CN1923341A - Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification - Google Patents
Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification Download PDFInfo
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- CN1923341A CN1923341A CNA2006100530906A CN200610053090A CN1923341A CN 1923341 A CN1923341 A CN 1923341A CN A2006100530906 A CNA2006100530906 A CN A2006100530906A CN 200610053090 A CN200610053090 A CN 200610053090A CN 1923341 A CN1923341 A CN 1923341A
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- nitrogen oxide
- liquid washing
- ozone
- alkali liquid
- boiler
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- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 238000006477 desulfuration reaction Methods 0.000 title claims description 19
- 230000003647 oxidation Effects 0.000 title claims description 19
- 238000007254 oxidation reaction Methods 0.000 title claims description 19
- 230000003009 desulfurizing Effects 0.000 title claims description 18
- 239000003517 fume Substances 0.000 title claims description 14
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 78
- 239000003513 alkali Substances 0.000 claims abstract description 31
- 229910052813 nitrogen oxide Inorganic materials 0.000 claims abstract description 26
- 238000005406 washing Methods 0.000 claims abstract description 25
- 239000000779 smoke Substances 0.000 claims abstract description 17
- AKEJUJNQAAGONA-UHFFFAOYSA-N Sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims abstract description 8
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000035484 reaction time Effects 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 27
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 26
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 19
- 239000003546 flue gas Substances 0.000 claims description 18
- 239000007921 spray Substances 0.000 claims description 15
- KWYUFKZDYYNOTN-UHFFFAOYSA-M potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 12
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 229910001868 water Inorganic materials 0.000 claims description 10
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 8
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium monoxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 8
- ZODDGFAZWTZOSI-UHFFFAOYSA-N nitric acid;sulfuric acid Chemical compound O[N+]([O-])=O.OS(O)(=O)=O ZODDGFAZWTZOSI-UHFFFAOYSA-N 0.000 claims description 5
- 229960003563 Calcium Carbonate Drugs 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 4
- 239000000920 calcium hydroxide Substances 0.000 claims description 4
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 4
- 239000000292 calcium oxide Substances 0.000 claims description 4
- 238000002425 crystallisation Methods 0.000 claims description 3
- 230000005712 crystallization Effects 0.000 claims description 3
- 230000001590 oxidative Effects 0.000 claims description 3
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 abstract 2
- 239000003344 environmental pollutant Substances 0.000 abstract 1
- 231100000719 pollutant Toxicity 0.000 abstract 1
- 230000003068 static Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 23
- 238000005200 wet scrubbing Methods 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 5
- 239000000428 dust Substances 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 238000005201 scrubbing Methods 0.000 description 5
- 239000002250 absorbent Substances 0.000 description 4
- 230000002745 absorbent Effects 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 235000019738 Limestone Nutrition 0.000 description 2
- 210000002381 Plasma Anatomy 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010894 electron beam technology Methods 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 230000001603 reducing Effects 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- DVARTQFDIMZBAA-UHFFFAOYSA-O Ammonium nitrate Chemical compound [NH4+].[O-][N+]([O-])=O DVARTQFDIMZBAA-UHFFFAOYSA-O 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910002089 NOx Inorganic materials 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000001264 neutralization Effects 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 230000000414 obstructive Effects 0.000 description 1
- 230000000607 poisoning Effects 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
The invention relates to a device for removing several pollutants of boiler smoke. Wherein, it comprises (1), before or after the static deduster 5 of smoke channel 4, ejecting into ozone O3 at low temperature section as 110-150Deg. C, while the ratio between ejected amount and nitrogen oxide is 0.5-1.5, to oxidize the low-level nitrogen oxide insoluble into soluble high-level nitrogen oxide, and the sulfur oxide is transformed into sulfur trioxide, and the reaction time is more then 0.5s; (3), feeding treated smoke into alkali washing tower 7 to wash, and absorbing high-level nitrogen oxide and sulfur oxide.
Description
Technical field
The present invention relates to environmental protection technical field, relate in particular to a kind of coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus and method thereof.
Background technology
The oxysulfide that produces in the using energy source process, nitrogen oxide have caused serious day by day harm to the atmospheric environment of China.Present existing desulfur technology can be divided into several classes such as dry method, semidry method and wet method.Dry method, semidry method investment operating cost is low, but often has the not high shortcoming of desulfuration efficiency, and large-sized boiler combustion apparatus such as station boiler etc. often can not reach environmental requirement.What station boiler extensively adopted at present is limestone/gypsum wet process of FGD technology (WFGD), and this method desulfuration efficiency height is stable, but exists water consumption big, waste discharge secondary pollution, investment and the more high shortcoming of operating cost.
The control technology of nitrogen oxide mainly contains two classes: the first generic stove combustion process control mode, mainly contain the low-NOx combustor technology, and OFA (Over fire air) technology, the low oxygen combustion technology, combustion technology etc. is controlled NO by the combustion process adjustment again
xDischarging, can be with NO
xBe controlled at medium emission level, general denitration efficiency is about 30～50%.But these technology cause combustion stability to descend easily on the one hand, and burner region forms local reduction atmosphere easily, cause ash fusion point to descend, and cause the pickup slagging scorification phenomenon of water-cooling wall, influence the normal safe operation of boiler.Along with the further raising of environmental requirement, be difficult to realize NO on the other hand
xFurther emission control.The second class technology is a gas denitrifying technology, and countries use such as the present U.S., Japan, Europe technology the most widely are SCR technology (SCR).SCR technology denitration efficiency height, stable, but under the high grey deployment scenarios in the flue gas higher dust granules cause the problems such as wearing and tearing, obstruction of catalyst easily, the heavy metal in the flying dust can cause the poisoning of catalyst, operation and investment cost be costliness very.Environmental Protection in China work is started late, the control of sulfur dioxide just just begins, nitrogen oxide certainly will be brought into schedule from now on, if the thinking that adopts developed country to administer item by item, adopt the desulfurization of wet process of FGD WFGD device, the method of selectivity catalysis SCR denitration certainly will increase huge investment, operating cost, and some old units even have problems such as difficult arrangement, so developing low-cost, high efficiency while desulphurization denitration technology just seem particularly important.
Flue gas and desulfurizing and denitrifying technology in research has dry method while desulphurization denitration technology in the stove, electro-catalysis while desulphurization denitration technology etc. at present.Electro-catalysis desulphurization denitration technology removal efficiency height simultaneously wherein, operating cost is low, is becoming the focus of people's research.Present electro-catalysis technology comprises electron beam technology, pulsed discharge plasma technology, technology such as steam ammonia corona discharge activation.Mainly utilize the neutral molecule (N in high energy electron and the flue gas
2, O
2, H
2O etc.) collision produces some living radicals (O, OH, O
3, HO
2Deng), the SO in these free radicals and the flue gas
2And NO
xMolecular reaction generates SO
3, high valence state nitrogen oxide, nitric acid, sulfuric acid etc. are at NH
3Generate byproducts such as ammonium sulfate, ammonium nitrate under the condition that exists.Advantage is a dry removal, does not produce waste water and dregs, and energy is desulphurization denitration simultaneously, and accessory substance can recycling.But because the free radical time-to-live is very short, the generation and the smoke reaction device of free radical need be united two into one, discharge at whole flue, and contain a large amount of N in the boiler smoke
2, CO
2, H
2Material such as O, dust, discharging condition is abominable, simultaneously N
2, CO
2Consume a large amount of input energy, cause capacity usage ratio low, overall operation expense costliness.
Summary of the invention
The objective of the invention is to discharge at whole flue at various electro-catalysis technology, the energy consumption problem of higher provides a kind of coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus and method thereof.
The coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus has boiler furnace, back-end ductwork, the alkali liquid washing tower that is connected successively, alkali liquid washing tower top is provided with demister, alkali liquid washing tower bottom is provided with reservoir, alkali liquid washing top of tower and chimney join, alkali liquid washing tower bottom and nitrate sulfate concentration and crystallization device join, back-end ductwork joins with ozone generating-device, dry filter oxygenerator successively, is provided with electrostatic precipitator on described back-end ductwork.
The coal-burning boiler fume ozone oxidation and simultaneous desulfurization method of denitration may further comprise the steps:
1) 110～150 ℃ of low-temperature zone spray into ozone O before or after the electrostatic precipitator (5) of boiler flue (4)
3The nitrogen oxide molar ratio that sprays in ozone and the boiler smoke is 0.5～1.5, water-fast lower valency nitrogen oxide in the boiler smoke is oxidized into high valence state nitrogen oxide soluble in water, oxidizing sulfur dioxide generates sulfur trioxide, and the reaction time was at least 0.5 second;
2) will send into alkali liquid washing tower (7) through the rapid boiler smoke of handling of previous step, in the alkali liquid washing tower, flue gas be washed, absorb high valence state nitrogen oxide and oxysulfide in the flue gas simultaneously.
Described alkali lye is that NaOH, potassium hydroxide, calcium hydroxide, calcium oxide, calcium carbonate, ammoniacal liquor are wherein at least a.
The invention has the beneficial effects as follows: flue gas and desulfurizing and denitrifying new method provided by the invention, can reach denitration efficiency and 95% above desulfuration efficiency more than 80% simultaneously, cheap 30～60% through estimation output investment ratio tradition SCR+WFGD mode, operating cost saves about 60%
Description of drawings
Fig. 1 is a coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus I structural representation;
Fig. 2 is a coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus II structural representation;
Among the figure: boiler furnace 1, dry filter oxygenerator 2, ozone generating-device 3, back-end ductwork 4, electrostatic precipitator 5, reservoir 6, alkali liquid washing tower 7, demister 8, chimney 9, nitrate sulphate crystal treating apparatus 10.
The specific embodiment
The present invention is directed to local air or oxygen discharge produces and to spray into flue behind the ozone nitrogen oxide and oxysulfide are carried out oxidation, afterbody removes simultaneously in conjunction with the wet scrubbing device, if wet desulphurization device being installed then can carry out effective combination with it, realize desulphurization denitration simultaneously.
O
3Extensively exist in electron beam, pulsed plasma discharge as a kind of of free radical, and O
3Life cycle is longer relatively, therefore can with little air or oxygen at first ionization generate O
3, send into boiler flue then, reduce the power consumption of system in just greatly, through estimation O
3Only need discharge and just can meet the demands the gas of total exhaust gas volumn about 3%.
Below in conjunction with the drawings and specific embodiments the present invention is described in further detail.
As shown in the figure, the coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus has boiler furnace 1, back-end ductwork 4, the alkali liquid washing tower 7 that is connected successively, alkali liquid washing tower top is provided with demister 8, alkali liquid washing tower bottom is provided with reservoir 6, alkali liquid washing top of tower and chimney 9 join, alkali liquid washing tower bottom and nitrate sulfate concentration and crystallization device 10 join, back-end ductwork 4 joins with ozone generating-device 3, dry filter oxygenerator 2 successively, is provided with electrostatic precipitator 5 on described back-end ductwork 4.
The coal-burning boiler fume ozone oxidation and simultaneous desulfurization method of denitration may further comprise the steps:
1) 110～150 ℃ of low-temperature zone spray into ozone O before or after the electrostatic precipitator 5 of boiler flue 4
3The nitrogen oxide molar ratio that sprays in ozone and the boiler smoke is 0.5～1.5, water-fast lower valency nitrogen oxide in the boiler smoke is oxidized into high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide, and the reaction time was at least 0.5 second;
2) will send into alkali liquid washing tower 7 through the rapid boiler smoke of handling of previous step, in the alkali liquid washing tower, flue gas be washed, absorb high valence state nitrogen oxide and oxysulfide in the flue gas simultaneously.
The NO of boiler smoke discharging
xIn, NO accounts for more than 95%, and other is NO
2, N
2O etc., and NO is water insoluble, is one of gaseous contamination material that is difficult to handle, and the NO of high valence state
2, NO
3, N
2O
5Can generate HNO with the water reaction
2, HNO
3, very easily removed by the wet scrubbing device.By spraying into ozone, O in 110～150 ℃ of temperature ranges of boiler flue
3/ NO molar ratio gets 0.5 ~ 1.5, NO can be oxidized to high valence state material soluble in water, removes part SO by the wet scrubbing tower
2Also can oxidized generation SO
3, wet scrubbing is to SO
2Remove quite effective, SO
3Compare SO
2Easier dissolving and water cooperate the wet scrubbing device just can realize efficient while desulphurization denitration at the ozone oxidation afterbody, and denitration efficiency is with to spray into ozone amount relevant.If be equipped with limestone/gypsum wet process of FGD equipment, perhaps water dust scrubber then can carry out integrating the cost of reducing investment outlay with this method after the appropriate reconstruction to it.
Detailed process is: spray into ozone in 110～150 ℃ of temperature ranges of boiler back end ductwork, spraying into the position can be before or after electrostatic precipitator, and the ozone straying quatity is pressed O according to NO concentration in the flue gas
3/ NO mol ratio 0.5～1.5: 1 is chosen, and nitrogen oxide after the oxidation and oxysulfide remove by the wet scrubbing tower, and absorption liquid is an alkali lye, and absorption liquid is recycling, sells behind the sulfate nitrate condensing crystallizing of enrichment or further handles.Further specify below in conjunction with accompanying drawing:
Embodiment 1
Coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitration arrangement I, as shown in Figure 1.The air drying is sent into the dry filter oxygenerator after purifying, the oxygen that produces is sent into ozone generating-device with the preparation high-concentrated ozone, the preceding temperature of electrostatic precipitator was about 150 ℃ dust-laden flue after ozone was sent into air preheater, straying quatity is according to flue gas nitrogen oxide concentration, press ozone and nitrogen oxide mol ratio and constantly adjust at 1.1: 1, guarantee the 0.5s reaction time at least.Spout adopts perforated grill to spray, and sprays into the position at air preheater exhanst gas outlet 1m place.Flue gas after the processing enters the wet scrubbing tower after electrostatic precipitator, absorption liquid is recycling, and flue gas is sent into chimney through wet scrubbing tower, demister after handling, and the sulfate of absorption and nitrate carry out condensing crystallizing to be handled.Scrubbing tower adopts alkali lye as absorbent, and scrubbing tower is spray column or packed tower.Alkali lye as absorbent is NaOH, also can be in water, potassium hydroxide, calcium hydroxide, calcium oxide, calcium carbonate or the ammoniacal liquor one or more.
Embodiment 2
Scheme II is put in the coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitration, as shown in Figure 2.Ozone is sent into electrostatic precipitator about about 110 ℃ low cloud of dust compression ring border afterwards, and the ozone straying quatity is pressed ozone and nitrogen oxide mol ratio 1.0 and is dynamically adjusted according to flue gas nitrogen oxide concentration, sprays into a position and guarantees apart from the scrubbing tower inlet above time of staying of 0.5s.Ozone adopts perforated grill shape spray regime to carry out, and the flue gas after the oxidation enters the alkali liquid washing tower and absorbs, and absorption liquid is recycling, and flue gas is sent into smoke stack emission after washing, demist, and the sulfate of absorption and nitrate carry out condensing crystallizing to be handled.Scrubbing tower adopts alkali lye as absorbent, and scrubbing tower is spray column or packed tower.Alkali lye as absorbent is NaOH, also can potassium hydroxide, in calcium hydroxide, calcium oxide, calcium carbonate or the ammoniacal liquor one or more.
At last, it is also to be noted that what more than enumerate only is specific embodiments of the invention.Obviously, the invention is not restricted to above embodiment, many distortion can also be arranged.
The present invention can summarize with other the concrete form without prejudice to spirit of the present invention and principal character.Therefore, no matter from which point, above-mentioned embodiment of the present invention all can only be thought can not limit the present invention to explanation of the present invention, claims have been pointed out scope of the present invention, and scope of the present invention is not pointed out in above-mentioned explanation, therefore, in implication suitable and any change in the scope, all should think to be included in the scope of claims with claims of the present invention.
Claims (3)
1. coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus, it is characterized in that, it has the boiler furnace (1) that is connected successively, back-end ductwork (4), alkali liquid washing tower (7), alkali liquid washing tower top is provided with demister (8), alkali liquid washing tower bottom is provided with reservoir (6), alkali liquid washing top of tower and chimney (9) join, alkali liquid washing tower bottom and nitrate sulfate concentration and crystallization device (10) join, back-end ductwork (4) successively with ozone generating-device (3), dry filter oxygenerator (2) joins, and is provided with electrostatic precipitator (5) on described back-end ductwork (4).
2. the coal-burning boiler fume ozone oxidation and simultaneous desulfurization method of denitration that use is installed according to claim 1 is characterized in that, may further comprise the steps:
1) 110～150 ℃ of low-temperature zone spray into ozone O before or after the electrostatic precipitator (5) of boiler flue (4)
3The nitrogen oxide molar ratio that sprays in ozone and the boiler smoke is 0.5～1.5, water-fast lower valency nitrogen oxide in the boiler smoke is oxidized into high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide, and the reaction time was at least 0.5 second;
2) will send into alkali liquid washing tower (7) through the rapid boiler smoke of handling of previous step, in the alkali liquid washing tower, flue gas be washed, absorb high valence state nitrogen oxide and oxysulfide in the flue gas simultaneously.
3, a kind of boiler smoke ozone oxidation and simultaneous desulfurization method of denitration according to claim 2 is characterized in that described alkali lye is one or more in NaOH, potassium hydroxide, calcium hydroxide, calcium oxide, calcium carbonate, the ammoniacal liquor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100530906A CN1923341A (en) | 2006-08-23 | 2006-08-23 | Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2006100530906A CN1923341A (en) | 2006-08-23 | 2006-08-23 | Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1923341A true CN1923341A (en) | 2007-03-07 |
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ID=37816274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2006100530906A Pending CN1923341A (en) | 2006-08-23 | 2006-08-23 | Device and method for coal-burning boiler fume ozone oxidation and simultaneous desulfurization and denitrification |
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| CN (1) | CN1923341A (en) |
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|---|---|---|---|---|
| CN101822937A (en) * | 2010-05-11 | 2010-09-08 | 武汉科技学院 | Method for synchronous desulfurization and denitrification of marine vessel exhaust |
| CN101385942B (en) * | 2008-10-13 | 2011-04-13 | 浙江天蓝环保技术有限公司 | Liquid-phase oxidation-absorption two-stage wet method flue-gas denitration technique |
| CN101485957B (en) * | 2009-01-08 | 2011-05-11 | 浙江大学 | Device and method of simultaneous desulfuration and denitration for flue gas using ozone oxygenation combined with double-tower washing |
| CN102240500A (en) * | 2011-06-28 | 2011-11-16 | 华北电力大学 | System and process for desulfuration and denitration by pure oxygen dielectric barrier discharge in flue |
| CN102350189A (en) * | 2011-08-24 | 2012-02-15 | 福建新大陆环保科技有限公司 | Half-dry low-temperature smoke denitrification system |
| CN102357332A (en) * | 2011-08-29 | 2012-02-22 | 秦皇岛双轮环保科技有限公司 | Denitration system for wet absorption of flue gas and method |
| CN102371110A (en) * | 2010-08-19 | 2012-03-14 | 中国石油化工股份有限公司 | Flue gas desulfurization and denitration method |
| CN102553428A (en) * | 2012-01-10 | 2012-07-11 | 华北电力大学（保定） | Absorption tower for desulfurization and denitrification combined with oxidant in forward-flow and back-flow spraying and method |
| CN102600709A (en) * | 2012-03-27 | 2012-07-25 | 佛山市三水佳利达纺织染有限公司 | Method and device for flue gas desulfurization and denitration by combination of ozone and alkali wastewater |
| CN101347710B (en) * | 2008-09-04 | 2012-10-03 | 北京博奇电力科技有限公司 | Purification system of flue gas and method |
| CN102949921A (en) * | 2012-11-19 | 2013-03-06 | 厦门城力机电设备有限公司 | High-pressure electrostatic dust collection electric field device of coal-fired unit for generating ozone and simultaneously desulfurizing and denitrating |
| CN103055672A (en) * | 2012-12-31 | 2013-04-24 | 浙江工商大学 | Two-step oxidation-reduction flue gas denitration method |
| CN103100294A (en) * | 2011-11-15 | 2013-05-15 | 中国石油化工股份有限公司 | Method for removing oxynitride from flue gas through ozone oxidation method |
| CN103100293A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Process method for flue gas denitrification through biological method |
| CN103566725A (en) * | 2013-10-15 | 2014-02-12 | 中国科学院过程工程研究所 | Device and method for jointly removing sulphur, saltpeter and mercury by semidry method through circulating fluidized bed |
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