CN202844865U - Denitration process system by high-temperature atomization wet method - Google Patents

Denitration process system by high-temperature atomization wet method Download PDF

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Publication number
CN202844865U
CN202844865U CN 201220302112 CN201220302112U CN202844865U CN 202844865 U CN202844865 U CN 202844865U CN 201220302112 CN201220302112 CN 201220302112 CN 201220302112 U CN201220302112 U CN 201220302112U CN 202844865 U CN202844865 U CN 202844865U
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Prior art keywords
tower
slurry
absorbent
denitration
temperature atomizing
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CN 201220302112
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周琪
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BEIJING CLEARTIMES ENVIRONMENTAL PROTECTION ENGINEERING-TECH CO LTD
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BEIJING CLEARTIMES ENVIRONMENTAL PROTECTION ENGINEERING-TECH CO LTD
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Abstract

The utility model relates to a denitration process system by a high-temperature atomization wet method. The denitration process system is characterized by comprising an absorption tower, wherein the absorption tower comprises a primary flue inlet, a tower bottom oxidation tank, a first reaction area tower body and a second reaction area tower body; the first reaction area tower body is provided with a slurry high-temperature atomization nozzle; the second reaction area tower body is provided with a plurality of spraying layers composed of slurry nozzles and a demisting layer; circulation pipelines are respectively connected between each slurry nozzle and the tower bottom oxidation tank, as well as between the slurry high-temperature atomization nozzle and the tower bottom oxidation tank; the circulation pipelines are also provided with slurry circulation pumps; and the high-temperature atomization nozzle is connected with a high-temperature steam pipeline. The denitration process system has the advantages of being small in investment, easy to operate, low in running cost, and high in denitration effect, and is especially suitable for denitration of smoke of a small and medium industrial boiler, heating in life and a hot water supply boiler.

Description

High-temperature atomizing wet denitration process system
Technical field
The utility model relates to the technical field that flue gas separates and purify, and the utility model relates to a kind of means that adopt the gas liquid contact specifically, the process system that under the condition of high-temperature atomizing flue gas or tail gas is carried out denitration.The utility model is specially adapted to the application of medium small boiler flue-gas denitration process.
Background technology
China is maximum in the world coal production state and country of consumption, also is one of a few country take coal as main energy sources in the world.Therefore, China's atmosphere pollution is take the bituminous coal type as main, and major pollutants are nitrogen oxide and flue dust.The present atmospheric environment situation of China still allows of no optimist, and Acid Rain Pollution has the trend that increases gradually.According to statistics, on the south the Changjiang river, to the east of the Qinghai-Tibet Platean and the Sichuan Basin, acid rain center pH value is minimum to be 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 been 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 the 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 present gas denitrifying technology, and it is method of denitration behind a kind of stove, is to utilize reducing agent (NH3, urea) under the metallic catalyst effect, optionally generates NO with the NOx reaction 2And H 2O, rather than by O 2Oxidation is so be called " selectively ".At present popular SCR technique mainly is divided into two kinds of ammonia process and urea methods in the world.These two kinds of methods all are to utilize ammonia to the restoring function of NOx, under the effect of catalyst NOx (mainly being NO) are reduced to the N on the few of impact of atmosphere 2And water, reducing agent is NH 3In addition, the bad adaptability of this technology centering, sulphur coal, the sulfureous in flue gas component can reduce catalyst life, and the coal sulfur content that China produces is generally higher.Therefore, from the present national conditions of China, SCR is difficult to widely popularize in China.
NOx itself is a kind of resource in the flue gas, and the removing process of present nitrogen oxide mainly concentrates on the control of NOx, has ignored the recycling of nitrogen element.Therefore, propose a kind of economically feasible, efficient, national conditions that flue-gas denitration process that can reclaim the nitrogen element not only meets China, also have wide market application foreground.In the wet denitration technology, the end-product of nitrogen oxide is nitrate and nitrite, might realize 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 made, 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 the oxidation 2, NO 3Or N 2O 5With the mixture that can generate nitrate and nitrite in the process of alkaline reaction, the wastewater treatment expense after the 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.
The utility model content
Need to use reducing agent ammoniacal liquor or liquefied ammonia for denitration technology of the prior art, perhaps 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 utility model has creatively proposed a kind of high-temperature atomizing wet denitration process system, and system of the present utility model adopts lime stone, activated coke and catalyst as denitrfying agent, can effectively remove the nitrogen oxide in the flue gas.High-temperature atomizing wet denitration process system of the present utility model also is particularly suitable for being applied to 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, the utility model relates to a kind of high-temperature atomizing wet denitration process system, it is characterized in that containing the absorption tower, the absorption tower is provided with former flue entrance, the absorption tower comprises oxidation trough at the bottom of the tower, the first reaction zone tower body and second reaction zone tower body, and described the first reaction zone tower body is provided with slurries high-temperature atomizing nozzle; Described second reaction zone tower body is provided with a plurality of spraying layers and the demist layer that is comprised of slurry nozzle, each slurry nozzle and slurries high-temperature atomizing nozzle respectively and be connected with circulation line at the bottom of the tower between the oxidation trough, circulation line also is provided with slurry circulating pump; Described high-temperature atomizing nozzle also is connected with high temperature steam pipeline.
In the described high-temperature atomizing wet denitration process system, also comprise absorbent with slurry groove, absorbent warehouse, absorbent warehouse bottom is connected with absorbent with slurry groove by lock gate hatch, absorbent with slurry groove top is provided with the fresh water (FW) import, absorbent with slurry trench bottom is provided with the slurries outlet, and slurry feeding pump is delivered to absorbent slurry by this slurries outlet the circulation line on absorption tower.
In the described high-temperature atomizing wet denitration process system, also be provided with agitator in the described absorbent with slurry groove.
In the described high-temperature atomizing wet denitration process system, oxidation trough also is provided with air intake at the bottom of the absorbing tower, and air is conveyed into oxidation trough at the bottom of the tower by booster fan from air intake.
In the described high-temperature atomizing wet denitration process system, the bottom of oxidation trough is provided with the slurries floss hole at the bottom of the absorbing tower, and the absorbent slurry of oxidation trough is delivered to cyclone by the slurries floss hole by the slurries emptying pump at the bottom of the tower.Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of the absorbing tower in the oxidation trough, and denseer underflow slurries flow in the sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent with slurry groove.
In the described high-temperature atomizing wet denitration process system, also have crystallizer in the described sedimentation basin, obtain the calcium nitrite crystal product by Crystallization Separation.
In the described high-temperature atomizing wet denitration process system, be provided with agitator at the bottom of the absorbing tower in the oxidation trough.
In the described high-temperature atomizing wet denitration process system, be provided with baffle door at the flue of supplied flue gases, so that denitrification process normally moves and bypass operation when breaking down.
In the described high-temperature atomizing wet denitration process system, also comprise chimney, for the flue gas behind the emission purification.
In the described high-temperature atomizing wet denitration process system, also comprise the electric meter control system.
The absorbent slurry that process system utilization of the present utility model comprises lime stone, activated coke, catalyst and water absorbs and removes NOx in the flue gas, generates Ca (NO 3) 2, and discharge CO 2Gas, absorption process comprise the first reactions steps and the second reactions steps, and the first reactions steps is utilized 200-500 ℃ high-temperature steam, with the absorbent slurry mixing and from the ejection of high-temperature atomizing device high speed and reverse contact of flue gas absorption and chemical reaction occur; The second reactions steps, this step are the flue gases of processing through the first reactions steps, utilize the atomization slurry of spray to continue and smoke reaction, 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。
Comprise the lime stone of 1.2-5wt%, the activated coke of 0.5-3.5wt%, the catalyst of 0.2-1.0wt% in the absorbent slurry.The ratio of absorbent slurry and flue gas is 5-50L/m 3More preferably, the ratio of absorbent slurry and flue gas is 10-20L/m 3In 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.The temperature of described high-temperature steam is preferably 300-400 ℃; More preferably 350 ℃
Denitration principle of the present utility model can briefly be expressed as follows:
Denitrification process of the present utility model mainly divides two steps to carry out.In the first reactions steps, after using high-temperature steam and calcium carbonate, activated coke and catalyst slurry mixing, spray from the high-temperature atomizing device, and with flue gas reverse contact in the turbulent flow uptake zone, when gas, liquid two-phase momentum balance, form one section the height turbulence the standing wave district, in this zone, gas-liquid two-phase fully contacts at short notice, constantly updates, and obtains the high velocity turbulent flow uptake zone of sufficient heat and mass transfer efficient in tower, thereby the absorption of the NO in the flue gas and Catalytic Oxygen are changed into NO 2In the second reactions steps, flue gas flow rate sharply descends and evenly distributes, and with the spray atomizing slurries continuation reaction from second reaction zone tower body top, the flue gas after the purification discharges from smokestack after demist; For the pH value of keeping system and the consumption that reduces absorbent, the control reaction sequence needs constantly to replenish absorption liquid, and the absorbent in the absorption tower has accelerated the uniform of it and dissolving under the stirring of agitator and oxidation air simultaneously.
Compared with prior art, the utlity model has following useful technique effect:
(1) compare with the used denitrfying agent ammoniacal liquor of SCR, SNCR, 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 that uses 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, using in densely inhabited district has very large restriction.And the used denitrfying agent of high-temperature atomizing wet denitration technique: the stable in properties such as lime stone, activated coke and catalyst, nontoxic nonirritant is dangerous little.The absorbent accumulating of the utility model use is convenient in addition, use cost is low, and liquefied ammonia, ammoniacal liquor are liquid state, and the transportation storage needs special pressure vessel, and is high to the anti-leak class requirement of equipment, if adopt urea then need special pyrolysis installation to produce ammoniacal liquor, operating cost is very high.
(2) compare with SCR, SNCR process system, system of the present utility model investment and operating cost are low, and device structure is simple, and is easy to operate, stable strong adaptability, and also denitration efficiency is high, NOx content 600mg-1000mg/m in the former flue gas 3In the situation, denitration efficiency is not less than 80-85%, reaches discharging standards.
Description of drawings
Fig. 1: the high-temperature atomizing wet denitration process system schematic diagram of an embodiment of the utility model;
The implication of Reference numeral representative is respectively among the figure: the former flue gas of 1-; The 2-high-temperature steam; The 3-air; The 4-fresh water (FW); 5-absorbent with slurry groove; The 6-absorption tower; The 7-chimney; The 8-cyclone; The 9-sedimentation basin; 61-the first reaction zone tower body; 62-second reaction zone tower body; Oxidation trough at the bottom of the 63-tower; 64-high-temperature atomizing nozzle; 65-spraying layer, 66-demister.
The specific embodiment
The below is described in detail the technical solution of the utility model, but accompanying drawing and specific embodiment be not as the restriction to the utility model patent.
Embodiment 1
Now take a boiler (10t/h) as example, carry out denitration according to high-temperature atomizing wet denitration process system described in the utility model and process.Comprise the lime stone of 1.2-5wt%, the activated coke of 2.5wt%, the di-iron trioxide catalyst of 0.5wt% in the experiment in the absorbent slurry; The ratio of absorbent slurry and flue gas is 15L/m 3In 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 contains NOx600mg/m 3Clean flue gas contains NOx100-120mg/m 3, the denitration rate reaches 80-85%.
Embodiment 2
Now take a boiler (20t/h) as example, carry out denitration according to high-temperature atomizing wet denitration process system described in the utility model and process.Comprise the lime stone of 1.2-5wt%, the activated coke of 3.5wt%, the di-iron trioxide catalyst of 1.0wt% in the experiment in the absorbent slurry; The ratio of absorbent slurry and flue gas is 15L/m 3In 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 contains NOx800mg/m 3Clean flue gas contains NOx120-150mg/m 3, the denitration rate reaches more than 80%.
Embodiment 3
Now take a boiler (10t/h) as example, carry out denitration according to high-temperature atomizing wet denitration process system described in the utility model and process.Comprise the lime stone of 1.2-5wt%, the activated coke of 2.5wt%, the di-iron trioxide catalyst of 0.2wt% in the experiment in the absorbent slurry; The ratio of absorbent slurry and flue gas is 15L/m 3In 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 contains NOx600mg/m 3Clean flue gas contains NOx100-120mg/m 3, the denitration rate reaches more than 80%.
High-temperature atomizing wet denitration process system of the present utility model has great economic and social profit to the mediumand smallscale industrial boilers denitrating flue gas, is worth promoting in China's economic construction process.

Claims (10)

1. high-temperature atomizing wet denitration process system, it is characterized in that containing the absorption tower, the absorption tower is provided with former flue entrance, and the absorption tower comprises oxidation trough at the bottom of the tower, the first reaction zone tower body and second reaction zone tower body, and described the first reaction zone tower body is provided with slurries high-temperature atomizing nozzle; Described second reaction zone tower body is provided with a plurality of spraying layers and the demist layer that is comprised of slurry nozzle, each slurry nozzle and slurries high-temperature atomizing nozzle respectively and be connected with circulation line at the bottom of the tower between the oxidation trough, circulation line also is provided with slurry circulating pump; Described high-temperature atomizing nozzle also is connected with high temperature steam pipeline.
2. high-temperature atomizing wet denitration process system according to claim 1, characterized by further comprising absorbent with slurry groove, absorbent warehouse, absorbent warehouse bottom is connected with absorbent with slurry groove by lock gate hatch, absorbent with slurry groove top is provided with the fresh water (FW) import, absorbent with slurry trench bottom is provided with the slurries outlet, and slurry feeding pump is delivered to absorbent slurry by this slurries outlet the circulation line on absorption tower.
3. high-temperature atomizing wet denitration process system claimed in claim 2 is characterized in that also being provided with agitator in the described absorbent with slurry groove.
4. high-temperature atomizing wet denitration process system claimed in claim 1, it is characterized in that absorbing tower at the bottom of oxidation trough also be provided with air intake, air is conveyed into oxidation trough at the bottom of the tower by booster fan from air intake.
5. high-temperature atomizing wet denitration process system claimed in claim 1 is characterized in that the bottom of oxidation trough is provided with the slurries floss hole at the bottom of the absorbing tower, and the absorbent slurry of oxidation trough is delivered to cyclone by the slurries floss hole by the slurries emptying pump at the bottom of the tower; Cyclone carries out concentrating and separating to absorbent slurry, and rarer ororrhea flows back at the bottom of the absorbing tower in the oxidation trough, and denseer underflow slurries flow in the sedimentation basin, and the clear liquid overflow on sedimentation basin top is to absorbent with slurry groove.
6. high-temperature atomizing wet denitration process system claimed in claim 1 is characterized in that also having crystallizer in the described sedimentation basin.
7. high-temperature atomizing wet denitration process system claimed in claim 1 is characterized in that being provided with agitator in the oxidation trough at the bottom of the tower on described absorption tower.
8. high-temperature atomizing wet denitration process system claimed in claim 1 is characterized in that being provided with baffle door at the flue of supplied flue gases.
9. high-temperature atomizing wet denitration process system claimed in claim 1 characterized by further comprising the electric meter control system.
10. high-temperature atomizing wet denitration process system claimed in claim 1 characterized by further comprising chimney.
CN 201220302112 2012-06-27 2012-06-27 Denitration process system by high-temperature atomization wet method Expired - Fee Related CN202844865U (en)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106731609A (en) * 2017-01-09 2017-05-31 山东兴达化工有限公司 Coal-fired flue gas desulfurization and denitration agent and its desulfurization denitration method
CN109092018A (en) * 2018-08-13 2018-12-28 大同新成新材料股份有限公司 A kind of flue gas desulfurization and denitration method and device
CN111974187A (en) * 2020-08-20 2020-11-24 长春净月潭供热有限公司 Flue gas desulfurization method using magnesium oxide as desulfurizer

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106731609A (en) * 2017-01-09 2017-05-31 山东兴达化工有限公司 Coal-fired flue gas desulfurization and denitration agent and its desulfurization denitration method
CN109092018A (en) * 2018-08-13 2018-12-28 大同新成新材料股份有限公司 A kind of flue gas desulfurization and denitration method and device
CN109092018B (en) * 2018-08-13 2020-06-05 大同新成新材料股份有限公司 Flue gas desulfurization and denitrification device
CN111974187A (en) * 2020-08-20 2020-11-24 长春净月潭供热有限公司 Flue gas desulfurization method using magnesium oxide as desulfurizer

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Granted publication date: 20130403

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