CN215388629U - Pollutant collaborative purification system for waste incineration flue gas - Google Patents
Pollutant collaborative purification system for waste incineration flue gas Download PDFInfo
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- CN215388629U CN215388629U CN202121638817.3U CN202121638817U CN215388629U CN 215388629 U CN215388629 U CN 215388629U CN 202121638817 U CN202121638817 U CN 202121638817U CN 215388629 U CN215388629 U CN 215388629U
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- filter tube
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- 239000003546 flue gas Substances 0.000 title claims abstract description 69
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 239000003344 environmental pollutant Substances 0.000 title claims abstract description 28
- 231100000719 pollutant Toxicity 0.000 title claims abstract description 27
- 238000000746 purification Methods 0.000 title abstract description 23
- 238000004056 waste incineration Methods 0.000 title abstract description 17
- 239000002918 waste heat Substances 0.000 claims abstract description 59
- 239000000919 ceramic Substances 0.000 claims abstract description 56
- 239000000835 fiber Substances 0.000 claims abstract description 56
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 23
- 238000004140 cleaning Methods 0.000 claims abstract description 14
- 230000003197 catalytic Effects 0.000 claims description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 239000010881 fly ash Substances 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 210000002381 Plasma Anatomy 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 8
- 238000005728 strengthening Methods 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 7
- 239000000843 powder Substances 0.000 claims description 4
- 239000010882 bottom ash Substances 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 40
- 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 23
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 14
- 239000000428 dust Substances 0.000 abstract description 13
- 239000003054 catalyst Substances 0.000 abstract description 11
- 239000002699 waste material Substances 0.000 abstract description 6
- 238000000034 method Methods 0.000 description 15
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 12
- 239000007789 gas Substances 0.000 description 8
- 239000003638 reducing agent Substances 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 229910002089 NOx Inorganic materials 0.000 description 5
- 238000006477 desulfuration reaction Methods 0.000 description 5
- 230000003009 desulfurizing Effects 0.000 description 5
- 229920000642 polymer Polymers 0.000 description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 4
- 239000002956 ash Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 238000003723 Smelting Methods 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 3
- PPBAJDRXASKAGH-UHFFFAOYSA-N azane;urea Chemical compound N.NC(N)=O PPBAJDRXASKAGH-UHFFFAOYSA-N 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- CWYNVVGOOAEACU-UHFFFAOYSA-N fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 3
- 229910052753 mercury Inorganic materials 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- -1 HCl Chemical compound 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N HCl Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 230000002195 synergetic Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- WKXHZKXPFJNBIY-UHFFFAOYSA-N [Ti][W][V] Chemical compound [Ti][W][V] WKXHZKXPFJNBIY-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000001808 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium(0) Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
Abstract
The utility model discloses a pollutant collaborative purification system for waste incineration flue gas, which comprises a waste incinerator (1), a waste heat boiler, a dry deacidification tower (4), a ceramic fiber filter tube integrated device (5), a waste heat boiler economizer (6), a low-temperature plasma reactor (7) and a discharge device which are connected in sequence; a denitration device (11) is arranged in the garbage incinerator (1); a plurality of mutually independent bins are formed in the ceramic fiber filter tube integrated device, and a catalyst ceramic fiber filter tube (52) is arranged in each bin; the low-temperature plasma reactor is connected with a cleaning device (71). The utility model can realize the cooperative purification treatment of deacidification, denitration and dust removal on the incineration flue gas, and simultaneously carry out secondary deepening removal on pollutants such as nitric oxide, dioxin, heavy metals and the like in the tail flue gas, thereby ensuring the standard emission of the flue gas.
Description
Technical Field
The utility model relates to a flue gas purification system, in particular to a pollutant collaborative purification system for waste incineration flue gas.
Background
At present, the main disposal method of municipal solid waste is incineration treatment, and has the advantages of harmlessness, reduction and the like. The domestic garbage is more and more widely used by adopting a grate furnace incineration mode, but the incineration process of the domestic garbage inevitably generates substances containing particulate matters, HCl and SO2、NOxAnd dioxin and other pollutants.
The flue gas purification device system in the prior art mainly adopts the series combination of multi-stage single pollutant (including deacidification, denitration, dust removal, dioxin removal and heavy metal removal) control systems to realize the removal of each pollutant in flue gas. For example, in the deacidification and dust removal process of the semi-dry method, the dry method and the bag-type dust remover adopted by the waste incineration plant at present, the problems of high failure rate of a rotary atomizer, high power consumption, risk in continuous operation and the like exist; meanwhile, the adopted SNCR (selective non-catalytic reduction) + SCR (selective catalytic reduction) denitration technology has the problems of large energy consumption, large floor area, short service life of the catalyst and the like; the adopted dioxin and heavy metal removal adopts an activated carbon injection process, so that the activated carbon and the flue gas are not uniformly mixed, and the excessive emission risk is caused. Along with the stricter environmental emission limit and the increased investment and operation cost, the flue gas purification technology is gradually upgraded from 'single pollutant control' to 'multi-pollutant cooperative control'.
The Chinese utility model patent ZL201820642378.5 discloses a desulfurization, denitrification and dedusting integrated device of a biomass boiler, which comprises a desulfurization absorption tower and a ceramic fiber filter tube deduster; the process has the defects that the process only comprises the treatment of sulfur, nitrate and dust, and has no treatment effect on pollutants such as dioxin, heavy metal and the like in flue gas generated by waste incineration, steel smelting, non-ferrous metal kilns and the like.
The chinese utility model patent application CN201910372454.4 discloses a flue gas desulfurization, denitrification, dioxin removal and dust removal integrated process, which comprises 4 modules of temperature adjustment, mixing of desulfurization and denitrification agents, a catalytic filter bag and heat exchange. The flue gas generated by waste incineration, steel smelting, non-ferrous metal kilns and the like has different requirements on the temperature of desulfurization, denitration and dioxin removal during purification, and the temperature of the flue gas after temperature adjustment cannot be controlled in different process ranges, so that the flue gas purification method cannot be applied to the flue gas purification of waste incineration, steel smelting, non-ferrous metal kilns and the like.
Disclosure of Invention
The utility model aims to provide a pollutant collaborative purification system for waste incineration flue gas, which can realize collaborative purification treatment of deacidification, denitration and dust removal on the incineration flue gas, and simultaneously carry out secondary deepening removal on pollutants such as nitric oxide, dioxin, heavy metals and the like in tail flue gas to ensure that the flue gas reaches the standard and is discharged.
The utility model is realized by the following steps:
a pollutant collaborative purification system for waste incineration flue gas comprises a waste incinerator, a waste heat boiler, a dry method deacidification tower, a ceramic fiber filter tube integrated device, a waste heat boiler economizer, a low-temperature plasma reactor and a discharge device; a denitration device is arranged in the garbage incinerator, an outlet of the garbage incinerator is connected with an inlet of a waste heat boiler, and an outlet of the waste heat boiler is connected with an inlet of a dry deacidification tower; the outlet of the dry deacidification tower is connected with the inlet of the ceramic fiber filter tube integrated device, a plurality of mutually independent bins are formed in the ceramic fiber filter tube integrated device, a catalyst ceramic fiber filter tube is installed in each bin, and the outlet of the ceramic fiber filter tube integrated device is connected with the inlet of the waste heat boiler economizer; the outlet of the waste heat boiler economizer is connected with the air inlet of the low-temperature plasma reactor, the cleaning device is connected to the low-temperature plasma reactor, and the air outlet of the low-temperature plasma reactor is connected with the discharging device.
The waste heat boiler comprises a waste heat boiler superheater and a waste heat boiler evaporator; the inlet of the waste heat boiler superheater is connected with the outlet of the garbage incinerator, the outlet of the waste heat boiler superheater is connected with the inlet of the waste heat boiler evaporator, and the outlet of the waste heat boiler evaporator is connected with the inlet of the dry deacidification tower.
The deacidification agent in the dry deacidification tower is solid powder with the grain diameter of 200-600 meshes.
An ammonia spraying system is arranged on a flue between an inlet of the ceramic fiber filter tube integrated device and an outlet of the dry-method deacidification tower; the length of each catalyst ceramic fiber filter tube in the ceramic fiber filter tube integrated device is 3-6m, and the porosity of the catalyst ceramic fiber filter tube is 50% -90%.
The low-temperature plasma reactor comprises a plurality of stages of plasma strengthening units which are arranged in series.
And the bottom ash discharge ports of the dry deacidification tower, the ceramic fiber filter tube integrated device, the waste heat boiler economizer and the low-temperature plasma reactor are connected to a fly ash conveying device.
Compared with the prior art, the utility model has the following beneficial effects:
1. the dry deacidification tower is adopted, the operation temperature is 320-350 ℃, the dry deacidification efficiency is high, the high-efficiency removal of the acid gas in the flue gas can be realized only by the dry deacidification tower, the ultralow emission standard of the acid gas is reached, other secondary deacidification processes such as wet deacidification and the like are not needed to be added at the rear end, the high-efficiency deacidification is ensured, and the equipment cost and the required arrangement space are reduced.
2. The utility model adopts the ceramic fiber filter tube integrated device based on the multi-chamber catalyst ceramic fiber filter tube, thereby being capable of treating nitrogen oxide and SO2And pollutants such as HCl, particulate matters and dioxin are subjected to synergistic purification treatment, so that gradient clean utilization of energy is realized.
3. The utility model adopts the low-temperature plasma reactor based on the plurality of stages of plasma strengthening units which are arranged in series, thereby being capable of treating NO in tail flue gasxAnd secondary deep removal of dioxin and heavy metal enables the emission of nitrogen oxides, dioxin and heavy metal to reach the standard all the time, an SCR reactor is not required to be arranged, a temperature rise measure is also not required, and energy consumption and equipment occupation space are reduced.
4. The utility model is based on the coupling of the ceramic fiber filter tube integrated device and the low-temperature plasma reactor, realizes the cooperative purification of multiple pollutants in the waste incineration flue gas, and solves the deep purification treatment and ultralow emission requirements of the waste incineration flue gas.
The utility model can realize the cooperative purification treatment of deacidification, denitration and dust removal on the incineration flue gas through the dry deacidification tower and the ceramic fiber filter tube integrated device in a high-temperature section, realizes the step clean utilization of energy, and simultaneously carries out secondary deepening removal on pollutants such as nitric oxide, dioxin, heavy metal and the like in the tail flue gas through the low-temperature plasma reactor, ensures the full-time standard emission of the flue gas, and is suitable for being widely applied to the purification treatment of various waste incineration flue gases.
Drawings
FIG. 1 is a front view of the system for the cooperative purification of pollutants from flue gas from the incineration of waste according to the present invention.
In the figure, 1 a garbage incinerator, 11 a denitration device, 2 a waste heat boiler superheater, 3 a waste heat boiler evaporator, 4 a dry method deacidification tower, 41 a dry powder injection system, 5 a ceramic fiber filter pipe integrated device, 51 an ammonia injection system, 52 a catalyst ceramic fiber filter pipe, 53 a fly ash conveying device, 6 a waste heat boiler economizer, 7 a low-temperature plasma reactor, 71 a cleaning device, 72 an air inlet, 73 a high-voltage power supply, 74 an air outlet, 8 an induced draft fan and 9 a chimney.
Detailed Description
The utility model is further described with reference to the following figures and specific examples.
Referring to the attached figure 1, a pollutant collaborative purification system for waste incineration flue gas comprises a waste incinerator 1, a waste heat boiler, a dry deacidification tower 4, a ceramic fiber filter tube integrated device 5, a waste heat boiler economizer 6, a low-temperature plasma reactor 7 and a discharge device; a denitration device 11 is arranged in the garbage incinerator 1, the outlet of the garbage incinerator 1 is connected with the inlet of a waste heat boiler, and the outlet of the waste heat boiler is connected with the inlet of the dry deacidification tower 4; the outlet of the dry deacidification tower 4 is connected with the inlet of the ceramic fiber filter tube integrated device 5, a plurality of mutually independent bins are formed in the ceramic fiber filter tube integrated device 5, a catalyst ceramic fiber filter tube 52 is installed in each bin, and the outlet of the ceramic fiber filter tube integrated device 5 is connected with the inlet of the waste heat boiler economizer 6; the outlet of the waste heat boiler economizer 6 is connected with the air inlet 72 of the low-temperature plasma reactor 7, the cleaning device 71 is connected on the low-temperature plasma reactor 7, the cleaning device 71 is provided with a high-voltage power supply 73, and the air outlet 74 of the low-temperature plasma reactor 7 is connected with a discharging device. The garbage incinerator 1 can adopt a grate furnace, domestic garbage is combusted in the garbage incinerator 1, the generated flue gas is cooled by a waste heat boiler and then enters a dry deacidification tower 4, part of acid gas in the flue gas is removed by spraying of a deacidification agent, the content of the acid gas in the flue gas is ensured to reach the emission standard, secondary deacidification is not needed, and the flue gas enters a ceramic fiber filter tube integrated device 5 for NO treatmentxRemoving dioxin and dust, enabling the purified flue gas to enter a waste heat boiler economizer 6 for heat exchange and temperature reduction, and finally entering a low-temperature plasma reactor 7 for residual NOxSecondary purifying and discharging device for heavy metals such as dioxin and mercuryAn induced draft fan 8 and a chimney 9 can be adopted, and the induced draft fan 8 sends the purified flue gas into the chimney 9 for emission.
The temperature window of the garbage incineration in the garbage incinerator 1 is 850-1150 ℃, so that Nitrogen Oxide (NO) is generatedxComponent) and a denitration reducing agent in the denitration device 11, and the denitrated flue gas enters the waste heat boiler for waste heat recovery and cooling.
The denitration device 11 adopts an SNCR denitration process, and denitration reducing agents of the SNCR denitration process are ammonia water and urea.
The denitration device 11 adopts a PNCR (polymer non-catalytic reduction, i.e., a solid particle polymer) denitration process, a denitration reducing agent of the PNCR denitration process is a solid polymer denitration agent, and the solid polymer denitration agent is a commercial polymer denitration agent and is formed by mixing various denitration substances.
The waste heat boiler comprises a waste heat boiler superheater 2 and a waste heat boiler evaporator 3; the inlet of the waste heat boiler superheater 2 is connected with the outlet of the garbage incinerator 1, the outlet of the waste heat boiler superheater 2 is connected with the inlet of the waste heat boiler evaporator 3, the outlet of the waste heat boiler evaporator 3 is connected with the inlet of the dry deacidification tower 4, and the incineration flue gas is cooled through the waste heat boiler superheater 2 and the waste heat boiler evaporator 3; the temperature of the flue gas output from the outlet of the waste heat boiler evaporator 3 is 320-350 ℃.
The deacidification agent in the dry deacidification tower 4 is solid powder with the grain diameter of 200-600 meshes, preferably, the deacidification agent is at least one of baking soda and slaked lime or other deacidification agents selected according to requirements, and the high-efficiency removal of the acid gas is realized by spraying the deacidification agent.
An ammonia spraying system 51 is arranged on a flue between an inlet of the ceramic fiber filter tube integrated device 5 and an outlet of the dry-method deacidification tower 4, an ammonia evaporator in the ammonia spraying system 51 evaporates the denitration reducing agent into ammonia gas and then sprays the ammonia gas into the flue so as to mix the ammonia gas with flue gas; the denitration reducing agent is ammonia water, or urea and other denitration reducing agents can be adopted, the temperature of the flue gas entering the ceramic fiber filter tube integrated device 5 is 320-350 ℃, the full reaction in the SCR denitration process is ensured, and the optimal denitration effect is achieved.
The inside of the substrate of the catalytic ceramic fiber filter tube 52 is loaded with at least one denitration catalyst such as vanadium-titanium, vanadium-tungsten-titanium, noble metal, etc., the denitration catalyst inside the catalytic ceramic fiber filter tube 52 can be regenerated after being deactivated, and the catalytic ceramic fiber filter tube 52 decomposes NO in flue gasxDioxin and a large amount of dust carrying heavy metals in the flue gas are blocked outside the pipe by the catalytic ceramic fiber filter pipe 52.
The length of the catalytic ceramic fiber filter tube 52 is 3-6m, the porosity of the catalytic ceramic fiber filter tube 52 is 50% -90%, and the flue gas sequentially passes through the catalytic ceramic fiber filter tubes 52 in a plurality of bins, so that NO is ensuredxAnd high-efficiency removal of dioxin and dust.
The low-temperature plasma reactor 7 comprises a plurality of stages of plasma strengthening units which are arranged in series, the temperature of the flue gas entering the first stage of plasma strengthening unit is 120-150 ℃, and the plasma strengthening units adopt dielectric barrier discharge and can remove pollutants such as nitric oxide, mercury and other heavy metals, dioxin and the like in the flue gas.
The residence time of the flue gas in the low-temperature plasma reactor 7 is 2-5s, so that secondary deep removal of pollutants such as nitrogen oxides, mercury and other heavy metals, dioxin and the like in the flue gas is ensured, and the ultralow emission standard of the flue gas is achieved.
The cleaning medium of the cleaning device 71 is compressed air, the pressure of the compressed air is 0.4MPa, and the low-temperature plasma reactor 7 can be cleaned by the compressed air, so that the dust deposition in the low-temperature plasma reactor 7 is avoided.
And the bottom ash outlets of the dry deacidification tower 4, the ceramic fiber filter tube integrated device 5, the waste heat boiler economizer 6 and the low-temperature plasma reactor 7 are connected to a fly ash conveying device 53 and used for collecting and concentrating fly ash.
After the domestic waste incineration flue gas is purified by the pollutant synergistic purification system, the following emission standards can be achieved: the emission concentration of the particulate matter can be controlled to 10mg/Nm3The following; NOxThe discharge concentration of (A) can be controlled to 30mg/Nm3The following; SO (SO)2Is discharged fromThe concentration can be controlled at 35mg/Nm3The following; the emission concentration of dioxin pollutants can be controlled to be 0.1ng TEQ/Nm3The following. Therefore, the utility model can be used for treating SO in the waste incineration flue gas2、NOxThe removal performance of the particulate matters and the dioxin is stable, and particularly the decomposition and removal efficiency of the nitrogen oxides and the dioxin in the flue gas is higher.
Example 1:
the pollutant collaborative purification system for the waste incineration flue gas is adopted to incinerate the household garbage, the waste incinerator 1 can adopt a grate furnace for the incineration of the household garbage, the incineration temperature window is 850-1150 ℃, the denitration device 11 in the waste incinerator 1 adopts an SNCR denitration process, and the denitration reducing agents of the SNCR denitration process are ammonia water and urea.
The flue gas generated by the incineration of the household garbage is cooled to 320-350 ℃ through the waste heat boiler superheater 2 and the waste heat boiler evaporator 3 and then enters the dry-method deacidification tower 4, and the high-efficiency removal of acid gas in the flue gas is realized through spraying solid sodium bicarbonate with 200-mesh and 600-mesh functions in the dry-method deacidification tower 4. When the flue gas enters the flue between the dry-method deacidification tower 4 and the ceramic fiber filter tube integrated device 5, ammonia water is evaporated into ammonia gas by an ammonia evaporator in the ammonia spraying system 51, the ammonia gas is sprayed into the flue to mix the ammonia gas with the flue gas, and then the flue gas enters the ceramic fiber filter tube integrated device 5, wherein the temperature of the flue gas entering the ceramic fiber filter tube integrated device 5 is 320-350 ℃. The bottom of the dry deacidification tower 4 is provided with an ash discharge port for discharging the fly ash in the dry deacidification tower 4 to a fly ash conveying device 53.
The flue gas passes through the catalytic ceramic fiber filter tubes 52 of a plurality of bins in turn in the ceramic fiber filter tube integrated device 5, the length of the catalytic ceramic fiber filter tube 52 is 6m, the porosity of the catalytic ceramic fiber filter tube 52 is 90 percent, and NO in the flue gas is treatedxAnd dioxin and dust with heavy metals are removed efficiently. Vanadium and titanium are loaded inside the substrate of the catalytic ceramic fiber filter tube 52 as a denitration catalyst. The bottom of the ceramic fiber filter tube integrated device 5 is provided with an ash discharge port for discharging the fly ash in the ceramic fiber filter tube integrated device 5 to the fly ash conveying device 53.
The purified flue gas enters the waste heat boiler economizer 6 for heat exchange and temperature reduction to 120-plus 150 ℃, and the bottom of the waste heat boiler economizer 6 is provided with an ash discharge port for discharging the fly ash in the waste heat boiler economizer 6 to a fly ash conveying device 53. The cooled flue gas enters the low-temperature plasma reactor 7 from the gas inlet 72, sequentially passes through the multi-stage plasma strengthening units, stays for 5s, is subjected to secondary deep removal of pollutants such as nitrogen oxides, mercury and other heavy metals, dioxin and the like in the flue gas through dielectric barrier discharge, enters the induced draft fan 8 from the gas outlet 74, and is discharged through the chimney 9. The bottom of the low-temperature plasma reactor 7 is provided with an ash discharge port, the high-voltage power supply 73 supplies power to the cleaning device 71, and the cleaning device 71 cleans the plasma strengthening unit through 0.4MPa of compressed air and is used for discharging the fly ash in the low-temperature plasma reactor 7 to the fly ash conveying device 53.
The flue gas pollutants discharged through the chimney 9 have the following contents: the particulate matter is not more than 10mg/Nm3，NOxNot more than 30mg/Nm3，SO2Not more than 35mg/Nm3The content of dioxin pollutants is not more than 0.1ng TEQ/Nm3。
The present invention is not limited to the above embodiments, and any modifications, equivalent replacements, improvements, etc. within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. The utility model provides a pollutant is clean system in coordination for msw incineration flue gas which characterized by: comprises a garbage incinerator (1), a waste heat boiler, a dry deacidification tower (4), a ceramic fiber filter tube integrated device (5), a waste heat boiler economizer (6), a low-temperature plasma reactor (7) and a discharge device; a denitration device (11) is arranged in the garbage incinerator (1), the outlet of the garbage incinerator (1) is connected with the inlet of a waste heat boiler, and the outlet of the waste heat boiler is connected with the inlet of a dry deacidification tower (4); the outlet of the dry deacidification tower (4) is connected with the inlet of the ceramic fiber filter tube integrated device (5), a plurality of mutually independent bins are formed in the ceramic fiber filter tube integrated device (5), a catalytic ceramic fiber filter tube (52) is installed in each bin, and the outlet of the ceramic fiber filter tube integrated device (5) is connected with the inlet of the waste heat boiler economizer (6); the outlet of the waste heat boiler economizer (6) is connected with the air inlet (72) of the low-temperature plasma reactor (7), the low-temperature plasma reactor (7) is connected with a cleaning device (71), and the air outlet (74) of the low-temperature plasma reactor (7) is connected with a discharging device.
2. The system of claim 1, wherein the system comprises: the waste heat boiler comprises a waste heat boiler superheater (2) and a waste heat boiler evaporator (3); the inlet of the waste heat boiler superheater (2) is connected with the outlet of the garbage incinerator (1), the outlet of the waste heat boiler superheater (2) is connected with the inlet of the waste heat boiler evaporator (3), and the outlet of the waste heat boiler evaporator (3) is connected with the inlet of the dry deacidification tower (4).
3. The system of claim 1, wherein the system comprises: the deacidification agent in the dry deacidification tower (4) is solid powder with the grain diameter of 200-600 meshes.
4. The system of claim 1, wherein the system comprises: an ammonia spraying system (51) is arranged on a flue between an inlet of the ceramic fiber filter tube integrated device (5) and an outlet of the dry deacidification tower (4); the length of the catalytic ceramic fiber filter tube (52) in the ceramic fiber filter tube integrated device (5) is 3-6m, and the porosity of the catalytic ceramic fiber filter tube (52) is 50% -90%.
5. The system of claim 1, wherein the system comprises: the low-temperature plasma reactor (7) comprises a plurality of stages of plasma strengthening units which are arranged in series.
6. The system of claim 1, wherein the system comprises: and the bottom ash discharge ports of the dry deacidification tower (4), the ceramic fiber filter tube integrated device (5), the waste heat boiler economizer (6) and the low-temperature plasma reactor (7) are connected to a fly ash conveying device (53).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121638817.3U CN215388629U (en) | 2021-07-19 | 2021-07-19 | Pollutant collaborative purification system for waste incineration flue gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121638817.3U CN215388629U (en) | 2021-07-19 | 2021-07-19 | Pollutant collaborative purification system for waste incineration flue gas |
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| CN215388629U true CN215388629U (en) | 2022-01-04 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114405260A (en) * | 2022-01-18 | 2022-04-29 | 长春三友智造科技发展有限公司 | Treatment system and process for flue gas generated by waste incineration |
| CN115463531A (en) * | 2022-10-12 | 2022-12-13 | 济南国能环境工程有限公司 | Ultralow-emission purification treatment system and method for sulfur and nitrate dust in flue gas at tail of biomass boiler |
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2021
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114405260A (en) * | 2022-01-18 | 2022-04-29 | 长春三友智造科技发展有限公司 | Treatment system and process for flue gas generated by waste incineration |
| CN115463531A (en) * | 2022-10-12 | 2022-12-13 | 济南国能环境工程有限公司 | Ultralow-emission purification treatment system and method for sulfur and nitrate dust in flue gas at tail of biomass boiler |
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