CN102350189B - Half-dry low-temperature smoke denitrification system - Google Patents
Half-dry low-temperature smoke denitrification system Download PDFInfo
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- CN102350189B CN102350189B CN201110263071.7A CN201110263071A CN102350189B CN 102350189 B CN102350189 B CN 102350189B CN 201110263071 A CN201110263071 A CN 201110263071A CN 102350189 B CN102350189 B CN 102350189B
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- 239000000779 smoke Substances 0.000 title claims abstract description 24
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 59
- 239000003513 alkali Substances 0.000 claims abstract description 46
- 230000005855 radiation Effects 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 114
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 86
- 239000003546 flue gas Substances 0.000 claims description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 33
- 238000002156 mixing Methods 0.000 claims description 27
- 239000007921 spray Substances 0.000 claims description 22
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 18
- 230000008676 import Effects 0.000 claims description 15
- 229920006395 saturated elastomer Polymers 0.000 claims description 14
- 238000005276 aerator Methods 0.000 claims description 12
- 230000007246 mechanism Effects 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- 239000011575 calcium Substances 0.000 claims description 6
- 239000000292 calcium oxide Substances 0.000 claims description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 3
- XGZRAKBCYZIBKP-UHFFFAOYSA-L disodium;dihydroxide Chemical compound [OH-].[OH-].[Na+].[Na+] XGZRAKBCYZIBKP-UHFFFAOYSA-L 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000000428 dust Substances 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 5
- 239000003245 coal Substances 0.000 abstract description 2
- 238000005507 spraying Methods 0.000 abstract 2
- 239000000446 fuel Substances 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 0.000 description 9
- 238000000034 method Methods 0.000 description 9
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 6
- 235000011941 Tilia x europaea Nutrition 0.000 description 6
- 239000004571 lime Substances 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 5
- 238000005273 aeration Methods 0.000 description 4
- 238000009434 installation Methods 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002912 waste gas Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 150000003254 radicals Chemical class 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- TUJKJAMUKRIRHC-UHFFFAOYSA-N hydroxyl Chemical compound [OH] TUJKJAMUKRIRHC-UHFFFAOYSA-N 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000001994 activation Methods 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 230000002153 concerted effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000005281 excited state Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
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Abstract
The invention provides a half-dry low-temperature smoke denitrification system which comprises a reactor, a dust remover, an exhauster, an alkali liquor and gas high pressure mixer, an ozone supply device and an ultraviolet radiation device, wherein the reactor comprises a smoke inlet, an ozone inlet, a purified gas outlet and a high pressure spraying device; the smoke inlet of the reactor is connected with a conveying pipeline of smoke to be purified; the purified gas outlet of the reactor is connected with the inlet of the dust remover; the outlet of the dust remover is connected with the exhauster or a heat recovery device; the ozone inlet is connected with the ozone supply device; the ultraviolet radiation device is arranged at a position, close to the smoke inlet, inside the reactor; an alkali liquor input port and a gas input port are formed on the alkali liquor and gas high pressure mixer; and the output end of the alkali liquor and gas high pressure mixer is connected with the high pressure spraying device in the reactor. The half-dry low-temperature smoke denitrification system can be applied to power plants, fire coal or fuel boilers and industrial kilns.
Description
Technical field:
The present invention relates to a kind of brand-new denitrating flue gas dust pelletizing system, belong to flue gases purification field.
Background technology;
Along with the day by day serious of domestic atmosphere pollution situation and the extensive utilization to the attention of flue gas desulfurization and sulfur removal technology, the sulfide being discharged in atmosphere significantly reduces, and NO
xthe impact of gas is started day by day to highlight, become China SO that continues
2after one of the important atmosphere pollution of urgently administering.
Current domestic flue gas desulfurization and denitrification adopts catalytic reduction flue gas denitration (SCR) technique and lime, lime stone---gypsum wet desulfurizing and denitrifying process more.
Described (SCR) technique and use therein catalyst need to be under the condition of high temperature approximately 350 ℃ of-450 ℃ of guarantees it is good in nitre effect, because most large medium-size boiler has all been equipped with heat recovery system, the heat in flue gas is recycled, the flue-gas temperature of final discharge is generally lower than 300 ℃, therefore described (SCR) system must be arranged on heat recovery system front end, this just need to offer a branch road and be connected with SCR system in exhaust gases passes, flue gas after SCR processes flows to heat recovery system again and carries out heat recovery, cause system architecture complex and cause thermal loss.
Lime, lime stone---gypsum wet desulfurizing and denitrifying process, powder adding set and/or absorption tower need to be set in system, in waste gas after processing, the residual quantity of lime or land plaster is large, increased the load of dust arrester, and adopted above-mentioned wet processing can produce liquid by-product to cause secondarily polluted water.
Therefore to have purification efficiency higher for above-mentioned technique, but its complex structure, absorption tower volume are very huge, system floor space is large, secondarily polluted water, equipment investment costliness are loaded greatly, had to deduster, the catalyst that the disadvantages such as operating cost is high, and the construction and installation cycle is long, operational management is difficult, especially denitration are used needs dependence on import, cost is high, has restricted it and has extensively promoted.
Therefore need a kind of be applicable to coal-fired plant boiler, Industrial Boiler and other Industrial Stoves simple in structure, volume is little, floor space is little, deduster load is little and meet actual needs without investment and the low reliable denitration device of economy of operating cost of secondarily polluted water.
Summary of the invention:
The object of the invention is at least overcome a deficiency of existing denitrating system, a kind of brand-new half dry type integrated fume denitration dust collecting system is provided, it is simple in structure, volume is little, floor space is little, deduster load is little and low without secondarily polluted water, investment and operating cost, and installation and maintenance is convenient.
Technical scheme of the present invention is to realize like this, a kind of half-dry low-temperature smoke denitrification system, it comprises reactor, deduster and exhaust apparatus, also comprise alkali lye and gas high pressure mixing device, ozone gas feeding mechanism, ultraviolet radiation facility, described reactor comprises a gas approach, ozone gas import, pure qi (oxygen) outlet and high pressure sprays fog equipment, its gas approach is connected with the conveyance conduit of flue gas to be clean after recuperation of heat is processed, its pure qi (oxygen) outlet is connected with the import of deduster, the outlet of deduster is connected with exhaust apparatus, ozone gas import is connected with ozone gas feeding mechanism, described ultraviolet radiation facility is arranged on inside reactor near gas approach place, on alkali lye and gas high pressure mixing device, alkali lye input port and gas input port are set, bottom at alkali lye and gas high pressure mixing device arranges ozone gas input port and aerator, the output of ozone generator is connected with aerator by ozone gas input port, the output of alkali lye and gas high pressure mixing device is connected with the high pressure sprays fog equipment in reactor.
For better denitration effect, technical characterstic of the present invention can also be specially following technical characterictic:
1. in the bottom of alkali lye and gas high pressure mixing device, ozone gas input port and aerator are set, the output of ozone generator is connected with aerator by ozone gas input port.
2. described in, ultraviolet radiation facility is arranged in reactor, and is arranged on the import department of flue gas and ozone gas;
3. described in, the spray particle diameter of high pressure sprays fog equipment is
spray amount is 0.052L * Δ T, and wherein L is flue gas flow m
3/ h (mark state), Δ T is temperature difference before and after flue gas is processed;
4. in input reactor, the temperature of flue gas, more than 100 ℃, below 300 ℃, is preferably 100～200 ℃.
5. what via the alkali lye input port on alkali lye and gas high pressure mixing device, input is high saturated aqueous slkali.
6. the aqueous slkali of above-mentioned alkali lye input port input is NaOH NaOH, calcium hydroxide Ca (OH)
2, potassium hydroxide KOH, calcium oxide CaO, ammonia NH
3one or more combination Deng the aqueous solution.
7. Compressed Gas input unit is set on the pipeline being connected with aerator at the output of ozone generator and to input the compressed gas to certain pressure, to strengthen the effect of aeration, makes to form the aqueous slkali of high saturated rich gas body and ozone; Described gas pressure is: 0.5～0.8MPa.
8. the gas via the gas input port input on alkali lye and gas high pressure mixing device is Compressed Gas, and described gas pressure is: 0.5～0.8MPa.
9. gas operated device is set to adjust the flow direction, flow velocity and the pressure of air-flow in the gas approach rear end of reactor 1.
In the present invention, the effect of UV mainly contains following two aspects:
1. ultraviolet light and ozone cooperative oxidation, in ultraviolet activation process, UV generates a large amount of hydroxyl radical free radicals by ozone, water decomposition, and the oxidability of these hydroxyl radical free radicals own is strong, but also can there are a series of chain reactions, produce more free radical, can be efficiently by NO
xoxidation, reaction mechanism is as follows:
O
3+hv→O(
1D)+O
2
O(
1D)+H
2O→2·OH
OH+NO→HNO
2
O
3+NO→NO
2+O
2
2NO
2+O
3→N
2O
5+O
2
2NO
2+O+H
2O→2HNO
3
N
2O
5+H
2O→2HNO
3
2. activate NO, accelerate the oxidation rate of NO, reaction mechanism is as follows:
NO+hv → NO*, (NO that NO* is excited state, characteristic is active)
Under normal circumstances, be not subject to the oxidation reaction mechanism of the NO that ultraviolet activates as follows:
Therefore, not compare with being subject to the normal condition of ultraviolet irradiation, ultraviolet ray can greatly activate NO, and makes itself and O
2reaction rate improve 10
3doubly, make itself and O
3reaction rate improve 10
7～10
9doubly.
Be below flue gas after ultraviolet and ozone reaction with the reaction equation of aqueous slkali, suppose that aqueous slkali is the high saturated solution of NaOH solution and Ca (OH) 2 here.
HNO
3+NaOH→NaNO
3+H
2O
2HNO
3+Ca(OH)
2→Ca(NO
3)
2+H
2O
Adopt the half-dry low-temperature smoke denitrification system of technical solution of the present invention to compare and have the following advantages with existing lime method:
1. described in, ultraviolet radiation facility is arranged in reactor, and is arranged on the import department of flue gas and ozone gas, can greatly activate NO, and makes itself and O
2or O
3reaction rate improve 10
7～10
9doubly, improve the speed of flue gas processing and the capacity of single device, save equipment investment cost and operating cost, energy-conserving and environment-protective;
2. in reactor, the temperature of flue gas is more than 100 ℃, and after reaction, the temperature of pure qi (oxygen) is also more than 100 ℃, and contained moisture is steam condition, makes reactor and deduster and exhaust apparatus inner dry, avoids corrosion, effectively reduces fault extension device life-span;
3. the temperature of the interior flue gas of reactor is below 300 ℃, can be further processed the cooled flue gas of cooling device in existing steam generator system, do not need existing system to transform, simplify entire system structure and save equipment investment, reduce installation workload, and can utilize energy, realize energy-saving and emission-reduction.
The aqueous slkali of the saturated rich gas body of vaporific height and ozone drip with through ultraviolet irradiation and O
3nO after concerted reaction
2deng gas, fully contact and react, generating pulverous nitrate, making the NO in flue gas completely curing;
The aqueous slkali of the saturated rich gas body of vaporific height and ozone drip can also with flue gas in SO
2carry out fully contact and generate pulverous sulfate, effectively solidify residual SO in flue gas
2, make the SO in flue gas
2completely solidify and play desulfidation, equipment can be realized desulfurization simultaneously, expands the equipment scope of application, and one-object-many-purposes, to contain NO and SO simultaneously
2flue gas treatment effect good, without desulfurization and denitrating system are set simultaneously, can significantly reduce equipment investment and operation and maintenance cost;
6. the high pressure sprays fog equipment of reactor ejects is that the aqueous slkali of high saturated rich gas body and ozone drips, therefore its water content is very low, the vaporific grain diameter of described high pressure sprays fog equipment ejection is small, the contact-making surface that can greatly increase aqueous slkali and ozone and gas to be absorbed improves reaction efficiency, and to make product be dried Powdered, without dehydration;
7. pass through and NO and remaining SO
2reacted product is all pulverous, and a small amount of moisture wherein also, with the form of steam, without secondarily polluted water, without carrying out further water treatment, can effectively reduce system equipment investment and operation water consumption, the investment of reduction system greatly and operating cost.
8. what in system, adopt is the aqueous slkali of high concentration, is not the alkali of powdery, and the alkali of the powdery of noresidue in the waste gas after processing reduces the load of deduster greatly; And do not need powder adding set, make system architecture simple, easily manufacture, installation and maintenance, effectively reduce equipment investment cost and operation expense.
9. denitrification process produces without waste liquid, and accessory substance is easily processed.
Accompanying drawing explanation:
Fig. 1 is an embodiment schematic diagram realizing technical scheme of the present invention
In figure, 1 is reactor, 101 is gas approach, 102 is ozone gas import, 103 is pure qi (oxygen) outlet, 104 is high pressure sprays fog equipment, 2 is alkali lye and gas high pressure mixing device, 201 is alkali lye input port, 202 is gas input port, 203 is the output of alkali lye and gas high pressure mixing device 2, 204 is ozone gas input port, 205 is aerator, 3 is ozone gas feeding mechanism, 4 is ultraviolet radiation facility, 5 is deduster, 6 is exhaust apparatus, 7 is alkali lye feeding mechanism, 8 is gas operated device, 9 is pressure-regulating device, 10 is gas compressor, 11 is supercharging device.
The specific embodiment:
Below in conjunction with 1 pair of one embodiment of the present of invention of accompanying drawing to the left specific descriptions of technical scheme of the present invention.
As shown in Figure 1, a kind of half-dry low-temperature smoke denitrification system, it comprises reactor 1, deduster 5 and exhaust apparatus 6, also comprise alkali lye and gas high pressure mixing device 2, ozone gas feeding mechanism 3, ultraviolet radiation facility 4, described reactor comprises a gas approach 101, ozone gas import 102, pure qi (oxygen) outlet 103 and high pressure sprays fog equipment 104, its gas approach 101 is connected at the smoke conveying duct to be clean below 300 ℃ with temperature after recuperation of heat is processed, its pure qi (oxygen) outlet 103 is connected with the import of deduster 5, the outlet of deduster 5 is connected with exhaust apparatus 6, ozone gas import 102 is connected to input ozone gas with ozone gas feeding mechanism 3, can on ozone conveyance conduit, add if desired supercharging device to increase input quantity and the dividing potential drop of ozone gas, described ultraviolet radiation facility is arranged in reactor, and be arranged on gas approach 101 and ozone gas import 102 places, on alkali lye and gas high pressure mixing device 2, alkali lye input port 201 and gas input port 202 are set, alkali lye input port 201 is connected with alkali lye feeding mechanism 7, the output 203 of alkali lye and gas high pressure mixing device 2 is connected with the high pressure sprays fog equipment 104 in reactor 1, for regulating the pressure of high pressure sprays fog equipment 104, in the present embodiment, in high pressure sprays fog equipment 104 connecting pipes in the output 203 of alkali lye and gas high pressure mixing device 2 and reactor 1, added pressure-regulating device 9 to regulate pressure and spray amount.
As shown in fig. 1, the present embodiment also arranges ozone gas input port 204 and aerator 205 in the bottom of alkali lye and gas high pressure mixing device 2, the output of ozone generator 3 is connected with aerator 205 through ozone gas input port 204, a part of ozone that ozone generator is produced leads in alkali lye water and gas high pressure mixing device and carries out aeration, sends in the high pressure sprays fog equipment 104 being arranged in reactor after making to form the saturated aqueous slkali of height of high concentration rich gas body and ozone.What wherein, via the alkali lye input port 201 on alkali lye and gas high pressure mixing device 2, input is high saturated aqueous slkali; Gas via gas input port 202 inputs on alkali lye and gas high pressure mixing device 2 is the gas with certain pressure of gas compressor 10 outputs, and its pressure is preferably 0.5～0.8MPa.The described alkali lye input port high saturated aqueous slkali of 201 input can be NaOH NaOH, calcium hydroxide Ca (OH)
2, potassium hydroxide KOH, calcium oxide CaO, ammonia NH
3one or more combination Deng the aqueous solution.
For strengthening aeration effect, 11 pairs of supercharging devices are set in the present embodiment on the pipeline that the output of ozone generator 3 is connected with aerator 205 and are input to ozone in alkali lye and gas high pressure mixing device 2 and carry out supercharging and with the effect of raising ozone gas dividing potential drop enhancing aeration, make to form the aqueous slkali of high saturated rich gas body and ozone; Described gas pressure is preferably 0.5～0.8Mpa.
In addition for waste gas is processed fully in reactor, gas operated device 8 is set in gas approach 101 rear ends of reactor 1 in embodiment and to adjust the flow direction, flow velocity and the pressure of air-flow, makes it be subject to ultraviolet abundant irradiation and fully contact and produce a series of oxidation reaction to reach degraded NO with the aqueous slkali of the ozone gas of input, the saturated rich gas body of vaporific height after atomization and ozone
xobject.
In the embodiment of the present invention, for better technique effect, the Compressed Gas that the gas of inputting via the gas input port 202 on alkali lye and gas high pressure mixing device 2 provides for gas compressor 10, described gas pressure is preferably 0.5～0.8MPa, and the spray particle diameter of the high pressure sprays fog equipment in reactor between
between, speed is 0.052L * Δ T, wherein L is flue gas flow m
3/ h (mark state), Δ T is temperature difference before and after flue gas is processed.In the present embodiment, the pressure of sprayer unit, from the aqueous slkali of alkali lye and 2 outputs of gas high pressure mixing device, can be set up supercharging device to increase the pressure of sprayer unit at its front end if desired.The nitrate producing after high pressure sprays fog equipment reaction is Powdered, because water content in the saturated aqueous slkali of vaporific height of ejection is few, and the temperature in reactor is more than 100 ℃, and water form with steam in reactor that therefore aqueous slkali of ejection produces after reaction exists, and without waste liquid, produces.
Main purpose of the present invention is the NO removing in waste gas, but the aqueous slkali of the saturated rich gas body of vaporific height and ozone drip can also with flue gas in SO
2carry out fully contact and generate pulverous sulfate, effectively solidify residual SO in flue gas
2, make the SO in flue gas
2completely solidify and play desulfidation, equipment can be realized desulfurization simultaneously, expands the equipment scope of application, and one-object-many-purposes, to contain NO and SO simultaneously
2flue gas treatment effect good, without desulfurization and denitrating system are set simultaneously, can significantly reduce equipment investment and operation and maintenance cost.
The half-dry low-temperature smoke denitrification system of employing technical solution of the present invention can be applied to desulfurization and the denitration of power plant, fire coal or oil burning boiler and industrial furnace smoke.
Claims (10)
1. a half-dry low-temperature smoke denitrification system, it comprises reactor (1), deduster (5) and exhaust apparatus (6), it is characterized in that: also comprise alkali lye and gas high pressure mixing device (2), ozone gas feeding mechanism (3), ultraviolet radiation facility (4), described reactor comprises a gas approach (101), ozone gas import (102), pure qi (oxygen) outlet (103) and high pressure sprays fog equipment (104), its gas approach (101) is connected with the conveyance conduit of flue gas to be clean, its pure qi (oxygen) outlet (103) is connected with the import of deduster (5), the outlet of deduster (5) is connected with exhaust apparatus (6), ozone gas import (102) is connected with ozone gas feeding mechanism (3), described ultraviolet radiation facility (4) is arranged in reactor (1), alkali lye input port (201) and gas input port (202) are set on alkali lye and gas high pressure mixing device (2), the output (203) of alkali lye and gas high pressure mixing device (2) is connected with the high pressure sprays fog equipment (104) in reactor (1), in the bottom of alkali lye and gas high pressure mixing device (2), ozone gas input port (204) and aerator (205) are set, the output of ozone generator (3) is connected with aerator (205) by ozone gas input port (204).
2. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, is characterized in that: described ultraviolet radiation facility is arranged in reactor, and is arranged on the import department of flue gas and ozone gas.
3. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, is characterized in that: the spray particle diameter of described high pressure sprays fog equipment (104) is
spray amount is 0.052L * Δ T, flue gas flow m when wherein L is for mark state
3/ h, Δ T is temperature difference before and after flue gas is processed.
4. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, is characterized in that: gas approach (101) rear end in reactor (1) arranges gas operated device.
5. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, it is characterized in that: the gas via gas input port (202) input on alkali lye and gas high pressure mixing device (2) is the gas with certain pressure through overcompression, and its pressure is between 0.5～0.8Mpa.
6. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, it is characterized in that: Compressed Gas input unit is set to input the compressed gas to certain pressure on the pipeline being connected with aerator (205) through ozone gas input port (204) at the output of ozone generator (3), its pressure is between 0.5～0.8Mpa.
7. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, is characterized in that: in input reactor, the temperature of flue gas is more than 100 ℃, below 300 ℃.
8. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 1, is characterized in that: the aqueous slkali via alkali lye input port (201) input on alkali lye and gas high pressure mixing device (2) is high saturated aqueous slkali.
9. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 8, is characterized in that: the saturated aqueous slkali of height via alkali lye input port (201) input on alkali lye and gas high pressure mixing device (2) is NaOH NaOH, calcium hydroxide Ca (OH)
2, potassium hydroxide KOH, calcium oxide CaO, ammonia NH
3one or more combination Deng the aqueous solution.
10. a kind of half-dry low-temperature smoke denitrification system as claimed in claim 7, is characterized in that: in input reactor, the temperature of flue gas is 100～200 ℃.
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|---|---|---|---|
| CN201110263071.7A CN102350189B (en) | 2011-08-24 | 2011-08-24 | Half-dry low-temperature smoke denitrification system |
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|---|---|---|---|
| CN201110263071.7A CN102350189B (en) | 2011-08-24 | 2011-08-24 | Half-dry low-temperature smoke denitrification system |
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