CN102350189A - Half-dry low-temperature smoke denitrification system - Google Patents
Half-dry low-temperature smoke denitrification system Download PDFInfo
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- CN102350189A CN102350189A CN2011102630717A CN201110263071A CN102350189A CN 102350189 A CN102350189 A CN 102350189A CN 2011102630717 A CN2011102630717 A CN 2011102630717A CN 201110263071 A CN201110263071 A CN 201110263071A CN 102350189 A CN102350189 A CN 102350189A
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- ozone
- flue gas
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- 239000000779 smoke Substances 0.000 title abstract description 9
- 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 48
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 47
- 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 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- 230000000694 effects Effects 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
- 238000005516 engineering process Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 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
- 239000002912 waste gas Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 230000008569 process Effects 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
- 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
- 239000002585 base Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 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
- 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
- 239000012047 saturated solution Substances 0.000 description 1
- 239000000243 solution Substances 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 the flue gases purification field.
Background technology;
Along with the serious day by day of domestic atmosphere pollution situation with to the attention of flue gas desulfurization and the extensive utilization of sulfur removal technology, the sulfide that is discharged in the atmosphere significantly reduces, and NO
xInfluence to gas begins to highlight day by day, has become China SO that continues
2After one of the important atmosphere pollution demanding urgently administering.
Present domestic flue gas desulfurization and denitrification adopts catalytic reduction flue gas denitration (SCR) technology and lime, lime stone---gypsum wet desulfurizing and denitrifying process more.
Need be under the condition of high temperature about 350 ℃ of-450 ℃ of ability of described (SCR) technology and use therein catalyst guarantee its good nitre effect of removing; Because most large medium-size boiler all has been equipped with heat recovery system the heat in the flue gas has been recycled; Final discharged flue gas temperature generally has been lower than 300 ℃; Therefore said (SCR) system must be arranged on the heat recovery system front end; This just need offer a branch road and be connected with the SCR system in exhaust gases passes; Flue gas after SCR handles flows to heat recovery system again and carries out heat recovery, causes the unusual complicacy of system architecture and causes thermal loss.
Lime, lime stone---gypsum wet desulfurizing and denitrifying process; Powder adding set and/or absorption tower need be set in system; The residual quantity of lime or land plaster is big in the waste gas after processing; Increased the load of dust arrester, and adopted above-mentioned wet processing can produce liquid by-product and cause secondary water to pollute.
Therefore to have purification efficiency higher for above-mentioned technology; But its complex structure, absorption tower volume are very huge; System's floor space is big; The pollution of secondary water, equipment investment costliness are loaded greatly, had to deduster; Operating cost is high, and the catalyst that disadvantages such as construction and installation cycle length, operational management difficulty, especially denitration are used needs dependence on import; Cost is high, has restricted its extensive popularization.
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, the deduster load is little and do not have investment that secondary water pollutes and the denitration device of the economic and reliable that operating cost is low satisfies actual needs.
Summary of the invention:
The objective of the invention is to overcome at least 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, the deduster load is little and it is low not have the pollution of secondary 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 type low-temperature denitration of flue gas system; It comprises reactor; Deduster and exhaust apparatus; Also comprise alkali lye and gas high pressure mixing device; The ozone gas feeding mechanism; Ultraviolet radiation facility; Said reactor comprises a gas approach; The 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 handled; Its pure qi (oxygen) outlet is connected with the import of deduster; The outlet of deduster is connected with exhaust apparatus; The ozone gas import is connected with the ozone gas feeding mechanism; Said ultraviolet radiation facility is installed in inside reactor near the gas approach place; On alkali lye and the 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 is provided with ozone gas input port and aerator; The output of ozone generator is connected with aerator through the ozone gas input port, and the output of alkali lye and gas high pressure mixing device is connected with the interior high pressure sprays fog equipment of 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 through the ozone gas input port.
2. said ultraviolet radiation facility is installed in the reactor, and is arranged on the import department of flue gas and ozone gas;
3. the spray particle diameter of said high pressure sprays fog equipment does
Spray amount is 0.052L * Δ T, and wherein L is flue gas flow m
3/ h (mark attitude), Δ T are temperature difference before and after flue gas is handled;
4. the temperature of flue gas below 300 ℃, is preferably 100～200 ℃ more than 100 ℃ in the input reactor.
5. be high saturated aqueous slkali via the alkali lye input port on alkali lye and gas high pressure mixing device input.
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. on the output of ozone generator and pipeline that aerator is connected, the Compressed Gas input unit is set and makes the aqueous slkali that forms high saturated rich gas body and ozone with the effect that strengthens aeration through the gas that is compressed to certain pressure with input; Said gas pressure is: 0.5～0.8MPa.
8. the gas via the input of the gas input port on alkali lye and the gas high pressure mixing device is Compressed Gas, and said gas pressure is: 0.5～0.8MPa.
9. the flow direction, flow velocity and the pressure of gas operated device with the adjustment air-flow is set in the gas approach rear end of reactor 1.
The effect of UV mainly contains following two aspects among the present invention:
1. ultraviolet light and ozone cooperative oxidation; In ultraviolet activation process, UV generates a large amount of hydroxyl radical free radicals with ozone, water decomposition, and the oxidability of these hydroxyl radical free radicals own is strong; But also can taking place, a series of chain reactions produce the more freedom base, can be efficiently with NO
xOxidation, reaction mechanism is following:
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, quicken the oxidation rate of NO, reaction mechanism is following:
NO+hv → NO*, (NO* is the NO of excited state, and characteristic is active)
Under the normal condition, be not subjected to the oxidation reaction mechanism of the NO that ultraviolet activates following:
Therefore, to compare with the normal condition that is not subjected to 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.
Below be flue gas behind ultraviolet and ozone reaction with the reaction equation of aqueous slkali, suppose that here aqueous slkali is the high saturated solution of NaOH solution and Ca (OH) 2.
HNO
3+NaOH→NaNO
3+H
2O
2HNO
3+Ca(OH)
2→Ca(NO
3)
2+H
2O
The half dry type low-temperature denitration of flue gas system of employing technical scheme of the present invention compares with existing lime method and has the following advantages:
1. said ultraviolet radiation facility is installed in the 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, practice thrift equipment investment cost and operating cost, energy-conserving and environment-protective;
2. the temperature of flue gas is more than 100 ℃ in the reactor, and the temperature of reaction back pure qi (oxygen) is also more than 100 ℃, and the moisture that is contained is steam condition, makes reactor and deduster and exhaust apparatus inner dry, avoids corrosion, effectively reduces fault and prolongs equipment life;
3. the temperature of the interior flue gas of reactor is below 300 ℃; Can further handle cooling device cooled smoke in existing steam generator system; Need not transform existing system; Simplify the entire system structure and practice thrift equipment investment; Reduce installation workload; And can utilize energy, realize energy-saving and emission-reduction.
4. the aqueous slkali of saturated rich gas body of vaporific height and ozone drip with through ultraviolet irradiation and O
3NO after the concerted reaction
2Fully contact and react Deng gas, generate pulverous nitrate, the NO in the flue gas is solidified fully;
5. the aqueous slkali of saturated rich gas body of vaporific height and ozone drip can also with the SO in the flue gas
2Fully contact and generate pulverous sulfate, effectively solidify SO residual in the flue gas
2, make the SO in the flue gas
2Solidify fully and play desulfidation, equipment can be realized desulfurization simultaneously, enlarges the equipment scope of application, and one-object-many-purposes is to contain NO and SO simultaneously
2The flue gas treatment effect good, need not to be provided with simultaneously desulfurization and denitrating system, 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 said high pressure sprays fog equipment ejection is small; The contact-making surface that can greatly increase aqueous slkali and ozone thereof and wait to absorb gas improves reaction efficiency; And to make product be dry Powdered, need not dehydration;
7. pass through and NO and remaining SO
2Reacted product all is pulverous, and small amount of moisture wherein is also with the form of steam, and no secondary water pollutes, and need not to carry out further water treatment, can effectively reduce system equipment investment and operation water consumption, 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 the processing reduces the load of deduster greatly; And do not need the powder adding set, make system architecture simple, manufacturing, installation and maintenance effectively reduce equipment investment cost and operation expense easily.
9. denitrification process does not have the waste liquid generation, and accessory substance is prone to handle.
Description of drawings:
Fig. 1 is an embodiment sketch map realizing technical scheme of the present invention
Among the figure, 1 is reactor, and 101 is gas approach; 102 is the ozone gas import; 103 are the pure qi (oxygen) outlet, and 104 is high pressure sprays fog equipment, and 2 is alkali lye and gas high pressure mixing device; 201 is the alkali lye input port; 202 is gas input port, and 203 is the output of alkali lye and gas high pressure mixing device 2, and 204 is the ozone gas input port; 205 is aerator; 3 is the ozone gas feeding mechanism, and 4 is ultraviolet radiation facility, and 5 is deduster; 6 is exhaust apparatus; 7 is the alkali lye feeding mechanism, and 8 is gas operated device, and 9 is pressure-regulating device; 10 is gas compressor, and 11 is supercharging device.
The specific embodiment:
Below in conjunction with 1 pair of one embodiment of the present of invention of accompanying drawing a technical scheme of the present invention left side is specifically described.
As shown in Figure 1; A kind of half dry type low-temperature denitration of flue gas 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; Said 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 the recuperation of heat processing; 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 with the input ozone gas; Can on the ozone conveyance conduit, add supercharging device in case of necessity to increase the input quantity and the dividing potential drop of ozone gas; Said ultraviolet radiation facility is installed in the reactor; And be arranged on gas approach 101 and ozone gas import 102 places; Alkali lye input port 201 and gas input port 202 are set on alkali lye and the gas high pressure mixing device 2; 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 reactor 1 interior high pressure sprays fog equipment 104; Be to regulate the pressure of high pressure sprays fog equipment 104, be connected with high pressure sprays fog equipment 104 in the reactor 1 at the output 203 of alkali lye and gas high pressure mixing device 2 in the present embodiment and added pressure-regulating device 9 on the pipeline with adjusting pressure and spray amount.
As shown in fig. 1; Present embodiment also is provided with 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 to into and carries out aeration in the alkali lye water and gas high pressure mixing device, makes to send into behind the high saturated aqueous slkali that forms high concentration rich gas body and ozone to be arranged in the interior high pressure sprays fog equipment 104 of reactor.Wherein, be high saturated aqueous slkali via the alkali lye input port on alkali lye and the gas high pressure mixing device 2 201 input; Gas via 202 inputs of the gas input port on alkali lye and the 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 said alkali lye input port high saturated aqueous slkali of 201 inputs 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.
Be to strengthen the aeration effect, the ozone that 11 pairs of supercharging devices are input to alkali lye and gas high pressure mixing device 2 in is set on the output of ozone generator 3 and pipeline that aerator 205 is connected in the present embodiment carries out supercharging makes high saturated rich gas body of formation and ozone with the effect of raising ozone gas dividing potential drop enhancing aeration aqueous slkali; Said gas pressure is preferably 0.5～0.8Mpa.
In addition for waste gas is handled in reactor fully, gas operated device 8 is set in gas approach 101 rear ends of reactor 1 among the embodiment makes it receive ultraviolet abundant irradiation with the flow direction, flow velocity and the pressure of adjustment air-flow and fully contact and produce a series of oxidation reaction to reach degraded NO with the ozone gas of input, the aqueous slkali of the saturated rich gas body of vaporific height and ozone after the atomizing
xPurpose.
In the embodiment of the invention; For better technique effect; Gas via 202 inputs of the gas input port on alkali lye and the gas high pressure mixing device 2 is the Compressed Gas that gas compressor 10 provides; Said gas pressure is preferably 0.5～0.8MPa, and the spray particle diameter of the high pressure sprays fog equipment in the reactor between
Between, speed is 0.052L * Δ T, wherein L is flue gas flow m
3/ h (mark attitude), Δ T are temperature difference before and after flue gas is handled.The pressure of sprayer unit can be set up supercharging device to increase the pressure of sprayer unit at its front end in case of necessity from the aqueous slkali of alkali lye and 2 outputs of gas high pressure mixing device in the present embodiment.The nitrate that after the high pressure sprays fog equipment reaction, produces is Powdered; Because water content is few in the saturated aqueous slkali of vaporific height of ejection; And the temperature in the reactor is more than 100 ℃, so there is no waste liquid generation in water form with steam in reactor that the aqueous slkali of ejection produces after reacting.
Main purpose of the present invention is the NO that removes in the waste gas, but the aqueous slkali of saturated rich gas body of vaporific height and ozone drip can also with the SO in the flue gas
2Fully contact and generate pulverous sulfate, effectively solidify SO residual in the flue gas
2, make the SO in the flue gas
2Solidify fully and play desulfidation, equipment can be realized desulfurization simultaneously, enlarges the equipment scope of application, and one-object-many-purposes is to contain NO and SO simultaneously
2The flue gas treatment effect good, need not to be provided with simultaneously desulfurization and denitrating system, can significantly reduce equipment investment and operation and maintenance cost.
The half dry type low-temperature denitration of flue gas system of employing technical scheme of the present invention can be applied to the desulfurization and the denitration of power plant, fire coal or oil burning boiler and Industrial Stoves flue gas.
Claims (10)
1. half dry type low-temperature denitration of flue gas 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); Said 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); Said ultraviolet radiation facility (4) is installed in the reactor (1); Alkali lye input port (201) and gas input port (202) are set on alkali lye and the gas high pressure mixing device (2), and the output (203) of alkali lye and gas high pressure mixing device (2) is connected with the interior high pressure sprays fog equipment (104) of reactor (1).
2. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system, it is characterized in that: said ultraviolet radiation facility is installed in the reactor, and is arranged on the import department of flue gas and ozone gas.
3. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system; It is characterized in that: 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) through ozone gas input port (204).
4 as claimed in claim 1, wherein a semi-dry flue gas denitrification temperature, characterized in that: said high-pressure spray device (104) a spray particle size of
spray volume of 0.052L × ΔT.
5. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system, it is characterized in that: gas approach (101) rear end in reactor (1) is provided with gas operated device.
6. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system; It is characterized in that: the gas via the input of the gas input port (202) on alkali lye and the gas high pressure mixing device (2) is the gas with certain pressure through overcompression, and its pressure is between 0.5～0.8Mpa.
7. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system; It is characterized in that: the output of ozone generator (3) on ozone gas input port (204) and pipeline that aerator (205) is connected, be provided with the Compressed Gas input unit with input through being compressed to the gas of certain pressure, its pressure is between 0.5～0.8Mpa.
8. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system, it is characterized in that: the temperature of flue gas is preferably 100～200 ℃ more than 100 ℃ in the input reactor.
9. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 1 system, it is characterized in that: the aqueous slkali via the input of the alkali lye input port (201) on alkali lye and the gas high pressure mixing device (2) is high saturated aqueous slkali.
10. a kind of half dry type low-temperature denitration of flue gas as claimed in claim 8 system, it is characterized in that: the high saturated aqueous slkali via the input of the alkali lye input port (201) on alkali lye and the gas high pressure mixing device (2) 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110263071.7A CN102350189B (en) | 2011-08-24 | 2011-08-24 | Half-dry low-temperature smoke denitrification system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110263071.7A CN102350189B (en) | 2011-08-24 | 2011-08-24 | Half-dry low-temperature smoke denitrification system |
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| Publication Number | Publication Date |
|---|---|
| CN102350189A true CN102350189A (en) | 2012-02-15 |
| CN102350189B CN102350189B (en) | 2014-02-26 |
Family
ID=45573897
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110263071.7A Expired - Fee Related CN102350189B (en) | 2011-08-24 | 2011-08-24 | Half-dry low-temperature smoke denitrification system |
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| CN102350189B (en) | 2014-02-26 |
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