CN214809730U - Waste incineration flue gas purification system - Google Patents
Waste incineration flue gas purification system Download PDFInfo
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- CN214809730U CN214809730U CN202120034819.5U CN202120034819U CN214809730U CN 214809730 U CN214809730 U CN 214809730U CN 202120034819 U CN202120034819 U CN 202120034819U CN 214809730 U CN214809730 U CN 214809730U
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- flue gas
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- dust remover
- dry
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- 239000003546 flue gas Substances 0.000 title claims abstract description 120
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 118
- 238000000746 purification Methods 0.000 title claims abstract description 20
- 238000004056 waste incineration Methods 0.000 title claims abstract description 19
- 239000000428 dust Substances 0.000 claims abstract description 59
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 55
- 239000002918 waste heat Substances 0.000 claims abstract description 32
- 238000010438 heat treatment Methods 0.000 claims abstract description 19
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 8
- 239000002699 waste material Substances 0.000 claims abstract description 8
- 239000000779 smoke Substances 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 23
- 239000007789 gas Substances 0.000 claims description 21
- 239000000919 ceramic Substances 0.000 claims description 16
- 239000000835 fiber Substances 0.000 claims description 16
- 239000000843 powder Substances 0.000 claims description 16
- 239000002250 absorbent Substances 0.000 claims description 12
- 230000002745 absorbent Effects 0.000 claims description 12
- 239000010881 fly ash Substances 0.000 claims description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 9
- UIIMBOGNXHQVGW-UHFFFAOYSA-M NaHCO3 Chemical group [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 6
- 239000003513 alkali Substances 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000002956 ash Substances 0.000 claims description 3
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 3
- 239000010813 municipal solid waste Substances 0.000 abstract description 8
- 239000003245 coal Substances 0.000 abstract description 5
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N p-dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 15
- 229910001385 heavy metal Inorganic materials 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitrogen oxide Substances O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 11
- 239000002245 particle Substances 0.000 description 10
- 238000004140 cleaning Methods 0.000 description 9
- 235000011114 ammonium hydroxide Nutrition 0.000 description 8
- 229910052813 nitrogen oxide Inorganic materials 0.000 description 7
- 239000002253 acid Substances 0.000 description 6
- 230000003197 catalytic Effects 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000002378 acidificating Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- 235000015450 Tilia cordata Nutrition 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 238000001035 drying Methods 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 231100000719 pollutant Toxicity 0.000 description 4
- 239000003638 reducing agent Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006011 modification reaction Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000001717 pathogenic Effects 0.000 description 1
- 244000052769 pathogens Species 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 230000002035 prolonged Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000001502 supplementation Effects 0.000 description 1
- 230000002588 toxic Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Abstract
The utility model relates to a waste incineration flue gas purification system, which comprises a waste incinerator (1), a dry deacidification tower (3), a dust remover (4), a wet deacidification tower (7), heat exchange equipment and a flue gas exhaust device; the flue gas purification system comprises an active carbon adsorption tower (8); the heat exchange equipment comprises a waste heat boiler heating surface (2), a waste heat boiler economizer (5) and a flue gas heat exchanger (6); the cooling channel of the flue gas heat exchanger comprises a first inlet and a first outlet, and the heating channel of the flue gas heat exchanger comprises a second inlet and a second outlet; the smoke exhaust device comprises an induced draft fan (9) and a chimney (10); the garbage incinerator is connected with the dry deacidification tower through the heating surface of the waste heat boiler, the dry deacidification tower is connected with the dust remover, the dust remover is connected with the first inlet through the coal economizer of the waste heat boiler, the first outlet is connected with the flue gas inlet of the wet deacidification tower, the flue gas outlet of the wet deacidification tower is connected with the second inlet, the second outlet is connected with the activated carbon adsorption tower, and the activated carbon adsorption tower is connected with the chimney through the induced draft fan.
Description
Technical Field
The utility model relates to a msw incineration gas cleaning technique, in particular to can satisfy waste incineration gas cleaning system of ultralow emission requirement.
Background
The waste incineration is a common method for treating the waste, and the waste incineration is one of the main methods for treating the municipal domestic waste because the waste is treated by the incineration method, the reduction effect is obvious, the land is saved, various pathogens can be killed, and toxic and harmful substances are converted into harmless substances. However, the flue gas generated in the incineration process of the garbage contains pollutants such as nitrogen oxides, acidic substances, particulate matters, dioxin, heavy metals and the like, and the existing garbage incinerator needs to be provided with a flue gas purification system so as to avoid secondary pollution to the environment.
At present, the mainstream waste incineration flue gas purification system in China adopts a process of SNCR, a semi-dry method, a dry method, activated carbon adsorption and a bag-type dust remover. The SNCR (selective non-catalytic reduction) is a commonly used flue gas denitration technology, ammonia water, urea solution and other amino reducing agents are sprayed into the SNCR denitration technology within a temperature window of 850-1100 ℃, and Nitrogen Oxides (NO) in flue gas are generated by the reducing agentsx) Reducing the waste gas into harmless nitrogen and water, but the denitration efficiency of the SNCR is low, and is usually between 30% and 60%. The semidry process mainly comprises the steps of atomizing lime slurry and then distributing the lime slurry on the surfaces of flue gas and flue gas particles for deacidification reaction, the dry process directly sprays lime powder into the flue gas, the semidry process and the dry process mostly adopt the lime powder for deacidification reaction, a rotary atomizer required in the semidry process has the problems that an atomizing disc and a nozzle are easily abraded due to high rotating speed, and the problems that the control standard of flue gas pollutants generated by burning garbage is increasingly strict, the reaction efficiency of the semidry process is low, equipment is easily broken down and the like are more prominent. The combined process of activated carbon adsorption and bag-type dust remover is commonly used in the technology of removing dioxin and heavy metals, and comprises the steps of spraying activated carbon into a flue gas pipeline entering the bag-type dust remover, adsorbing heavy metal pollutants such as the dioxin, Hg and the like by using the activated carbon, and then using the activated carbonAnd the flue gas particles enter the bag type dust collector and are isolated on the surface of the filter bag, and finally the purpose of removing the particles, dioxin and heavy metals in the flue gas is achieved, but the activated carbon and the flue gas are easy to mix unevenly, and the risk of pollutant overproof emission is increased.
Disclosure of Invention
An object of the utility model is to provide a waste incineration gas cleaning system can effectively get rid of acidic material, nitrogen oxide, dust particulate matter, dioxin and heavy metal in the flue gas to take the second grade deacidification to acidic material, take the second grade desorption to dioxin and heavy metal, can satisfy ultralow emission requirement.
The utility model discloses a realize like this:
a waste incineration flue gas purification system comprises a waste incinerator, a dry deacidification tower, a dust remover, a wet deacidification tower, heat exchange equipment and a flue gas exhaust device;
the flue gas purification system comprises an activated carbon adsorption tower; the heat exchange equipment comprises a waste heat boiler heating surface, a waste heat boiler economizer and a flue gas heat exchanger; the flue gas heat exchanger comprises a cooling channel and a heating channel, the cooling channel comprises a first inlet and a first outlet, and the heating channel comprises a second inlet and a second outlet; the smoke exhaust device comprises an induced draft fan and a chimney;
the flue gas outlet of the garbage incinerator is connected with the flue gas inlet of the dry deacidification tower through the heating surface of the waste heat boiler, the flue gas outlet of the dry deacidification tower is connected with the flue gas inlet of the dust remover, a pipeline between the dry deacidification tower and the dust remover is connected with an ammonia water supply device, the flue gas outlet of the dust remover is connected with the first inlet through a waste heat boiler economizer, the first outlet is connected with the flue gas inlet of the wet deacidification tower, the flue gas outlet of the wet deacidification tower is connected with the second inlet, the second outlet is connected with the flue gas inlet of the activated carbon adsorption tower, and the flue gas outlet of the activated carbon adsorption tower is connected with a chimney through an induced draft fan.
The bottom of the dry-method deacidification tower is provided with a flue gas inlet and a dry powder inlet, the dry powder inlet is connected with a dry powder supply device and used for spraying the deacidification absorbent into the dry-method deacidification tower, and the top of the dry-method deacidification tower is provided with a flue gas outlet.
The deacidification absorbent is sodium bicarbonate powder or hydrated lime.
The bottom of dust remover sets up the flue gas entry, and the top of dust remover sets up the exhanst gas outlet, sets up a plurality of bins in the dust remover, sets up catalyst ceramic fiber filter tube in every bin, and the surface of catalyst ceramic fiber filter tube sets up catalyst.
The catalyst is one or a combination of V-Ti, V-W-Ti, Ce-W-Ti and Cu-Fe-Ce-Ti.
The bottom of the dust remover and the bottom of the waste heat boiler economizer are both provided with fly ash outlets, and the fly ash outlets are connected with a fly ash storage bin through an ash conveying system.
And the outside of the wet deacidification tower is connected with an alkali liquor supplementing system.
The active carbon adsorption tower is in a fixed bed type.
The utility model discloses msw incineration gas cleaning system at first, has increased wet process deacidification tower again behind the dust remover on dry process deacidification tower's basis for further carry out high-efficient deacidification to the flue gas, the requirement that the second grade deacidification technology that realizes from this can satisfy the ultralow emission of acid gas, and possesses super high deacidification efficiency. Moreover, the traditional semi-dry deacidification process is not adopted, the problems of abrasion of an atomizing disc and a nozzle and the like caused by high rotating speed of a rotary atomizer can be avoided, and the equipment failure rate is obviously reduced.
Secondly, the denitration treatment of the flue gas is to spray reducing agent ammonia water at 280-350 ℃, and catalyst ceramic fiber filter tubes in the dust remover are provided with catalyst catalysts for denitration, so that NO in the flue gas can be decomposedxAnd dioxin can also be intercepted, solid dust particles generated by the reaction of an acid substance and a deacidification absorbent in a dry-method deacidification tower in the flue gas can be intercepted, the integration of deacidification, dust removal and denitration of the flue gas is realized, and the dust particles intercepted by the catalyst ceramic fiber filter tube have a certain removing effect on the dioxin and the heavy metals. And the denitration treatment does not adopt an SCR (selective catalytic reduction) reactor, does not need an independent heating measure, reduces energy waste and is beneficial to the energy gradient full utilization of the flue gas waste heat.
Furthermore, the activated carbon adsorption tower is adopted to further adsorb dioxin and heavy metals in the flue gas, the characteristic that the activated carbon in the activated carbon adsorption tower has a large specific surface area is utilized, and indexes of the dioxin and the heavy metals in the flue gas meet the requirement of ultralow emission all the time. In addition, the traditional combined process of activated carbon adsorption and bag-type dust remover is not adopted, the problem of uneven mixing of activated carbon and flue gas can be avoided, and the over-standard emission risk is reduced.
Finally, the heating surface of the waste heat boiler and the coal economizer of the waste heat boiler in the heat exchange equipment are arranged in front and back two sections, the coal economizer of the waste heat boiler is arranged behind the dust remover to realize waste heat utilization, and the flue gas entering the coal economizer of the waste heat boiler is efficiently deacidified, denitrated and dedusted, so that the problems of blockage of the coal economizer of the waste heat boiler, corrosion of fly ash and the like can be avoided. And the flue gas waste heat passes through the waste heat boiler heating surface and the waste heat boiler economizer to realize sufficient heat exchange, and the gradient clean utilization of energy is gradually realized.
Compared with the prior art, the utility model, following beneficial effect has: the requirement of ultralow emission of acid gas, dioxin and heavy metal is met, the content of the dioxin and the heavy metal in the flue gas reaches the standard all the time, the deacidification is thorough, the efficiency is high, the failure rate of equipment is low, and the energy gradient clean utilization is facilitated.
Drawings
FIG. 1 is a schematic structural view of the waste incineration flue gas purification system of the present invention;
in the figure, 1 a garbage incinerator, 2 a waste heat boiler heating surface, 3 a dry method deacidification tower, 31 a dry powder supply device, 4 a dust remover, 41 an ammonia water supply device, 42 a fly ash storage bin, 5 a waste heat boiler economizer, 6 a flue gas heat exchanger, 7 a wet method deacidification tower, 71 an alkali liquor replenishing system, 8 an active carbon adsorption tower, 9 an induced draft fan and 10 a chimney.
Detailed Description
The invention will be further explained with reference to the drawings and the specific embodiments.
Referring to fig. 1, a waste incineration flue gas purification system comprises a waste incinerator 1, a dry deacidification tower 3, a dust remover 4, a wet deacidification tower 7, an activated carbon adsorption tower 8, heat exchange equipment and a flue gas exhaust device. The heat exchange equipment comprises a waste heat boiler heating surface 2, a waste heat boiler economizer 5 and a flue gas heat exchanger 6. The flue gas heat exchanger 6 comprises a cooling channel and a warming channel, the cooling channel comprises a first inlet and a first outlet, and the warming channel comprises a second inlet and a second outlet. The smoke exhaust device comprises an induced draft fan 9 and a chimney 10.
The connection relationship of the components is as follows: the flue gas outlet of the garbage incinerator 1 is connected with the flue gas inlet of the dry deacidification tower 3 through the heating surface 2 of the waste heat boiler, the flue gas outlet of the dry deacidification tower 3 is connected with the flue gas inlet of the dust remover 4, a pipeline between the dry deacidification tower 3 and the dust remover 4 is connected with an ammonia water supply device 41, the flue gas outlet of the dust remover 4 is connected with the first inlet through the waste heat boiler economizer 5, the first outlet is connected with the flue gas inlet of the wet deacidification tower 7, the flue gas outlet of the wet deacidification tower 7 is connected with the second inlet, the second outlet is connected with the flue gas inlet of the activated carbon adsorption tower 8, and the flue gas outlet of the activated carbon adsorption tower 8 is connected with a chimney 10 through an induced draft fan 9.
The bottom of the dry-method deacidification tower 3 is provided with a flue gas inlet and a dry powder inlet, the dry powder inlet is connected with a dry powder supply device 31 and used for spraying the deacidification absorbent into the dry-method deacidification tower 3, and the top of the dry-method deacidification tower 3 is provided with a flue gas outlet. Preferably, the deacidification absorbent is sodium bicarbonate powder or hydrated lime.
The bottom of dust remover 4 sets up the flue gas entry, and the top of dust remover 4 sets up the exhanst gas outlet, sets up a plurality of bins in the dust remover 4, and every bin is vertical type welding steel structure container and inside sets up the bearing structure who is used for supporting catalyst ceramic fiber filter tube, and the entry and the flue gas entry intercommunication of dust remover 4 of bin, the export of bin is connected with the air-purifying chamber through the guide plate, the air-purifying chamber communicates with the exhanst gas outlet of dust remover 4. The flue gas enters the bin chamber through the flue gas inlet of the dust remover 4 and the inlet of the bin chamber in sequence, then passes through the surface of the catalytic ceramic fiber filter tube and is discharged from the central hole of the catalytic ceramic fiber filter tube, then enters the gas purifying chamber through the outlet of the bin chamber, and finally is discharged out of the dust remover through the flue gas outlet of the dust remover 4. The surface of the catalytic ceramic fiber filter tube is provided with a catalytic catalyst. Preferably, the catalyst is one or a combination of V-Ti, V-W-Ti, Ce-W-Ti and Cu-Fe-Ce-Ti. The components of the catalyst are similar to those of the conventional SCR catalyst, and the catalystThe catalyst is uniformly distributed on the catalyst ceramic fiber filter tube and is used for decomposing NO in the flue gasxAnd dioxins, so that the contact area is large, the residence time and the removal efficiency are maximized. The dust remover is characterized in that solid dust particles generated by the reaction of acidic materials and a deacidification absorbent in a dry-method deacidification tower in flue gas are intercepted on the surface of a catalytic ceramic fiber filter tube, and a compressed air pulse is also arranged in the dust remover and used for removing the dust particles intercepted on the surface of the catalytic ceramic fiber filter tube.
The bottom of the dust remover 4 and the bottom of the waste heat boiler economizer 5 are both provided with fly ash outlets which are connected with a fly ash storage bin 42 through an ash conveying system.
The outside of the wet deacidification tower 7 is connected with an alkali liquor replenishing system 71.
The activated carbon adsorption tower 8 is of a fixed bed type.
Referring to fig. 1, the direction of the arrows is the smoke direction. Specifically, after high-temperature flue gas generated by the garbage incinerator exchanges heat with the heating surface of the waste heat boiler, the temperature of the flue gas is reduced to about 350 ℃; the method comprises the following steps that flue gas enters a dry deacidification tower to be subjected to primary deacidification, the flue gas is sprayed into the dry deacidification tower from a flue gas inlet at the bottom of the dry deacidification tower, a deacidification absorbent is sprayed into the dry deacidification tower from a dry powder inlet at the bottom of the dry deacidification tower, acidic substances and the deacidification absorbent in the flue gas flow in the same direction from bottom to top in the dry deacidification tower and undergo acid-base neutralization reaction, then the flue gas and the deacidification absorbent are discharged to a pipeline between the dry deacidification tower and a dust remover from a flue gas outlet at the top of the dry deacidification tower, a denitration reducing agent ammonia water is sprayed into the pipeline from an ammonia water supply device, and the flue gas and the ammonia water are fully mixed and then enter the dust remover at a temperature window of 280-350 ℃; the flue gas passes through the catalyst ceramic fiber filter tube and the gas purifying chamber from bottom to top in sequence and then is discharged, and NO in the flue gasxAnd dioxin is decomposed by a catalyst in the dust remover, solid dust particles generated by the reaction of an acid substance and a deacidification absorbent in a dry-method deacidification tower in the smoke are intercepted on the catalyst ceramic fiber filter tube, and the dioxin and heavy metals attached to the surface of the dust particles are removed; the flue gas enters a waste heat boiler economizer after coming out of the dust remover, and the flue gas is subjected to efficient deacidification, denitration and dust removal treatment, so that the residual flue gas isThe hot boiler economizer can not face the problems of fly ash blockage, acid gas corrosion and the like, the service life of the economizer can be greatly prolonged, and the temperature of flue gas discharged from the waste heat boiler economizer is reduced to 180-200 ℃; then, cooling the flue gas through a cooling channel of a flue gas heat exchanger, and then entering a wet deacidification tower for secondary deacidification to efficiently and thoroughly remove acid gas and further remove solid dust particles, and heating the flue gas to 100-150 ℃ through a heating channel of the flue gas heat exchanger; and finally, the flue gas enters an activated carbon adsorption tower for further adsorbing dioxin and heavy metals in the flue gas, and then enters a chimney through a draught fan for emission.
The utility model discloses a "dry process deacidification + catalyst ceramic fiber filter tube dust removal + wet process deacidification + fixed bed active carbon adsorption" technology, be different from conventional gas cleaning system, the flue gas realizes the deacidification at 280~350 ℃, denitration and dust removal integration, realize energy step clean utilization, and combine two-stage deacidification and active carbon adsorption to handle, gas cleaning system's each item emission index is superior to national standard and EU standard, possess the efficient and safe and reliable's advantage of desorption, provide a brand-new solution for solving msw incineration flue gas deep purification processing and reaching the ultralow emission requirement of flue gas, very extensive application prospect has.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and should not be taken as limiting the scope of the present invention, therefore, any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention should be included in the scope of the present invention.
Claims (8)
1. A waste incineration flue gas purification system comprises a waste incinerator (1), a dry deacidification tower (3), a dust remover (4), a wet deacidification tower (7), heat exchange equipment and a flue gas exhaust device; the method is characterized in that:
the flue gas purification system comprises an activated carbon adsorption tower (8); the heat exchange equipment comprises a waste heat boiler heating surface (2), a waste heat boiler economizer (5) and a flue gas heat exchanger (6); the flue gas heat exchanger (6) comprises a cooling channel and a heating channel, the cooling channel comprises a first inlet and a first outlet, and the heating channel comprises a second inlet and a second outlet; the smoke exhaust device comprises an induced draft fan (9) and a chimney (10);
the flue gas inlet of dry deacidification tower (3) is connected through exhaust-heat boiler heated surface (2) to the exhanst gas outlet of waste incinerator (1), the flue gas inlet of dust remover (4) is connected to the exhanst gas outlet of dry deacidification tower (3), pipeline access aqueous ammonia feeding mechanism (41) between dry deacidification tower (3) and dust remover (4), the exhanst gas outlet of dust remover (4) is first entry through exhaust-heat boiler economizer (5) connection, the flue gas inlet of wet deacidification tower (7) is connected to first export, the exhanst gas outlet of wet deacidification tower (7) is connected the second entry, the flue gas inlet of second exit linkage active carbon adsorption tower (8), the exhanst gas outlet of active carbon adsorption tower (8) connects chimney (10) through draught fan (9).
2. The waste incineration flue gas purification system according to claim 1, characterized in that: the bottom of the dry deacidification tower (3) is provided with a flue gas inlet and a dry powder inlet, the dry powder inlet is connected with a dry powder supply device (31) and used for spraying the deacidification absorbent into the dry deacidification tower (3), and the top of the dry deacidification tower (3) is provided with a flue gas outlet.
3. The waste incineration flue gas purification system according to claim 2, characterized in that: the deacidification absorbent is sodium bicarbonate powder or hydrated lime.
4. The waste incineration flue gas purification system according to claim 1, characterized in that: the bottom of dust remover (4) sets up the flue gas entry, and the top of dust remover (4) sets up the exhanst gas outlet, sets up a plurality of bins in dust remover (4), sets up catalyst ceramic fiber filter tube in every bin, and the surface of catalyst ceramic fiber filter tube sets up catalyst.
5. The waste incineration flue gas purification system according to claim 4, characterized in that: the catalyst is one or a combination of V-Ti, V-W-Ti, Ce-W-Ti and Cu-Fe-Ce-Ti.
6. The waste incineration flue gas purification system according to claim 1, characterized in that: the bottom of the dust remover (4) and the bottom of the waste heat boiler economizer (5) are both provided with fly ash outlets, and the fly ash outlets are connected with a fly ash storage bin (42) through an ash conveying system.
7. The waste incineration flue gas purification system according to claim 1, characterized in that: and the outside of the wet deacidification tower (7) is connected with an alkali liquor replenishing system (71).
8. The waste incineration flue gas purification system according to claim 1, characterized in that: the active carbon adsorption tower (8) is in a fixed bed type.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120034819.5U CN214809730U (en) | 2021-01-07 | 2021-01-07 | Waste incineration flue gas purification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120034819.5U CN214809730U (en) | 2021-01-07 | 2021-01-07 | Waste incineration flue gas purification system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214809730U true CN214809730U (en) | 2021-11-23 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120034819.5U Active CN214809730U (en) | 2021-01-07 | 2021-01-07 | Waste incineration flue gas purification system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214809730U (en) |
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2021
- 2021-01-07 CN CN202120034819.5U patent/CN214809730U/en active Active
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