reactor 204 creates a layer of relatively cool gas adjacent to secondary reactor 206 wall to cool and protect the wall from high temperature damage.
  • the potential for high temperature damage is much greater for oxygen fired fuel combustion relative to air fired fuel combustion since the flame temperature attained using oxygen can be as much as 1500° F higher than the temperature attained with air, and the reaction rates can be increased by a factor of 10 or more relative to combustion with air.
  • transverse mixing can largely be eliminating. That is, the initial mixing between oxidizer (e.g. oxidizer) and reactant occurs can be confined to a shear layer between the two fluids.
  • oxidizer e.g. oxidizer
  • secondary reactor 206 may include recycled flue gas 214 provided or injected to bound or otherwise surround the stream of secondary oxygen 224.
  • recycled flue gas 214 provided or injected to bound or otherwise surround the stream of secondary oxygen 224.
  • the advantage of this is that it provides an additional buffer to protect against high temperature gases and/or particulate coming into contact with the walls of secondary reactor 206 while permitting intimate contact between the oxygen and products from primary reactor 204.
  • it permits more aggressive reactant mixing within secondary reactor 206 without increasing the risk of high temperature damage.
  • the use of recycled flue gas 214 in secondary reactor 206 may be mixed with stream of secondary oxygen 224 by means of a swirler generator 502.
  • other techniques known in the art for enhancing mixing stream of secondary oxygen 224 and partially combusted gaseous product 216 may be included.
  • Mixing the stream of secondary oxygen 224 and partially combusted gaseous product 216 provides control for adjusting the momentum of the gases discharged from secondary reactor 206 into the furnace 208. That is, adding more of the recycled flue gas 214 increases the momentum of partially combusted gaseous product 216, while reducing the amount of recycled flue gas 214 reduces the momentum.
  • secondary reactor 206 may include at least one oxygen injector 223 providing the stream of tertiary oxygen 225 (see also Figure 1 ) immediately adjacent to the area bounding a secondary reactor expellant 222 being transported from secondary reactor 206 to furnace 208 (not shown in Figure 6).
  • the stream of tertiary oxygen 225 illustrated in Figure 6 enables increased control over the properties of the reacting mixture exiting secondary reactor 206, which can afford certain performance advantages. For example, it may in certain circumstances be advantageous to operate the system with a stoichiometric ratio less than 1.0 at the exit of secondary reactor 206 instead of adding tertiary oxygen to complete the combustion process.
  • Operation in this manner should extend the reaction zone (or flame) farther into furnace 208, thereby lowering the peak temperature and creating a more evenly distributed heat release pattern. Delaying of the completion of combustion also extends the life of transient, but highly radiative species, in the flame. This enhancement of the radiant species of the flame will further assist in lowering the peak flame temperature and in improving the efficiency of heat transfer from the flame to the surroundings.
  • tertiary oxygen 225 is also advantageous in that it can be introduced into secondary reactor expellant 222 in such a way as to promote rapid mixing without the constraint of overheating the secondary reactor walls.
  • tertiary oxygen 225 can be introduced through a plurality of swirl vanes 702 as illustrated in Figure 7, or through a plurality of converging nozzles 802 as illustrated in Figure 8.
  • tertiary oxygen 225 can be introduced through a plurality of swirl vanes 702 as illustrated in Figure 7, or through a plurality of converging nozzles 802 as illustrated in Figure 8.
  • Figure 9 illustrates an embodiment wherein stream of quaternary oxygen 227 is premixed with recycled flue gas 214 prior to introduction into secondary reactor 206 (see also Figure 3).
  • the embodiment in Figure 10 does not include quaternary oxygen 227, but relies solely on oxygen in recycled flue gas 215 as the oxidizing agent. Since coal combustion system 202 is operated with some excess oxygen, recycled flue gas 214 typically includes oxygen.
  • Secondary reactor 206 may include one or more local combustion instruments 220 arranged and disposed to provide information (including, but not limited to, feedback signals to the fuel control system, the oxygen control system and/or the recycled flue gas control system) regarding conditions within secondary reactor 206.
  • local combustion instruments 220 generally are disposed on or within each of secondary reactors 206 in the system.
  • Local combustion instrument 220 may be selected from the group of instruments consisting of a flame scanner, a thermocouple, a non-intrusive instrument such as a tunable diode laser, an optical or acoustic sensor, and other instruments. Local combustion instrument 220 may provide information including, but not limited to, fluid temperature, fluid composition, and/or temperature of portions of furnace 208. Local combustion instruments 220 may be located at any point within secondary reactor 206 or furnace 208 permitting local combustion instrument 220 to measure properties of secondary reactor expellant 222 discharged from secondary reactor 206 to furnace 208. Information from local combustion instrument 220 may subsequently deliver a control signal based upon the measurement by local combustion instrument 220.
  • the control signal may result, for example, in adjustment of the individual flow rate of secondary oxygen 224 or tertiary oxygen 225 to the radiant to secondary reactor 206.
  • local combustion instrument 220 may include a transmitter 223 and/or a receiver 233.
  • local combustion instrument 220 may include a thermocouple 235.
  • an additional "global" combustion instrument 902 is included to sample the mixed products of combustion, in particular the concentrations of excess oxygen and carbon monoxide (CO), from all of secondary reactors 206.
  • the control system is configured to take both the local and global measurements as input. Signals from global measurement instrument 902 are used by a controller 905 to determine whether or not more or less total oxygen is required, while signals from local combustion instruments 220 are used to determine the balance of combustion conditions among all parallel reactors. If, for example, controller 905 indicates that more oxygen is needed to improve combustion efficiency (i.e.
  • Another mode of operation of the embodiment illustrated in Figure 15 includes the use of stream of quaternary oxygen 227 (see also Figure 2) and/or recycled flue gas 219 in a region of furnace 208 downstream of secondary reactors 206. This would be desirable for operating with a stoichiometric ratio below 1.0, as may be necessary after addition of tertiary oxygen 225. Such an operating mode should be advantageous, for example, to reduce emissions of NO x .
  • the use of the recycled flue gas in this area has a two-fold advantage. First, it may help to promote mixing of gases.
  • the embodiment of coal combustion system 202 includes heat exchangers in convective pass section 912.
  • the heat exchangers may include a secondary superheater 914, a reheat superheater 916, and a primary superheater 918.
  • an economizer is also included.
  • additional heat exchangers may be included.
  • primary reactor 204 delivers a partially oxidized gas stream to a plurality of secondary reactors 206 configured as described above. It will be appreciated by those of ordinary skill in the art that an advantage of this embodiment is the reduction in solid fuel handling, metering and transport equipment needed compared to a system wherein multiple primary reactors are employed. A further advantage is simplification of the balancing of secondary reactors 206. This is because a principal cause of secondary reactor 206 imbalance in a system employing a plurality of primary reactors 204 is the relative imbalance of fuel and oxygen flows to each of primary reactors 204. The simplification of secondary reactor 206 balancing operation should lead to improved system reliability and the ability to achieve complete combustion at even lower excess oxygen level than attainable in coal combustion system 202 including a plurality of primary reactors 204.

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

Abstract

L'invention concerne un système de combustion qui comprend un réacteur primaire conçu et disposé pour recevoir un combustible solide et un premier flux d'oxygène et fournir ensuite un premier produit sensiblement gazeux ainsi qu'un produit sensiblement solide ou fondu, qui comprend également un réacteur secondaire en communication fluidique avec le réacteur primaire, et qui comprend enfin un fourneau en communication fluidique avec le réacteur secondaire.
EP09792976A 2008-09-26 2009-09-25 Système de combustion oxygaz pratiquement dépourvu ou dépourvu d'oxygène excédentaire Withdrawn EP2340395A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US12/238,612 US20100077942A1 (en) 2008-09-26 2008-09-26 Oxy/fuel combustion system with little or no excess oxygen
PCT/US2009/058286 WO2010036840A1 (fr) 2008-09-26 2009-09-25 Système de combustion oxygaz pratiquement dépourvu ou dépourvu d'oxygène excédentaire

Publications (1)

Publication Number Publication Date
EP2340395A1 true EP2340395A1 (fr) 2011-07-06

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EP09792976A Withdrawn EP2340395A1 (fr) 2008-09-26 2009-09-25 Système de combustion oxygaz pratiquement dépourvu ou dépourvu d'oxygène excédentaire

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Country Link
US (1) US20100077942A1 (fr)
EP (1) EP2340395A1 (fr)
CN (1) CN102165259A (fr)
CA (1) CA2733243C (fr)
WO (1) WO2010036840A1 (fr)

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US20100077942A1 (en) 2010-04-01
WO2010036840A1 (fr) 2010-04-01

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