CN106642089A - Combustion method and combustion device for desulfuration and denitration of circulating fluid bed - Google Patents

Combustion method and combustion device for desulfuration and denitration of circulating fluid bed Download PDF

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Publication number
CN106642089A
CN106642089A CN201610972036.5A CN201610972036A CN106642089A CN 106642089 A CN106642089 A CN 106642089A CN 201610972036 A CN201610972036 A CN 201610972036A CN 106642089 A CN106642089 A CN 106642089A
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China
Prior art keywords
wind
combustion
fluidized bed
burner hearth
recirculating fluidized
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CN201610972036.5A
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Chinese (zh)
Inventor
李诗媛
涂秋亚
周托
王海刚
那永洁
包绍麟
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Institute of Engineering Thermophysics of CAS
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Institute of Engineering Thermophysics of CAS
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Priority to CN201610972036.5A priority Critical patent/CN106642089A/en
Publication of CN106642089A publication Critical patent/CN106642089A/en
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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
    • 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
    • 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
    • F23J15/003—Arrangements of devices for treating smoke or fumes for supplying chemicals to fumes, e.g. using injection devices
    • 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
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • 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
    • F23L9/00—Passages or apertures for delivering secondary air for completing combustion of fuel 
    • 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
    • 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 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/06041—Staged supply of oxidant
    • 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
    • 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
    • F23J2215/20—Sulfur; Compounds thereof

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

Abstract

The invention discloses a combustion method and a combustion device for desulfuration and denitration of a circulating fluid bed. The combustion method comprises the following steps: a fuel, a desulfurizing agent, and combustion air with the quantity being higher than theoretical combustion air quantity and lower than routine combustion air quantity are supplied to a lower area of a hearth of the circulating fluid bed; a gas and solid mixture generated by combustion in the hearth of the circulating fluid bed enters a cyclone separator from the upper part of the hearth, particles in the gas and solid mixture are separated and sent back to the hearth of the circulating fluid bed, smoke in the gas and solid mixture flows into a tail flue via a center barrel at the top of the cyclone separator and then via an exit flue; complementary combustion air nozzles are formed in the part of the hearth, at the height where a fluidizing velocity is 2.5-4 times that of an air distribution plate, of the circulating fluid bed, and formed in the upper part of the hearth, and/or in an inlet section of the cyclone separator, and complementary combustion air is supplied to the complementary combustion air nozzles. The combustion device has the characteristics of system simplicity, low project investment cost, small floor area, and the like.

Description

The combustion method and device of recirculating fluidized bed desulphurization denitration
Technical field
The present invention relates to the combustion method and device of a kind of CFBB, in particular it relates to a kind of ciculation fluidized The combustion method and device of combined desulfurization and denitration in pool furnace.
Background technology
Sulfur dioxide and nitrogen oxides (NOx) are important atmosphere pollutions, are the weights for causing acid rain and photochemical pollution Want material.Sulfur dioxide is reached after finite concentration into air, and people, animals and plants will be worked the mischief；More importantly in phase It is larger to humidity, in the presence of having particulate matter, it may occur that catalytic oxidation generates SO3And sulfuric acid mist, toxicity is bigger than sulfur dioxide 10 times.It is fewer than sulfur dioxide in discharged nitrous oxides total amount in coal-burning boiler, but its potential hazard degree to environment It is more serious than sulfur dioxide, wherein NO and NO2It is the main component of atmosphere pollution, human body poisoning, plant damage, acid rain acid can be caused Mist etc., and photochemical fog is formed with hydrocarbon, cause the destruction of ozone layer.Therefore, coal fired boiler of power plant is controlled Sulfur dioxide and discharged nitrous oxides are most important.China's regulation is newly-built, reconstruct and extend coal-burning power plant, it is necessary to reaches and meets Environmentally friendly discharging standards；Newest《Thermal power plant atmosphere pollutants emission standardses (GB-13223-2011)》Require all Firepower electrical plant boiler has to carry out SO2And NOxIt is below 100mg/Nm3Discharge standard, and at present CFBB is original Sulfur dioxide and the discharged nitrous oxides concentration overwhelming majority can not be directly up to standard.Therefore CFBB is faced with necessary Further reduce the problem of sulfur dioxide and discharged nitrous oxides.
The coal-fired sulfur dioxide for producing of control at present mainly has three class desulfurization technologies, that is, desulfurization in desulfurization, burning before burning And flue gas desulfurization.Flue gas desulfurization is to control coal-burning power plant SO at present2Gas discharges most effective and most widely used technology.According to The state flue gas desulfurization of desulfurizing agent and desulphurization reaction thing can be divided into wet method, dry method and semidry method three major types.Wet desulfurizing process Ripe, efficiency high, but invest and operating cost costliness；Dry process has small investment, and equipment is simple and product is easily handled The advantages of, but there is a problem of that removal efficiency and absorbent utilization rate are low.The desulfurization product of semi-dry process is in dry state, is easy to place Reason, but the easy fouling of system and blocking, need special equipment to carry out the preparation of absorbent, and investment cost is larger, and desulfurization Efficiency is with the utilization rate of absorbent be not as high as wet method.
The technology of CFBB control NOx emission can be divided into two classes：One is to reduce firing by various technological means NOx generation amount during burning, i.e. low NOx combusting technology；Two is to take off the NOx to generate from flue gas by technological means Remove, i.e. gas denitrifying technology.Gas denitrifying technology complex process, investment and operating cost height, undoubtedly reduce recirculating fluidized bed The market competitiveness of boiler.Traditional low NOx combusting technology is mainly included low oxygen combustion, is fired using air classification in burner hearth Burning, fuel-staged combustion, flue gas recirculation etc..
To reach restriction requirement of the national environmental standard for Air Pollutant Emission, large-scale thermal power boiler nitrogen oxidation Thing and the maturation process of sulfur dioxide control are using SCR (SCR) technology or SNCR (SNCR) technology combines afterbody desulfurization, and this is classification administration way.Not only floor space is big for this mode, and invests and run It is costly, it is difficult to extensively application.And because the optimum operating temperature of SCR is at 350～450 DEG C or so, also there is cigarette after desulfurization The problem of gas reheating.If operation is improper, SO2Content is raised will make SCR catalyst be poisoned.Both at home and abroad existing more correlation is ground Study carefully, but there is the shortcoming in terms of technology and economic dispatch mostly, it is difficult to which development can be the technology of more practicality.So exploitation at present was both General trend that is cheap and efficiently being flue gases purification research with the new technology of simultaneous SO_2 and NO removal, new equipment.
Chinese patent application 201310539752.0 proposes a kind of efficiently low nitrogen combustion of the multiple classification of CFBB Firing method and combustion system, combustion air distinguishes the corresponding entrances of Jing and enters burner hearth, by controlling each area's excess air coefficient by stove Thorax is divided into different regions, makes fuel be uniformly dispersed in burner hearth burning.But the method can only reduce formation of nitrogen oxides and The discharge of sulfide cannot be reduced.Additionally, Chinese patent application 201310723729.7 provides a kind of CFBB The combustion method of low-nitrogen oxide discharging, by secondary air channel air port upper, middle and lower-ranking is set to, and per layer of scope is limited to necessarily Height, make Oxygen Amount in Flue Gas be maintained at 2% to 3% low excess air operation while reducing primary air flow and secondary air flow, while should The temperature that method also has many other requirements, such as bed keeps the thickness of sunken bed temperature, bed to keep low material position, air compartment blast Keep low pressure etc..Although the method can effectively reduce the discharge of nitrogen oxides but cannot be while meeting removing sulfureous in flue gas The demand of thing.
The content of the invention
The purpose of the present invention is that a kind of combustion of simultaneous SO_2 and NO removal in circulating fluid bed boiler is proposed for above-mentioned deficiency Firing method and device.
According to an aspect of the present invention, there is provided a kind of combustion method of recirculating fluidized bed desulphurization denitration, step：
A) fuel, desulfurizing agent are passed through into recirculating fluidized bed burner hearth lower area and higher than theoretical combustion air but are less than The burning wind of conventional combustion air capacity, the atmosphere for making recirculating fluidized bed burner hearth lower area is maintained at reducing atmosphere, wherein A part for burning wind is passed through from the air distribution plate of burner hearth bottom；
B) gas-solid mixture that Circulation fluidized-bed furnace chamber inner combustion is produced is made to enter cyclone separator, gas-solid from upper furnace Particle in mixture is separated and is sent back to recirculating fluidized bed burner hearth, at the top of the flue gas Jing cyclone separators in gas-solid mixture Central tube, then Jing exhaust pass inflow back-end ductwork；And
C) at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, upper furnace and/or Cyclone inlet section arranges afterburning wind snout, is passed through aftercombustion wind in the afterburning wind snout, it is ensured that in flue gas Sulfur dioxide and desulfurizing agent can fully react, wherein fluidizing velocity unit：Long measure/s.
According to a specific embodiment, step d) is also included after step c)：Outside central tube and/or exhaust pass Afterburning wind snout is also provided with, aftercombustion wind is passed through, makes carbon monoxide and fly ash combustible material in flue gas burn completely.
According to a specific embodiment, the burning air quantity being passed through to recirculating fluidized bed burner hearth bottom in the step b) For：So that lower area burner hearth excess air coefficient is 1.05-1.08.
According to a specific embodiment, the aftercombustion wind total amount in step c) and step d) is accounted for and is input to burner In total air 10%-15%.
According to a specific embodiment, the aftercombustion wind total amount in step c) and step d) makes total in burner Excess air coefficient reaches 1.15-1.2.
According to a specific embodiment, the aftercombustion wind in step c) and step d) is provided by air collecting box.
According to a further aspect in the invention, there is provided a kind of burner of recirculating fluidized bed combined desulfurization and denitration, including following Ring fluid bed furnace thorax, cyclone separator and back-end ductwork, wherein,
The recirculating fluidized bed burner hearth includes lower area and upper area, and the lower area is opened up for fuel, desulfurization The first passage that agent and burning wind are passed through, the upper area opens up the second of the gas-solid mixture outflow produced for burning and leads to Road；
The cyclone separator is connected with the second channel, and the flue gas after cyclone separator top is opened up for separating flows out Central tube, the central tube Jing exhaust pass is connected to back-end ductwork；
Wherein, at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, burner hearth Top and/or cyclone inlet section arrange afterburning wind snout, are passed through for aftercombustion wind, wherein fluidizing velocity unit： Long measure/s.
According to a specific embodiment, afterburning wind snout is also provided with outside the central tube and/or exhaust pass, for mending Fill burning to be passed through with wind.
According to a specific embodiment, the burner also includes air collecting box, and it is connected to each afterburning wind snout, is used for Aftercombustion wind is provided.
By above-mentioned technical proposal, can learn the beneficial effects of the present invention is：
(1) burner of the invention has the features such as simple system, engineering investment cost are low, floor space is little, is suitable to The transformation of existing power plant and Industrial Boiler and newly constructed boiler.
(2) desulfurizing agent is repeatedly circulated in fluid bed, and violent turbulent mixture between gas-solid, sorbent utilization is higher.And Desulfurizing agent is long with the smoke contacts time, therefore desulfuration efficiency is higher, and desulfurization product can be comprehensively utilized.
Description of the drawings
Fig. 1 is the combustion method schematic flow sheet of the recirculating fluidized bed desulphurization denitration of one embodiment of the invention.
Fig. 2 is the combustion method schematic flow sheet of the recirculating fluidized bed desulphurization denitration of another embodiment of the present invention.
Fig. 3 is the burner schematic diagram of the recirculating fluidized bed desulphurization denitration of the embodiment of the present invention.
Specific embodiment
In the art, excess air coefficient is represented in the case of air capacity actually used during burning and full combustion of fuel The ratio of the air capacity that should be used in theory.Due in combustion process the blending of fuel and air be unable to reach it is uniform in ideal Degree, excess air coefficient can not realize that fuel burns completely when being equal to 1, in the engineering practice of boiler design and operation, Excess air coefficient is typically chosen in 1.2 or so generally at furnace outlet, therefore air when excess air coefficient is equal into 1 is used Amount is referred to as theoretical combustion air, and air consumption when excess air coefficient is equal to 1.2 is referred to as conventional combustion air capacity.At this Bright middle burning wind and afterburning wind refer both to air.
Fluidizing velocity refers to that what is commonly used in fluidized bed combustion process uses wind fluidizing velocity in the present invention, for example, typically flow Change speed is 4-6m/s, but above-mentioned typical fluidizing velocity is merely illustrative, is not limited to the present invention.
To make the object, technical solutions and advantages of the present invention become more apparent, below in conjunction with specific embodiment, and reference Accompanying drawing, the present invention is described in further detail.
According to present invention inventive concept generally, the combustion method and device of recirculating fluidized bed desulphurization denitration, wherein, ginseng As shown in Figure 1, combustion method includes step：
A) fuel, desulfurizing agent are passed through into recirculating fluidized bed burner hearth lower area and higher than theoretical combustion air but are less than The burning wind of conventional combustion air capacity, the atmosphere for making recirculating fluidized bed burner hearth lower area is maintained at reducing atmosphere, wherein A part for burning wind is passed through from the air distribution plate of burner hearth bottom；
B) gas-solid mixture that Circulation fluidized-bed furnace chamber inner combustion is produced is made to enter cyclone separator, gas-solid from upper furnace Particle in mixture is separated and is sent back to recirculating fluidized bed burner hearth, at the top of the flue gas Jing cyclone separators in gas-solid mixture Central tube, then Jing exhaust pass inflow back-end ductwork；And
C) at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, upper furnace and/or Cyclone inlet section arranges afterburning wind snout, is passed through aftercombustion wind in the afterburning wind snout, it is ensured that in flue gas Sulfur dioxide and desulfurizing agent can fully react, wherein fluidizing velocity unit：Long measure/s.
Preferably, shown in Figure 2, above-mentioned combustion method also includes step d) after step c)：Central tube and/ Or afterburning wind snout is also provided with outside exhaust pass, and aftercombustion wind is passed through, make carbon monoxide and flying dust in flue gas flammable Thing burns completely.
Shown in Figure 3, burner includes recirculating fluidized bed burner hearth 1, cyclone separator 2 and back-end ductwork 6, wherein：
The recirculating fluidized bed burner hearth 1 includes lower area and upper area, and the lower area is opened up for fuel, desulfurization The first passage that agent and burning wind are passed through, the upper area opens up the second of the gas-solid mixture outflow produced for burning and leads to Road；
The cyclone separator 2 is connected with the second channel, and the top of cyclone separator 2 is opened up for the flue gas stream after separation The central tube 4 for going out, the central tube Jing exhaust pass 5 is connected to back-end ductwork 6；
Wherein, at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, burner hearth Top and/or cyclone inlet section arrange afterburning wind snout 7, are passed through for aftercombustion wind, wherein fluidizing velocity unit： Long measure/s.
Burner and combustion method are combined below the present invention is explained and is illustrated.
In combustion process of the fuel in recirculating fluidized bed, sulfur dioxide and nitrogen oxides (NOx) are generated, while lime stone Decomposition discharges carbon dioxide.Nitrogen oxides is mainly nitric oxide (NO), and its ratio is up to 95%.What general coal combustion was generated The nitrogen source of NOx can be divided into fuel N and heating power N, N of the fuel bound nitrogen in fuel, Ns of the heating power N in combustion air, Only heating power N is possible to be converted into NOx under high temperature (more than 1100 DEG C).For burning of coal in recirculating fluidized bed, The generation of nitrogen oxides is mainly derived from the nitrogen in coal.Under general burning condition, the compound of nitrogen content of coal is warm first Solution is into HCN and NH3Deng intermediate product, as volatile matter is together separated out from coal, referred to as volatile matter N, in remaining on coke Nitrogen be referred to as char N；And in oxidizing atmosphere, the nitrogen oxygen generated by volatile matter N during coal combustion in CFBB The ratio that compound is accounted for only accounts for 20%-40% up to 60%-80%, the nitrogen oxides that coke burning is produced.
In combustion process in recirculating fluidized bed burner hearth, emulsion zone burning and dilute-phase zone burning are broadly divided into.In circulation Fluid bed emulsion zone, after coal enters burner hearth, through burner hearth high temperature pyrolysis and separates out volatile matter, and titanium dioxide is contained in volatile matter Sulphur, and generate the presoma HCN and NH of nitrogen oxides3Deng composition containing N, volatile matter N is run into feeding burner hearth in combustion air Oxygen, NO is oxidized to rapidly.Due to not being passed through combustion air excessive enough in burner hearth, generate in combustion Certain density CO.The key reaction equation of emulsion zone combustion process is as follows：
S+O2- ＞ SO2
C+O2- ＞ CO2, CO
Fuel-N- ＞ NH3, HCN ...
NH3, HCN+O2- ＞ NO
Fuel-N+O2- ＞ NO
CaCO3- ＞ CaO+CO2
CaO+SO2+1/2O2- ＞ CaSO4
In recirculating fluidized bed dilute-phase zone, the coke after pyrolysis of coal continues to be burnt with oxygen, without fully excessive Combustion air under the conditions of, generate CO2And CO.In addition, emulsion zone produce NO in dilute-phase zone by the CO and Jiao in flue gas Charcoal is reduced, and as controls the main path of discharged nitrous oxides.The key reaction equation of dilute-phase zone combustion process is as follows：
C+O2- ＞ CO2, CO
NO+CO- ＞ CO2+N2
NO+C- ＞ CO2+N2
CaO+SO2+1/2O2- ＞ CaSO4
It can be seen that, as long as the atmosphere that can control CFBC is reducing atmosphere, then can suppress nitrogen oxides Produce, if but burning carry out under reducing atmosphere all the time, the insufficient, efficiency of combustion that means to burn is low, and is passed through Lime stone do not reach the effect of complete desulfurization yet, the sulfur dioxide for producing that burns cannot fully suppress.
In the embodiment shown in fig. 3, away from 2.5 times～4 times fluidizing velocity values of air distribution plate (stream in recirculating fluidized bed burner hearth 1 Change speed unit：Long measure/s) height at and upper furnace, cyclone inlet, central tube and central tube outlet cigarette Road arranges afterburning wind snout 7, afterburning wind snout 7 and external channel, afterburning wind is passed through in burner hearth 1, the entrance of cyclone separator 2 In section and central tube 4.
During the combustion method of the embodiment of the present invention is realized, referring to shown in Fig. 1 and Fig. 2, respectively to ciculation fluidized The bottom of pool furnace thorax 1 is passed through fuel and desulfurizing agent, and higher than theoretical combustion air but less than the combustion of conventional combustion air capacity Burning wind, makes the nitrogen oxides in the combustion product of the bottom of recirculating fluidized bed burner hearth 1 be inhibited, and generation is included with titanium dioxide Sulphur, a small amount of nitrogen oxides, the flue gas of carbon monoxide and the gas-solid mixture with a certain amount of coke granule thing；Make recirculating fluidized bed The gas-solid mixture that burner hearth 1 is produced enters cyclone separator 2, and the most of particle in gas-solid mixture is separated, Jing material returning devices 3 Recirculating fluidized bed burner hearth 1 is sent back to again with the returning charge mouth on recirculating fluidized bed burner hearth 1, flue gas carries a small amount of fine grained secretly and enters center Cylinder 4；By afterburning wind snout 7 to burner hearth 1 away from 2.5 times～4 times fluidizing velocity value (fluidizing velocity units of air distribution plate：Long measure/ S) at height and/or upper furnace, and/or the entrance of cyclone separator 2, in central tube 4 and/or exhaust pass 5 supplement is passed through Burning wind, makes the combustible components such as the sulfur dioxide in flue gas, carbon monoxide and flying dust carbon residue burn completely.
According to an embodiment of the present, the fuel being passed through into recirculating fluidized bed burner hearth 1 and the amount of burning wind are So that excess air coefficient is 1.05-1.08, so can be so that the bottom of CFBB 1 be maintained at reproducibility gas Atmosphere, in turn ensure that most of combustible component completes burning in burner hearth, and remaining combustible component is less, in burner hearth, cyclonic separation Can after-flame in device entrance and central tube.
In a kind of exemplary embodiment, to the top of burner hearth 1 and the entrance of cyclone separator 2 and central tube 4 and outlet cigarette The amount of the aftercombustion wind being passed through in road 5 accounts for the 10%-15% of burner total air, and the air quantity passes through upper furnace, Cyclone inlet section, central tube and exhaust pass strengthen flow of flue gas when being passed through, by the afterburning mouth structure of optimization design And arrangement, the blending of flue gas and afterburning wind is improved, reach the purpose for improving reaction and efficiency of combustion.To burner hearth 1 away from cloth wind 2.5 times～4 times fluidizing velocity value (fluidizing velocity units of plate：Long measure/s) height at and/or upper furnace, and/or rotation The amount of the aftercombustion wind being passed through in the entrance of wind separator 2, central tube 4 and/or exhaust pass 5 makes the mistake in burner Amount air coefficient reaches 1.15-1.2.So, can make contained flammable in the gas-solid mixture discharged from recirculating fluidized bed burner hearth 1 Composition fully burns, so as to ensure boiler combustion efficiency.
According to a preferred embodiment of the present invention, by air collecting box to recirculating fluidized bed burner hearth away from air distribution plate 2.5 times～4 Times fluidizing velocity value (fluidizing velocity unit：Long measure/s) height at and upper furnace, cyclone inlet section, center Cylinder and central tube exhaust pass are passed through aftercombustion wind, and the air collecting box includes：With the air intake vent of ft connection, and with follow Ring fluid bed furnace thorax is away from 2.5 times～4 times fluidizing velocity value (fluidizing velocity units of air distribution plate：Long measure/s) height at and stove The air outlet of thorax top, cyclone inlet section, central tube and the connection of central tube exhaust pass inside.
In the combustion method described in embodiments in accordance with the present invention, 1 is slightly larger than by controlling excess air coefficient, especially It is the burning wind of 1.05-1.08, and is aided with the aftercombustion wind of matching value, makes the burning of recirculating fluidized bed burner hearth bottom In hypoxia (conventional combustion excess air coefficient is 1.2), reducing atmosphere is formed, but produce certain density CO therewith (concentration is 1000-2000ppm), the NO for producing that burns is reduced by the CO in flue gas, thereby inhibiting the discharge of nitrogen oxides；And The cooperation of burning air quantity and aftercombustion air quantity, it is ensured that sulfur dioxide in flue gas, the low emission of nitrogen oxides and burning The balance of efficiency.Further, the combustion method described in the embodiment of the present invention is also arranged the supply position of aftercombustion wind In recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity value (fluidizing velocity units of air distribution plate：Long measure/s) height at And/or upper furnace, and/or cyclone inlet section, it is the sulfur dioxide and reactive desulfurizing agent in flue gas and in circulating ash There is provided oxygen-rich area, it is ensured that desulfuration in furnace reaction has oxygen amount and the reaction time of abundance.Meanwhile, also in central tube and/or go out Mouthful flue arranges afterburning mouth, provides enough combustion space and time for the carbon residue in carbon monoxide and flying dust in flue gas, most Cause eventually to ensure that nitrogen oxides and sulfur dioxide are generated on the basis of control in stove at the same time, unburned is completely flammable in flue gas Thing is fully converted, and realizes high burning efficiency.
Further, since the position that is passed through of aftercombustion wind is arranged on into recirculating fluidized bed burner hearth away from air distribution plate 2.5 times～4 Times fluidizing velocity value (fluidizing velocity unit：Long measure/s) height at and/or upper furnace, and/or cyclone separator enter Mouth section, central tube and/or exhaust pass, therefore no longer need additional combustion space (such as after-burner), to have saved equipment Cost and occupation of land space, and can realize that the present invention is implemented on regular circulation fluidized bed combustor by small-scale transformation The combustion method of example, has expanded the range of application of this method.
Particular embodiments described above, has been carried out further in detail to the purpose of the present invention, technical scheme and beneficial effect Describe in detail bright, it should be understood that the foregoing is only the specific embodiment of the present invention, be not limited to the present invention, it is all Within the spirit and principles in the present invention, any modification, equivalent substitution and improvements done etc. should be included in the protection of the present invention Within the scope of.

Claims (9)

1. a kind of combustion method of recirculating fluidized bed desulphurization denitration, it is characterised in that including step：
A) fuel, desulfurizing agent are passed through and higher than theoretical combustion air but less than routine into recirculating fluidized bed burner hearth lower area The burning wind of combustion air amount, the atmosphere for making recirculating fluidized bed burner hearth lower area is maintained at reducing atmosphere, wherein burning It is passed through from the air distribution plate of burner hearth bottom with a part for wind；
B) gas-solid mixture that Circulation fluidized-bed furnace chamber inner combustion is produced is made to enter cyclone separator, gas-solid mixing from upper furnace Particle in thing is separated and is sent back to recirculating fluidized bed burner hearth, the center at the top of flue gas Jing cyclone separators in gas-solid mixture Cylinder, then Jing exhaust pass inflow back-end ductwork；And
C) at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, upper furnace and/or whirlwind Separator inlet section arranges afterburning wind snout, is passed through aftercombustion wind in the afterburning wind snout, it is ensured that the dioxy in flue gas Changing sulphur and desulfurizing agent can fully react, wherein fluidizing velocity unit：Long measure/s.
2. combustion method according to claim 1, it is characterised in that also include step d) after step c)：At center Afterburning wind snout is also provided with outside cylinder and/or exhaust pass, aftercombustion wind is passed through, carbon monoxide and flying dust in flue gas is made Combustible burns completely.
3. combustion method according to claim 1, it is characterised in that
The burning being passed through to recirculating fluidized bed burner hearth bottom in the step b) is with air quantity：So that lower area burner hearth is excessive empty Gas coefficient is 1.05-1.08.
4. combustion method according to claim 1, it is characterised in that
Aftercombustion wind total amount in step c) and step d) accounts for the 10%- of the total air being input in burner 15%.
5. combustion method according to claim 1, it is characterised in that
Aftercombustion wind total amount in step c) and step d) makes the total excess air coefficient in burner reach 1.15- 1.2。
6. combustion method according to claim 1, it is characterised in that
Aftercombustion wind in step c) and step d) is provided by air collecting box.
7. a kind of burner of recirculating fluidized bed combined desulfurization and denitration, including recirculating fluidized bed burner hearth, cyclone separator and tail Portion's flue, it is characterised in that：
The recirculating fluidized bed burner hearth includes lower area and upper area, the lower area open up for fuel, desulfurizing agent and The first passage that burning wind is passed through, the upper area opens up the second channel that the gas-solid mixture produced for burning flows out；
The cyclone separator is connected with the second channel, and cyclone separator top is opened up in flowing out for the flue gas after separation Heart cylinder, the central tube Jing exhaust pass is connected to back-end ductwork；
Wherein, at the height in recirculating fluidized bed burner hearth away from 2.5 times～4 times fluidizing velocity values of air distribution plate, upper furnace And/or cyclone inlet section arranges afterburning wind snout, is passed through for aftercombustion wind, wherein fluidizing velocity unit：Length Unit/s.
8. burner according to claim 7, it is characterised in that outside the central tube and/or exhaust pass Afterburning wind snout is set, is passed through for aftercombustion wind.
9. burner according to claim 7, it is characterised in that the burner also includes air collecting box, its connection To each afterburning wind snout, for providing aftercombustion wind.
CN201610972036.5A 2016-10-31 2016-10-31 Combustion method and combustion device for desulfuration and denitration of circulating fluid bed Pending CN106642089A (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107420925A (en) * 2017-07-07 2017-12-01 江苏盐环实业有限公司 A kind of environmentally friendly novel denitration desulphurization plant
CN111076214A (en) * 2019-11-25 2020-04-28 中国科学院工程热物理研究所 Preheating combustion ignition system and method, preheating combustion boiler equipment
CN111503645A (en) * 2019-01-31 2020-08-07 中国科学院工程热物理研究所 Flue gas denitration process and flue gas denitration device

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0049592A1 (en) * 1980-10-06 1982-04-14 The Energy Equipment Company Limited Fluidised bed combustion units
CN101240196A (en) * 2007-02-07 2008-08-13 中国科学院工程热物理研究所 Fine coal pressurization dense phase transporting bed gasification method and device
CN101670237A (en) * 2008-09-10 2010-03-17 中国科学院工程热物理研究所 Method and device for desulfurizing and dechlorinating flue gas of circulating fluidized bed
CN103471093A (en) * 2013-09-06 2013-12-25 中国科学院工程热物理研究所 Air distribution method of oxygen-enriched combustion of circulating fluidized bed
CN103884013A (en) * 2014-03-26 2014-06-25 东方电气集团东方锅炉股份有限公司 Combustion method and device of coupled environment-friendly fluidized bed boiler
CN105180160A (en) * 2015-08-26 2015-12-23 中国科学院工程热物理研究所 Combustion device capable of reducing emissions of nitric oxides of circulating fluidized bed

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0049592A1 (en) * 1980-10-06 1982-04-14 The Energy Equipment Company Limited Fluidised bed combustion units
CN101240196A (en) * 2007-02-07 2008-08-13 中国科学院工程热物理研究所 Fine coal pressurization dense phase transporting bed gasification method and device
CN101670237A (en) * 2008-09-10 2010-03-17 中国科学院工程热物理研究所 Method and device for desulfurizing and dechlorinating flue gas of circulating fluidized bed
CN103471093A (en) * 2013-09-06 2013-12-25 中国科学院工程热物理研究所 Air distribution method of oxygen-enriched combustion of circulating fluidized bed
CN103884013A (en) * 2014-03-26 2014-06-25 东方电气集团东方锅炉股份有限公司 Combustion method and device of coupled environment-friendly fluidized bed boiler
CN105180160A (en) * 2015-08-26 2015-12-23 中国科学院工程热物理研究所 Combustion device capable of reducing emissions of nitric oxides of circulating fluidized bed

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107420925A (en) * 2017-07-07 2017-12-01 江苏盐环实业有限公司 A kind of environmentally friendly novel denitration desulphurization plant
CN111503645A (en) * 2019-01-31 2020-08-07 中国科学院工程热物理研究所 Flue gas denitration process and flue gas denitration device
CN111076214A (en) * 2019-11-25 2020-04-28 中国科学院工程热物理研究所 Preheating combustion ignition system and method, preheating combustion boiler equipment
CN111076214B (en) * 2019-11-25 2021-03-09 中国科学院工程热物理研究所 Preheating combustion ignition system and method, preheating combustion boiler equipment

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Application publication date: 20170510