CN204678329U - Recirculating fluidized bed oxygen-enriched burning device - Google Patents
Recirculating fluidized bed oxygen-enriched burning device Download PDFInfo
- Publication number
- CN204678329U CN204678329U CN201520291103.8U CN201520291103U CN204678329U CN 204678329 U CN204678329 U CN 204678329U CN 201520291103 U CN201520291103 U CN 201520291103U CN 204678329 U CN204678329 U CN 204678329U
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- China
- Prior art keywords
- air
- oxygen
- flue gas
- gas
- fluidized bed
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- 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
- F23C9/00—Combustion apparatus characterised by arrangements for returning combustion products or flue gases to the combustion chamber
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- 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
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- 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
- F23C10/18—Details; Accessories
- F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
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- 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
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- 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
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- 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
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The utility model discloses recirculating fluidized bed oxygen-enriched burning device, economizer bottom is connected with middle temperature cyclone separator, middle temperature cyclone separator is connected with air compartment with First air oxygen injector by a gas recirculating fan successively, and middle temperature cyclone separator bottom is connected with air-distribution device with Secondary Air oxygen injector by secondary flue gas recirculation blower successively, economizer bottom is connected with air-introduced machine by smoke-gas preheater, deduster successively, and air-introduced machine is away from smoke-gas preheater one end and CO
2compression purification devices is connected.In employing, warm flue gas is as First air and Secondary Air, enters burner hearth respectively as reduced air, and notes oxygen respectively to First air and Secondary Air, realizes the adjustment of note oxygen amount, simultaneously for hearth combustion provides oxidant, can make the CO that CFBB is discharged
2concentration enrichment, to more than 80%, to be beneficial to after coal combustion CO in flue gas
2trapping.
Description
Technical field
The utility model relates to a kind of recirculating fluidized bed flue gas recirculation oxygen-enriched burning device, belongs to the technical field of boiler manfacturing and energy-saving environment protection engineering, specifically, refers to a kind of recirculating fluidized bed oxygen-enriched burning device.
Background technology
Carbon dioxide is generally considered one of major reason causing global warming because having greenhouse effects, the utilization of fossil energy is most important CO2 source in air, if Global Emissions of Greenhouse Gas amount is pressed industry statistic, power industry is maximum emission source.And coal fired power generation is the main source of CO2 discharge in power industry, global power industry coal fired power generation accounts for 40%.There is a large amount of fossil fired power plants in the whole world in operation, and this just needs to find a kind of CO2 for fossil fuel power to reduce discharging solution.Therefore, international community has carried out broad co-operation to Against Global Climate Changes on United Nations Framework Convention on Climate Change basis.Contracting party sets in the Kyoto Protocol of signing in 1997 target that major industrialized country reduces greenhouse gas emission.Reduce CO2 discharge and from then on become the target that global reply climate change is made joint efforts.
Oxygen-enriched combusting is in existing station boiler system-based, oxygen-enriched combustion system replaces air as the oxide isolation of combustion of fossil fuel with pure oxygen or oxygen enrichment, combustion product is CO2 and steam mainly, also have unnecessary oxygen in addition to ensure that burning is complete, and in fuel, the oxidation product of repertoire, fuel or leakage enter the inert fraction etc. in the air of system.After supercooled water steam-condensation, in flue gas, CO2 content is between 80% ~ 98%.The CO2 of such high concentration is through overcompression, drying and carry out utilizing or storing after further purifying; thus to realize forever sealing up for safekeeping or recycling of CO2 after less cost condensation compression; comparatively easily realize large-scale CO2 enrichment and reduction of discharging; and because this new combustion mode and existing power station combustion system have good connection in technology, also easily accepted by power industry.
There is CO in existing oxygen-enriched burning device
2the problems such as a large amount of discharges, cause CO
2the problem that capture rate is low, meanwhile, after a large amount of flue gas directly discharges, causes the waste of resource.
Utility model content
The purpose of this utility model is to provide a kind of recirculating fluidized bed oxygen-enriched burning device, the deficiency that prior art exists can be improved, in employing, warm flue gas is as First air and Secondary Air, enter burner hearth respectively as reduced air, and respectively oxygen is noted to First air and Secondary Air, realize the adjustment of note oxygen amount, simultaneously for hearth combustion provides oxidant, the CO that CFBB is discharged can be made
2concentration enrichment, to more than 80%, to be beneficial to after coal combustion CO in flue gas
2trapping.
The utility model is achieved through the following technical solutions:
Recirculating fluidized bed oxygen-enriched burning device, comprise air compartment, the burner hearth being arranged on the air-distribution device above air compartment and being arranged on above air-distribution device, high temperature cyclone separator is connected with in described upper furnace, heating surface is connected with on described high temperature cyclone separator top, economizer is connected with in described heating surface bottom, described high temperature cyclone separator lower end is connected with air-distribution device by material returning device, described economizer bottom is connected with middle temperature cyclone separator, described middle temperature cyclone separator is connected with air compartment with First air oxygen injector by a gas recirculating fan successively, and described middle temperature cyclone separator bottom is connected with air-distribution device with Secondary Air oxygen injector by secondary flue gas recirculation blower successively, smoke-gas preheater is passed through successively in described economizer bottom, deduster is connected with air-introduced machine, described air-introduced machine is away from smoke-gas preheater one end and CO
2compression purification devices is connected, and described air-distribution device is provided with and broadcasts coal pipe.
Make bed material even fluidizing by air-distribution device, prevent bulky grain bed material from depositing, avoid slagging scorification and leak slag, through in warm cyclone separator and gas recirculating fan, in being extracted by gas recirculating fan, warm and humid flue gas carries out flue gas recirculation, in warm and humid flue gas contain a large amount of steam, wet flue gas enters burner hearth, a large amount of steam is brought in stove, is equivalent to be humidified in stove, improve desulfuration efficiency.The flue gas exported by middle temperature cyclone separator is input to burner hearth, as First air after injecting oxygen through a gas recirculating fan and by First air oxygen injector; The flue gas exported by middle temperature cyclone separator through the supercharging of secondary flue gas recirculation blower, and is input to burner hearth as Secondary Air after injecting oxygen by Secondary Air oxygen injector.Because First air and Secondary Air inject oxygen respectively, note oxygen ratio therefore can be adjusted as required.The unnecessary flue gas removing oxysulfide in stove directly can deliver to CO
2compression purification devices carries out compression purifying, as the raw material of industry or seal up for safekeeping, also can directly through chimney discharged to air.
Owing to recycling as First air and Secondary Air after flue gas note oxygen warm in employing, for hearth combustion provides oxidant, the CO that CFBB is discharged can be made
2concentration enrichment, to more than 80%, to be beneficial to after coal combustion CO in flue gas
2trapping; And warm and humid flue gas participates in process recycling in passing through, wet flue gas enters burner hearth, can a large amount of steam be brought in stove, be equivalent to be humidified in stove, desulfuration efficiency can be improved, thus afterbody does not need to arrange the emission request that special desulfurizer can meet oxysulfide, can reduce the scale of afterbody equipment, reduce costs.
Further, for better realizing the utility model, described air-introduced machine is connected with cigarette cooler away from smoke-gas preheater one end, and described cigarette cooler is connected with smoke-gas preheater by cold flue gas recirculation blower away from air-introduced machine one end, described smoke-gas preheater with broadcast coal pipe and be connected.For moisture as received coal content higher than the coal of more than 10%, need to process, therefore adopt dry and cold flue gas after the process of cigarette cooler condensation dehydration, and using dry and cold flue gas after the supercharging of cold flue gas recirculation blower as coal spread wind.Adopt cigarette cooler to realize condensation dehydration process, oxygen-enriched combusting flue gas recirculation process sulphur oxide can be avoided, enrichment appears in steam, cause flue gas recycled pipeline and the problem such as heated surface corrosion and the dry difficulty of transportation of pulverized coal preparation system.
Further, for better realizing the utility model, described cold flue gas recirculation blower is away from CO
2compression purification devices one end is connected with roots blower, described roots blower respectively with material returning device, broadcast coal pipe and be connected.For moisture as received coal content higher than more than 10% coal, in order to prevent coal dust to be scattered, the utility model arrange roots blower pressurized treatment is carried out to the cold flue gas after the process of cigarette cooler condensation dehydration after as broadcasting coal sealing air.
Further, for better realizing the utility model, the delivery outlet of described secondary flue gas recirculation blower is connected with described coal pipe of broadcasting.For moisture as received coal content not higher than 10% coal, can adopt in the utility model secondary flue gas recirculation blower export, note oxygen before middle temperature flue gas as coal spread wind.
Further, for better realizing the utility model, the delivery outlet of a described gas recirculating fan is connected with the described entrance broadcasting coal pipe.For moisture as received coal content not higher than 10% coal, adopt middle temperature flue gas before the outlet of gas recirculating fan, note oxygen as broadcasting coal sealing air in the utility model, for preventing coal dust anti-channeling.
Further, for better realizing the utility model, between described economizer and smoke-gas preheater, be provided with gas baffle.In order to adjust the amount of the flue gas entered in smoke-gas preheater, the resistance in adjustment flue, the utility model adjusts thermal discharge in flue by arranging gas baffle, and the thermal discharge of adjustment gas baffle both sides realizes the effect regulating steam temperature.
Further, for better realizing the utility model, described air-distribution device being provided with lime stone and adding mouth.The mode desulfurization adding lime stone in stove can be adopted, and by the high temperature cyclone separator that is arranged in furnace outlet by separating containing a large amount of unreacted lime stone or lime of carrying out through flue gas, and send burner hearth continuation participation desulfurization back to by feeding back device and material returning device, improve the utilization rate of lime stone and improve desulfuration efficiency.Adopt lime stone, the oxysulfide SOx in flue gas can be removed, prevent the oxysulfide in flue gas from occurring the problem of enrichment with flue gas recirculation, control at circulating flue gas and discharge sulfureous in flue gas oxide concentration in suitable scope, preventing flue and heating surface acid corrosion.
Further, for better realizing the utility model, broadcasting on coal pipe described in described lime stone interpolation mouth is positioned at and/or being positioned on the feed back leg of described material returning device.The position that lime stone adds mouth can be arranged according to boiler capacity, for heavy duty boiler, for improving desulfuration efficiency, ensure that lime stone is as far as possible evenly spread out in stove, lime stone add mouth can be arranged in broadcast coal pipe coal feeding hole on or material returning device feed back leg on, also can be arranged on the feed back leg of coal feeding hole or material returning device simultaneously.
Further, for better realizing the utility model, between described smoke-gas preheater and deduster, be provided with low-level (stack-gas) economizer.
Further, for better realizing the utility model, in air compartment or air channel, be provided with bottom ignition device.
The utility model compared with prior art, has following beneficial effect:
(1) the utility model recycles after warm flue gas note oxygen in adopting, and as bed material fluidizing agent and combustion oxidant, effectively controls CO in boiler exhaust gas
2concentration enrichment, to more than 80%, to be beneficial to after coal combustion CO in flue gas
2trapping;
(2) the utility model adopts the desulfurization of stove sodalime stone, by in warm and humid flue gas recirculation, wet flue gas enters burner hearth, a large amount of steam is brought in stove, be equivalent to be humidified in stove, improve desulfuration efficiency, afterbody does not need to arrange that special desulfurizer can meet the emission request of oxysulfide SOx;
(3) the utility model adopts and arranges rich oxygen ignition device under bed in air channel or in air compartment, adopts oxygen-enriched ignition mode under bed, improves Fire-under bed in Application of CFB Boiler combustion stability;
(4) the utility model adopts and is furnished with arrangement apparatus in lower furnace portion, makes bed material even fluidizing, prevents bulky grain bed material from depositing, and avoids slagging scorification and leaks slag;
(5) the utility model adopt in note oxygen in warm and humid flue gas, fully after mixing as combustion oxidant, and primary and secondary air separately notes oxygen by different proportion, can realize regulating note oxygen amount as required, realizes First air and the convenient of Secondary Air oxygen content regulates;
(6) the utility model sealing air and the material returning device elegance circulating flue gas not noting oxygen, security is higher;
(7) warm and humid flue gas recirculation in the utility model employing, system afterbody part of appliance scale reduces greatly, reduces initial cost and operating cost;
(8) the utility model adopts for hydrogenous coal and arrange cigarette cooler in oxygen-enriched combustion boiler system, oxygen-enriched combusting flue gas recirculation process sulphur oxide is avoided in condensation dehydration process, enrichment appears in steam, causes flue gas recycled pipeline and the problem such as heated surface corrosion and the dry difficulty of transportation of pulverized coal preparation system coal dust.
Accompanying drawing explanation
Fig. 1 is the utility model embodiment 1 structural representation;
Fig. 2 is the utility model embodiment 2 structural representation.
Wherein: 101-air compartment; 102-air-distribution device; 103-burner hearth; 104-high temperature cyclone separator; 105-material returning device; 106-heating surface; 107-economizer; 108-middle temperature cyclone separator; 109-gas recirculating fan; 110-secondary flue gas recirculation blower; 111-First air oxygen injector; 112-Secondary Air oxygen injector; 113-gas baffle; 114-smoke-gas preheater; 115-deduster; 116-air-introduced machine; 117-cigarette cooler; 118-CO
2compression purification devices; 119-cold flue gas recirculation blower; 120-roots blower; 125-broadcast coal pipe.
Detailed description of the invention
Below in conjunction with specific embodiment, the utility model is described in further detail, but embodiment of the present utility model is not limited thereto.
As shown in Figure 1, this recirculating fluidized bed oxygen-enriched burning device comprises air compartment 101, air-distribution device 102, burner hearth 103, high temperature cyclone separator 104, material returning device 105, heating surface 106, economizer 107, middle temperature cyclone separator 108, gas recirculating fan 109, secondary flue gas recirculation blower 110, oxygen injector 111, secondary oxygen injector 112, smoke-gas preheater 114, deduster 115, air-introduced machine 116, cigarette cooler 117, CO
2compress purification devices 118, cold flue gas recirculation blower 119, broadcast coal pipe 125, in running, after burner hearth 103 sent into by coal and desulfurizing agent, surrounded by the inertia high-temperature material be in a large number in sulfided state immediately, abundant mixing, rapid ignition, carry out desulphurization reaction simultaneously, in ascending air, under gravity and External Force Acting, primary air is departed from after oversize grain enters suspension region, thus adherent dirty, strengthen the transmission of furnace heat to working medium in heating surface 106, thus ensure that slightly large coal particle iterative cycles in stove burns completely.Gas-solid mixture containing tiny material enters high temperature cyclone separator 104 after leaving burner hearth 103, be separated returns to burner hearth 103 to a large amount of solid particles (inert material, unburnt coal grain, desulfurizing agent) in Dual-Phrase Distribution of Gas olid, again the fluidisation in stove and combustion heat-exchange is participated in, circulating combustion.
The fine particle be not separated becomes flying dust, back-end ductwork is entered with flue gas, exchange heat is carried out through heating surface 106, absorb the heat in flue gas through economizer 107 after, in warp, the flue gas of 350 DEG C-450 DEG C of warm cyclone separator 108 dedusting is divided into two-way: a road is First air loop, after being boosted by a gas recirculating fan 109, enter First air oxygen injector 111 oxygen of the 40%-60% needed for burning is injected, and by First air oxygen injector 111, oxygen is mixed with circulating flue gas, as First air, burner hearth 3 is entered as fluidized wind by air-distribution device 102 through isobaric air compartment 101, fluidization is risen to bed material, and as the oxide isolation of coal combustion, another road is Secondary Air loop, after being boosted by secondary flue gas recirculation blower 110, enter Secondary Air oxygen injector 112 oxygen of the 60%-40% needed for burning is injected, and by Secondary Air oxygen injector 112, oxygen is mixed with circulating flue gas, entering burner hearth 103 by overfiren air port, is supplementary oxygen amount of burning.
Fuel is entered by coal feeder and broadcasts coal pipe 125, under the effect of coal spread wind, sows into burner hearth 103.The effect of coal spread wind is mainly in order to ensure that the heat smoke in stove is not altered outward; The coal got off to feeder can better be sowed in siege, preventing fuel broadcasting coal pipe 125 formation accumulation, to make the thermal material in coal and burner hearth 103 better mix, impelling homogeneous temperature in burner hearth 103.
Coal spread wind source described in the utility model can be two kinds of modes, for high-moisture coal (moisture as received coal content is higher than more than 10%), as shown in Figure 1, adopt the dry and cold flue gas after the process of cigarette cooler 117 condensation dehydration, dry and cold flue gas, again after cold flue gas recirculation blower 119 supercharging, is input to and broadcasts coal pipe 125 as coal spread wind after smoke-gas preheater 114; For the coal (moisture as received coal content is not higher than 10%) that moisture is not high, as shown in Figure 2, adopt secondary flue gas recirculation blower 110 to export, note oxygen before middle temperature flue gas as coal spread wind.
Contaminated environment is exposed in order to prevent coal dust, the coal spread wind in the corresponding two kinds of sources of the utility model, correspondingly can arrange two kinds and broadcast coal sealing air, for high-moisture coal, as shown in Figure 1, broadcast coal sealing air and adopt cold flue gas after the process of cigarette cooler 117 condensation dehydration, cold flue gas again after roots blower 120 supercharging as broadcasting coal sealing air; For the coal that moisture is not high, as shown in Figure 2, adopt gas recirculating fan 109 to export, note oxygen before middle temperature flue gas as broadcasting coal sealing air.
The flue gas that burning produces enters high temperature cyclone separator 104 through burner hearth 103 outlet, and the soot particle separated sends burner hearth 103 back to by the material returning device 105 of high temperature cyclone separator 104 bottom.From high temperature cyclone separator 104 flue gas out after heating surface 106 at different levels and economizer 107, warm cyclone separator 108 during major part flue gas (about 50%-65%) is drawn under the effect of a gas recirculating fan 109 and secondary flue gas recirculation blower 110, flue gas in middle temperature cyclone separator 108 after final dusting, respectively as First air and Secondary Air; The flue gas of remaining 40%-30%, successively after smoke-gas preheater 114, deduster 115, air-introduced machine 116, extracts about 15%-30% through the process of cigarette cooler 117 condensation dehydration, and as material returning device 105 wind and broadcast coal wind, remaining desulfurization neat stress delivers to CO
2compression purification devices 118 compresses purifying or enters air by chimney.
Comparatively coal-powder boiler is good to the adaptability of coal for CFBB, and pollutant emission is also low than coal-powder boiler.For oxygen-enriched combusting coal-powder boiler, because pulverized coal preparation system needs to adopt the medium that a large amount of circulation dry flue gas is dry as coal dust and carry, boiler tail air and gas system needs to arrange bulky desulfurizer and cigarette cooler.Adopt the Oxygen enriched Combustion Technology on Circulating Fluidized Bed Test-facility of heat smoke recirculation as a kind of brand-new combustion system, realize comparatively low emission and the large-scale CO of pollutant in coal-burning power plant
2enrichment, reduce discharging and will have larger potentiality.
Embodiment 1:
As shown in Figure 1, a kind of recirculating fluidized bed oxygen-enriched burning device is disclosed in the present embodiment, comprise air compartment 101, the burner hearth 103 being arranged on the air-distribution device 102 above air compartment 101 and being arranged on above air-distribution device 102, high temperature cyclone separator 104 is connected with on described burner hearth 103 top, heating surface 106 is connected with on described high temperature cyclone separator 104 top, economizer 107 is connected with in described heating surface 106 bottom, described high temperature cyclone separator 104 lower end is connected with air-distribution device 102 by material returning device 105, described economizer 107 bottom is connected with middle temperature cyclone separator 108, described middle temperature cyclone separator 108 is connected with air compartment 101 with First air oxygen injector 111 by a gas recirculating fan 109 successively, and described middle temperature cyclone separator 108 bottom is connected with air-distribution device 102 with Secondary Air oxygen injector 112 by secondary flue gas recirculation blower 110 successively, described economizer 107 bottom is successively by smoke-gas preheater 114, deduster 115 is connected with air-introduced machine 116, described air-introduced machine 116 is away from smoke-gas preheater 114 one end and CO
2compression purification devices 118 is connected, and described air-distribution device 102 is provided with and broadcasts coal pipe 125.
In the present embodiment, adopt high temperature cyclone separator 104 and middle temperature cyclone separator 108, the flue gas that gas recirculating fan 109 exports after First air oxygen injector 111 mixture of oxygen as First air, secondary flue gas recirculation blower 110 export flue gas after Secondary Air oxygen injector 112 mixture of oxygen as Secondary Air, because First air and Secondary Air army adopt the flue gas of economizer exit, a gas recirculating fan 109 and secondary flue gas recirculation blower 110 all adopt separate configurations, First air and Secondary Air all can adopt separately different proportion note oxygen, the air quantity controlling First air and Secondary Air respectively can be facilitated, and then effectively control goods fluid in burner hearth 103.And material returning device 105 is with wind with broadcast coal pipe 125 wind and all can adopt flue gas through cigarette cooler 117 condensation dehydration.
In order to make the wind being input to smoke-gas preheater 114 have certain pressure, preferably, in the present embodiment, between described economizer 107 and smoke-gas preheater 114, be provided with gas baffle 113.By arranging gas baffle 113, a barrier can be formed in airduct, the flue gas of gas baffle 113 both sides can not be altered mutually, realize sealing function.
In order to improve the desulfurized effect of this device, in the present embodiment, preferably, described air-distribution device 102 is provided with lime stone and adds mouth.Add lime stone in CFBB, normally running under bed temperature (850 DEG C-900 DEG C), pulverized limestone is sintered into calcium oxide (850 DEG C is the best desulfurization temperature of calcium-based desulfurizing agent), thus reaches with sulfur dioxide in conjunction with desulfurized effect.After coal and lime stone burn, most of particle carries out gas solid separation through cyclone separator, is sent back to burner hearth 103 from bottom.Limestone desulfurizer, at the desulfurization performance of fluidized bed combustion indoor, adopts to remove certain content SO usually
2the CaCO added
3represent with the ratio of the amount of substance of sulfur content in coal amount, be called mol ratio.In the utility model, First air and Secondary Air are the wet flue gas containing a large amount of steam, and it enters in stove and is equivalent to be humidified in stove, plays the effect of humidification desulfurization, greatly can improve desulfuration efficiency, can omit afterbody desulphurization system.Preferably, in the present embodiment, broadcast on coal pipe 125 described in lime stone interpolation mouth is positioned at or be positioned on the feed back leg of described material returning device 105, two lime stones also can be set simultaneously and add mouths.
In order to ensure the safe operation of deduster 115, in the present embodiment, preferably, between described smoke-gas preheater 114 and deduster 115, low-level (stack-gas) economizer is provided with.Flue-gas temperature can be dropped to the temperature range that deduster 115 allows by low-level (stack-gas) economizer, guarantees the safe operation of deduster 115, and meanwhile, can play the effect absorbing fume afterheat, recovery section waste heat, realizes Btu utilization.
Preferably, the utility model adopts bottom ignition device to realize igniting, is namely provided with bottom ignition device in air compartment 101 or air channel.When igniter being arranged in air compartment 101, igniter is arranged on rear side of air compartment 101, one is respectively established on rear side of two isobaric air compartments 101 below recirculating fluidized bed air distribution plate, every platform igniter joins a torch oil gun, First air out after, enter an air compartment 101 from air compartment 101 both sides and two igniters respectively, main air duct and every platform igniter arrange air door.
In the present embodiment, air-distribution device 102 is provided with slag-drip opening, utilizes the mobility of Dual-Phrase Distribution of Gas olid that unnecessary material is discharged burner hearth 103, thus realize the balance of material turnover in stove, maintain material at zone of reasonableness.
Applicant tests discovery, the utility model recirculating fluidized bed oxygen-enriched burning device, afterbody deduster 115 after economizer 107 and the exhaust gas volumn of air-introduced machine 116 are only equivalent to about 30% of regular air burning, flue gas through cigarette cooler 117 is also only the 5%-10% of total exhaust gas volumn, the part of appliance scale of afterbody air and gas system greatly reduces, and can play the effect reducing initial cost and operating cost.
Embodiment 2:
The present embodiment is on the basis of embodiment 1, and described cold flue gas recirculation blower 119 is away from CO
2compression purification devices 118 one end is connected with roots blower 120, described roots blower 120 respectively with material returning device 105, broadcast coal pipe 125 and be connected.The delivery outlet of described secondary flue gas recirculation blower 110 is connected with described coal pipe 125 of broadcasting.
As shown in Figure 2, from high temperature cyclone separator 104 flue gas out after heating surface 106 at different levels and economizer 107, flue gas is divided into two parts, and a part enters middle temperature cyclone separator 108(and accounts for 70% of flue gas), another part enters CO through afterbody deduster etc.
2compression purification devices 118 compresses purifying or enters air through chimney.In warp, the flue gas of warm cyclone separator 108 dedusting is divided into three tunnels: a road is as First air loop, First air oxygen injector 111 is entered through gas recirculating fan 109 boosting, thus the oxygen of the 40%-60% needed for burning is injected, and by First air oxygen injector 111, oxygen is mixed with circulating flue gas, as First air, burner hearth 103 is entered as fluidized wind by air-distribution device 102 after isobaric air compartment 101, fluidization is risen to bed material, and as the oxide isolation of coal combustion, and export at a gas recirculating fan 109, a part is extracted as coal spread wind before First air oxygen injector 111, second tunnel is secondary circuit, after being boosted by secondary flue gas recirculation blower 110, enter Secondary Air oxygen injector 112 oxygen of the 60%-40% needed for burning is injected, and by Secondary Air oxygen injector 112, oxygen is mixed with circulating flue gas, entering burner hearth 103 by overfiren air port, is coal combustion supplemental oxygen, 3rd tunnel is Roots's wind loop, and after being boosted by roots blower 120, a part is as fluidized wind, feedback air, the loosening wind of material returning device 105, and a part is as the sealing air of boiler measuring point etc.
Afterbody enters CO
2compression purification devices 118 compresses the flue gas that purifying or chimney enter air, before deduster 115, realize cooling by low-level (stack-gas) economizer.
Claims (10)
1. recirculating fluidized bed oxygen-enriched burning device, comprise air compartment (101), be arranged on the air-distribution device (102) of air compartment (101) top and be arranged on the burner hearth (103) of air-distribution device (102) top, high temperature cyclone separator (104) is connected with on described burner hearth (103) top, heating surface (106) is connected with on described high temperature cyclone separator (104) top, economizer (107) is connected with in described heating surface (106) bottom, it is characterized in that: described high temperature cyclone separator (104) lower end is connected with air-distribution device (102) by material returning device (105), described economizer (107) bottom is connected with middle temperature cyclone separator (108), described middle temperature cyclone separator (108) is connected with air compartment (101) with First air oxygen injector (111) by a gas recirculating fan (109) successively, and described middle temperature cyclone separator (108) bottom is connected with air-distribution device (102) with Secondary Air oxygen injector (112) by secondary flue gas recirculation blower (110) successively, described economizer (107) bottom is successively by smoke-gas preheater (114), deduster (115) is connected with air-introduced machine (116), described air-introduced machine (116) is away from smoke-gas preheater (114) one end and CO
2compression purification devices (118) is connected, and described air-distribution device (102) is provided with and broadcasts coal pipe (125).
2. recirculating fluidized bed oxygen-enriched burning device according to claim 1, it is characterized in that: described air-introduced machine (116) is connected with cigarette cooler (117) away from smoke-gas preheater (114) one end, described cigarette cooler (117) is connected with smoke-gas preheater (114) by cold flue gas recirculation blower (119) away from air-introduced machine (116) one end, described smoke-gas preheater (114) with broadcast coal pipe (125) and be connected.
3. recirculating fluidized bed oxygen-enriched burning device according to claim 2, is characterized in that: described cold flue gas recirculation blower (119) is away from CO
2compression purification devices (118) one end is connected with roots blower (120), described roots blower (120) respectively with material returning device (105), broadcast coal pipe (125) and be connected.
4. recirculating fluidized bed oxygen-enriched burning device according to claim 1, is characterized in that: the delivery outlet of described secondary flue gas recirculation blower (110) is connected with described coal pipe (125) of broadcasting.
5. recirculating fluidized bed oxygen-enriched burning device according to claim 4, is characterized in that: the delivery outlet of a described gas recirculating fan (109) is connected with the described entrance broadcasting coal pipe (125).
6. the recirculating fluidized bed oxygen-enriched burning device according to any one of claim 1-5, is characterized in that: between described economizer (107) and smoke-gas preheater (114), be provided with gas baffle (113).
7. the recirculating fluidized bed oxygen-enriched burning device according to any one of claim 1-5, is characterized in that: on described air-distribution device (102), be provided with lime stone add mouth.
8. recirculating fluidized bed oxygen-enriched burning device according to claim 7, is characterized in that: broadcast on coal pipe (125) described in described lime stone interpolation mouth is positioned at and/or be positioned on the feed back leg of described material returning device (105).
9. the recirculating fluidized bed oxygen-enriched burning device according to any one of claim 1-5, is characterized in that: between described smoke-gas preheater (114) and deduster (115), be provided with low-level (stack-gas) economizer.
10. the recirculating fluidized bed oxygen-enriched burning device according to any one of claim 1-5, is characterized in that: in air compartment (101) or air channel, be provided with bottom ignition device.
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Also Published As
| Publication number | Publication date |
|---|---|
| CN104848213A (en) | 2015-08-19 |
| WO2016161821A1 (en) | 2016-10-13 |
| CN104848213B (en) | 2017-03-15 |
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