CN204478080U - A kind of incinerator smoke desulfuring and denitrifying apparatus - Google Patents
A kind of incinerator smoke desulfuring and denitrifying apparatus Download PDFInfo
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- CN204478080U CN204478080U CN201520028432.3U CN201520028432U CN204478080U CN 204478080 U CN204478080 U CN 204478080U CN 201520028432 U CN201520028432 U CN 201520028432U CN 204478080 U CN204478080 U CN 204478080U
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
Abstract
A kind of incinerator smoke desulfuring and denitrifying apparatus, comprise incinerator, waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, in described waste heat regenerator, one-time surface evaporimeter is installed, the entrance point of one-time surface evaporimeter is connected with the high-pressure outlet end of organic working medium circulating pump, the port of export of one-time surface evaporimeter is connected with the upper flange interface of organic working medium steam turbine after pipeline.The utility model can remove the SO in the flue gas of domestic waste incineration 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 incinerator smoke desulfuring and denitrifying apparatus, specifically for the flue gas that purifying consumer waste incinerator produces, belongs to environmental technology field.
Background technology
In prior art, the flue gas of house refuse after fully burning between produce 850 DEG C ~ 1100 DEG C, denitrating technique is mainly by ammonia spirit, aqueous solution of urea or other liquid nitrogenous reducing agent, ammonia is decomposed into after directly spraying into exhaust gases passes 850 DEG C ~ 1100 DEG C temperature province atomizations, nitrogen oxide generation reduction reaction in ammonia and flue gas, generate the harmless object such as nitrogen and water, then enter waste heat boiler, carry out removing S0 after the flue gas of 550 DEG C ~ 600 DEG C of waste heat boiler outflow is down to 180 DEG C by misting cooling cooling system
2gas, then carries out the filtration of dust granules, wherein SO
2the removal methods of gas adopts semidry method or wet processing, and said method exists shortcomings:
1, the waste heat boiler flue gas of 550 DEG C ~ 600 DEG C is out down to 180 DEG C by misting cooling cooling system, and this part waste heat does not utilize, and is wasted.
2, dedusting after misting cooling cooling, increases the content of water in flue gas, not only makes cloth bag harden, also easily cause water and dust bonding, cause system equipment to block.
3, 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.
4, 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.
5, denitrating technique is mainly by ammonia spirit, aqueous solution of urea or other liquid nitrogenous reducing agent, ammonia is decomposed into after directly spraying into exhaust gases passes 850 DEG C ~ 1100 DEG C temperature province atomizations, nitrogen oxide generation reduction reaction in ammonia and flue gas, generate the harmless object such as nitrogen and water, this technique is that SNCR method (SNCR) belongs to wet denitration, and denitration efficiency is low, this system equipment is more complicated, control loaded down with trivial details, take up an area large, equipment investment and maintenance cost higher.
Summary of the invention
The purpose of this utility model is to overcome above-mentioned weak point, thus a kind of incinerator smoke desulfuring and denitrifying apparatus is provided, this device can not only the thermal energy to greatest extent in recovered flue gas be high-grade electric energy, the exhaust temperature of flue gas can be reduced simultaneously, improve dust collection capacity, obtain good dust removing effects; 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 up to 90%; 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; Adopt selective catalytic reduction (SCR), under catalyst action, reduction of nitrogen oxide is become nitrogen by amino in reducing agent at relatively low temperature, and denitration efficiency is high; 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 70mg/Nm
3, the concentration of emission 40mg/Nm of HCL
3, the concentration of emission 200mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB18485-2014 standard " consumer waste incineration Environmental capacity standard " (SO
2< 80mg/Nm
3, HCL < 50mg/Nm
3, NOx < 250mg/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 incinerator smoke desulfuring and denitrifying apparatus, comprise incinerator, waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, in described waste heat regenerator, one-time surface evaporimeter is installed, the entrance point of one-time surface evaporimeter is connected with the high-pressure outlet end of organic working medium circulating pump, the port of export of one-time surface evaporimeter is connected with the upper flange interface of organic working medium steam turbine after pipeline, the lower interface of organic working medium steam turbine is connected with the air inlet of shell-and-tube cooler by pipeline, the liquid-phase outlet of shell-and-tube cooler is connected with the low pressure inlet end of organic working medium circulating pump by pipeline, organic working medium steam turbine is connected with threephase generator, an end flange interface of shell-and-tube cooler is connected with water circulating pump, another end of shell-and-tube cooler connects cooling tower, cooling tower is connected with water circulating pump, connecting bypass pipeline between described waste heat regenerator 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, described heat exchange of heat pipe connects steam drum, steam drum connects steam accumulator by pipeline, catalyst layer is provided with in the middle of described SCR reactor, SCR reactor top is connected with ammonia/air mixer, ammonia/air mixer one tunnel is connected with dilution ammonia blower fan, another road exports with ammonia dashpot and is connected, described ammonia gasifier, comprise fin heat exchange pipe, feed tube, escape pipe, tube connector, frame, fin heat exchange pipe is totally eight row, often row ten arranges symmetrical composition, conducting is connected by tube connector, along the flow direction of liquid medium, fin number from less to more, fin heat exchange pipe is fixed in frame, first fin heat exchange pipe lower end connects feed tube, first fin heat exchange pipe side sets gradually the second fin heat exchange pipe, 3rd fin heat exchange pipe, 4th fin heat exchange pipe, 5th fin heat exchange pipe, 6th fin heat exchange pipe, 7th fin heat exchange pipe, 8th fin heat exchange pipe, 9th fin heat exchange pipe, tenth fin heat exchange pipe, first fin heat exchange pipe is the heat exchanger tube of band 4 fins, second fin heat exchange pipe is the heat exchanger tube of band 8 fins, 3rd fin heat exchange pipe, 4th fin heat exchange pipe, 5th fin heat exchange pipe, 6th fin heat exchange pipe, 7th fin heat exchange pipe, 8th fin heat exchange pipe, 9th fin heat exchange pipe, tenth fin heat exchange pipe is the heat exchanger tube of band 12 fins, first fin heat exchange pipe upper end is connected with the second fin heat exchange pipe upper end by tube connector, second fin heat exchange pipe lower end is connected with the 3rd fin heat exchange pipe lower end by tube connector, 3rd fin heat exchange pipe upper end is connected with the 4th fin heat exchange pipe upper end by tube connector, 4th fin heat exchange pipe lower end is connected with the 5th fin heat exchange pipe lower end by tube connector, 5th fin heat exchange pipe upper end is connected with the 6th fin heat exchange pipe upper end by tube connector, 6th fin heat exchange pipe lower end is connected with the 7th fin heat exchange pipe lower end by tube connector, 7th fin heat exchange pipe upper end is connected with the 8th fin heat exchange pipe upper end by tube connector, 8th fin heat exchange pipe lower end is connected with the 9th fin heat exchange pipe lower end by tube connector, 9th fin heat exchange pipe upper end is connected with the tenth fin heat exchange pipe upper end by tube connector, tenth fin heat exchange pipe lower end connects escape pipe, escape pipe is connected with the import of ammonia dashpot.
It is further characterized in that: adopt R717 to be circulation organic working medium.
The beneficial effects of the utility model are: this device can not only the thermal energy to greatest extent in recovered flue gas be high-grade electric energy, can reduce the exhaust temperature of flue gas simultaneously, improve dust collection capacity, obtain good dust removing effects; 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 up to 90%; 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; Adopt selective catalytic reduction (SCR), under catalyst action, reduction of nitrogen oxide is become nitrogen by amino in reducing agent at relatively low temperature, and denitration efficiency is high; 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 70mg/Nm
3, the concentration of emission 40mg/Nm of HCL
3, the concentration of emission 200mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB18485-2014 standard " consumer waste incineration Environmental capacity standard " (SO
2< 80mg/Nm
3, HCL < 50mg/Nm
3, NOx < 250mg/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. 4 is C magnified partial view in Fig. 1.
Fig. 5 is the main TV structure schematic diagram of part 8 ammonia gasifier in Fig. 1.
Fig. 6 is the plan structure schematic diagram of part 8 ammonia gasifier in Fig. 1.
Fig. 7 is the left TV structure schematic diagram of part 8 ammonia gasifier in Fig. 1.
Fig. 8 is D place enlarged drawing in Fig. 5.
Fig. 9 is E-E place sectional view in Fig. 5.
Figure 10 is F-F place sectional view in Fig. 5.
Figure 11 is G-G place enlarged drawing in Fig. 5.
Fig. 1, Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6, Fig. 7, Fig. 8, Fig. 9, Figure 10, in Figure 11, 1. incinerator, 2. waste heat regenerator, 3. electronic air inlet valve, 4. reaction tower, 5. sack cleaner, 6. heat exchange of heat pipe, 7.SCR reactor, 8. ammonia gasifier, 9. main air blower, 10. chimney, 11. one-time surface evaporimeters, 12. organic working medium circulating pumps, 13. water circulating pumps, 14. shell-and-tube coolers, 15. organic working medium steam turbines, 16. threephase generators, 17. cooling towers, 18. water tanks, 19. water pumps, 20. reaction tower air intakes, 21. taper ash collection slots, 22. electric cinder valves, 23. calcium hydroxides dust mouth, 24. active carbon entrances, 25. water jets, 26. trunnions, 27. exhanst gas outlets, 28. recycle feed valves, 29. reaction tower circulating lines, 30. ash silo motor-driven valves, 31. ash silos, 32. electric cinder valves, 33. calcium hydroxide playpipes, 34. calcium hydroxide dry powder feed bins, 35. dischargers, 36. electron helicals claim, 37. frequency conversion rotary feeders, 38. high pressure roots blower fans, 39. mixture generators, 40. active carbon playpipes, 41. active carbon feed bins, 42. dischargers, 43. electron helicals claim, 44. frequency conversion rotary feeders, 45. high pressure roots blower fans, 46. mixture generators, 47. by-passing valves, 48. by-pass lines, 49. air flumes, roots blower is pressed in 50., 51. steam drums, 52. steam accumulators, 53. catalyst layers, 54. dilution ammonia blower fans, 55. ammonias/air mixer, 56. ammonia dashpots, 81. first fin heat exchange pipes, 82. second fin heat exchange pipes, 83. the 3rd fin heat exchange pipes, 84. the 4th fin heat exchange pipes, 85. the 5th fin heat exchange pipes, 86. the 6th fin heat exchange pipes, 87. the 7th fin heat exchange pipes, 88. the 8th fin heat exchange pipes, 89. the 9th fin heat exchange pipes, 810. the tenth fin heat exchange pipes, 811. feed tube, 812. escape pipe, 813. frame.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is further described.
As Fig. 1, Fig. 2, Fig. 3, Fig. 4, Fig. 5, Fig. 6, Fig. 7, Fig. 8, Fig. 9, Figure 10, shown in Figure 11, the utility model is a kind of incinerator smoke desulfuring and denitrifying apparatus, comprise incinerator 1, waste heat regenerator 2, electronic air inlet valve 3, reaction tower 4, sack cleaner 5, heat exchange of heat pipe 6, SCR reactor 7, ammonia gasifier 8, main air blower 9, chimney 10, it is characterized in that: described incinerator 1 is linked in sequence waste heat regenerator 2, electronic air inlet valve 3, reaction tower 4, sack cleaner 5, heat exchange of heat pipe 6, SCR reactor 7, ammonia gasifier 8, main air blower 9, chimney 10, in described waste heat regenerator 2, one-time surface evaporimeter 11 is installed, the entrance point of one-time surface evaporimeter 11 is connected with the high-pressure outlet end of organic working medium circulating pump 12, the port of export of one-time surface evaporimeter 11 is connected with the upper flange interface of organic working medium steam turbine 15 after pipeline, the lower interface of organic working medium steam turbine 15 is connected by the air inlet of pipeline with shell-and-tube cooler 14, the liquid-phase outlet of shell-and-tube cooler 14 is connected with the low pressure inlet end of organic working medium circulating pump 12 by pipeline, organic working medium steam turbine 15 is connected with threephase generator 16, an end flange interface of shell-and-tube cooler 14 is connected with water circulating pump 13, another end of shell-and-tube cooler 14 connects cooling tower 17, cooling tower 17 is connected with water circulating pump 13, connecting bypass pipeline 48 between described waste heat regenerator 2 and electronic air inlet valve 3 import, by-pass line 48 is connected with main air blower 9 import, by-pass line 48 is provided with by-passing valve 47, described electronic air inlet valve 3 outlet is connected with reaction tower air intake 20, reaction tower air intake 20 bottom is connected with taper ash collection slot 21, taper ash collection slot 21 connects electric cinder valve 22, reaction tower air intake 20 top is connected with trunnion 26, the trunnion 26 top calcium hydroxide that has been linked in sequence dusts mouth 23, active carbon entrance 24, water jet 25, water jet 25 top is connected with exhanst gas outlet 27, exhanst gas outlet 27 connects sack cleaner 5, sack cleaner 5 bottom is connected with air flume 49, middle pressure roots blower 50 is connected with bottom air flume 49, air flume 49 side coupled reaction tower circulating line 29, reaction tower circulating line 29 1 tunnel connects recycle feed valve 28, another road connects ash silo motor-driven valve 30, ash silo motor-driven valve 30 connects ash silo 31, ash silo 31 bottom connects electric cinder valve 32, the reaction tower calcium hydroxide mouth 23 that dusts connects mixture generator 39 by calcium hydroxide playpipe 33, mixture generator 39 1 tunnel connects high pressure roots blower fan 38, frequency conversion rotary feeder 37 is connected above mixture generator 39, frequency conversion rotary feeder 37 connects electron helical and claims 36, electron helical claims 36 connection dischargers 35, discharger 35 connects calcium hydroxide dry powder feed bin 34, reaction tower active carbon entrance 24 connects mixture generator 46 by active carbon playpipe 40, mixture generator 46 1 tunnel connects high pressure roots blower fan 45, frequency conversion rotary feeder 44 is connected above mixture generator 46, frequency conversion rotary feeder 44 connects electron helical and claims 43, electron helical claims 43 connection dischargers 42, discharger 42 connects active carbon feed bin 41, reaction tower water jet 25 connects water pump 19 by pipeline, water pump 19 connects water tank 18, described heat exchange of heat pipe 6 connects steam drum 51, steam drum 51 connects steam accumulator 52 by pipeline, catalyst layer 53 is provided with in the middle of described SCR reactor 7, SCR reactor 7 top is connected with ammonia/air mixer 55, ammonia/air mixer 55 1 tunnel is connected with dilution ammonia blower fan 54, another road exports with ammonia dashpot 56 and is connected, described ammonia gasifier 8, comprise fin heat exchange pipe, feed tube 811, escape pipe 812, tube connector, frame 813, it is characterized in that: fin heat exchange pipe is totally eight row, often row ten arranges symmetrical composition, conducting is connected by tube connector, along the flow direction of liquid medium, fin number from less to more, fin heat exchange pipe is fixed in frame 813, first fin heat exchange pipe 81 lower end connects feed tube 811, first fin heat exchange pipe 81 side sets gradually the second fin heat exchange pipe 82, 3rd fin heat exchange pipe 83, 4th fin heat exchange pipe 84, 5th fin heat exchange pipe 85, 6th fin heat exchange pipe 86, 7th fin heat exchange pipe 87, 8th fin heat exchange pipe 88, 9th fin heat exchange pipe 89, tenth fin heat exchange pipe 810, first fin heat exchange pipe 81 is the heat exchanger tube of band 4 fins, second fin heat exchange pipe 82 is the heat exchanger tube of band 8 fins, 3rd fin heat exchange pipe 83, 4th fin heat exchange pipe 84, 5th fin heat exchange pipe 85, 6th fin heat exchange pipe 86, 7th fin heat exchange pipe 87, 8th fin heat exchange pipe 88, 9th fin heat exchange pipe 89, tenth fin heat exchange pipe 810 is the heat exchanger tube of band 12 fins, first fin heat exchange pipe 81 upper end is connected with the second fin heat exchange pipe 82 upper end by tube connector, second fin heat exchange pipe 82 lower end is connected with the 3rd fin heat exchange pipe 83 lower end by tube connector, 3rd fin heat exchange pipe 83 upper end is connected with the 4th fin heat exchange pipe 84 upper end by tube connector, 4th fin heat exchange pipe 84 lower end is connected with the 5th fin heat exchange pipe 85 lower end by tube connector, 5th fin heat exchange pipe 85 upper end is connected with the 6th fin heat exchange pipe 86 upper end by tube connector, 6th fin heat exchange pipe 86 lower end is connected with the 7th fin heat exchange pipe 87 lower end by tube connector, 7th fin heat exchange pipe 87 upper end is connected with the 8th fin heat exchange pipe 88 upper end by tube connector, 8th fin heat exchange pipe 88 lower end is connected with the 9th fin heat exchange pipe 89 lower end by tube connector, 9th fin heat exchange pipe 89 upper end is connected with the tenth fin heat exchange pipe 810 upper end by tube connector, tenth fin heat exchange pipe 810 lower end connects escape pipe 812, escape pipe 812 is connected with ammonia dashpot 56 import.
Described organic working medium is R717, the power pressure entering low boiling working fluid steam turbine is 2.5MPa, and when the power pressure after expansion work is 0.55MPa, system electromotive power output is 500KW, Rankine cycle efficiency is 18.5%, and the flue-gas temperature that system is discharged is 150 DEG C.
The course of work of the present utility model: 500t/d domestic waste incineration 1, exhaust gas volumn 14 ~ 15 × 10
4m
3/ h, flue-gas temperature 550 ~ 600 DEG C, SO
2concentration 300 ~ 700mg/Nm
3, the concentration 800 ~ 1200mg/Nm of HCL
3, the concentration 400 ~ 500mg/Nm of NOx
3, dust concentration 20 ~ 30g/Nm
3, the oxygen content 8% ~ 12% of flue gas, the water capacity 15% ~ 25% of flue gas, the flue gas of domestic waste incineration 1 enters in waste heat regenerator 2 by the suction function of main air blower 9, simultaneously, organic working medium is driven by organic working medium circulating pump 12, first being installed on the heat absorbing fume afterheat carrier in the one-time surface evaporimeter 11 in waste heat regenerator 2, become saturated vapor, after pressure regulator valve, working substance steam is expansion work in organic working medium steam turbine 15, and drive threephase generator 16 to generate electricity, the working substance steam of discharging from organic working medium steam turbine 15 is condensed into saturated liquid by shell-and-tube cooler 14, send in one-time surface evaporimeter 11 after worker quality liquid being pressurizeed by organic working medium circulating pump 12 again, start new round circulation, from shell-and-tube cooler 14 recirculated water out, cooled by cooling tower 17, send in shell-and-tube cooler 14 through water circulating pump 13, start new round circulation, the electric energy that system sends is three-phase alternating current, rated voltage is 380V, electrical network in factory is incorporated to after pressure regulation, or directly give electrical equipment use,
Enter reaction tower 4 from waste heat regenerator 2 flue gas out, accelerated at trunnion 26 place after flue gas enters reaction tower 4, high velocity air forms strong turbulent flow in reaction tower 4, produces efficient sufficient gas-solid contact; Through desulfurization process containing high concentrate dust flue gas from reaction tower 4 top exhanst gas outlet 27 out after, udst separation is carried out in the sack cleaner 5 entering rear portion, flue gas through purification flows out sack cleaner 5, enters the outer row of chimney 10 by main air blower 9 and clean flue; When the flue-gas temperature entering sack cleaner 5 exceedes the operating temperature of cloth bag, open by-passing valve 47, close electronic air inlet valve 3, make flue gas enter main air blower 9 by by-pass line 48, then discharged by chimney 10, protection cloth bag;
Claim 36 by calcium hydroxide dry powder feed bin 34, discharger 35, electron helical, calcium hydroxide injection apparatus that frequency conversion rotary feeder 37, high pressure roots blower fan 38, mixture generator 39, calcium hydroxide playpipe 33 etc. form, according to the exhaust gas volumn of incinerator 1 and the amount of generation sulfide, calculate Ca (OH)
2consumption, claim after 36 Weighings through electron helical, by frequency conversion rotary feeder 37, according to operating mode, powder delivering amount is adjusted by the mode changing rotating speed, powder delivering amount sends into blender 39, from the wind-force of high pressure roots blower fan 38, the powder falling into blender 39 is sent into the calcium hydroxide mouth 23 that dusts by calcium hydroxide playpipe 33 to be entered in reaction tower 4, in reaction tower 4, 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 can reach 90%, due to SO
3, the sour gas such as HF, HCL compares SO
2easier and calcium hydroxide reacts, SO in reaction tower 4
3, HF, HCL removal efficiency can reach more than 98%, in reaction tower 4, reacted calcium hydroxide is by air flume 49, reaction tower circulating line 29 and reaction tower 4 carry out calcium hydroxide iterative cycles, its internal circulating load is controlled by recycle feed valve 28, middle pressure roots blower 50 is provided with bottom air flume 49, calcium hydroxide in air flume 49 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 30, by desulfurization product, dust in flue gas enters ash silo 31, the circulatory system is discharged by electric cinder valve 32, 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 4, 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 4; The particle becoming thicker in sweetening process because of conglomeration drops in reaction tower taper ash collection slot 21 under gravity, and bottom reaction tower, electric cinder valve 22 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, with the SO entering deduster
2flue gas reacts further.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 SO
2smoke reaction.Ca (OH)
2iterative cycles and smoke contacts, Ca (OH)
2utilization rate is high, improves desulfuration efficiency;
Claim 43 by active carbon feed bin 41, discharger 42, electron helical, injection apparatus that frequency conversion rotary feeder 44, high pressure roots blower fan 45, mixture generator 46, active carbon playpipe 40 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 43 Weighings through electron helical, by frequency conversion rotary feeder 44, according to operating mode, active carbon conveying capacity is adjusted by the mode changing rotating speed, active carbon sends into blender 46, from the wind-force of high pressure roots blower fan 45, the active carbon falling into blender 46 is sent into active carbon entrance 24 by active carbon playpipe 40 enter in reaction tower 4, 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 18 pumps in the water jet 25 of reaction tower 4 by water pump 19, and water, with vaporific ejection, improves Ca (OH)
2with SO
2, SO
3, the gas reaction speed such as HF, HCL, there is neutralization reaction, remove the sour gas in flue gas;
From sack cleaner flue gas out, temperature, at 150 ~ 160 DEG C, enters heat exchange of heat pipe 6, and smoke absorption is from the heat of steam accumulator 52, and flue-gas temperature is elevated to 180 ~ 190 DEG C, meets the requirement of denitrating technique to flue-gas temperature;
Denitrification process: liquefied ammonia is transported to liquid ammonia storage tank by tank car, the liquefied ammonia of output becomes ammonia after ammonia gasifier 8, is delivered to ammonia dashpot 56 for subsequent use; Ammonia in ammonia dashpot 56 is sent in ammonia/air mixer 55 after decompression, after mixing from the air diluting ammonia blower fan 54, sprayed in flue gas by the nozzle of spray ammonia barrier and also fully mix with it, then SCR reactor 7 is entered, when flue gas flows through the catalyst layer 53 of SCR reactor 7, catalytic reaction occurs, and NOx is optionally reduced:
4NH
3+ 4NO+O
2→ 4N
2ten 6H
2o
8NH
3+6NO
2→7N
2+12H
2O
In reactor, NOx is reduced to N
2and water;
As can be seen here, the utility model can not only the thermal energy to greatest extent in recovered flue gas be high-grade electric energy, can reduce the exhaust temperature of flue gas simultaneously, improve dust collection capacity, obtain good dust removing effects; 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 up to 90%; 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; Adopt selective catalytic reduction (SCR), under catalyst action, reduction of nitrogen oxide is become nitrogen by amino in reducing agent at relatively low temperature, and denitration efficiency is high; 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 70mg/Nm
3, the concentration of emission 40mg/Nm of HCL
3, the concentration of emission 200mg/Nm of NOx
3, dust emission concentration 15mg/Nm
3, be better than GB18485-2014 standard " consumer waste incineration Environmental capacity standard " (SO
2< 80mg/Nm
3, HCL < 50mg/Nm
3, NOx < 250mg/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 (2)
1. an incinerator smoke desulfuring and denitrifying apparatus, comprise incinerator, waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, it is characterized in that: described incinerator is linked in sequence waste heat regenerator, electronic air inlet valve, reaction tower, sack cleaner, heat exchange of heat pipe, SCR reactor, ammonia gasifier, main air blower, chimney, in described waste heat regenerator, one-time surface evaporimeter is installed, the entrance point of one-time surface evaporimeter is connected with the high-pressure outlet end of organic working medium circulating pump, the port of export of one-time surface evaporimeter is connected with the upper flange interface of organic working medium steam turbine after pipeline, the lower interface of organic working medium steam turbine is connected with the air inlet of shell-and-tube cooler by pipeline, the liquid-phase outlet of shell-and-tube cooler is connected with the low pressure inlet end of organic working medium circulating pump by pipeline, organic working medium steam turbine is connected with threephase generator, an end flange interface of shell-and-tube cooler is connected with water circulating pump, another end of shell-and-tube cooler connects cooling tower, cooling tower is connected with water circulating pump, connecting bypass pipeline between described waste heat regenerator 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, described heat exchange of heat pipe connects steam drum, steam drum connects steam accumulator by pipeline, catalyst layer is provided with in the middle of described SCR reactor, SCR reactor top is connected with ammonia/air mixer, ammonia/air mixer one tunnel is connected with dilution ammonia blower fan, another road exports with ammonia dashpot and is connected, described ammonia gasifier, comprise fin heat exchange pipe, feed tube, escape pipe, tube connector, frame, fin heat exchange pipe is totally eight row, often row ten arranges symmetrical composition, conducting is connected by tube connector, along the flow direction of liquid medium, fin number from less to more, fin heat exchange pipe is fixed in frame, first fin heat exchange pipe lower end connects feed tube, first fin heat exchange pipe side sets gradually the second fin heat exchange pipe, 3rd fin heat exchange pipe, 4th fin heat exchange pipe, 5th fin heat exchange pipe, 6th fin heat exchange pipe, 7th fin heat exchange pipe, 8th fin heat exchange pipe, 9th fin heat exchange pipe, tenth fin heat exchange pipe, first fin heat exchange pipe is the heat exchanger tube of band 4 fins, second fin heat exchange pipe is the heat exchanger tube of band 8 fins, 3rd fin heat exchange pipe, 4th fin heat exchange pipe, 5th fin heat exchange pipe, 6th fin heat exchange pipe, 7th fin heat exchange pipe, 8th fin heat exchange pipe, 9th fin heat exchange pipe, tenth fin heat exchange pipe is the heat exchanger tube of band 12 fins, first fin heat exchange pipe upper end is connected with the second fin heat exchange pipe upper end by tube connector, second fin heat exchange pipe lower end is connected with the 3rd fin heat exchange pipe lower end by tube connector, 3rd fin heat exchange pipe upper end is connected with the 4th fin heat exchange pipe upper end by tube connector, 4th fin heat exchange pipe lower end is connected with the 5th fin heat exchange pipe lower end by tube connector, 5th fin heat exchange pipe upper end is connected with the 6th fin heat exchange pipe upper end by tube connector, 6th fin heat exchange pipe lower end is connected with the 7th fin heat exchange pipe lower end by tube connector, 7th fin heat exchange pipe upper end is connected with the 8th fin heat exchange pipe upper end by tube connector, 8th fin heat exchange pipe lower end is connected with the 9th fin heat exchange pipe lower end by tube connector, 9th fin heat exchange pipe upper end is connected with the tenth fin heat exchange pipe upper end by tube connector, tenth fin heat exchange pipe lower end connects escape pipe, escape pipe is connected with the import of ammonia dashpot.
2. a kind of incinerator smoke desulfuring and denitrifying apparatus according to claim 1, is characterized in that: adopt R717 to be circulation organic working medium.
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| CN201520028432.3U CN204478080U (en) | 2015-01-09 | 2015-01-09 | A kind of incinerator smoke desulfuring and denitrifying apparatus |
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| CN201520028432.3U CN204478080U (en) | 2015-01-09 | 2015-01-09 | A kind of incinerator smoke desulfuring and denitrifying apparatus |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621773A (en) * | 2016-12-30 | 2017-05-10 | 中南大学 | Ammonia-carbon combined desulfurization and denitration method for sintering flue gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106621773A (en) * | 2016-12-30 | 2017-05-10 | 中南大学 | Ammonia-carbon combined desulfurization and denitration method for sintering flue gas |
| CN106621773B (en) * | 2016-12-30 | 2019-11-26 | 中南大学 | A kind of sintering flue gas ammonia charcoal combined desulfurization and denitration method |
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