CN102773001B - High-temperature atomization wet denitration process system and denitration method - Google Patents
High-temperature atomization wet denitration process system and denitration method Download PDFInfo
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- CN102773001B CN102773001B CN201210213149.9A CN201210213149A CN102773001B CN 102773001 B CN102773001 B CN 102773001B CN 201210213149 A CN201210213149 A CN 201210213149A CN 102773001 B CN102773001 B CN 102773001B
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- 238000000034 method Methods 0.000 title claims abstract description 67
- 238000000889 atomisation Methods 0.000 title claims abstract description 5
- 239000003546 flue gas Substances 0.000 claims abstract description 52
- 239000002250 absorbent Substances 0.000 claims abstract description 35
- 230000002745 absorbent Effects 0.000 claims abstract description 34
- 239000000571 coke Substances 0.000 claims abstract description 12
- 235000019738 Limestone Nutrition 0.000 claims abstract description 11
- 239000006028 limestone Substances 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 50
- 239000002002 slurry Substances 0.000 claims description 41
- 238000006243 chemical reaction Methods 0.000 claims description 33
- 239000003054 catalyst Substances 0.000 claims description 17
- 238000010521 absorption reaction Methods 0.000 claims description 14
- 238000012545 processing Methods 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 4
- 239000000779 smoke Substances 0.000 claims description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 abstract description 22
- 239000003795 chemical substances by application Substances 0.000 abstract description 7
- 231100000252 nontoxic Toxicity 0.000 abstract description 5
- 230000003000 nontoxic effect Effects 0.000 abstract description 5
- 230000003197 catalytic effect Effects 0.000 abstract description 2
- 238000006477 desulfuration reaction Methods 0.000 abstract description 2
- 230000023556 desulfurization Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract 2
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 abstract 2
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract 1
- 239000001569 carbon dioxide Substances 0.000 abstract 1
- 239000002737 fuel gas Substances 0.000 abstract 1
- 239000002085 irritant Substances 0.000 abstract 1
- 231100000021 irritant Toxicity 0.000 abstract 1
- 210000004911 serous fluid Anatomy 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 14
- 238000007254 oxidation reaction Methods 0.000 description 14
- 230000003647 oxidation Effects 0.000 description 13
- 238000005516 engineering process Methods 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 229910021529 ammonia Inorganic materials 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 4
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 4
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 4
- 239000004202 carbamide Substances 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 239000013505 freshwater Substances 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 3
- 238000003916 acid precipitation Methods 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate group Chemical group [N+](=O)([O-])[O-] NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000012360 testing method Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 241000628997 Flos Species 0.000 description 2
- DQMUQFUTDWISTM-UHFFFAOYSA-N O.[O-2].[Fe+2].[Fe+2].[O-2] Chemical compound O.[O-2].[Fe+2].[Fe+2].[O-2] DQMUQFUTDWISTM-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- XURIQWBLYMJSLS-UHFFFAOYSA-N 1,4,7,10-tetrazacyclododecan-2-one Chemical compound O=C1CNCCNCCNCCN1 XURIQWBLYMJSLS-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000000383 hazardous chemical Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000003863 metallic catalyst Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- RAFRTSDUWORDLA-UHFFFAOYSA-N phenyl 3-chloropropanoate Chemical compound ClCCC(=O)OC1=CC=CC=C1 RAFRTSDUWORDLA-UHFFFAOYSA-N 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
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- 238000003860 storage Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention relates to a high-temperature atomization wet denitration process system and a denitration method. An absorbent serous fluid containing limestone, activated coke, catalytic agents and water is used for absorbing and removing nitric oxide in fuel gases to form calcium nitrate and release carbon dioxide gases. The high-temperature atomization wet denitration process system and the denitration method have the advantages of being small in investment, simple in operation and high in denitration efficiency; used absorbents are non-toxic, non-irritant, small in dangerousness, convenient to store and transport and low in using costs; and the process is particularly suitable for desulfurization and denitration of flue gases of small and medium-sized industrial boilers, live heating boilers and hot water supply boilers.
Description
Technical field
The present invention relates to the technical field that flue gas is separated and purify, the present invention relates to specifically a kind of means that adopt gas liquid contact, process system and the out of stock method of under the condition of high-temperature atomizing, flue gas or tail gas being carried out to denitration.The present invention is specially adapted to the application of medium small boiler flue-gas denitration process.
Background technology
China is maximum in the world coal production Guo He country of consumption, is also that a few take one of country that coal is main energy sources in the world.Therefore, China's atmosphere pollution be take bituminous coal type as main, and major pollutants are nitrogen oxide and flue dust.The current atmospheric environment situation of China still allows of no optimist, and Acid Rain Pollution has the trend increasing gradually.According to statistics, on the south the Changjiang river, to the east of Qinghai-Tibet Platean and the Sichuan Basin, acid rain center pH value is minimum is 4.0, and acid rain frequency reaches 80%.
For protection of the environment, realize the target of sustainable development, State Environmental Protection Administration's upgrading pollutant emission standard, has taked more strict requirement and measure to fume emission; And along with taking place frequently of acid rain, denitrating flue gas (removing and purifying of nitrogen oxide) also becomes the emphasis of smoke gas treatment day by day.
In prior art, the selective catalytic reduction technology of the main method of denitrating flue gas (SCR), SNCR technology (SNCR), wet process complex absorption techniques, liquid phase oxidation-absorption techniques, gaseous oxidation-absorption techniques etc.
SCR is the most ripe current gas denitrifying technology, and it is method of denitration after a kind of stove, is to utilize reducing agent (NH3, urea) under metallic catalyst effect, optionally reacts with NOx and generates NO
2and H
2o, rather than by O
2oxidation, therefore be called " selectively ".At present popular SCR technique is mainly divided into two kinds of ammonia process and urea methods in the world.These two kinds of methods are all to utilize the restoring function of ammonia to NOx, under the effect of catalyst, NOx (being mainly NO) are reduced to the N on the few of impact of atmosphere
2and water, reducing agent is NH
3.In addition, the bad adaptability of this technology centering, sulphur coal, sulfureous in flue gas component can reduce catalyst life, and the coal sulfur content that China produces is generally higher.Therefore,, from the current national conditions of China, SCR is difficult to widely popularize in China.
In flue gas, NOx itself is a kind of resource, and the removing process of current nitrogen oxide mainly concentrates on the control of NOx, has ignored the recycling of nitrogen element.Therefore, propose a kind of economically feasible, the national conditions that efficient, flue-gas denitration process that can reclaim nitrogen element not only meets China, also have wide market application foreground.In wet denitration technology, the end-product of nitrogen oxide is nitrate and nitrite, likely realizes the recycling of nitrogen element.As important industrial chemicals, nitrate and nitrite all have higher economic worth, are widely used in the corrosion inhibitor of medical industry, organic synthesis and lubricating oil, in concrete is manufactured, are again a kind of good promoter and antifreezing agent.
Patent application CN1923341A discloses a kind of coal-burning boiler fume ozone oxidation and simultaneous desulfurization denitrification apparatus and method thereof, but its amount that sprays into ozone is larger, be about 0.5-1.5 with nitric oxide production mol ratio, affected the economy of the method, and high valence state nitrogen oxide NO soluble in water after oxidation
2, NO
3or N
2o
5with in the process of alkaline reaction, can generate the mixture of nitrate and nitrite, the wastewater treatment expense after absorption is high, is unfavorable for the recycling of resource.
Patent application CN101352644A discloses a kind of method of utilizing hydrogen peroxide or ozone oxidation agent to carry out denitration, but because the use amount of oxidant is very large, has affected the economy of the method.
Summary of the invention
For denitration technology of the prior art, need to use reducing agent ammoniacal liquor or liquefied ammonia, or strong oxidizer ozone or hydrogen peroxide and many technical problems of causing, for example acquisition cost and cost of transportation are high; And these matter-poles are volatile, have strong impulse, the improper explosion danger that has of accumulating.The present invention has creatively proposed a kind of high-temperature atomizing wet denitration process system and method for denitration, and system and method for the present invention adopts lime stone, activated coke and catalyst as denitrfying agent, can effectively remove the nitrogen oxide in flue gas; And than prior art, also there is absorbent nontoxic, nonirritant is dangerous little; And the advantage that accumulating is convenient, use cost is low.Because safety non-toxic, system and method for the present invention is also particularly suitable for densely inhabited district, for example the denitration of medium and small Industrial Boiler flue gas and heating for residential area and supplying hot water boiler.
In order to solve the problems of the technologies described above, a first aspect of the present invention relates to a kind of high-temperature atomizing wet denitration method, utilizes the absorbent slurry that comprises lime stone, activated coke, catalyst and water to absorb and removes the NOx in flue gas, generates Ca (NO
3)
2, and discharge CO
2gas, is characterized in that: comprise the first reactions steps, this step is utilized the high-temperature steam of 200-500 ℃, mixes and from reverse contact of the ejection of high-temperature atomizing device high speed and flue gas, absorption and chemical reaction occur with absorbent slurry, and main chemical reactions is:
(1)NO+1/2O
2→NO
2
(2)NO+NO
2+H
2O→HNO
2
(3)2HNO
2+CaCO
3→Ca(NO
2)
2+CO
2+H
2O。
In described high-temperature atomizing wet denitration method, also comprise the second reactions steps, this step is the flue gas to processing through the first reactions steps, utilizes the atomization slurry of spray to continue and smoke reaction.
In described high-temperature atomizing wet denitration method, described catalyst is Fe
2o
3.
Preferably, described catalyst is Fe
2o
3, TiO
2-xand Cu
2the composition that B forms, the content of wherein X=0.2-0.8, and each component is respectively Fe
2o
3account for 35-50wt%, TiO
2-xaccount for 25-35wt%, Cu
2b accounts for 25-30wt%.
In described high-temperature atomizing wet denitration method, absorbent slurry comprises the lime stone of 1.2-5wt%, the catalyst of the activated coke of 0.5-3.5wt%, 0.2-1.0wt%.
In described high-temperature atomizing wet denitration method, the ratio of absorbent slurry and flue gas is 5-50L/m
3; More preferably, the ratio of absorbent slurry and flue gas is 10-20L/m
3.
In described high-temperature atomizing wet denitration method, in the first reactions steps, flue gas flow rate is 15-35m/s; More preferably, flue gas flow rate is 20-25m/s.In the second reactions steps, flue gas flow rate is 3-10m/s; More preferably, flue gas flow rate is 3-5m/s.
In described high-temperature atomizing wet denitration method, the temperature of described high-temperature steam is preferably 300-400 ℃; More preferably 350 ℃
A second aspect of the present invention relates to a kind of high-temperature atomizing wet denitration process system, contain absorption tower, absorption tower is provided with former flue entrance, it is characterized in that absorption tower comprises oxidation trough at the bottom of tower, the first reaction zone tower body and second reaction zone tower body, the bottom of described the first reaction zone tower body is provided with slurries high-temperature atomizing nozzle; The middle and upper part of described second reaction zone tower body is provided with a plurality of spraying layers and the demist layer being comprised of slurry nozzle, and respectively and at the bottom of tower, between oxidation trough, be connected with circulation line, circulation line is also provided with slurry circulating pump for each slurry nozzle and slurries high-temperature atomizing nozzle; Described high-temperature atomizing nozzle is also connected with high temperature steam pipeline.
In described high-temperature atomizing wet denitration process system, also comprise absorbent groove with slurry, absorbent warehouse, absorbent warehouse bottom is connected by lock gate hatch and absorbent groove with slurry, absorbent groove with slurry top is provided with fresh water (FW) import, absorbent trench bottom with slurry is provided with slurries outlet, and slurry feeding pump is delivered to absorbent slurry the circulation line on absorption tower by this slurries outlet.
In described high-temperature atomizing wet denitration process system, in described absorbent groove with slurry, be also provided with agitator.
In described high-temperature atomizing wet denitration process system, at the bottom of absorbing tower, oxidation trough is also provided with air intake, and air is conveyed into oxidation trough at the bottom of tower by booster fan from air intake.
In described high-temperature atomizing wet denitration process system, at the bottom of absorbing tower, the bottom of oxidation trough is provided with slurries floss hole, and at the bottom of tower, the absorbent slurry of oxidation trough is delivered to cyclone by slurries floss hole by slurries emptying pump; Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of absorbing tower in oxidation trough, and denseer underflow slurries flow in sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent groove with slurry.
In described high-temperature atomizing wet denitration process system, in described sedimentation basin, also there is crystallizer, by Crystallization Separation, obtain calcium nitrite crystal product.
In described high-temperature atomizing wet denitration process system, at the bottom of absorbing tower, in oxidation trough, be provided with agitator.
In described high-temperature atomizing wet denitration process system, on the flue of supplied flue gases, be provided with baffle door, so that denitrification process bypass operation when normally moving and breaking down.
In described high-temperature atomizing wet denitration process system, also comprise electric meter control system.
Denitration principle of the present invention can briefly be expressed as follows:
Denitrification process of the present invention mainly divides two steps to carry out.In the first reactions steps, the present invention utilizes foamed cleaning technology, after using high-temperature steam to mix with calcium carbonate, activated coke and catalyst slurry, from high-temperature atomizing device, spray, and with flue gas reverse contact in turbulent flow uptake zone, when gas, liquid two-phase momentum balance, form the standing wave district of one section of height turbulence, in this region, gas-liquid two-phase fully contacts at short notice, constantly updates, obtain the high velocity turbulent flow uptake zone of sufficient heat and mass transfer efficiency in tower, thereby NO absorption Catalytic Oxygen in flue gas are changed into NO
2.In the second reactions steps, flue gas flow rate has sharply declined and has been uniformly distributed, and continues to react with the spray atomizing slurries from tower body top, second reaction zone, and the flue gas after purification discharges from smokestack after demist; In order to maintain the pH value of system and to reduce the consumption of absorbent, control reaction sequence, need to constantly supplement absorption liquid, the absorbent in absorption tower, under the stirring of agitator and oxidation air, has accelerated the uniform of it and dissolving simultaneously.
Compared with prior art, the present invention has following useful technique effect:
(1) compare with SCR, SNCR denitrfying agent ammoniacal liquor used, liquefied ammonia or urea, the denitrfying agent that high-temperature atomizing wet denitration technique adopts is that lime stone, activated coke and catalyst absorber are nontoxic, and nonirritant is dangerous little.And the absorbents such as the ammoniacal liquor that conventional method adopts, liquefied ammonia are because the absorbent using is NH
3, highly volatile, has strong impulse, and human body sucks excessive meeting and causes death, the improper explosion danger that has of accumulating.Belong to controlled hazardous chemical, in densely inhabited district, use and have very large restriction.And high-temperature atomizing wet denitration technique denitrfying agent used: the stable in properties such as lime stone, activated coke and catalyst, nontoxic nonirritant is dangerous little.The absorbent accumulating of the present invention's use is convenient in addition, use cost is low, and liquefied ammonia, ammoniacal liquor are liquid state, transportation storage needs special pressure vessel, high to the anti-leak class requirement of equipment, if adopt urea, need special pyrolysis installation to produce ammoniacal liquor, operating cost is very high.
(2) compare with SCR, SNCR process system, system investment of the present invention and operating cost are low, and device structure is simple, easy to operate, stable strong adaptability, and also denitration efficiency is high, NOx content 600mg-1000mg/m in former flue gas
3in situation, denitration efficiency is not less than 80-85%, reaches discharging standards.
Accompanying drawing explanation
Fig. 1: the high-temperature atomizing wet denitration process chart of one embodiment of the invention.
In figure, the implication of Reference numeral representative is respectively: the former flue gas of 1-; 2-high-temperature steam; 3-air; 4-fresh water (FW); 5-absorbent groove with slurry; 6-absorption tower; 7-chimney; 8-cyclone; 9-sedimentation basin; 61-the first reaction zone tower body; 62-second reaction zone tower body; Oxidation trough at the bottom of 63-tower; 64-high-temperature atomizing nozzle; 65-spraying layer, 66-demister.
The specific embodiment
To be described in detail technical scheme of the present invention below, but accompanying drawing and specific embodiment be not as the restriction to patent of the present invention.
Embodiment 1
The boiler (10t/h) of now take is example, according to high-temperature atomizing wet denitration process system of the present invention and method of denitration, carries out denitration processing.In experiment, absorbent slurry comprises the lime stone of 5wt%, the di-iron trioxide catalyst of the activated coke of 2.5wt%, 0.5wt%; The ratio of absorbent slurry and flue gas is 15L/m
3.In the first reactions steps, flue gas flow rate is 20-25m/s.In the second reactions steps, flue gas flow rate is 3-5m/s; The temperature of high-temperature steam is preferably 350 ℃.
Test gained basic data is as follows:
Flue gas total flow: 12000m
3/ h; Flue gas is containing NOx 600mg/m
3.Clean flue gas is containing NOx 100-120mg/m
3, denitration rate reaches 80-85%.
Embodiment 2
The boiler (20t/h) of now take is example, according to high-temperature atomizing wet denitration process system of the present invention and method of denitration, carries out denitration processing.In experiment, absorbent slurry comprises the lime stone of 1.2wt%, the di-iron trioxide catalyst of the activated coke of 3.5wt%, 1.0wt%; The ratio of absorbent slurry and flue gas is 15L/m
3.In the first reactions steps, flue gas flow rate is 20-25m/s.In the second reactions steps, flue gas flow rate is 3-5m/s; The temperature of high-temperature steam is preferably 350 ℃.
Test gained basic data is as follows:
Flue gas total flow: 25000m
3/ h; Flue gas is containing NOx 800mg/m
3.Clean flue gas is containing NOx 120-150mg/m
3, denitration rate reaches more than 80%.
Embodiment 3
The boiler (10t/h) of now take is example, according to high-temperature atomizing wet denitration process system of the present invention and method of denitration, carries out denitration processing.In experiment, absorbent slurry comprises the lime stone of 4.5wt%, the catalyst of the activated coke of 2.5wt%, 0.2wt%; Described catalyst is Fe
2o
3, TiO
2-xand Cu
2the composition that B forms, the content of wherein X=0.5, and each component is respectively Fe
2o
3account for 50wt%, TiO
2-xaccount for 25wt%, Cu
2b accounts for 25wt%.
The ratio of absorbent slurry and flue gas is 15L/m
3.In the first reactions steps, flue gas flow rate is 20-25m/s.In the second reactions steps, flue gas flow rate is 3-5m/s; The temperature of high-temperature steam is preferably 350 ℃.
Test gained basic data is as follows:
Flue gas total flow: 25000m
3/ h; Flue gas is containing NOx 600mg/m
3.Clean flue gas is containing NOx 80-100mg/m
3, denitration rate reaches more than 85%.
High-temperature atomizing wet denitration process system of the present invention has great economic and social profit to mediumand smallscale industrial boilers denitrating flue gas, in China's economic construction process, is worth promoting.
Claims (3)
1. a high-temperature atomizing wet denitration method, utilizes the absorbent slurry that comprises lime stone, activated coke, catalyst and water to absorb and removes the NOx in flue gas, generates Ca (NO
3)
2, and discharge CO
2gas, is characterized in that: comprise the first reactions steps, this step is utilized the high-temperature steam of 200-500 ℃, mixes and from reverse contact of the ejection of high-temperature atomizing device high speed and flue gas, absorption and chemical reaction occur with absorbent slurry, and main chemical reactions is:
(1)NO+1/2O
2→NO
2
(2)NO+NO
2+H
2O→HNO
2
(3)2HNO
2+CaCO
3→Ca(NO
2)
2+CO
2+H
2O；
Wherein, described absorbent slurry comprises the lime stone of 1.2-5wt%, the catalyst of the activated coke of 0.5-3.5wt%, 0.2-1.0wt%; And described catalyst is Fe
2o
3, TiO
2-xand Cu
2the composition that B forms, the content of wherein X=0.2-0.8, and each component is respectively Fe
2o
3account for 35-50wt%, TiO
2-xaccount for 25-35wt%, Cu
2b accounts for 25-30wt%.
2. high-temperature atomizing wet denitration method according to claim 1, characterized by further comprising the second reactions steps, and this step is the flue gas to processing through the first reactions steps, utilizes the atomization slurry of spray to continue and smoke reaction.
3. high-temperature atomizing wet denitration method according to claim 2, the ratio that it is characterized in that absorbent slurry and flue gas is 10-20L/m
3, in the first reactions steps, flue gas flow rate is 20-25m/s, and in the second reactions steps, flue gas flow rate is 3-5m/s, and the temperature of high-temperature steam is 300-400 ℃.
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| CN112121567A (en) * | 2020-10-15 | 2020-12-25 | 航天环境工程有限公司 | A system and method for dust removal and treatment of flue gas from hot stewing pool of steel slag |
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