CN204469514U - A kind of boiler smoke denitration in the stove device - Google Patents
A kind of boiler smoke denitration in the stove device Download PDFInfo
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- CN204469514U CN204469514U CN201520028434.2U CN201520028434U CN204469514U CN 204469514 U CN204469514 U CN 204469514U CN 201520028434 U CN201520028434 U CN 201520028434U CN 204469514 U CN204469514 U CN 204469514U
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- connects
- reaction tower
- flue gas
- frequency conversion
- rotary feeder
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- 239000000779 smoke Substances 0.000 title claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims abstract description 94
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 43
- 239000003546 flue gas Substances 0.000 claims abstract description 43
- 239000000203 mixture Substances 0.000 claims abstract description 34
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000004202 carbamide Substances 0.000 claims abstract description 33
- 239000008187 granular material Substances 0.000 claims abstract description 30
- 239000007789 gas Substances 0.000 claims abstract description 19
- 238000012544 monitoring process Methods 0.000 claims abstract description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 30
- 239000000920 calcium hydroxide Substances 0.000 claims description 30
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 24
- 229910052799 carbon Inorganic materials 0.000 claims description 24
- 239000003818 cinder Substances 0.000 claims description 10
- 239000000843 powder Substances 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 7
- 238000005859 coupling reaction Methods 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 21
- 229910001385 heavy metal Inorganic materials 0.000 abstract description 8
- 239000003344 environmental pollutant Substances 0.000 abstract description 7
- 231100000719 pollutant Toxicity 0.000 abstract description 7
- 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 6
- 238000010521 absorption reaction Methods 0.000 abstract description 4
- 230000001473 noxious effect Effects 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 19
- 238000006477 desulfuration reaction Methods 0.000 description 15
- 239000011575 calcium Substances 0.000 description 12
- 230000008569 process Effects 0.000 description 11
- 239000000428 dust Substances 0.000 description 10
- 230000023556 desulfurization Effects 0.000 description 8
- 239000004744 fabric Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 239000003638 chemical reducing agent Substances 0.000 description 5
- 238000001035 drying Methods 0.000 description 4
- 239000003517 fume Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 230000009471 action Effects 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002803 fossil fuel Substances 0.000 description 3
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000005303 weighing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002114 biscuit porcelain Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- -1 hydrogen calcium oxide Chemical class 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
Landscapes
- Treating Waste Gases (AREA)
Abstract
A kind of boiler smoke denitration in the stove device, comprise incinerator, flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, described flue gas Online Monitoring Control device connects frequency conversion rotary feeder, connect electron helical above frequency conversion rotary feeder to claim, electron helical claims to connect discharger, discharger connects urea granules feed bin, mixture generator is connected below frequency conversion rotary feeder, mixture generator one tunnel connects high pressure roots blower fan, urea granules playpipe of separately leading up to connects urea granules jet.The utility model can remove the SO in the flue gas of coal-burning boiler generation
2gas, nitrogen oxide, the noxious pollutant such as dioxin, heavy metal in absorption flue gas, makes flue gas qualified discharge, avoids environment.
Description
Technical field
The utility model relates to a kind of boiler smoke denitration in the stove device, specifically for the flue gas that purification coal-burning boiler produces, belongs to environmental technology field.
Background technology
Coal-burning boiler coal dust used is after 1200 DEG C ~ 1500 DEG C high-temperature firings, the flue-gas temperature discharged is mostly between 120 ~ 160 DEG C, residing flue gas environmental condition is more severe, oxygen content that is as higher in dust concentration, flue gas is higher, water capacity is comparatively large, heavy metal concentration is more high, fire coal boiler fume SO
2concentration of emission reach 600 ~ 800mg/Nm
3, the concentration of emission of NOx reaches 150 ~ 200g/Nm
3, severe contamination is caused to environment.
At present, for the process of fire coal boiler fume, denitrating technique mainly with ammoniacal liquor (or urea liquid) for reducing agent, with reaction of nitrogen oxides in burner hearth; Then carry out removing SO
2gas, wherein SO
2the removal methods of gas adopts semidry method or wet processing, and said method exists shortcomings:
1, denitrating technique mainly with ammoniacal liquor (or urea liquid) for reducing agent, with reaction of nitrogen oxides in burner hearth; Its shortcoming is that ammoniacal liquor and liquefied ammonia are that dangerous cargo is not easy to transport and stores; And urea liquid need be prepared at the scene, carries, dilutes, mix to be injected in burner hearth again and go, denitration efficiency is low, complex process, and cost of investment and regular maintenance are costly.
2, semi-dry desulphurization sprays in reactor by nozzle or rotary sprayer by lime white, forms the drop that particle diameter is less, make SO
2gas and lime white react and generate salt, and its shortcoming is that the preparation of lime white is complicated, and desulfuration efficiency is limited.
3, wet desulphurization then adopts scrubbing tower form, can produce the waste water containing the inorganic villaumite of high concentration and heavy metal, and produce secondary pollution, need be equipped with Waste Water Treatment, cost of investment is high, and operating cost is also high.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned weak point, thus provides a kind of boiler smoke denitration in the stove device, and this device denitrating technique is mainly reducing agent with urea granules, and with reaction of nitrogen oxides in burner hearth, in burner hearth, NOx is reduced to N
2and water; Desulfurization adopts circulation dry process, and doctor solution consumption is few and utilization rate is high, and in cyclic process, sorbent particle is under mutual rubbing action, constantly the exposed surface that makes new advances, and desulphurization reaction is constantly carried out fully, and desulfurization degree is high; In whole sweetening process, operating temperature is higher than dew point, and not corrosion or condensation, produces without waste water, do not produce secondary pollution; It is high that this device has desulfuration efficiency, and denitration efficiency is high, and investment operating cost is low, and reliability is high, and energy consumption is low, safeguards easily, the advantages such as floor space is little, system long service life, SO
2concentration of emission 40mg/Nm
3, the concentration of emission 80mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB13223-2011 standard " fossil-fuel power plant atmospheric pollutant emission standard " (SO
2< 50mg/Nm
3, NOx < 100mg/Nm
3, dust emission concentration < 20mg/Nm
3), the noxious pollutant such as dioxin, heavy metal in absorption flue gas, makes flue gas qualified discharge, avoids environment.
The technical solution of the utility model is: a kind of boiler smoke denitration in the stove device, comprise incinerator, flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, described flue gas Online Monitoring Control device connects frequency conversion rotary feeder, connect electron helical above frequency conversion rotary feeder to claim, electron helical claims to connect discharger, discharger connects urea granules feed bin, mixture generator is connected below frequency conversion rotary feeder, mixture generator one tunnel connects high pressure roots blower fan, urea granules playpipe of separately leading up to connects urea granules jet, urea granules jet is positioned at above the sidewall of incinerator burner hearth, connecting bypass pipeline between described flue gas Online Monitoring Control device and electronic air inlet valve import, by-pass line is connected with main air blower import, by-pass line is provided with by-passing valve, described electronic air inlet valve outlet is connected with reaction tower air intake, reaction tower air intake bottom is connected with taper ash collection slot, taper ash collection slot connects electric cinder valve, reaction tower air intake top is connected with trunnion, the trunnion top calcium hydroxide that has been linked in sequence dusts mouth, active carbon entrance, water jet, water jet top is connected with exhanst gas outlet, exhanst gas outlet connects sack cleaner, sack cleaner bottom is connected with air flume, middle pressure roots blower is connected with bottom air flume, air flume side coupled reaction tower circulating line, reaction tower circulating line one tunnel connects recycle feed valve, another road connects ash silo motor-driven valve, ash silo motor-driven valve connects ash silo, ash silo bottom connects electric cinder valve, reaction tower calcium hydroxide dusts mouth by calcium hydroxide playpipe connection mixture generator, mixture generator one tunnel connects high pressure roots blower fan, frequency conversion rotary feeder is connected above mixture generator, frequency conversion rotary feeder connects electron helical and claims, electron helical claims to connect discharger, discharger connects calcium hydroxide dry powder feed bin, reaction tower active carbon entrance connects mixture generator by active carbon playpipe, mixture generator one tunnel connects high pressure roots blower fan, frequency conversion rotary feeder is connected above mixture generator, frequency conversion rotary feeder connects electron helical and claims, electron helical claims to connect discharger, discharger connects active carbon feed bin, reaction tower water jet connects water pump by pipeline, water pump connects water tank.
The beneficial effects of the utility model are: this device denitrating technique is mainly reducing agent with urea granules, and with reaction of nitrogen oxides in burner hearth, in burner hearth, NOx is reduced to N
2and water; Desulfurization adopts circulation dry process, and doctor solution consumption is few and utilization rate is high, and in cyclic process, sorbent particle is under mutual rubbing action, constantly the exposed surface that makes new advances, and desulphurization reaction is constantly carried out fully, and desulfurization degree is high; In whole sweetening process, operating temperature is higher than dew point, and not corrosion or condensation, produces without waste water, do not produce secondary pollution; It is high that this device has desulfuration efficiency, and denitration efficiency is high, and investment operating cost is low, and reliability is high, and energy consumption is low, safeguards easily, the advantages such as floor space is little, system long service life, SO
2concentration of emission 40mg/Nm
3, the concentration of emission 80mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB13223-2011 standard " fossil-fuel power plant atmospheric pollutant emission standard " (SO
2< 50mg/Nm
3, NOx < 100mg/Nm
3, dust emission concentration < 20mg/Nm
3), the noxious pollutant such as dioxin, heavy metal in absorption flue gas, makes flue gas qualified discharge, avoids environment.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Fig. 2 is part A enlarged drawing in Fig. 1.
Fig. 3 is part B enlarged drawing in Fig. 1.
Fig. 1, Fig. 2, in Fig. 3, 1. incinerator, 2. electronic air inlet valve, 3. reaction tower air intake, 4. taper ash collection slot, 5. electric cinder valve, 6. trunnion, 7. calcium hydroxide dusts mouth, 8. active carbon entrance, 9. water jet, 10. water tank, 11. water pumps, 12. reaction towers, 13. exhanst gas outlets, 14. recycle feed valves, 15. reaction tower circulating lines, 16. sack cleaners, 17. air flumes, roots blower is pressed in 18., 19. ash silo motor-driven valves, 20. ash silos, 21. electric cinder valves, 22. calcium hydroxide dry powder feed bins, 23. dischargers, 24. electron helicals claim, 25. frequency conversion rotary feeders, 26. high pressure roots blower fans, 27. mixture generators, 28. calcium hydroxide playpipes, 29. active carbon feed bins, 30. dischargers, 31. electron helicals claim, 32. frequency conversion rotary feeders, 33. high pressure roots blower fans, 34. mixture generators, 35. active carbon playpipes, 36. by-passing valves, 37. by-pass lines, 38. main air blowers, 39. chimneys, 40. urea granules feed bins, 41. dischargers, 42. electron helicals claim, 43. frequency conversion rotary feeders, 44. high pressure roots blower fans, 45. mixture generators, 46. urea granules playpipes, 47. urea granules jets, 48. flue gas Online Monitoring Control devices.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is further described.
As Fig. 1, Fig. 2, shown in Fig. 3, the utility model is a kind of boiler smoke denitration in the stove device, comprise incinerator 1, flue gas Online Monitoring Control device 48, electronic air inlet valve 2, reaction tower 12, sack cleaner 16, main air blower 38, chimney 39, it is characterized in that: described incinerator 1 is linked in sequence flue gas Online Monitoring Control device 48, electronic air inlet valve 2, reaction tower 12, sack cleaner 16, main air blower 38, chimney 39, described flue gas Online Monitoring Control device 48 connects frequency conversion rotary feeder 43, connect electron helical above frequency conversion rotary feeder 43 and claim 42, electron helical claims 42 connection dischargers 41, discharger 41 connects urea granules feed bin 40, mixture generator 45 is connected below frequency conversion rotary feeder 43, mixture generator 45 1 tunnel connects high pressure roots blower fan 44, urea granules playpipe 46 of separately leading up to connects urea granules jet 47, urea granules jet 47 is positioned at above the sidewall of incinerator 1 burner hearth, connecting bypass pipeline 37 between described flue gas Online Monitoring Control device 48 and electronic air inlet valve 2 import, by-pass line 37 is connected with main air blower 38 import, by-pass line 37 is provided with by-passing valve 36, described electronic air inlet valve 2 outlet is connected with reaction tower air intake 3, reaction tower air intake 3 bottom is connected with taper ash collection slot 4, taper ash collection slot 4 connects electric cinder valve 5, reaction tower air intake 3 top is connected with trunnion 6, the trunnion 6 top calcium hydroxide that has been linked in sequence dusts mouth 7, active carbon entrance 8, water jet 9, water jet 9 top is connected with exhanst gas outlet 13, exhanst gas outlet 13 connects sack cleaner 16, sack cleaner 16 bottom is connected with air flume 17, middle pressure roots blower 18 is connected with bottom air flume 17, air flume 17 side coupled reaction tower circulating line 15, reaction tower circulating line 15 1 tunnel connects recycle feed valve 14, another road connects ash silo motor-driven valve 19, ash silo motor-driven valve 19 connects ash silo 20, ash silo 20 bottom connects electric cinder valve 21, the reaction tower calcium hydroxide mouth 7 that dusts connects mixture generator 27 by calcium hydroxide playpipe 28, mixture generator 27 1 tunnel connects high pressure roots blower fan 26, frequency conversion rotary feeder 25 is connected above mixture generator 27, frequency conversion rotary feeder 25 connects electron helical and claims 24, electron helical claims 24 connection dischargers 23, discharger 23 connects calcium hydroxide dry powder feed bin 22, reaction tower active carbon entrance 8 connects mixture generator 34 by active carbon playpipe 35, mixture generator 34 1 tunnel connects high pressure roots blower fan 33, frequency conversion rotary feeder 32 is connected above mixture generator 34, frequency conversion rotary feeder 32 connects electron helical and claims 31, electron helical claims 31 connection dischargers 30, discharger 30 connects active carbon feed bin 29, reaction tower water jet 9 connects water pump 11 by pipeline, water pump 11 connects water tank 10.
The course of work of the present utility model: 170t/h coal-burning boiler 1, exhaust gas volumn 380000m
3/ h, flue-gas temperature 120 ~ 160 DEG C, SO
2concentration 600 ~ 800mg/Nm
3, the concentration 150 ~ 200mg/Nm of NOx
3, dust concentration 15g/Nm
3, oxygen content is 5% ~ 8%;
Claim 42 by urea granules feed bin 40, discharger 41, electron helical, urea granules injection apparatus that frequency conversion rotary feeder 43, high pressure roots blower fan 44, mixture generator 45, urea granules playpipe 46, urea granules jet 47 etc. form, the exhaust gas volumn of flue gas Online Monitoring Control device 48 pairs of incinerators 1 and the amount of generation NOx detect, and feed back to PLC control system, PLC control system calculates the consumption of urea, claim after 42 Weighings through electron helical, by frequency conversion rotary feeder 43, according to operating mode, conveying capacity is adjusted by the mode changing rotating speed, conveying capacity sends into blender 45, from the wind-force of high pressure roots blower fan 44, the urea granules falling into blender 45 is sent into urea granules jet 47 by urea granules playpipe 46 to be entered in incinerator 1 burner hearth, in incinerator 1 burner hearth, nitrogen oxide generation chemical reaction in urea granules and flue gas:
2CO(NH
2)
2+4NO+O
2＝4N
2+4H
2O+2CO
2
4CO(NH
2)
2+4NO
2＝6N
2+8H
2O+2CO
2
In burner hearth, NOx is reduced to N
2and water;
The flue gas of coal-burning boiler 1, after denitration process, enters reaction tower 12 by the suction function of main air blower 38, is accelerated after flue gas enters reaction tower 12 at trunnion 6 place, and high velocity air forms strong turbulent flow in reaction tower 12, produces efficient sufficient gas-solid contact; Through desulfurization process containing high concentrate dust flue gas from reaction tower 12 top exhanst gas outlet 13 out after, udst separation is carried out in the sack cleaner 16 entering rear portion, flue gas through purification flows out sack cleaner 16, enters the outer row of chimney 39 by main air blower 38 and clean flue; When the flue-gas temperature entering sack cleaner 16 exceedes the operating temperature of cloth bag, open by-passing valve 36, close electronic air inlet valve 2, make flue gas enter main air blower 38 by by-pass line 37, discharged by chimney 39, protection cloth bag;
Claim 24 by calcium hydroxide dry powder feed bin 22, discharger 23, electron helical, calcium hydroxide injection apparatus that frequency conversion rotary feeder 25, high pressure roots blower fan 26, mixture generator 27, calcium hydroxide playpipe 28 etc. form, according to the exhaust gas volumn of incinerator 1 and the amount of generation acidulants, calculate Ca (OH)
2consumption, claim after 24 Weighings through electron helical, by frequency conversion rotary feeder 25, according to operating mode, powder delivering amount is adjusted by the mode changing rotating speed, powder delivering amount sends into blender 27, from the wind-force of high pressure roots blower fan 26, the powder falling into blender 27 is sent into the calcium hydroxide mouth 7 that dusts by calcium hydroxide playpipe 28 to be entered in reaction tower 12, in reaction tower 12, spread in calcium hydroxide particle in flue gas under mutual rubbing action, constantly (Asia) calcium sulfate of calcium hydroxide particle Surface Creation is removed, make the calcium hydroxide of the granule interior constantly exposed surface that makes new advances, desulphurization reaction is constantly gone on fully, SO in flue gas
2removal efficiency high, due to SO
3, the sour gas such as HF, HCL compares SO
2easier and calcium hydroxide reacts, SO in reaction tower 12
3, HF, HCL removal efficiency high, in reaction tower 12, reacted calcium hydroxide is by air flume 17, reaction tower circulating line 15 and reaction tower 12 carry out calcium hydroxide iterative cycles, its internal circulating load is controlled by recycle feed valve 14, middle pressure roots blower 18 is provided with bottom air flume 17, calcium hydroxide in air flume 17 is in suspended state all the time, that guarantees to have occurred removes reaction, when after desulfurization operation a period of time, open ash silo motor-driven valve 19, by desulfurization product, dust in flue gas enters ash silo 20, the circulatory system is discharged by electric cinder valve 21, calcium hydroxide induction system is by calcium hydroxide iterative cycles and smoke contacts, circulating ratio reaches 150 ~ 260 times, calcium hydroxide utilization rate is high,
A series of chemical change is there is in above-mentioned technical process:
Ca(OH)
2+SO
2+1/2H
2O→CaSO
3.1/2H
2O+H
2O
Ca(OH)
2+SO
3+H
2O→CaSO
4.2H
2O
Ca(OH)
2+2HCL→CaCL
2.2H
2O
Ca(OH)
2+2HF→CaF
2.2H
2O
CaSO
3.1/2H
2O+1/2O
2+2/3H
2O→CaSO
4.2H
2O
Ca(OH)
2+CO
2→CaCO
3+H
2O
In reaction tower 12, the drying of mixture is relatively uniform, and recycle hydrogen calcium oxide has fabulous mobility, can guarantee the stable of operating mode in reaction tower 12; The particle becoming thicker in sweetening process because of conglomeration drops in reaction tower taper ash collection slot 4 under gravity, and bottom reaction tower, electric cinder valve 5 is discharged;
Secondary desulfuration reaction on cloth bag: under the effect of negative pressure, Ca (OH)
2powder adsorption forms one deck Ca (OH) on cloth bag surface
2bisque, reacts further with the acid fume gas that contains entering deduster.In course of reaction, adopt deduster import and export pressure differential to control deashing frequency, prescribe a time limit when pressure differential exceedes the upper of setting, deashing is carried out to cloth bag, so that Ca (OH)
2powder is constantly adsorbed on cloth bag surface and contains acid fume solid/liquid/gas reactions.Ca (OH)
2iterative cycles and smoke contacts, Ca (OH)
2utilization rate is high, improves desulfuration efficiency;
Claim 31 by feed bin active carbon 29, discharger 30, electron helical, injection apparatus that frequency conversion rotary feeder 32, high pressure roots blower fan 33, mixture generator 34, active carbon playpipe 35 etc. form active carbon; According to the exhaust gas volumn of incinerator 1 and the amount of harmful substance such as generation dioxin, heavy metal etc., the consumption of calculated activity charcoal, claim after 31 Weighings through electron helical, by frequency conversion rotary feeder 32, according to operating mode, active carbon conveying capacity is adjusted by the mode changing rotating speed, active carbon sends into blender 34, from the wind-force of high pressure roots blower fan 33, the active carbon falling into blender 34 is sent into active carbon entrance 8 by active carbon playpipe 35 enter in reaction tower 12, the active carbon sprayed into adsorbs harmful substances such as the dioxin in flue gas and heavy metals;
Water for industrial use in water tank 10 pumps in the water jet 9 of reaction tower 12 by water pump 11, and water, with vaporific ejection, improves Ca (OH)
2with SO
2, SO
3, the gas such as HF, HCL mass transfer, heat transfer efficiency, improve reaction rate, neutralization reaction occur, remove the sour gas in flue gas;
As can be seen here, the utility model denitrating technique is mainly reducing agent with urea granules, and with reaction of nitrogen oxides in burner hearth, in burner hearth, NOx is reduced to N
2and water; Desulfurization adopts circulation dry process, and doctor solution consumption is few and utilization rate is high, and desulfuration efficiency is high; In whole sweetening process, operating temperature is higher than dew point, and not corrosion or condensation, produces without waste water, do not produce secondary pollution; It is high that this device has desulfuration efficiency, and denitration efficiency is high, and investment operating cost is low, and reliability is high, and energy consumption is low, safeguards easily, the advantages such as floor space is little, system long service life, SO
2concentration of emission 40mg/Nm
3, the concentration of emission 80mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB13223-2011 standard " fossil-fuel power plant atmospheric pollutant emission standard " (SO
2< 50mg/Nm
3, NOx < 100mg/Nm
3, dust emission concentration < 20mg/Nm
3), the noxious pollutant such as dioxin, heavy metal in absorption flue gas, makes flue gas qualified discharge, avoids environment.
Claims (1)
1. a boiler smoke denitration in the stove device, comprise incinerator, flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence flue gas Online Monitoring Control device, electronic air inlet valve, reaction tower, sack cleaner, main air blower, chimney, described flue gas Online Monitoring Control device connects frequency conversion rotary feeder, connect electron helical above frequency conversion rotary feeder to claim, electron helical claims to connect discharger, discharger connects urea granules feed bin, mixture generator is connected below frequency conversion rotary feeder, mixture generator one tunnel connects high pressure roots blower fan, urea granules playpipe of separately leading up to connects urea granules jet, urea granules jet is positioned at above the sidewall of incinerator burner hearth, connecting bypass pipeline between described flue gas Online Monitoring Control device and electronic air inlet valve import, by-pass line is connected with main air blower import, by-pass line is provided with by-passing valve, described electronic air inlet valve outlet is connected with reaction tower air intake, reaction tower air intake bottom is connected with taper ash collection slot, taper ash collection slot connects electric cinder valve, reaction tower air intake top is connected with trunnion, the trunnion top calcium hydroxide that has been linked in sequence dusts mouth, active carbon entrance, water jet, water jet top is connected with exhanst gas outlet, exhanst gas outlet connects sack cleaner, sack cleaner bottom is connected with air flume, middle pressure roots blower is connected with bottom air flume, air flume side coupled reaction tower circulating line, reaction tower circulating line one tunnel connects recycle feed valve, another road connects ash silo motor-driven valve, ash silo motor-driven valve connects ash silo, ash silo bottom connects electric cinder valve, reaction tower calcium hydroxide dusts mouth by calcium hydroxide playpipe connection mixture generator, mixture generator one tunnel connects high pressure roots blower fan, frequency conversion rotary feeder is connected above mixture generator, frequency conversion rotary feeder connects electron helical and claims, electron helical claims to connect discharger, discharger connects calcium hydroxide dry powder feed bin, reaction tower active carbon entrance connects mixture generator by active carbon playpipe, mixture generator one tunnel connects high pressure roots blower fan, frequency conversion rotary feeder is connected above mixture generator, frequency conversion rotary feeder connects electron helical and claims, electron helical claims to connect discharger, discharger connects active carbon feed bin, reaction tower water jet connects water pump by pipeline, water pump connects water tank.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520028434.2U CN204469514U (en) | 2015-01-09 | 2015-01-09 | A kind of boiler smoke denitration in the stove device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520028434.2U CN204469514U (en) | 2015-01-09 | 2015-01-09 | A kind of boiler smoke denitration in the stove device |
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| CN204469514U true CN204469514U (en) | 2015-07-15 |
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| CN201520028434.2U Expired - Fee Related CN204469514U (en) | 2015-01-09 | 2015-01-09 | A kind of boiler smoke denitration in the stove device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106345244A (en) * | 2016-10-17 | 2017-01-25 | 浙江大学 | Device and method for removing sulfur trioxide from coal-fired flue gas |
| CN108786409A (en) * | 2018-08-17 | 2018-11-13 | 深圳市凯盛科技工程有限公司 | A kind of high temperature desulfurizing denitration flue gas dust collecting system |
| CN108905620A (en) * | 2018-08-17 | 2018-11-30 | 深圳市凯盛科技工程有限公司 | A kind of high temperature desulfurizing denitration flue gas dust collecting system based on catalyst filter element |
| CN109745840A (en) * | 2019-01-30 | 2019-05-14 | 浙江大维高新技术股份有限公司 | The processing unit and method of blast furnace gas burning flue gas |
| CN111450674A (en) * | 2020-04-23 | 2020-07-28 | 自贡市东方联合机械配套有限公司 | Tail gas reoxidation device for removing acidic oxide smoke exhaust pipeline |
-
2015
- 2015-01-09 CN CN201520028434.2U patent/CN204469514U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106345244A (en) * | 2016-10-17 | 2017-01-25 | 浙江大学 | Device and method for removing sulfur trioxide from coal-fired flue gas |
| CN108786409A (en) * | 2018-08-17 | 2018-11-13 | 深圳市凯盛科技工程有限公司 | A kind of high temperature desulfurizing denitration flue gas dust collecting system |
| CN108905620A (en) * | 2018-08-17 | 2018-11-30 | 深圳市凯盛科技工程有限公司 | A kind of high temperature desulfurizing denitration flue gas dust collecting system based on catalyst filter element |
| CN109745840A (en) * | 2019-01-30 | 2019-05-14 | 浙江大维高新技术股份有限公司 | The processing unit and method of blast furnace gas burning flue gas |
| CN111450674A (en) * | 2020-04-23 | 2020-07-28 | 自贡市东方联合机械配套有限公司 | Tail gas reoxidation device for removing acidic oxide smoke exhaust pipeline |
| CN111450674B (en) * | 2020-04-23 | 2022-02-08 | 自贡市东方联合机械配套有限公司 | Tail gas reoxidation device for removing acidic oxide smoke exhaust pipeline |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150715 Termination date: 20160109 |