CN102233230A - Waste burning smoke purification process and purification system - Google Patents
Waste burning smoke purification process and purification system Download PDFInfo
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- CN102233230A CN102233230A CN2011101997127A CN201110199712A CN102233230A CN 102233230 A CN102233230 A CN 102233230A CN 2011101997127 A CN2011101997127 A CN 2011101997127A CN 201110199712 A CN201110199712 A CN 201110199712A CN 102233230 A CN102233230 A CN 102233230A
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Abstract
The invention discloses a waste burning smoke purification process. The process comprises a denitration step and an acid removal step. The denitration step comprises a combination step of a smoke recycling process and a selective non-catalytic reduction (SNCR) denitration process; the acid removal step comprises a primary acid removal step and a secondary acid removal step; and a spray drying method is used for removing acid in the primary acid removal step, and a suspension boiling method is used for removing acid in the secondary acid removal step. The generation of NOx is inhibited by the smoke recycling process, acidic gases in the smoke are removed by the secondary acid removal process, and the burned smoke is efficiently purified with relatively low operating cost. The deep purification effect of the smoke is achieved by organically combining several processes.
Description
Technical field
The present invention relates to a kind of discarded object as house refuse, medical waste, hazardous waste and industrial refuse etc. adopt grate furnace to burn the purification techniques of the flue gas that produces, particularly relate to a kind of wastes incineration flue gas technology and cleaning system thereof.
Background technology
Along with the development of urbanization process and industry, medical and health care system, the processing handling problems of all kinds of discarded objects more and more is subjected to people's attention.Waste incineration has obtained using more widely as one of means of the most effective disposal of refuse.
Because rubbish is the mixture of composition more complicated, with the house refuse is example, contains some organic compound and chloride, sulfide, fluoride etc., also contains the heavy metal of larger amt, show according to related data, the content of chromium is generally 100～450 g/t, and nickel is 50～200g/t, and copper is 450～2500 g/t, zinc is 900～3500g/t, lead is 750～2500g/t, and cadmium is 10～40 g/t, and mercury is 2～7g/t; Heavy metal in the rubbish removes small part and is present in the bottom ash with oxide and free state form except that a small amount of heavy metal when temperature garbage burns, and other heavy metal will be present in the flue gas with different shape.The waste incineration process also will produce HCl, SO
2, pollutant such as sour gas such as HF, NOx and dioxin is blended in the flue gas; Typical original concentration such as the following table of each pollutant in flue gas:
| Pollutant | Typical range | Pollutant | Typical range |
| HCL mg/Nm 3 | 200～1600 | Pb mg/Nm 3 | 1～50 |
| HF mg/Nm 3 | 0.5～5 | Hg mg/Nm 3 | 0.1～10 |
| SOx mg/Nm 3 | 20～800 | Cd mg/Nm 3 | 0.05～2.5 |
| NOx mg/Nm 3 | 90～500 | Cr+Cu+Mn+Ni mg/Nm 3 | 10～100 |
Pollutant in the above-mentioned flue gas can be discharged in the atmosphere after must reaching relevant criterion through purification.
In the existing garbage-incineration smoke purifying technology, the control of NOx is mainly contained with " burning control+reducing process " removal nitrogen oxide NOx, wherein, reducing process comprises SNCR SNCR and two kinds of modes of SCR SCR; The denitration efficiency of tradition SNCR technology is generally 30～80%, the escaping of ammonia＜10pmm; Denitration efficiency on engineering is generally 50%; The denitration efficiency of SCR technology is generally 50-90%, and the denitration efficiency on engineering is generally 60%.Adopt the SNCR technology separately, on engineering, continue to satisfy European Union's 2000 standards than difficulty; When adopting the SCR technology, for satisfying the reaction temperature of catalyst, the flue gas after generally dedusting, depickling need being handled is heated to about 200 ℃ once more, consumes bigger heat energy, and equipment investment and operating cost are all higher.
Treatment technology for sour gas such as the HCl in the flue gas, SOx, HF mainly contains dry process, spray-drying semidry process, wet processing and ciculation fluidized bed process.
The dry method depickling has dual mode, and a kind of is that dryness medicament (generally adopting calcium hydroxide) and sour gas react in reaction tower; Another kind is to spray into the dryness medicament in the flue before entering deduster, in flue and deduster surface and sour gas reaction.
Adopt the dry method deacidifying process, when calcium acid ratio was 2:1, the clearance of HCl can reach more than 95%, and the clearance of SOx can reach more than 90%.According to garbage burning factory flue gas pollutant original concentration reference value, the original concentration of HCl is at 200～1600 mg/Nm
3, SOx original concentration at 200～800 mg/Nm
3The time, the HCl concentration in the smoke evacuation should be at 10～80 mg/Nm
3, SOx concentration should be 20～80 mg/Nm
3, generally can not satisfy the discharge index of higher standard.
Calcium oxide (CaO) or calcium hydroxide (Ca (OH) are generally adopted in the depickling of spray-drying semidry method
2) be raw material, be prepared into aqua calcis (lime white).Utilize nozzle or rotary sprayer that aqua calcis (lime white) is sprayed in the reactor, form the minimum drop of particle diameter, react with sour gas.Moisture is evaporated fully in the course of reaction, so no waste water produces.When calcium acid when being 1.2, the HCl clearance of semidry method can reach more than 95%, the SOx clearance can reach about 80%, when calcium acid ratio is 2:1, it is nearly 97% that the clearance of HCL can reach, and the clearance of SOx can reach 95%, that is: the HCl concentration in the smoke evacuation can be controlled at 6～48 mg/Nm
3Between, SOx concentration can be controlled in 10～40 mg/Nm
3Between, lasting concentration of emission still can not satisfy European Union's 2000 standards.And along with the raising that deacidification efficiency requires, the consumption of absorbent is more and more uneconomical.The spray-drying semidry method has following shortcoming: 1) for obtaining deacidification efficiency preferably, require the lime white spraying system to keep atomizing effect preferably, cause system's power consumption to promote, the spraying system equipment attrition is more serious, and operation and maintenance cost is bigger; 2) when acidic gas concentration is higher in the raw flue gas, the straying quatity of lime white is subjected to the restriction of reaction tower outlet temperature, adjustable scope is less, need to improve the concentration of lime white, can cause that stock line stops up, aggravates problems such as nozzle wear, reduction atomizing effect, influences the depickling system to move continually and steadily and improve lime white concentration; 3) lime white that sprays into has part lime to fail fully to react with acidic gas in flue gas, is blended in the flying dust, together is collected discharge with flying dust, has caused bigger waste.
The wet method deacidifying process absorbs medicament and generally adopts caustic soda (NaOH) or sulfide lime solution (Ca(OH)
2).The absorbent solution that configures sprays into the wet scrubbing tower, reacts with acidic gas in flue gas.The waste water that scrubbing tower produces needs discharging after treatment, and the flue gas after the processing needs heating again.
Generally speaking, the clearance of the HCl of wet method can reach more than 99.5%, and the clearance of SOx can reach more than 99%.Can satisfy the standard limit of smog release requirement of European Union 2000.The subject matter of wet method depickling is to produce a large amount of waste water and absorbent product, in addition, owing in the flue gas higher salt content is arranged, causes follow-up flue gas heater fouling serious.
Ciculation fluidized method technology is emerging deacidifying flue gas technology of nearly more than ten years, adopts suspended pattern, makes absorbent at absorption reaction tower inner suspension, in many times of circulating ratio processes, with the acid contaminant haptoreaction in the flue gas; Bump between the lime particle, rub, constantly expose new unreacted lime surface, further fully react, realize depickling with acid contaminant.This technology and above-mentioned three technologies compare, and its combination property is better, but deacidification efficiency and semidry method are basic identical, can not satisfy higher fume emission requirement.
It is " charcoal absorption+sack cleaner " that heavy metal commonly used at present and dioxin are removed technology.Heavy metal and dioxin with solid-state, glue is solid-state and the form of gaseous state enters smoke processing system, be adsorbed in the flue gas and the active carbon on cloth bag surface in, together collect with flying dust.Adopt active carbon absorption technology, at the performance, straying quatity, the adsorption time that guarantee active carbon and use under the situation of high-quality sack cleaner, can satisfy the emission request of European Union's 2000 standards heavy metal and dioxin.
To main electrostatic precipitator or the sack cleaner of adopting of the control of the dust concentration in the flue gas.Electrostatic precipitator efficiency of dust collection and flue gas flow, the distribution of particle particle diameter, coherency, more relevant than factors such as resistance, battery lead plate distance, voltage and electric currents are removed the particle particle size range at 0.05-20um, and the removal efficient of particle diameter below 1.0um is lower.Total removal efficient generally can reach 95%-99.5%.By exemplary reference value 3g/Nm3, the kind of dust after the udst separation is about 15-150 mg/Nm3 in the raw flue gas dust content, and therefore, general independent use electrostatic precipitator can not satisfy existing flue gas of refuse burning discharge standard as dust suppression.
Sack cleaner is when making flue gas arrive filter bag, by based on sieving actoion, the short distance physical effect that has inertial collision, interception, diffusion simultaneously, and electrostatic effect under given conditions and gravitational effect etc., carry out gas solid separation, particle is trapped on the filter bag, again with regularly or hinder control mode surely, by the filter of effect removing controls of dust such as vibration, winding-up.The particulate matter removal efficiencies of particle diameter in the 0.2-0.4um scope is lower.Total efficiency of dust collection reaches more than 99.9%.Discharging dust contained flue gas concentration generally can be controlled in 10mg/Nm
3Below, can satisfy the soot emissions index of European Union's 2000 standards.
In order to satisfy the flue gas of refuse burning discharge standard improve constantly, particularly solve the problem that the depickling system effectiveness is low, cost is high, must employing can satisfy more advanced, more economical, flue gas New Process for Treatment more efficiently.
Summary of the invention
One object of the present invention is to provide a kind of advanced person, more economical, more efficient wastes incineration flue gas technology.
Another object of the present invention is to provide a kind of wastes incineration flue gas system, it can be under the situation than low operating cost, effectively reduce the waste incineration process and produce material with hazardous waste feature, reduce the concentration of all kinds of sour gas pollutants in the discharging flue gas, satisfy European Union's 2000 environmental emission standards.
For achieving the above object, technical solution of the present invention is:
The present invention is a kind of wastes incineration flue gas technology, and it comprises denitrification step and deacidification step.
Described denitrification step comprises the integrating step of smoke gas recirculating technology and SNCR denitrating technique; Circulating flue gas in the described smoke gas recirculating technology is taken between the superheater and economizer of waste heat boiler, and flue-gas temperature herein is 300～400 ℃, and flue gas recycled is delivered to the dryer section bellows of grate furnace through the inlet pitch by blower fan; Described deacidification step comprises one-level deacidification step and secondary deacidification step; Described one-level deacidification step is the spray drying process deacidification, and its reactant directly enters secondary deacidification step; Secondary deacidification step is suspend fluidized method deacidification, wherein the major part of suspend fluidized absorbent is participated in the lime that reacts from the reactant and the part of lime that sprays in the first order reaction tower and flue gas, another part comes the self-loopa returning charge, also has than the fresh active carbon of small part and the mixture of nitre ashes.
The present invention is an a kind of wastes incineration flue gas system, and it comprises incinerator, absorbent preparation and feed system, spray-drying reaction tower, suspend fluidized reaction tower, material-returning device, active carbon and pulverized limestone injection system, sack cleaner, air-introduced machine; The exhaust pass of described incinerator is sent flue gas into the spray-drying reaction tower by the inlet of pipeline connection spray-drying reaction tower; Preparation of described absorbent and feed system are connected the inlet of spray-drying reaction tower by pipeline, and the outlet of spray-drying reaction tower connects suspend fluidized reaction tower bottom inlet, and the top of suspend fluidized reaction tower exports connection circulation material-returning device; Described active carbon and lime injection system connect with suspend fluidized reaction tower; The returning charge outlet of described material-returning device connects with suspend fluidized reaction tower, and its exhanst gas outlet is connected with sack cleaner.
Spray-drying reaction tower bottom is not provided with conventional ash discharging hole, and the outlet connection of spray-drying reaction tower bottom enters suspend fluidized reaction tower, and flue gas and solid reactant and flying dust together enter suspend fluidized reaction tower by the outlet of its bottom.
After adopting such scheme, technology of the present invention has the following advantages:
1, by integrated multiple flue gas treating process,, satisfies the discharge index of European Union's 2000 standards with most economical means comprehensively; By reducing the acidic gas concentration in the incineration flue gas, and remove the reaction system technology of sour gas pollutant, the flue gas of emission abatement in conjunction with high efficiency.Its feature is at first passed through, and smoke gas recirculating technology suppresses the generation of NOx, again by the secondary deacidifying process, removes acidic gas in flue gas, with lower operating cost, purifies incineration flue gas efficiently.It is characterized in that combination, reach the effect of flue gas deep purifying by several technologies.
2, adopt independently high temperature flue gas recycled garbage drying and dilution flue gas, reduce the primary air flow that is used for drying garbage and burning in the traditional handicraft, give full play to the combustion-supporting of secondary wind and to the perturbation action of flue gas, by control to first and second air quantity and proportioning thereof, reduce the oxygen content in the flue gas effectively, thereby suppress the generation of NOx.It is characterized by a high temperature flue gas recycled and insert grate furnace dryer section bellows, reduce the primary air flow that is used for drying garbage, reduce excess air factor; In dry rubbish efficiently, circulating flue gas has played the diluting effect to combustion product gases.
3, adopt the secondary smoke process for purifying, can remove the acid contaminant in the flue gas efficiently, under lower operating cost situation, satisfy strict standard limit of smog release.It is characterized by flue gas through secondary depickling purified treatment.
4, two kinds of organically combinations of deacidifying flue gas technology, give full play to two kinds of deacidification technologies in the characteristics that respectively HCl and SOx clearance respectively had superiority, improve to remove the overall efficiency of acid contaminants such as HCl in the flue gas and SOx, thereby realize high efficiency, purify flue gas at low cost.It is characterized by and scientifically combine two kinds of different flue gas treating process, the reacting rear material of first order reactor is applied to second level reactor, participate in second level deacidification.
5, owing to adopt the secondary deacidifying process, can adjust the calcium acid ratio of every order reaction process economically, the efficient of reasonable distribution secondary depickling reaction, the consumption of reduction absorbent under the lower situation of total lime excess coefficient, is realized higher deacidification efficiency.
6, owing to reduced the consumption of absorbent lime, cause final flying dust amount to descend, save the operating cost that is used for the flying dust processing.
Wastes incineration flue gas of the present invention system has the following advantages:
1), the present invention is a kind of new garbage-incineration smoke purifying combination technique, can satisfy strict European Union's 2000 environmental emission standards.
2), the present invention adopts unique smoke gas recirculating technology, can suppress the generation of NOx efficiently, reduces excess air factor, reduces smoke discharge amount; Be aided with the denitration of SNCR system, can satisfy the stricter requirement of discharged nitrous oxides concentration with lower operating cost.
3), in conjunction with two kinds of deacidification technology different to HCl respectively characteristics with the SOx clearance, improve the overall efficiency of acid contaminants such as the HCl that removes in the flue gas and SOx, thereby realize high efficiency, purify flue gas at low cost.
4) in the first order reaction tower in the reacted solid material, the excessive and unreacted Ca of part (OH)
2To in the reaction tower of the second level, further react, thereby improve the utilization rate of absorbent, reduce the consumption that flue gas is handled adsorbent, reduce the generation of flying dust simultaneously, and save flue gas and handle and the flying dust processing cost with sour gas.
The present invention is further illustrated below in conjunction with the drawings and specific embodiments.
Description of drawings
Fig. 1 is a system schematic of the present invention.
The specific embodiment
One, technology
The present invention is a kind of wastes incineration flue gas technology, and it comprises denitrification step and deacidification step.
Described denitrification step comprises flue gas recirculation step and SNCR denitrification step; Circulating flue gas in the described flue gas recirculation step is taken between the superheater and economizer of waste heat boiler, and flue-gas temperature herein is 300～400 ℃, and flue gas recycled is delivered to the dryer section bellows of grate furnace through the inlet pitch by blower fan.A wind that is used for waste incineration is no longer toward the dryer section air feed, only for burning zone and burning segment; Adopt this flue gas recirculation mode, gas cleaning there are three effects: 1) reduce primary air flow, the primary air that is used for garbage drying in the traditional handicraft is replaced by the high temperature flue gas recycled, more help bringing into play in the auxiliary air control flue gas oxygen content and to the perturbation action of combustion product gases; Realize low air ratio burning; 2) because the oxygen content of flue gas descends, help reducing the generation of NOx; Related experiment proves, the every decline 1% of the oxygen content in the flue gas, NOx about 10mg/Nm that will descend
3; 3) suppress the generation of NOx effectively, have data to show, account for the combustion air ratio and be 15% flue gas recycled, the NOx generation that reduces 50%; Like this, by the flue gas recirculation mode, be aided with the SNCR denitrating technique, the discharge standard that can satisfy fully in European Union's 2000 standards NOx requires and has now the standard that best practicable technology can reach.
Described deacidification step comprises one-level deacidification step and secondary deacidification step; Described one-level deacidification step is the spray drying process deacidification, and its reactant, flying dust and flue gas together enter secondary deacidification step; Secondary deacidification step is suspend fluidized method deacidification, and its reactant directly enters secondary deacidification step; Wherein the major part of suspend fluidized absorbent is participated in the lime that reacts from the reactant and the part of lime that sprays in the first order reaction tower and flue gas, and another part comes the self-loopa returning charge, also has the fresh active carbon of small part and the mixture of nitre ashes.
Technological work principle of the present invention:
At first, suppress the growing amount of NOx, reduce the NOx concentration in the flue gas, pass through conventional SNCR technology denitration again, make the NOx concentration in the flue gas meet strict European Union's 2000 standards by the effect of flue gas recycled.
The boiler export flue gas, the inlet by first order reaction tower enters, and does the backspin motion after the deflector effect, with the lime slurry haptoreaction of atomizing, simultaneously, and flue gas heat release cooling, lime white droplet moisture evaporates rapidly; Solid granulates and a small amount of unreacted lime that course of reaction generates, and original flue dust in the flue gas with the flue gas Venturi tube below the exhanst gas outlet at the bottom of reaction tower and the suspend fluidized reaction tower together, enter the suspend fluidized reaction tower in the second level.For preventing that solid particle in the flue gas from building up in reaction tower bottom, bonding, can one mechanical ash discharge or breaker be set in the reaction tower bottom.
Enter the solid material in the suspend fluidized reaction tower, with recycle stock and new fresh lime together, in reaction tower, form suspend fluidized bed, by with the strong mass-and heat-transfer process of flue gas, carry out sufficient combination reaction with the acid contaminant in the flue gas, further remove acidic gas in flue gas.
Usually, in spray-drying deacidification course of reaction, under suitable reaction temperature, when calcium acid when being 1.2, the HCl clearance can reach more than 95%, the SOx clearance can reach about 80%.Therefore, calculate as can be known according to the original acidic gas concentration of flue gas, spray-drying reaction tower outlet acidic gas in flue gas concentration can be respectively: HCl=10～80 mg/Nm
3; SOx=40～160 mg/Nm
3
In suspend fluidized reaction tower, the solid suspension particle constantly bumps, rubs, the new surface that makes solid particle constantly expose the unreacted calcium hydroxide, with the new fresh lime of part together, with acidic gas in flue gas combination reaction taking place once more, reaches the effect of degree of depth deacidification.Adopt suspend fluidized reaction process, the removal efficient of HCl and SOx all can reach more than 90%, and promptly through the flue gas after the secondary depickling, the concentration of HCl can be lower than 8 mg/Nm
3; The concentration of SOx is lower than 16 mg/Nm
3; Satisfy European Union's 2000 standards fully.
Secondary deacidification main chemical reactions process is:
2HCl+Ca(OH)
2→CaCl
2+H
2O
SO
2+Ca(OH)
2→CaSO3+H
2O
2CaSO
3+O
2→2CaSO
4
SO
3+Ca(OH)
2→CaSO
4+H
2O
Dioxin organic matter in the flue gas and heavy metal remove acid tower and flue at flue gas by the second level, and the time by sack cleaner filter bag surface, together from flue gas, separated by charcoal absorption and flying dust, enter atmosphere by air-introduced machine through the flue gas that purifies.
Two, system
As shown in Figure 1, the present invention is an a kind of wastes incineration flue gas system, and it comprises incinerator 1, absorbent preparation and feed system 2, spray-drying reaction tower 3, suspend fluidized reaction tower 4, material-returning device 5, active carbon and pulverized limestone injection system 6, sack cleaner 7, air-introduced machine 8; The exhaust pass of described incinerator 1 is sent flue gas into spray-drying reaction tower 3 by the inlet of pipeline connection spray-drying reaction tower 3;
Described absorbent prepares the inlet that is connected spray-drying reaction tower 3 with feed system 2 by pipeline, 3 outlets of spray-drying reaction tower connect suspend fluidized reaction tower 4 bottoms inlet, the top outlet of suspend fluidized reaction tower 4 connects circulation material-returning device 5(or has the sack cleaner of material-returning device), described active carbon and lime injection system 6 connect with suspend fluidized reaction tower 4; The exhanst gas outlet of described material-returning device 5 is connected with sack cleaner 7; Its ash discharging hole is connected with suspend fluidized reaction tower 4 by returning charge bucket (returning charge outlet).
Described spray-drying reaction tower 3 constitutes secondary depickling system jointly with suspend fluidized reaction tower 4.Spray-drying reaction tower 3 bottoms are not provided with conventional ash discharging hole, and the outlet connection of spray-drying reaction tower 3 bottoms enters suspend fluidized reaction tower 4, and flue gas and solid reactant and flying dust together enter suspend fluidized reaction tower 4 by the outlet of its bottom.The flue gas that waste incineration produces is through spray-drying reaction tower 3 and suspend fluidized reaction tower 4, form flue gas and dust, reacted product and not absorption, the adsorbent of complete reaction, during by material-returning device 5, the part particulate material falls into the returning charge bucket of material-returning device 5, and flue gas and part fine dust enter the sack cleaner 7 that links with material returning device; Purification flue gas after sack cleaner 7 filters enters atmosphere by air-introduced machine 8.
The flue 11, the flue gas recirculation system 12 that comprise incinerator in the described incinerator 1.Described flue gas recirculation system 12 comprises high-temperature flue gas inlet scoop, recirculation blower, flue gas recycled control baffle plate, reduced air inlet etc.
Described absorbent preparation and feed system 2 comprise: lime silo, metering device, lime white blending tank, lime white storage tank, lime white conveyance conduit, lime white delivery pump etc.;
Described active carbon and pulverized limestone injection system 6 comprise: spray blower fan, active carbon metering device, pulverized limestone metering device, conveyance conduit, nozzle etc.;
Described spray-drying reaction tower 3 comprises that gas approach, guiding device, lime white nozzle, reaction tower bottom are provided with exhanst gas outlet, links with suspend fluidized reaction tower inlet;
Described suspend fluidized reaction tower 4 comprises: compositions such as gas approach, venturi accelerating sections, reaction tower body, pulverized limestone and active carbon entrance, returning charge inlet, humidification temperature adjustment nozzle, exhanst gas outlet, exhanst gas outlet inserts exhanst gas outlet.
Described material-returning device 5 can be mechanical type or centrifugal material-returning device, also can be mounted in the material-returning device of sack cleaner bottom; Returning charge is transfused to suspend fluidized reaction tower
Claims (3)
1. wastes incineration flue gas technology is characterized in that: it comprises denitrification step and deacidification step;
Described denitrification step comprises the denitrification step that combines of smoke gas recirculating technology and SNCR technology; Circulating flue gas in the described smoke gas recirculating technology is taken between the superheater and economizer of waste heat boiler, and flue-gas temperature herein is 300～400 ℃, and flue gas recycled is delivered to the dryer section bellows of grate furnace through the inlet pitch by blower fan; Described deacidification step comprises one-level deacidification step and secondary deacidification step; Described one-level deacidification step is the spray drying process deacidification, and its reactant directly enters secondary deacidification step; Secondary deacidification step is suspend fluidized method deacidification, the lime that wherein suspend fluidized absorbent is not mainly participated in reaction from the reactant and the part of lime that sprays in the first order reaction tower and flue gas, another part comes the self-loopa returning charge, also has the fresh active carbon of part and the mixture of nitre ashes.
2. the wastes incineration flue gas system of a technological design according to claim 1, it is characterized in that: it comprises incinerator, absorbent preparation and feed system, spray-drying reaction tower, suspend fluidized reaction tower, material-returning device, active carbon and pulverized limestone injection system, sack cleaner, air-introduced machine; The exhaust pass of described incinerator is sent flue gas into the spray-drying reaction tower by the inlet of pipeline connection spray-drying reaction tower; Preparation of described absorbent and feed system are connected the inlet of spray-drying reaction tower by pipeline, and the outlet of spray-drying reaction tower connects suspend fluidized reaction tower bottom inlet, and the top of suspend fluidized reaction tower exports connection circulation material-returning device; Described active carbon and lime injection system connect with suspend fluidized reaction tower; The returning charge outlet of described material-returning device connects with suspend fluidized reaction tower, and its exhanst gas outlet is connected with sack cleaner.
3. wastes incineration flue gas according to claim 1 system is characterized in that: the outlet of described spray-drying reaction tower bottom connects and enters suspend fluidized reaction tower.
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|---|---|---|---|
| CN2011101997127A CN102233230A (en) | 2011-07-18 | 2011-07-18 | Waste burning smoke purification process and purification system |
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|---|---|---|---|
| CN2011101997127A CN102233230A (en) | 2011-07-18 | 2011-07-18 | Waste burning smoke purification process and purification system |
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| CN112902193A (en) * | 2021-02-23 | 2021-06-04 | 山东大学 | Garbage incinerator system and catalytic removal method for garbage incineration flue gas purification hearth |
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| CN104923013A (en) * | 2015-05-25 | 2015-09-23 | 山东百川同创能源有限公司 | Fume treatment technique in process of treating biomass solid waste and hazardous waste |
| CN105435615A (en) * | 2015-12-15 | 2016-03-30 | 盐城市兰丰环境工程科技有限公司 | Method for recycling cement kiln SNCR denitrification reducing agent |
| CN105782991A (en) * | 2016-05-17 | 2016-07-20 | 上海市环境工程设计科学研究院有限公司 | Efficient and clean incinerator |
| CN105782991B (en) * | 2016-05-17 | 2019-02-01 | 上海市环境工程设计科学研究院有限公司 | High-efficiency cleaning incinerator |
| CN105841164A (en) * | 2016-06-04 | 2016-08-10 | 上海市环境工程设计科学研究院有限公司 | Garbage incinerator for extracting headspace hot flue gases at burned-out zone and introducing into drying zone |
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| CN106765242A (en) * | 2016-11-22 | 2017-05-31 | 上海交通大学 | A kind of combined biomass clean and effective combustion system |
| CN106642075A (en) * | 2016-12-21 | 2017-05-10 | 天津市星拓科技发展有限公司 | Ash settling, denitrifying and cooling all-in-one machine for flue gas of straw combustion boiler and implementation method |
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| CN110508076A (en) * | 2019-07-30 | 2019-11-29 | 重庆科技学院 | Ganlei's garbage flying ash multistage purification control system |
| CN110715287A (en) * | 2019-10-29 | 2020-01-21 | 辽宁绿源能源环保科技集团有限责任公司 | Layer-combustion boiler structure and boiler desulfurization and denitrification method |
| CN111495136A (en) * | 2020-04-23 | 2020-08-07 | 生态环境部华南环境科学研究所 | Full-flow low-temperature dry-method deep treatment system for waste heat treatment flue gas |
| CN112902193A (en) * | 2021-02-23 | 2021-06-04 | 山东大学 | Garbage incinerator system and catalytic removal method for garbage incineration flue gas purification hearth |
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