CN111589260B - Near-zero emission treatment system and process for waste incineration flue gas - Google Patents
Near-zero emission treatment system and process for waste incineration flue gas Download PDFInfo
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- CN111589260B CN111589260B CN202010681816.0A CN202010681816A CN111589260B CN 111589260 B CN111589260 B CN 111589260B CN 202010681816 A CN202010681816 A CN 202010681816A CN 111589260 B CN111589260 B CN 111589260B
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 239000003546 flue gas Substances 0.000 title claims abstract description 76
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000004056 waste incineration Methods 0.000 title claims abstract description 20
- 230000008569 process Effects 0.000 title claims abstract description 16
- 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 37
- 239000007788 liquid Substances 0.000 claims description 37
- 239000007921 spray Substances 0.000 claims description 34
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 21
- 239000012717 electrostatic precipitator Substances 0.000 claims description 16
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 14
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 13
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 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
- 238000009825 accumulation Methods 0.000 claims description 10
- 230000003213 activating effect Effects 0.000 claims description 6
- 229910052799 carbon Inorganic materials 0.000 claims description 6
- 239000000498 cooling water Substances 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 10
- 231100000719 pollutant Toxicity 0.000 abstract description 10
- 239000004744 fabric Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 7
- 239000000376 reactant Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 238000006555 catalytic reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 230000007420 reactivation Effects 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
- 239000012530 fluid Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229920002430 Fibre-reinforced plastic Polymers 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010531 catalytic reduction reaction Methods 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
- 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
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 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
- 239000003245 coal Substances 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 150000002013 dioxins Chemical class 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
- 238000004519 manufacturing process Methods 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
- 239000013618 particulate matter Substances 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
- 230000000750 progressive 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
Classifications
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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
-
- 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 a near-zero emission treatment 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 garbage incineration flue gas with different pollutant contents, the whole system is stable and reliable to operate, 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 a waste incineration flue gas near-zero emission treatment process.
Background
The urban garbage problem becomes one of the most difficult problems restricting the current urban development, the garbage incineration treatment technology accords with the garbage treatment policies of innocuity, reduction and reclamation, and has the advantages of high treatment speed, good volume reduction effect, small occupied area, small environmental impact and the like, and the urban garbage treatment technology has been rapidly developed at home and abroad in recent years. However, the flue gas generated after the incineration of the household garbage contains a large amount of pollutants such as smoke dust, acid gas, heavy metal, dioxins and the like, and various pollutants have high content and are unstable, so that the environment is seriously harmed if the flue gas is not treated effectively. So the harmless treatment of the household garbage incineration flue gas has become a key problem of public attention, and the near zero emission system and process of the flue gas are the current research key and research and development hot spot.
At present, the semi-dry deacidification technology is generally adopted in domestic garbage incineration plants to remove acid gas in flue gas, and the requirements of the current national environmental protection emission index can be basically met. However, in order to further realize reduction, recycling and harmless treatment of the garbage, the discharge index of the acidic pollutants in the garbage incineration flue gas is further reduced, and the semi-dry deacidification technology needs to have breakthrough progress. Meanwhile, although the wet deacidification technology can efficiently remove acid pollutants in the flue gas, the generated wastewater is difficult to treat, and the traditional dry technology has the problems of poor deacidification effect, large consumption of slaked lime and active carbon, large generation amount of incineration fly ash and the like.
Disclosure of Invention
Therefore, 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 the 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 above purpose, the present invention provides the following technical solutions:
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 precipitator, an SCR (selective catalytic reduction) reaction tower, a coal economizer, a spray tower, a dry mixer, a bag-type dust remover, an induced draft fan, a wet reaction tower and a chimney, 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 curing bin, the fly ash curing bin is connected with the bag-type dust remover, the spray tower is connected with a cooling water storage tank and a waste liquid collection tank, and the wet reaction tower is connected with a sodium hydroxide solution storage tank and a waste liquid collection tank.
Further, the dry mixer is of a U-shaped tubular structure, and the upper part of the inner side of the U-shaped bottom is connected with the fly ash curing bin.
Further, the dry mixer is provided with a necked down cone section at the inlet side near the bottom of its U-shape.
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 cured and activated fly ash back into the dry mixer through a screw conveying device connected with the bin barrel.
Further, the treatment system also comprises a fly ash storage tank which is connected with the electrostatic precipitator, the SCR reaction tower, the economizer, the spray tower and the bag-type dust remover and is used for receiving the fly ash produced by each treatment system.
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 effusion area which are respectively connected, and the two effusion areas are respectively connected with a sodium hydroxide solution storage tank and a waste liquid collection tank; the cooling absorption part is connected with the induced draft fan, the dehumidifying part is provided with a liquid drop separator above the liquid accumulation area in the dehumidifying part, and the top of the dehumidifying part is connected with the chimney.
The invention also provides a near-zero emission treatment process of the waste incineration flue gas, which adopts the near-zero emission treatment system of the waste incineration flue gas and comprises the following steps:
1) The flue gas produced by the incinerator is discharged by a chimney after passing through an electrostatic precipitator, an SCR reaction tower, an economizer, a spray tower, a dry mixer, a bag-type dust remover and a wet reaction tower in sequence;
2) Collecting fly ash produced in an electrostatic precipitator, an SCR 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 collector, curing and activating the fly ash by a fly ash curing bin, and then spraying the fly ash back into the dry-method mixer;
4) And sending the effusion produced in the two effusion areas of the wet reaction tower into a spray tower.
The beneficial effects of the invention are as follows:
1. the treatment system disclosed by the invention adopts a combination of electrostatic dust collection, SCR (selective catalytic reduction), dry deacidification, cloth bag dust collection and wet deacidification, can comprehensively treat the waste incineration flue gas with different pollutant contents, is stable and reliable in operation, and can achieve near zero emission standard of the discharged flue gas.
2. The invention adopts a process combining electrostatic dust removal and cloth bag dust removal, and effectively reduces the contents of particles and fly ash in the flue gas.
3. The treatment system of the invention uses fly ash slaking reactivation technology, effectively improves the dry reaction efficiency, and reduces the slaked lime consumption and the fly ash production.
4. The dry mixer of the treatment system can form turbulent fluid with high-speed disturbance in the pipeline body so as to solve the problem of thorough mixing of flue gas and reactants in the pipeline body.
5. The treatment system of the invention arranges the economizer between the SCR reaction tower and the spray tower, and aims to improve the energy balance of the incineration plant and effectively improve the power generation efficiency.
6. In order to maintain the balance of salt concentration in the reaction tower, the treatment system of the invention can discharge the wastewater in the effusion area into a spray tower to be used as cooling water, and the system has no wastewater 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 objects and other advantages of the invention may be realized and obtained by means of the instrumentalities and combinations particularly pointed out in the specification.
Drawings
For the purpose of making the objects, technical solutions and advantages of the present invention more apparent, the present invention will be described in the following preferred detail with reference to the accompanying drawings, in which:
FIG. 1 is a schematic diagram of a processing system;
FIG. 2 is a schematic flow diagram of the present processing system;
reference numerals: the garbage incinerator 1, the electrostatic precipitator 2, the SCR reaction tower 3, the economizer 4, the spray tower 5, the dry mixer 6, the bag-type dust collector 7, the induced draft fan 8, the wet reaction tower 9, the chimney 10, the fly ash curing bin 11, the ammonia water storage tank 12, the activated carbon storage tank 13, the slaked lime storage tank 14, the sodium hydroxide solution storage tank 15, the fly ash storage tank 16, the cooling water storage tank 17 and the waste liquid collection tank 18.
Detailed Description
The invention is further described below in connection with the following detailed description. Wherein the drawings are for illustrative purposes only and are shown in schematic, non-physical, and not intended to be limiting of the present patent; for the purpose of better illustrating embodiments of the invention, certain elements of the drawings may be omitted, enlarged or reduced and do not represent the size of the actual product; it will be appreciated 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 the waste incineration flue gas in the present embodiment is used for treating the flue gas generated by the waste incineration furnace 1, and comprises an electrostatic precipitator 2, an SCR reaction tower 3, an economizer 4, a spray tower 5, a dry mixer 6, a bag-type dust remover 7, a draught fan 8, a wet reaction tower 9 and a chimney 10 which are sequentially arranged according to the flue gas treatment procedure, wherein the SCR reaction tower 3 is connected with an ammonia water storage tank 12, the dry mixer 6 is connected with an active carbon storage tank 13, a slaked lime storage tank 14 and a fly ash curing bin 11, the fly ash curing bin is connected with a bag-type dust remover, part of fly ash collected by the bag-type dust remover is used for curing activation, the spray tower 5 is connected with a cooling water storage tank 17 and a waste liquid collection tank 18, the wet reaction tower 9 is connected with a sodium hydroxide solution storage tank 15 and a 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 into the spray tower 5; a fly ash storage tank 16 connected to the electrostatic precipitator, the SCR reaction tower, the economizer, the spray tower, and the bag-type dust remover and receiving fly ash generated by each; and the fly ash curing bin 11 is connected with the bag-type dust collector and is used for receiving the fly ash generated by the bag-type dust collector, and the fly ash curing bin sprays the cured and activated fly ash back into the dry mixer.
With reference to fig. 2, the process of the garbage incineration flue gas near-zero emission treatment system mainly comprises the following steps:
1) The flue gas produced by the incinerator is discharged by a chimney after passing through an electrostatic precipitator, an SCR reaction tower, an economizer, a spray tower, a dry mixer, a bag-type dust remover and a wet reaction tower in sequence;
2) Collecting fly ash produced in an electrostatic precipitator, an SCR 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 the fly ash produced by the bag-type dust collector, curing and activating the fly ash by a fly ash curing bin, and then spraying the fly ash back into a dry mixer;
4) And (3) feeding the accumulated liquid produced by the wet reaction tower into a spray tower in a progressive manner.
Specifically, hot flue gas discharged from the garbage incinerator 1 directly enters the electrostatic precipitator 2, and the main function of the hot flue gas is to prevent large particles from entering the SCR reaction tower 3, so that the blockage of the SCR reactor and the poisoning of a catalyst are effectively inhibited; the number of the electrodes of the electrostatic precipitator can be designed according to the dust content of the flue gas, and the emission electrode charges particles in the flue gas so as to enable the particles to flow to the collecting electrode; the bottom of the electrostatic precipitator 2 is provided with a particulate matter collecting device, and the particulate matters are crushed and then sent 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 spray 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 reaction tower 3 to fully mix smoke and the atomized ammonia water, the smoke and the atomized ammonia water enter the SCR reaction tower 3 uniformly, and the hot smoke can provide a certain amount of heat for the ammonia water to evaporate ammonia from 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 closely distributed on the cross section of the whole SCR reaction tower, and each catalytic reaction module is solidified with a special honeycomb-shaped channel containing a catalyst; the optimal reaction temperature is 268 ℃, and the pollutant at the outlet of the SCR reaction tower comprises a certain amount of NOx, HCl, SO 2 And NH 3 Etc.; then, the flue gas from the SCR reaction tower enters the economizer 4, and the main function of the flue gas is to improve the energy balance of an incineration plant and improve the heat energy utilization efficiency of the power plant; the temperature of the outer surface of the inner heat exchanger pipeline is above 120 ℃, and the inlet/outlet water supply temperature is 120 ℃/165 ℃; a soot blower is arranged in the economizer 4, the outside fly ash of the pipeline is purged, a fly ash collecting device is arranged at the bottom of the heat exchanger, and the collected fly ash is sent to 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, and 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 higher than that of the flue gas entering the dry mixerKeeping consistency; a cooling water storage tank 17 is arranged outside the spray tower, so that the 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, and the flow process in the dry mixer is subjected to numerical simulation according to the actual flue gas flow rate to obtain the optimal section size and bending radius of a flow channel, so that the flue gas and the reactant in the dry mixer can be fully mixed to form turbulent fluid with high-speed disturbance; the reactant comprises fly ash after slaking and reactivation, unreacted powdery slaked lime and active carbon powder; then, the flue gas at the outlet of the dry mixer 6 enters a cloth bag dust collector 7, and a circular filter cloth bag is uniformly arranged in the whole cloth bag dust collector through numerical calculation, so that the flue gas uniformly flows in the cloth bag dust collector, and the temperature of the flue gas entering the cloth bag dust collector is close to the acid dew point of the flue gas, so that the filter cloth bag needs to use special corrosion-resistant materials; a soot blower and a fly ash collecting device are arranged in the bag-type dust remover, one part of the collected fly ash enters a fly ash curing bin 11, and the other part enters a fly ash storage tank 16; the fly ash circulation rate of the collected fly ash is determined according to the pollutant content in the flue gas, and then the proportion of the fly ash which is distributed into the fly ash curing barn 11 and the fly ash storage tank 16 is carried out; then, the flue gas at the outlet of the bag-type dust collector 7 enters an induced draft fan 8 which mainly compensates the pressure drop generated in the flue gas treatment process; then, the flue gas at the outlet of the induced draft fan 8 enters a wet reaction tower 9, and the wet reaction tower mainly comprises two parts: the cooling absorption part and the dehumidifying part are mutually communicated and are provided with an atomizer and a effusion area; cooling absorption portion: the flue gas enters a wet reaction tower and passes through a cooling absorption part, a condensate atomizer is arranged on the cooling absorption part, condensate in a liquid accumulation area of the cooling absorption part is atomized into small liquid drops to be fully mixed with high-temperature flue gas, and part of HCl and SO in the flue gas is absorbed 2 Waiting for the liquid after the reaction to circulate into the effusion area; dehumidifying 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, fiber reinforced plastic is filled in a middle filling area, and the contact area of the flue gas and alkaline liquid is increased; the dehumidifying part is provided with a liquid drop separator, and passes through the dehumidifying partThe treated flue gas contains small liquid drops, the small liquid drops are condensed on the surface of the flue gas when flowing through a liquid drop separator, the small liquid drops are continuously condensed into larger liquid drops, then the larger liquid drops are dripped into a filler area filled with fiber reinforced plastics, then the filler area enters a liquid accumulation area of a cooling absorption part and a dehumidifying part, sodium hydroxide solution is pumped into the liquid accumulation areas of the cooling absorption part and the dehumidifying part, the PH value of the liquid accumulation is adjusted, the liquid accumulation is continuously circulated in a wet tower until the salinity of the liquid accumulation reaches a certain value and then is discharged into a waste liquid collecting box, so that the liquid accumulation is circulated in each area, the alkali liquid is used for adjusting the PH value of the liquid accumulation of each part, and waste water in the waste liquid collecting box can be pumped into a spray tower to cool the flue gas; finally, the cleaned flue gas is discharged to the atmosphere through a stack 10.
The fly ash collected by the bag-type dust collector is conveyed to a fly ash curing bin for curing and activating in a mechanical transportation mode, the activated fly ash can be input into a fly ash temporary storage bin through a feeder, and the collected fly ash is sprayed into a dry mixer for recycling after being crushed; only a part of unreacted reagent in the fly ash which is not cured can be used for dry reaction, and the curing and activating 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 mixed with CaCl coated on the surface of slaked lime through a diffusion process 2 The molecules react to generate CaClOH, the generation efficiency of the CaClOH is related to the crushing state and the residence time of the fly ash in the fly ash curing bin, and the adjustment is required according to the actual condition of a power plant; the generated CaClOH is sprayed back into a dry mixer and can react with acid gas; the fly ash curing bin comprises a bin barrel, a rotary drum and spiral conveying equipment, wherein the bin barrel is used for storing fly ash and is used as a reaction vessel for fly ash curing and reactivation, the rotary drum is used for stirring the fly ash in the curing bin to crush and mix the fly ash, and meanwhile, the rotary drum is connected with the spiral conveying equipment to push the fly ash to enter the conveying equipment; the spiral conveying equipment is used for conveying the fly ash after curing and activating in the curing bin to the dry mixer.
The dry mixer 6 in the embodiment is of a U-shaped tubular structure, and the cross section of the dry mixer is square, so that the square tube is easy to process, has high comprehensive mechanical property, good weldability, good cold/hot processing property and corrosion resistance, and good toughness; the inlet side of the U-shaped bottom is provided with a necking cone section to promote the mixing effect of the pipeline body, the upper part of the inner side of the U-shaped bottom is connected with the fly ash curing bin 11 through a spiral conveying device, and the inlet side of the U-shaped bottom is connected with the active carbon storage tank 13 and the slaked lime storage tank 14. The inlet of the pipeline body of the dry mixer 6 is connected with the spray tower 5, the outlet of the dry mixer is connected with the cloth belt dust remover 7, and the reactant in the reactant spraying pipe is a mixture of slaked lime and active carbon; the fly ash sprayed back is the fly ash after curing and reactivation. The slaked lime and the activated carbon are conveyed pneumatically (using compressed air) into a mixer, and the slaked and reactivated fly ash (including fly ash, unreacted powdered slaked lime, activated carbon powder and the like) is conveyed into a dry mixer by using screw conveying equipment. The dry mixer can form turbulent fluid with high-speed disturbance in the pipeline body so as to solve the problem of thorough mixing of the flue gas and the reactant in the dry mixer.
Finally, it is noted that the above embodiments are only for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications and equivalents may be made thereto without departing from the spirit and scope of the present invention, which is intended to be covered by the claims of the present invention.
Claims (4)
1. The near-zero emission treatment system for the waste incineration flue gas is used for treating the flue gas generated by a waste incinerator (1), and is characterized by comprising an electrostatic precipitator (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 procedure, wherein the SCR reaction tower is connected with an ammonia water storage tank (12), the dry mixer is connected with an active carbon storage tank (13), a slaked lime storage tank (14) and a fly ash curing bin (11), the fly ash curing bin is connected with the bag-type dust collector, the spray tower is connected with a cooling water storage tank (17) and a waste liquid collection box (18), and the wet reaction tower is connected with a sodium hydroxide solution storage tank (15) and the waste liquid collection box; the dry mixer is of a U-shaped tubular structure, the upper part of the inner side of the U-shaped bottom of the dry mixer is connected with the fly ash curing bin, and the inlet side of the dry mixer, which is close to the U-shaped bottom of the dry mixer, is provided with a necking cone section; the treatment system further comprises a fly ash storage tank (16) which is connected with the electrostatic precipitator, the SCR reaction tower, the economizer, the spray tower and the bag-type dust remover and is used for receiving the fly ash produced by each treatment system.
2. The near zero emission treatment system of waste incineration flue gas according to claim 1, wherein 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 cured and activated fly ash back into the dry mixer through a screw conveying device connected with the bin barrel.
3. The near-zero emission treatment system for the waste incineration flue gas according to 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 effusion area which are respectively connected, and the two effusion areas are respectively connected with a sodium hydroxide solution storage tank and a waste liquid collection tank; the cooling absorption part is connected with the induced draft fan, the dehumidifying part is provided with a liquid drop separator above the liquid accumulation area in the dehumidifying part, and the top of the dehumidifying part is connected with the chimney.
4. A process for treating the near-zero emission of waste incineration flue gas, which is characterized in that a system for treating the near-zero emission of the waste incineration flue gas according to any one of claims 1 to 3 is adopted, and the process comprises the following steps:
1) The flue gas produced by the incinerator is discharged by a chimney after passing through an electrostatic precipitator, an SCR reaction tower, an economizer, a spray tower, a dry mixer, a bag-type dust remover and a wet reaction tower in sequence;
2) Collecting fly ash produced in an electrostatic precipitator, an SCR 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 collector, curing and activating the fly ash by a fly ash curing bin, and then spraying the fly ash back into the dry-method mixer;
4) And sending the effusion produced in the two effusion areas of the wet reaction tower into a spray tower.
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| CN2020101824127 | 2020-03-16 |
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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 |
| 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 |
| 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 |
| CN121017231B (en) * | 2025-09-30 | 2026-04-10 | 生态环境部华南环境科学研究所(生态环境部生态环境应急研究所) | Method for strengthening condensation and short-range enrichment of heavy metals in waste incineration fly ash based on front end |
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