CN111203065A - Waste incineration flue gas near-zero emission treatment system and process - Google Patents
Waste incineration flue gas near-zero emission treatment system and process Download PDFInfo
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- CN111203065A CN111203065A CN202010182412.7A CN202010182412A CN111203065A CN 111203065 A CN111203065 A CN 111203065A CN 202010182412 A CN202010182412 A CN 202010182412A CN 111203065 A CN111203065 A CN 111203065A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 75
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000004056 waste incineration Methods 0.000 title claims abstract description 23
- 230000008569 process Effects 0.000 title claims abstract description 18
- 239000002699 waste material Substances 0.000 claims abstract description 16
- 239000010881 fly ash Substances 0.000 claims description 87
- 238000006243 chemical reaction Methods 0.000 claims description 52
- 239000000428 dust Substances 0.000 claims description 52
- 239000007788 liquid Substances 0.000 claims description 45
- 239000007921 spray Substances 0.000 claims description 30
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 16
- 238000009825 accumulation Methods 0.000 claims description 16
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 14
- 238000001816 cooling Methods 0.000 claims description 13
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 12
- 239000000920 calcium hydroxide Substances 0.000 claims description 12
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 12
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 11
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 7
- 230000032683 aging Effects 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 6
- 239000003245 coal Substances 0.000 claims description 5
- 230000004913 activation Effects 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 230000003213 activating effect Effects 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 2
- 239000012717 electrostatic precipitator Substances 0.000 claims description 2
- 238000001035 drying Methods 0.000 claims 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims 1
- 238000004891 communication Methods 0.000 claims 1
- 239000003344 environmental pollutant Substances 0.000 abstract description 11
- 231100000719 pollutant Toxicity 0.000 abstract description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 7
- 239000004744 fabric Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 5
- 239000000376 reactant Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 238000001994 activation Methods 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 239000003153 chemical reaction reagent Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 230000007420 reactivation Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229920002430 Fibre-reinforced plastic Polymers 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000011151 fibre-reinforced plastic Substances 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000004071 soot Substances 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/68—Halogens or halogen compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a near-zero emission treatment system and process for waste incineration flue gas, which belong to the technical field of waste incineration flue gas treatment and are used for treating flue gas generated by a waste incinerator. The treatment system can comprehensively treat the waste incineration flue gas with different pollutant contents, the whole system is stable and reliable in operation, and the discharged flue gas can reach the near-zero emission standard.
Description
Technical Field
The invention belongs to the technical field of waste incineration flue gas treatment, and particularly relates to a waste incineration flue gas near-zero emission treatment system and process.
Background
The urban garbage problem becomes one of the biggest problems restricting the development of the current cities, the garbage incineration treatment technology conforms to the garbage treatment policy of harmlessness, reduction and reclamation, and has the advantages of high treatment speed, good volume reduction effect, small occupied area, small environmental influence and the like, and the garbage incineration treatment technology is rapidly developed at home and abroad in recent years. However, the flue gas generated after the domestic garbage is incinerated contains a large amount of pollutants such as smoke dust, acid gas, heavy metal, dioxin and the like, the content of various pollutants is high and unstable, and serious harm is caused to the environment if the pollutants are not effectively treated. Therefore, the harmless treatment of the household garbage incineration flue gas becomes a key problem concerned by the public, and a near zero emission flue gas system and process are the current research focus and research and development hotspots.
At present, domestic garbage incineration plants commonly adopt a semidry deacidification technology to remove acid gas in smoke, and can basically meet the requirements of the current national environmental protection emission indexes. However, in order to further realize the reduction, recycling and harmless treatment of the garbage, and further reduce the emission index of acidic pollutants in the waste incineration flue gas, the semi-dry deacidification technology needs to have breakthrough progress. Meanwhile, although the wet deacidification technology can efficiently remove acidic pollutants in the flue gas, the generated wastewater is difficult to treat, and the traditional dry deacidification technology has the problems of poor deacidification effect, large consumption of hydrated lime and activated carbon, large generation amount of incineration fly ash and the like.
Disclosure of Invention
In view of this, the invention aims to provide a near-zero emission treatment system and process for waste incineration flue gas, so as to reduce the content of harmful pollutants in the flue gas, improve the comprehensive treatment effect of waste incineration flue gas with different pollutant contents, and effectively reduce the harm of the incineration flue gas to the environment.
In order to achieve the purpose, the invention provides the following technical scheme:
the invention provides a near-zero emission treatment system for waste incineration flue gas, which is used for treating the flue gas generated by a waste incinerator and comprises an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, a coal economizer, a spray tower, a dry mixer, a cloth bag dust collector, an induced draft fan, a wet reaction tower and a chimney which are sequentially arranged according to a flue gas treatment process, wherein the SCR reaction tower is connected with an ammonia water storage tank, the dry mixer is connected with an active carbon storage tank, a slaked lime storage tank and a fly ash slaking bin, the fly ash slaking bin is connected with the cloth bag dust collector, the spray tower is connected with a cooling water storage tank and a waste liquid collecting box, and the wet reaction tower is connected.
Further, the dry mixer is in a U-shaped tubular structure, and the upper part of the inner side of the U-shaped bottom of the dry mixer is connected with the fly ash curing bin.
Further, the dry mixer is provided with a necking cone section at the inlet side near the U-shaped bottom thereof.
Further, the fly ash curing bin comprises a bin barrel and a rotary drum arranged in the bin barrel, and the fly ash curing bin sprays the fly ash after curing activation back into the dry mixer through a spiral conveying device connected with the bin barrel.
Furthermore, the treatment system also comprises a fly ash storage tank which is connected with the electrostatic dust collector, the SCR reaction tower, the economizer, the spray tower and the bag-type dust collector and is used for receiving respective produced fly ash.
Further, the wet reaction tower is provided with a cooling absorption part and a dehumidifying part which are communicated from bottom to top, the cooling absorption part and the dehumidifying part are respectively provided with an atomizer and a liquid accumulation area which are respectively connected, and the two liquid accumulation areas are respectively connected with a sodium hydroxide solution storage tank and a waste liquid collecting box; the cooling absorption portion is connected with the induced draft fan, the dehumidifying portion is provided with a liquid drop separator above a liquid accumulation area in the dehumidifying portion, and the top of the dehumidifying portion is connected with the chimney.
The invention also provides a near-zero emission treatment process for waste incineration flue gas, which adopts the near-zero emission treatment system for waste incineration flue gas and comprises the following steps:
1) the flue gas produced by the incinerator sequentially passes through an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, a coal economizer, a spray tower, a dry mixer, a bag-type dust collector and a wet reaction tower and then is discharged by a chimney;
2) collecting fly ash produced in an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, an economizer, a spray tower and a bag-type dust collector by a fly ash storage tank;
3) leading out the fly ash produced by the bag-type dust remover, activating the fly ash by a fly ash curing bin, and spraying the fly ash back to the dry-method mixer;
4) and (4) conveying the accumulated liquid produced by the two accumulated liquid areas of the wet reaction tower into the spray tower.
The invention has the beneficial effects that:
1. the treatment system disclosed by the invention adopts the combination of electrostatic dust removal, SCR, dry deacidification, cloth bag dust removal and wet deacidification, can comprehensively treat the waste incineration flue gas with different pollutant contents, is stable and reliable in operation, and can reach the near-zero emission standard.
2. The invention adopts the process of combining electrostatic dust collection and cloth bag dust collection, and effectively reduces the content of particulate matters and fly ash in the flue gas.
3. The treatment system of the invention uses the fly ash slaking reactivation technology, effectively improves the dry reaction efficiency, and reduces the consumption of slaked lime and the generation of fly ash.
4. The dry mixer of the treatment system can form high-speed turbulent flow in the pipeline body so as to solve the problem of fully mixing the smoke and the reactant in the pipeline body.
5. The treatment system of the invention arranges the coal economizer between the SCR reaction tower and the spray tower, aiming at improving the energy balance of the incineration plant and effectively improving the power generation efficiency.
6. The treatment system is additionally provided with a wet type reaction tower at the tail part, in order to maintain the balance of the salt concentration in the reaction tower, the waste water in the liquid accumulation area can be discharged into the spray tower to be used as cooling water, and the system has no waste water discharge.
Additional advantages, objects, and features of the invention will be set forth in part in the description which follows and in part will become apparent to those having ordinary skill in the art upon examination of the following or may be learned from practice of the invention. The objectives and other advantages of the invention may be realized and attained by the means of the instrumentalities and combinations particularly pointed out hereinafter.
Drawings
For the purposes of promoting a better understanding of the objects, aspects and advantages of the invention, reference will now be made to the following detailed description taken in conjunction with the accompanying drawings in which:
FIG. 1 is a schematic diagram of the present processing system;
FIG. 2 is a schematic flow diagram of the present processing system;
reference numerals: the system comprises a garbage incinerator 1, an electrostatic precipitator 2, an SCR (selective catalytic reduction) reaction tower 3, an economizer 4, a spray tower 5, a dry mixer 6, a bag-type dust remover 7, an induced draft fan 8, a wet reaction tower 9, a chimney 10, a fly ash curing bin 11, an ammonia water storage tank 12, an activated carbon storage tank 13, a slaked lime storage tank 14, a sodium hydroxide solution storage tank 15, a fly ash storage tank 16, a cooling water storage tank 17 and a waste liquid collecting box 18.
Detailed Description
The present invention will be further described with reference to the following embodiments. Wherein the showings are for the purpose of illustration only and are shown by way of illustration only and not in actual form, and are not to be construed as limiting the present patent; to better illustrate the embodiments of the present invention, some parts of the drawings may be omitted, enlarged or reduced, and do not represent the size of an actual product; it will be understood by those skilled in the art that certain well-known structures in the drawings and descriptions thereof may be omitted.
As shown in fig. 1, the near-zero emission treatment system for waste incineration flue gas in this embodiment is used for treating flue gas generated by a waste incinerator 1, and includes an electrostatic dust collector 2, an SCR reaction tower 3, an economizer 4, a spray tower 5, a dry mixer 6, a bag-type dust collector 7, an induced draft fan 8, a wet reaction tower 9 and a chimney 10, which are sequentially arranged according to a flue gas treatment process, the SCR reaction tower 3 is connected with an ammonia water storage tank 12, the dry mixer 6 is connected with an activated carbon storage tank 13, a slaked lime storage tank 14 and a fly ash slaking bin 11, the fly ash slaking bin is connected with the bag-type dust collector, the system comprises a spraying tower 5, a wet reaction tower 9, a cooling water storage tank 17, a waste liquid collection tank 18, a sodium hydroxide solution storage tank 15 and a waste liquid collection tank 18, wherein the spraying tower 5 is used for leading out part of fly ash collected by a bag-type dust collector for curing and activating, the wet reaction tower 9 is connected with the waste liquid collection tank 18, and waste liquid generated by the wet reaction tower 9 is collected by the waste liquid collection tank 18 and then sent to the spraying tower 5; a fly ash storage tank 16 which is connected with the electrostatic dust collector, the SCR reaction tower, the economizer, the spray tower and the bag-type dust collector and is used for receiving fly ash generated respectively; and a fly ash curing bin 11 connected with the bag-type dust collector and used for receiving fly ash generated by the bag-type dust collector, wherein the fly ash curing bin sprays the fly ash after being cured and activated back into the dry-method mixer.
With reference to fig. 2, the process of the waste incineration flue gas near-zero emission treatment system mainly comprises the following steps:
1) the flue gas produced by the incinerator sequentially passes through an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, a coal economizer, a spray tower, a dry mixer, a bag-type dust collector and a wet reaction tower and then is discharged by a chimney;
2) collecting fly ash produced in an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, an economizer, a spray tower and a bag-type dust collector by a fly ash storage tank;
3) leading out a part of fly ash produced by the bag-type dust remover, and spraying the fly ash back into the dry-method mixer after the fly ash is cured and activated by a fly ash curing bin;
4) and (4) gradually sending the accumulated liquid produced by the wet reaction tower into the spray tower.
Specifically, hot flue gas discharged from the garbage incinerator 1 directly enters the electrostatic dust collector 2, and the main function of the electrostatic dust collector is to prevent large particles from entering the SCR reaction tower 3, so that the blockage of the SCR reactor and the catalyst poisoning are effectively inhibited; the number of electrodes of the electrostatic dust collector can be designed according to the dust content of the flue gas, and the electrodes are emitted to enable particles in the flue gas to be in contact with the particlesCharging the particulate matter, thereby causing the particulate matter to flow toward the collecting electrode; the bottom of the electrostatic dust collector 2 is provided with a particle collecting device which crushes particles and sends the crushed particles into a fly ash storage tank 16; the flue gas after dust removal enters an SCR reaction tower 3; the reaction reagent in the SCR reaction tower 3 is ammonia water, the prepared ammonia water is stored in an ammonia water storage tank 12, the ammonia water is sprayed through a specially designed regulating valve and a specially designed nozzle, the ammonia water is mixed with compressed air in the spraying process to atomize the ammonia water, guide vanes are arranged in a guide pipe of the SCR reactor 3 to fully mix flue gas and the atomized ammonia water, so that the flue gas and the atomized ammonia water uniformly enter the SCR reaction tower 3, and hot flue gas can provide certain heat for the ammonia water to evaporate the ammonia water; meanwhile, a plurality of catalytic reaction layers are arranged in the SCR reaction tower 3, each layer comprises a plurality of catalytic reaction modules, the catalytic reaction modules are tightly distributed on the cross section of the whole SCR reaction tower, and a special honeycomb-shaped channel containing a catalyst is solidified on each catalytic reaction module; the optimal reaction temperature is 268 ℃, and pollutants at the outlet of the SCR reaction tower comprise certain amounts of NOx, HCl and SO2And NH3Etc.; then, the flue gas from the SCR reaction tower enters an economizer 4, which mainly has the functions of improving the energy balance of a burning plant and improving the heat energy utilization efficiency of a power plant; the temperature of the outer surface of the pipeline of the internal heat exchanger is above 120 ℃, and the temperature of inlet/outlet feed water is 120 ℃/165 ℃; a soot blower is arranged in the economizer 4 to blow off fly ash outside the pipeline, a fly ash collecting device is arranged at the bottom of the heat exchanger, and the collected fly ash is sent into a fly ash storage tank 16; then, the flue gas at the outlet of the economizer 4 enters a spray tower 5, water is atomized through the spray tower, the flue gas is treated, and the spray tower is provided with a self-operated differential pressure regulating valve, so that the temperature of the flue gas entering the dry mixer is kept consistent; a cooling water storage tank 17 is arranged outside the spray tower, so that the feed water can uniformly enter the spray tower; then, the flue gas at the outlet of the spray tower 5 is sent into a dry mixer 6, the dry mixer is mainly a section of U-shaped square tube, numerical simulation is carried out on the flowing process in the dry mixer according to the actual flue gas flow velocity, and the optimal section size and the bending radius of a flow channel are obtained, so that the flue gas and the reactant in the dry mixer can be fully mixed to form high-speed turbulent flow; the reactant comprisesGasifying the reactivated fly ash, unreacted powdered hydrated lime and activated carbon powder; then, the flue gas at the outlet of the dry mixer 6 enters a bag-type dust remover 7, and the circular filter bag is uniformly arranged in the whole bag-type dust remover through numerical calculation, so that the flue gas uniformly flows in the bag-type dust remover, and the temperature of the flue gas entering the bag-type dust remover is close to the acid dew point of the flue gas, so that the filter bag needs to use a special corrosion-resistant material; arranging a soot blower and a fly ash collecting device in the bag-type dust collector, wherein one part of the collected fly ash enters a fly ash curing bin 11, and the other part of the collected fly ash enters a fly ash storage tank 16; determining the fly ash circulation rate of the collected fly ash according to the content of pollutants in the flue gas, and then distributing the fly ash into the fly ash curing bin 11 and the fly ash storage tank 16 according to the proportion of the fly ash; then, the flue gas at the outlet of the bag-type dust collector 7 enters an induced draft fan 8, and the induced draft fan mainly compensates the pressure drop generated in the flue gas treatment process; then, the flue gas from the outlet of the induced draft fan 8 enters a wet reaction tower 9, which mainly comprises two parts: the cooling absorption part and the dehumidifying part are communicated with each other and are provided with an atomizer and a liquid accumulation area; a cooling absorption part: the flue gas enters a wet reaction tower and firstly passes through a cooling absorption part, a condensate atomizer is arranged in the cooling absorption part, the condensate in a condensate accumulation area of the cooling absorption part is atomized into small droplets to be fully mixed with the high-temperature flue gas, and part of HCl and SO in the absorbed flue gas2And the liquid after reaction circularly enters the liquid accumulation area; a dehumidification part: the cooled flue gas enters a dehumidifying part, a condensate atomizer is arranged at the dehumidifying part, condensate is sprayed from top to bottom, the flue gas flows from bottom to top, and a filler region in the middle is filled with fiber reinforced plastics, so that the contact area between the flue gas and alkaline liquid is increased; the dehumidifying part is provided with a liquid drop separator, the flue gas treated by the dehumidifying part contains small liquid drops, the small liquid drops are condensed on the surface of the flue gas when flowing through the liquid drop separator, the small liquid drops are continuously condensed into larger liquid drops in the flue gas, then the liquid drops are dropped into a filler area filled with fiber reinforced plastics and then enter liquid accumulation areas of the cooling absorbing part and the dehumidifying part, a sodium hydroxide solution is pumped to liquid accumulation areas of the cooling absorbing part and the dehumidifying part, the pH value of the liquid accumulation is adjusted, the liquid accumulation is continuously circulated in the wet tower until the salinity of the liquid accumulation reaches a certain value and then discharged into a waste liquid collecting box, and the liquid accumulation circulates in each areaThe alkali liquor is used for adjusting the pH value of each accumulated liquid, and the waste water in the waste liquid collecting box can be pumped to the spray tower to cool the flue gas; finally, the purified flue gas is discharged to the atmosphere through a chimney 10.
The fly ash collected by the bag-type dust collector is conveyed to a fly ash curing bin for curing and activation in a mechanical conveying mode, the activated fly ash can be input into a fly ash temporary storage bin through a feeder, and the collected fly ash is crushed and then sprayed into a dry-method mixer for recycling; only a part of unreacted reagents of the fly ash which is not subjected to aging treatment can be used for dry reaction, and the aging activation process of the fly ash can increase the content of the reactive part in the fly ash and improve the utilization rate of the deacidification reagent. The hydroxide in the fly ash can be coated on CaCl on the surface of the hydrated lime through a diffusion process2The molecules react to generate CaClOH, the generation efficiency of the CaClOH is related to the crushing state and the retention time of the fly ash in a fly ash curing bin, and the CaClOH needs to be debugged according to the actual situation of a power plant; the generated CaClOH is sprayed back to the dry mixer and can react with acid gas; the fly ash curing bin comprises a bin barrel, a rotary drum and a spiral conveying device, wherein the bin barrel is used for storing fly ash and used as a reaction container for curing and reactivating the fly ash, the rotary drum is used for stirring the fly ash in the curing bin, crushing and mixing the fly ash, and meanwhile, the rotary drum is connected with the spiral conveying device and pushes the fly ash to enter the conveying device; the spiral conveying equipment is used for conveying the fly ash subjected to curing activation in the curing bin to the dry mixer.
The dry mixer 6 in the embodiment is in a U-shaped tubular structure, and the cross section of the dry mixer is square, so that the square tube is easy to process, high in comprehensive mechanical property, good in weldability, good in cold/hot processing performance and corrosion resistance, and good in toughness; the inlet side of the U-shaped bottom is provided with a necking conical section to improve the mixing effect of the pipeline body, the upper part of the inner side of the U-shaped bottom is connected with a fly ash slaking bin 11 through a screw conveying device, and the inlet side of the U-shaped bottom is connected with an activated carbon storage tank 13 and a slaked lime storage tank 14. An inlet arranged on a pipeline body of the dry mixer 6 is connected with a spray tower 5, an outlet thereof is connected with a cloth belt dust remover 7, and a reactant sprayed into the pipe is a mixture of hydrated lime and activated carbon; the fly ash sprayed back is the fly ash after aging and reactivation. Slaked lime and activated carbon are fed into a mixer in a pneumatic conveying mode (using compressed air), and fly ash (including fly ash, unreacted powdery slaked lime, activated carbon powder and the like) after slaking and reactivation is fed into a dry mixer by adopting a screw conveying device. The dry mixer can form turbulent flow with high speed disturbance in the pipeline body to solve the problem of fully mixing the smoke and the reactant in the pipeline body.
Finally, the above embodiments are only intended to illustrate the technical solutions of the present invention and not to limit the present invention, and although the present invention has been described in detail with reference to the preferred embodiments, it will be understood by those skilled in the art that modifications or equivalent substitutions may be made on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions, and all of them should be covered by the claims of the present invention.
Claims (7)
1. The utility model provides a nearly zero release processing system of msw incineration flue gas for handle the flue gas that msw incineration (1) produced, a serial communication port, include electrostatic precipitator (2) according to flue gas treatment process order setting, SCR reaction tower (3), economizer (4), spray column (5), dry process mixer (6), sack cleaner (7), draught fan (8), wet-type reaction tower (9) and chimney (10), the SCR reaction tower is connected with aqueous ammonia storage tank (12), the dry process mixer is connected with active carbon storage tank (13), slaked lime storage tank (14) and flying dust curing storehouse (11), flying dust curing storehouse is connected with the sack cleaner, the spray column is connected with cooling water storage tank (17) and waste liquid collecting box (18), the wet-type reaction tower is connected with sodium hydroxide solution storage tank (15) and waste liquid collecting box.
2. The waste incineration flue gas near-zero emission treatment system of claim 1, wherein the dry mixer is in a U-shaped tubular structure, and the upper part of the inner side of the U-shaped bottom of the dry mixer is connected with a fly ash curing bin.
3. The waste incineration flue gas near-zero emission treatment system according to claim 2, wherein the dry mixer is provided with a necking cone section on an inlet side near a U-shaped bottom of the dry mixer.
4. The system for treating waste incineration flue gas with near zero emission according to any one of claims 1 to 3, wherein the fly ash aging bin comprises a bin and a rotary drum arranged in the bin, and the fly ash aging bin injects the fly ash after the aging activation back into the dry mixer through a screw conveying device connected with the bin.
5. The waste incineration flue gas near-zero emission treatment system according to claim 1, further comprising a fly ash storage tank (16) connected with the electrostatic dust collector, the SCR reaction tower, the economizer, the spray tower and the bag-type dust collector and used for receiving respective produced fly ash.
6. The near-zero emission treatment system for waste incineration flue gas as claimed in claim 1, wherein the wet reaction tower is provided with a cooling absorption part and a dehumidifying part which are communicated from bottom to top, the cooling absorption part and the dehumidifying part are respectively provided with an atomizer and a liquid accumulation area which are respectively connected, and the two liquid accumulation areas are respectively connected with a sodium hydroxide solution storage tank and a waste liquid collecting box; the cooling absorption portion is connected with the induced draft fan, the dehumidifying portion is provided with a liquid drop separator above a liquid accumulation area in the dehumidifying portion, and the top of the dehumidifying portion is connected with the chimney.
7. A waste incineration flue gas near-zero emission treatment process is characterized in that the waste incineration flue gas near-zero emission treatment system according to any one of claims 1 to 6 is adopted, and the process comprises the following steps:
1) the flue gas produced by the incinerator sequentially passes through an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, a coal economizer, a spray tower, a dry mixer, a bag-type dust collector and a wet reaction tower and then is discharged by a chimney;
2) collecting fly ash produced in an electrostatic dust collector, an SCR (selective catalytic reduction) reaction tower, an economizer, a spray tower and a bag-type dust collector by a fly ash storage tank;
3) leading out the fly ash produced by the bag-type dust remover, activating the fly ash by a fly ash curing bin, and spraying the fly ash back to the dry-method mixer;
4) and (4) conveying the accumulated liquid produced by the two accumulated liquid areas of the wet reaction tower into the spray tower.
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| CN202010182412.7A CN111203065A (en) | 2020-03-16 | 2020-03-16 | Waste incineration flue gas near-zero emission treatment system and process |
| CN202010681816.0A CN111589260B (en) | 2020-03-16 | 2020-07-15 | Near-zero emission treatment system and process for waste incineration flue gas |
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| CN202010681816.0A Active CN111589260B (en) | 2020-03-16 | 2020-07-15 | Near-zero emission treatment system and process for waste incineration flue gas |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112870918A (en) * | 2021-01-15 | 2021-06-01 | 中国瑞林工程技术股份有限公司 | Processing system and method |
| CN115488137A (en) * | 2022-09-23 | 2022-12-20 | 重庆三峰环境集团股份有限公司 | System and method for degrading dioxin in waste incineration fly ash |
| CN115779658A (en) * | 2022-11-07 | 2023-03-14 | 北京首创环境科技有限公司 | Fly ash-slaked lime composite slurry desulfurizer as well as preparation method and application thereof |
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| US5795548A (en) * | 1996-03-08 | 1998-08-18 | Mcdermott Technology, Inc. | Flue gas desulfurization method and apparatus |
| CN101797472A (en) * | 2009-05-04 | 2010-08-11 | 上海蓝鸟环境科技发展有限公司 | Smoke processing technology |
| CN204973572U (en) * | 2015-10-08 | 2016-01-20 | 盐城市富仕环保科技有限公司 | Dry process desulfurization system |
| CN106621754A (en) * | 2016-12-31 | 2017-05-10 | 上海康恒环境股份有限公司 | Garbage incineration fume ultralow emission purifying system |
| CN207628210U (en) * | 2018-03-30 | 2018-07-20 | 中冶节能环保有限责任公司 | A kind of dry desulfurization denitration reaction tower gas approach structure and flue gas flow guiding device |
| CN109569228A (en) * | 2018-12-26 | 2019-04-05 | 浙江大维高新技术股份有限公司 | The exhaust system and technique of flue gas of garbage furnace |
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| CN110624384A (en) * | 2019-10-17 | 2019-12-31 | 中国环境保护集团有限公司 | Purification treatment method and purification treatment device for waste incineration flue gas |
| CN212396274U (en) * | 2020-03-16 | 2021-01-26 | 重庆三峰环境集团股份有限公司 | Waste incineration flue gas near-zero emission treatment system |
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- 2020-03-16 CN CN202010182412.7A patent/CN111203065A/en active Pending
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112870918A (en) * | 2021-01-15 | 2021-06-01 | 中国瑞林工程技术股份有限公司 | Processing system and method |
| CN115488137A (en) * | 2022-09-23 | 2022-12-20 | 重庆三峰环境集团股份有限公司 | System and method for degrading dioxin in waste incineration fly ash |
| CN115488137B (en) * | 2022-09-23 | 2024-05-28 | 重庆三峰环境集团股份有限公司 | System and method for degrading dioxin in waste incineration fly ash |
| CN115779658A (en) * | 2022-11-07 | 2023-03-14 | 北京首创环境科技有限公司 | Fly ash-slaked lime composite slurry desulfurizer as well as preparation method and application thereof |
| CN115779658B (en) * | 2022-11-07 | 2023-10-24 | 北京首创环境科技有限公司 | Fly ash-slaked lime composite slurry desulfurizing agent and preparation method and application thereof |
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| CN111589260B (en) | 2024-01-23 |
| CN111589260A (en) | 2020-08-28 |
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