CN215138502U - Advanced treatment system for waste incineration flue gas - Google Patents
Advanced treatment system for waste incineration flue gas Download PDFInfo
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- CN215138502U CN215138502U CN202023136436.3U CN202023136436U CN215138502U CN 215138502 U CN215138502 U CN 215138502U CN 202023136436 U CN202023136436 U CN 202023136436U CN 215138502 U CN215138502 U CN 215138502U
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- advanced treatment
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- sodium bicarbonate
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- 239000003546 flue gas Substances 0.000 title claims abstract description 73
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 238000004056 waste incineration Methods 0.000 title claims description 12
- 239000000428 dust Substances 0.000 claims abstract description 35
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000011575 calcium Substances 0.000 claims abstract description 7
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 7
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 42
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 28
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 21
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 21
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- 238000005507 spraying Methods 0.000 claims description 17
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 14
- 239000000843 powder Substances 0.000 claims description 14
- 238000002347 injection Methods 0.000 claims description 9
- 239000007924 injection Substances 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 5
- 239000000243 solution Substances 0.000 claims description 5
- 238000010531 catalytic reduction reaction Methods 0.000 claims description 4
- 239000002699 waste material Substances 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims 1
- 239000000376 reactant Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 22
- 239000003054 catalyst Substances 0.000 abstract description 16
- 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 abstract description 12
- 230000008901 benefit Effects 0.000 abstract description 5
- 239000012717 electrostatic precipitator Substances 0.000 abstract description 5
- 206010008428 Chemical poisoning Diseases 0.000 abstract description 4
- 238000005299 abrasion Methods 0.000 abstract description 4
- 229920006395 saturated elastomer Polymers 0.000 abstract description 3
- 239000010791 domestic waste Substances 0.000 abstract 1
- 239000003344 environmental pollutant Substances 0.000 description 14
- 231100000719 pollutant Toxicity 0.000 description 14
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 13
- 235000011114 ammonium hydroxide Nutrition 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000010813 municipal solid waste Substances 0.000 description 9
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 229910001385 heavy metal Inorganic materials 0.000 description 4
- 230000002779 inactivation Effects 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000005200 wet scrubbing Methods 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 229910052815 sulfur oxide Inorganic materials 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 229910002089 NOx Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 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
- 239000012716 precipitator Substances 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treating Waste Gases (AREA)
- Chimneys And Flues (AREA)
Abstract
The utility model discloses a garbageIncineration flue gas advanced treatment system belongs to the municipal domestic waste field of burning. The utility model discloses at first carry out deacidification in advance through spouting calcium in the stove and reduce HCl, SO2Concentration, denitration in SNCR furnace reduces NOx concentration, and dust and SO are pre-dedusted by electrostatic precipitator2And (3) flue gas with a lower concentration of 250-270 ℃ enters the SCR reactor for denitration, so that the abrasion and chemical poisoning of the catalyst are reduced, and the temperature interval for re-synthesizing dioxin at the temperature of 300-500 ℃ is avoided. The utility model discloses a flue gas advanced treatment method reduces saturated steam's consumption, increases the economizer heat transfer volume when reaching the ultra-clean emission, improves the plant thermal efficiency ~ 5%, reduces equipment area, improves economic benefits.
Description
Technical Field
The utility model belongs to the technical field of municipal solid waste burns and specifically relates to a waste incineration flue gas advanced treatment system and processing method thereof.
Background
In recent years, the incineration of municipal solid waste has been rapidly developed, and the incineration of waste is gradually developing into a mainstream manner of treating municipal solid waste. The flue gas that can produce among the waste incineration process contains the pollutant, mainly includes HCl, SOx, NOx, heavy metal, dioxin, particulate matter etc. therefore need discharge after purification unit. With the increasing environmental situation, the standard of the flue gas emission is increased, and the application of the ultra-clean emission flue gas purification process is increased.
The conventional ultra-clean emission flue gas purification process usually adopts an SNCR + SCR denitration process, an SCR catalyst usually adopts a corrugated plate type or a honeycomb type, and is easy to block when encountering high-dust-content flue gas, so that the SCR catalyst is usually arranged behind a bag type dust collector, the flue gas temperature is low after bag type dust collection, and the SCR catalyst is easy to form ammonium bisulfate with sulfur oxides at low temperature and is attached to the surface of the catalyst to cause inactivation. Therefore, saturated steam is needed to heat the flue gas and then the flue gas enters the reactor to perform catalytic denitration reaction, so that the heat loss is large, and the economic cost is high.
The conventional ultra-clean emission flue gas purification process usually adopts a semidry method and a wet deacidification process, SO that HCl and SO are greatly reduced2In order to prolong the service life of the SCR catalyst, a process that an SCR reactor is arranged behind a wet scrubbing system is gradually adopted in domestic projects. In order to meet the respective reaction temperature interval requirements of a wet system and an SCR system, two flue gas-flue gas heat exchangers are required to be arranged between the systems for heat transfer, so that the heat loss caused by direct water spraying cooling and steam heating is reduced. But the resistance of the flue gas-flue gas heat exchanger is large, thereby causing the energy consumption of the induced draft fan to be greatly increased and reducing the overall economy.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the not enough of prior art existence, provide a waste incineration flue gas advanced treatment method, adopt the stove to spout calcium and carry out deacidification in advance and adopt electrostatic precipitator to carry out 250 ~ 270 ℃ flue gas after removing dust in advance and get into the medium temperature SCR denitration, adopt plate catalyst reduce system resistance, improve the dust trafficability characteristic, reduce the steam consumption of the preceding section that heats of conventional SCR simultaneously, improve the thermal efficiency of whole factory. The flue gas of which the rear end is subjected to heat exchange by the economizer is deacidified by a dry method and a wet method, so that the heat loss caused by the temperature drop of deacidification by a semi-dry method is reduced, and the economic benefit is further improved while the ultra-clean emission is achieved.
In order to achieve the purpose of the utility model, the following technical proposal is adopted:
advanced treatment system for waste incineration flue gas, comprisingThe following parts are respectively a device for spraying calcium in a furnace and pre-deacidifying: a calcium carbonate storage bin and a calcium carbonate injection device; denitration equipment: the system comprises an SNCR (selective non-catalytic reduction) injection device, an SCR (selective catalytic reduction) reactor, an ammonia water storage tank, an ammonia water evaporation mixer and a flue gas reflux fan; dust removal equipment: electrostatic precipitators, bag house precipitators; dry deacidification equipment: a sodium bicarbonate storage bin and a sodium bicarbonate injection device; and (3) wet deacidification equipment: a wet scrubbing tower and a sodium hydroxide storage tank; waste heat utilization and heat exchange equipment: low-temperature coal economizer, flue gas-flue gas heat exchanger. The utility model discloses process flow is as follows: firstly, calcium carbonate powder is sprayed into a garbage incinerator for pre-deacidification, meanwhile, an ammonia water solution is sprayed for SNCR denitration reaction, flue gas at about 270 ℃ after heat utilization of the flue gas by a boiler enters an electrostatic precipitator for pre-dedusting, and the flue gas after pre-dedusting enters an SCR reactor for catalytic denitration reaction. And (4) enabling the denitrified clean flue gas to enter a low-temperature economizer for heat exchange and cooling to about 150 ℃, and then entering a bag type dust collector. Spraying sodium bicarbonate powder into the front flue of the bag type dust collector, and further removing SO by utilizing the efficient deacidification capability of the sodium bicarbonate powder in the temperature range2And HCl, and simultaneously spraying activated carbon to adsorb and remove heavy metals and dioxin. One part of flue gas after bag type dust removal flows back to the incinerator through a flue gas reflux fan to form a local low-oxygen combustion area and reduce the generation amount of NOx, most of the flue gas enters a flue gas-flue gas heat exchanger to be cooled to about 90 ℃ and enters a wet washing tower for deacidification, and low-temperature flue gas after deacidification enters the flue gas-flue gas heat exchanger to be heated to about 120 ℃ and is discharged into the atmosphere through a chimney.
A method for deeply treating waste incineration flue gas comprises the following steps:
by multi-stage combined control according to SO detected at chimney2Adjusting the amount of a sodium hydroxide solution in wet deacidification by using the HCl pollutant concentration, and controlling the pollutant concentration to be below 90% of an emission limit value; and controlling the discharge amount of the wet-process wastewater according to the salinity in the wet-process tower, draining water when the salinity is more than 3%, and stopping draining water when the salinity is less than or equal to 2%. According to SO detected at the outlet of the bag type dust collector2Adjusting the spray quantity of the sodium bicarbonate dry powder by the concentration of the HCl pollutants, and controlling the concentration of the pollutants at the outlet of the dust remover to meet the design requirementLess than 90%. According to SO detected by SCR inlet2And adjusting the spraying amount of the calcium carbonate powder by the concentration of the HCl pollutants, and controlling the concentration of the pollutants below the design requirement.
Furthermore, a 250-270 ℃ medium temperature catalyst is arranged in front of the economizer to carry out SCR denitration reaction, so that the smoke temperature rising section before conventional SCR denitration is reduced, and the energy consumption of the system is reduced by-4%;
furthermore, before the medium-temperature SCR reactor, calcium carbonate is sprayed in the furnace for pre-deacidification and electrostatic dust removal for pre-dedusting, SO that HCl and SO are reduced2Dust, and reduces chemical poisoning inactivation and mechanical abrasion of the SCR catalyst;
further, electrostatic dust removal and SCR denitration at 250-270 ℃ are adopted, so that a dioxin generation temperature interval of 300-500 ℃ is avoided, the dioxin is prevented from being resynthesized, and the dioxin is ensured to meet the emission requirement of European Union 2010 after being treated;
furthermore, after the low-temperature economizer is arranged at the medium-temperature SCR, the flue gas dust content is low, the concentration of acidic pollutants is low, the corrosivity is low, the heat exchange efficiency of the economizer is improved, and the service life of the tube bundle is prolonged.
Furthermore, efficient sodium bicarbonate is adopted for dry deacidification after SCR, the temperature range of efficient reaction is large, the deacidification efficiency is high, the temperature drop of semi-dry deacidification is avoided, the low-temperature economizer can exchange heat of the flue gas to 150 ℃, and the heat recovery rate is improved by-1%.
Furthermore, clean flue gas after bag type dust removal partially flows back to the incinerator, so that the oxygen content in the area is reduced, the generation of NOx is reduced, and the NOx stably reaches the standard by combining with SNCR and medium temperature SCR to form a combined denitration process.
Furthermore, the dry method and the wet method of calcium spraying and sodium bicarbonate inside the furnace are combined with the deacidification process, so that the fly ash yield is reduced.
Denitration control principle: and adopting multi-stage combined control, adjusting the ammonia injection amount of the SCR according to the concentration of the NOx pollutants detected at the chimney, and controlling the concentration of the pollutants to be below 90% of an emission limit value. The ammonia injection amount of the SNCR is adjusted based on the NOx pollutant concentration detected at the SCR inlet to control the pollutant concentration below 90% of the emission limit.
Compared with the prior art, the utility model, have following substantive characteristics and advantage:
1. the utility model discloses set up 250 ~ 270 ℃ middle temperature catalyst before the economizer and carry out the SCR denitration reaction, reaction efficiency is high, the catalyst quantity is few, the difficult poisoning inactivation of catalyst, and the catalyst producer at home and abroad all possesses the productivity effect, can reduce catalyst purchasing cost. Meanwhile, the flue gas temperature rise section before SCR denitration in the conventional ultra-clean emission flue gas purification process is reduced, the system energy consumption is reduced by 4 percent, a dioxin generation temperature range of 300-500 ℃ is avoided, the dioxin is prevented from being synthesized again, and the reduction of the treated dioxin to 0.1ng TEQ/Nm is ensured3The eu 2010 emissions requirements are met below. In addition, before the medium-temperature SCR reactor, calcium carbonate is sprayed in the furnace for pre-deacidification and electrostatic dust removal for pre-dedusting, SO that HCl and SO are reduced2And dust, and reduces chemical poisoning inactivation and mechanical abrasion of the SCR catalyst.
2. The utility model discloses low temperature economizer sets up behind medium temperature SCR, and flue gas dust content is low, acid pollutant concentration is lower, corrosivity is little, and economizer heat exchange efficiency improves and tube bank life-span extension. Meanwhile, the clean flue gas after bag type dust removal partially flows back to the incinerator, so that the oxygen content in the area is reduced, the generation of NOx is reduced, the waste heat of the flue gas is further recycled, and the heat efficiency of the whole plant is improved.
3. The utility model discloses adopt high-efficient sodium bicarbonate dry process deacidification behind the SCR, the temperature interval of high-efficient reaction is big, and the temperature drop of semidry deacidification has just been avoided to the deacidification efficient, and the low temperature economizer can be with flue gas heat transfer to 150 ℃, is less than conventional 190 ℃, and heat recovery efficiency improves ~ 1%, has reduced flying dust output through sodium bicarbonate efficient deacidification reaction simultaneously, has reduced treatment cost.
Drawings
FIG. 1 is a flow chart of a method for advanced treatment of waste incineration flue gas.
Detailed Description
In order to make the utility model discloses a purpose, technical scheme and advantage are more clear, combine below the utility model discloses a drawing, it is right the utility model discloses clear complete description carries out:
as shown in the flow chart of the advanced treatment method of the waste incineration flue gas in fig. 1, the process mainly comprises the following steps: (1) the device comprises a garbage incinerator, (2) a calcium carbonate storage bin, (3) a calcium carbonate injection device, (4) an ammonia water storage tank, (5) an SNCR injection device, (6) an ammonia water evaporation mixer, (7) an electrostatic dust collector, (8) an SCR reactor, (9) a low-temperature economizer, (10) a sodium bicarbonate storage bin, (11) a sodium bicarbonate injection device, (12) a bag type dust collector, (13) a flue gas reflux fan, (14) a flue gas-flue gas heat exchanger, (15) a wet washing tower and (16) a sodium hydroxide storage tank.
(1) And (2) burning the garbage in the garbage incinerator to generate flue gas, spraying calcium carbonate powder into the first flue of the garbage incinerator to perform pre-deacidification, and spraying an ammonia water solution to perform SNCR denitration. Calcium carbonate powder is stored in the calcium carbonate storage bin (2) and is sprayed into the furnace through the calcium carbonate spraying device (3). And (4) storing ammonia water in the ammonia water storage tank (4), and spraying the ammonia water into the furnace through the SNCR spraying device (5). And (3) enabling the flue gas at about 270 ℃ after heat utilization by the boiler to enter (7) an electrostatic dust collector for pre-dedusting, and enabling the pre-dedusted flue gas to enter (8) an SCR reactor for catalytic denitration reaction. And (3) conveying ammonia water in the ammonia water storage tank (4) to the ammonia water evaporation mixer (6) for evaporation, spraying the ammonia water into the SCR reactor, fully mixing the ammonia gas with flue gas, and then feeding the ammonia gas into the reactor. And (3) feeding the denitrified clean flue gas into a low-temperature economizer (9), performing heat exchange and cooling to 150 ℃, and feeding the denitrified clean flue gas into a bag type dust collector (12). Spraying sodium bicarbonate powder into the front flue of the (12) bag type dust collector, and further removing SO by utilizing the efficient deacidification capability of the sodium bicarbonate powder in the temperature range2And HCl, and simultaneously spraying activated carbon to adsorb and remove heavy metals and dioxin. And (3) storing sodium bicarbonate powder in a sodium bicarbonate storage bin (10), and spraying the sodium bicarbonate powder into the flue through a sodium bicarbonate spraying device (11). After bag type dust removal, one part of the flue gas flows back to the incinerator through a flue gas reflux fan (13), and the majority of the flue gas enters a flue gas-flue gas heat exchanger (14) and is cooled to about 90 ℃ and enters a wet washing tower (15) for deacidification. The sodium hydroxide solution used for deacidification of the wet scrubbing tower is stored in a sodium hydroxide storage tank (16). The deacidified low-temperature flue gas enters a flue gas-flue gas heat exchanger (14), the temperature is raised to about 120 ℃, and the flue gas is discharged into the atmosphere through a chimney.
The utility model relates to a waste incineration flue gas advanced treatment system and processing method belongs to the municipal solid waste incineration field. The utility model discloses at first carry out deacidification in advance through spouting calcium in the stove and reduce HCl, SO2Concentration, denitration in SNCR furnace reduces NOx concentration, and dust and SO are pre-dedusted by electrostatic precipitator2And (3) flue gas with a lower concentration of 250-270 ℃ enters the SCR reactor for denitration, so that the abrasion and chemical poisoning of the catalyst are reduced, and the temperature interval for re-synthesizing dioxin at the temperature of 300-500 ℃ is avoided. After denitration, the flue gas enters a low-temperature economizer to be cooled to about 150 ℃, and heat is utilized to the utmost extent. The dust content and the pollutant concentration of the flue gas entering the low-temperature economizer are low, the heat exchange efficiency of the economizer can be improved, and the service life of the equipment can be prolonged. And then the flue gas enters a bag type dust collector for deep dust collection. Sodium bicarbonate powder and active carbon are sprayed into the front flue of the bag type dust collector to perform deacidification and adsorption removal of dioxin and heavy metals. After bag type dust removal, the flue gas with the temperature of 150 ℃ enters a flue gas-flue gas heat exchanger to be cooled to about 90 ℃ and then enters a wet washing tower for deep deacidification, the purified flue gas enters the flue gas-flue gas heat exchanger to be heated to about 120 ℃ and then is discharged into the atmosphere through a chimney, and chimney corrosion and white smoke generation are reduced. The utility model discloses a flue gas advanced treatment method reduces saturated steam's consumption, increases the economizer heat transfer volume when reaching the ultra-clean emission, improves the plant thermal efficiency ~ 5%, reduces equipment area, improves economic benefits.
Claims (1)
1. A waste incineration flue gas advanced treatment system is used for treating flue gas generated by incineration of a waste incinerator and is characterized by comprising a calcium spraying and pre-deacidification device in the incinerator, an SNCR (selective non catalytic reduction) in-furnace denitration device, an electrostatic dust collector, a medium-temperature SCR (selective catalytic reduction) reactor, a low-temperature economizer, a sodium bicarbonate dry powder injection device, a bag type dust collector, a flue gas reflux device and a wet washing tower; calcium carbonate as a reactant sprayed with calcium in the furnace is stored in a calcium carbonate storage bin, sodium bicarbonate powder is stored in a sodium bicarbonate storage bin, and a sodium hydroxide solution used by a wet washing tower is stored in an alkali liquor tank.
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| CN202023136436.3U CN215138502U (en) | 2020-12-23 | 2020-12-23 | Advanced treatment system for waste incineration flue gas |
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| CN202023136436.3U CN215138502U (en) | 2020-12-23 | 2020-12-23 | Advanced treatment system for waste incineration flue gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112546832A (en) * | 2020-12-23 | 2021-03-26 | 上海康恒环境股份有限公司 | Advanced treatment system and treatment method for waste incineration flue gas |
| CN115990401A (en) * | 2023-03-22 | 2023-04-21 | 中国恩菲工程技术有限公司 | Purification process and device for waste incineration flue gas |
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2020
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112546832A (en) * | 2020-12-23 | 2021-03-26 | 上海康恒环境股份有限公司 | Advanced treatment system and treatment method for waste incineration flue gas |
| CN115990401A (en) * | 2023-03-22 | 2023-04-21 | 中国恩菲工程技术有限公司 | Purification process and device for waste incineration flue gas |
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