CN102500206A - System and method for desulfurizing and denitrating smoke based on action of hydrogen peroxide - Google Patents
System and method for desulfurizing and denitrating smoke based on action of hydrogen peroxide Download PDFInfo
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- CN102500206A CN102500206A CN2011103547702A CN201110354770A CN102500206A CN 102500206 A CN102500206 A CN 102500206A CN 2011103547702 A CN2011103547702 A CN 2011103547702A CN 201110354770 A CN201110354770 A CN 201110354770A CN 102500206 A CN102500206 A CN 102500206A
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Abstract
The invention relates to a system and a method for desulfurizing and denitrating a smoke based on the action of hydrogen peroxide. The system comprises a smoke generator, a deduster connected with the smoke generator through a flue, and an absorption tower connected with the deduster through the flue; the top of the adsorption tower is connected with a chimney, the bottom of the absorption tower is connected with an oxidation fan and a liquid dedusting device; the liquid dedusting device is connected with a saline solution concentration crystallization device which is connected with a finished product packaging device; and the flue is connected with a hydrogen peroxide vaporization system which is used for providing a hydrogen peroxide gas. The system for desulfurizing and denitrating the smoke based on the action of hydrogen peroxide, which allows the smoke denitration rate to reach above 85% and the smoke desulfurization rate to reach above 95%, and has the advantages of low investment cost, low energy consumption and use convenience, is far beyond an SCR (selective catalytic reduction) method and an ozone oxidation denitration method.
Description
Technical field
The present invention relates to a kind of based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system and method.
Background technology
Fire coal, natural gas, heavy oil etc. in utilizing process and the nitrogen oxide that produces in some Chemical Manufacture and oxysulfide atmospheric environment has been caused serious harm.The desulfur technology of at present air contaminant treatment generally being taked has several types of dry method, semidry method and wet methods etc.There are the not high shortcoming of desulfuration efficiency in dry method and semidry method.Limestone/gypsum method, ammonia process, magnesium oxide method, wet methods such as two subtractions are the methods that extensively adopt at present, but these several kinds technology just seem powerless aspect denitration.
The removal of nitrogen oxide method mainly contains two types: one type is the generation through the Combustion Process Control nitrogen oxide, and efficient is about 30～50%, and this method efficient is low, and causes the slagging scorification of stove interior conduit easily.Second type of gas denitrifying technology is SCR technology SCR American-European, the Japan and other countries extensive use, and denitration efficiency is generally 60%, but this method is in high temperature section; Dust is more in the flue gas; Be prone to cause obstruction, the wearing and tearing of catalyst, the heavy metal in the flyash also can cause catalyst poisoning, and operation and investment cost are very expensive; Therefore, the exploitation of the denitration technology of low-cost high-efficiency is imperative.
Summary of the invention
The present invention is directed to the above-mentioned deficiency that existing desulphurization denitration technology exists, provide a kind of based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system and method.
The technical scheme that the present invention solves the problems of the technologies described above is following: a kind ofly based on the hydrogen peroxide effect flue gas and desulfurizing and denitrifying system is comprised the flue gas generation device; The deduster that links to each other with said flue gas generation device through flue; The absorption tower that links to each other with said deduster through flue; The top on said absorption tower is connected with chimney; The bottom on said absorption tower is connected with oxidation fan and liquid dust arrester, is connected with the saline solution concentration and crystallization device on the said liquid dust arrester, is connected with the finished product packing device on the said saline solution concentration and crystallization device; Be connected with the hydrogen peroxide carburetion system on the said flue, said hydrogen peroxide carburetion system is used to provide hydrogen peroxide gas.
On the basis of technique scheme, the present invention can also do following improvement.
Further, be provided with alkaline solution in the said absorption tower, the bottom on said absorption tower is connected with supply pump, is connected with a plurality of solution shower nozzles on the said supply pump; Said alkaline solution is NaOH, KOH, Ca (OH)
2, CaO, MgO, CaCO
3, NH
3H
2O, NH
4HCO
3With one or more the mixture in the seawater.
Further, being provided with weight ratio in the said absorption tower is the alkaline solution of 1:1 and the mixture of organic catalyst; Said organic catalyst is the product LEXFINE that Israel Lextran company produces, and said alkaline solution is NaOH, KOH, Ca (OH)
2, CaO, MgO, CaCO
3, NH
3H
2O, NH
4HCO
3With one or more the mixture in the seawater.
Further; Said flue is provided with reaction warehouse; Said reaction warehouse comprises first hollow cylinder and second hollow cylinder that is set in said first hollow cylinder; The length of said second hollow cylinder is less than the length of first hollow cylinder; One end of said first hollow cylinder and an end of second hollow cylinder are connected to the two ends of a hollow round platform sidewall, and the other end of the other end of said first hollow cylinder and second hollow cylinder is connected to the two ends of another hollow round platform sidewall; Said hydrogen peroxide carburetion system comprises first air inlet, second air inlet, the 3rd air inlet and gas outlet; Said first air inlet is connected on the flue between flue gas generation device and the deduster through first pipeline, and said first pipeline is provided with first control valve; Said second air inlet is connected on the flue between deduster and the absorption tower through second pipeline, and said second pipeline is provided with second control valve; Said the 3rd air inlet is through the external outside air of the 3rd pipeline, and said the 3rd pipeline is provided with the 3rd control valve; Said gas outlet is connected on the flue between flue gas generation device and the deduster through the 4th pipeline, perhaps is connected on the flue between deduster and the absorption tower.
Further, said hydrogen peroxide carburetion system comprises filter, blower fan, heater and hydrogen peroxide storage tank; One end of said filter links to each other with first pipeline, second pipeline and the 3rd pipeline respectively, and the other end links to each other with blower fan; The other end of said blower fan links to each other with heater, and the other end of said heater is connected with the 5th pipeline, and an end of said the 5th pipeline and the 4th pipeline links to each other, and the other end of said the 4th pipeline is connected with distribution device in gas-fluid; Be provided with atomizer in said the 5th pipeline, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with the hydrogen peroxide storage tank on the said supply pump.
Further, said distribution device in gas-fluid is arranged in the flue between flue gas generation device and the deduster, and said reaction warehouse is arranged between distribution device in gas-fluid and the deduster.
Further, said distribution device in gas-fluid is arranged in the flue between deduster and the absorption tower, and said reaction warehouse is arranged between distribution device in gas-fluid and the absorption tower.
Further, said hydrogen peroxide carburetion system comprises vapourizing unit and hydrogen peroxide storage tank; Said vapourizing unit links to each other with the hydrogen peroxide storage tank, and said vapourizing unit is connected with distribution device in gas-fluid through the 4th pipeline; Be provided with atomizer in the said vapourizing unit, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with the hydrogen peroxide storage tank on the said supply pump.
Further, said distribution device in gas-fluid is arranged in the flue between flue gas generation device and the deduster, and said reaction warehouse is arranged between distribution device in gas-fluid and the deduster.
Further, said distribution device in gas-fluid is arranged in the flue between deduster and the absorption tower, and said reaction warehouse is arranged between distribution device in gas-fluid and the absorption tower.
Further, said vapourizing unit is ultrasonic wave vaporized hydrogen peroxide device, electrical heating vaporized hydrogen peroxide device or oil bath heating vaporized hydrogen peroxide device.
The present invention also provides a kind of technical scheme that solves the problems of the technologies described above following: a kind of flue gas and desulfurizing and denitrifying method may further comprise the steps based on the hydrogen peroxide effect: at first, hydrogen peroxide gas that the hydrogen peroxide carburetion system is provided sprays in the flue; The lower valency nitrogen oxide that the flue gas generation device is produced and get in the interior flue gas of flue is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
Further, said method comprising the steps of: at first, a gas or a plurality of gases in the flue gas in the flue between the flue gas with in the flue between outside air, flue generation device and the deduster, deduster and the absorption tower introduce filter; Then, the gas after filtering through filter gets into heater through blower fan and is heated to after temperature is greater than or equal to 170 ℃, gets into the 5th pipeline; Then; Hydrogenperoxide steam generator in the hydrogen peroxide storage tank extracts the back and sprays in the 5th pipeline through atomizer; Make that vaporization forms hydrogen peroxide gas under the effect of its gas that is greater than or equal to 170 ℃ in temperature; Hydrogen peroxide gas gets into the 4th pipeline again and sprays in the flue between flue gas generation device and the deduster through distribution device in gas-fluid, thereby the flue gas middle or low price attitude nitrogen oxide that the flue gas generation device produces is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Hydrogen peroxide gas that wherein sprays into and the nitrogen oxide mol ratio in the flue gas>0.5, reaction time >=0.3 second; Then, flue gas and hydrogen peroxide gas get into reaction warehouse simultaneously and carry out further oxidation, thereby guarantee that the lower valency nitrogen oxide in the flue gas is completely oxidized to high valence state nitrogen oxide soluble in water, and the sulfur dioxide complete oxidation generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower after getting into the deduster dedusting again, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
Further, said method comprising the steps of: at first, the flue gas that produces of flue gas generation device gets into deduster and carry out dedusting; Then, a gas in the flue gas in the flue between the flue gas in the flue between outside air, flue generation device and the deduster, deduster and the absorption tower or a plurality of gas are introduced filter; Then, the gas after filtering through filter gets into heater through blower fan and is heated to after temperature is greater than or equal to 170 ℃, gets into the 5th pipeline; Then; Hydrogenperoxide steam generator in the hydrogen peroxide storage tank extracts the back and sprays in the 5th pipeline through atomizer; Make that vaporization forms hydrogen peroxide gas under the effect of its gas that is greater than or equal to 170 ℃ in temperature; Hydrogen peroxide gas gets into the 4th pipeline again through in the flue between distribution device in gas-fluid deduster and the absorption tower, thereby the flue gas middle or low price attitude nitrogen oxide that the flue gas generation device produces is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Hydrogen peroxide gas that wherein sprays into and the nitrogen oxide mol ratio in the flue gas>0.5, reaction time >=0.3 second; Then; Flue gas after the dedusting and hydrogen peroxide gas get into reaction warehouse simultaneously and carry out further oxidation; Thereby the lower valency nitrogen oxide in the flue gas after the assurance dedusting is completely oxidized to high valence state nitrogen oxide soluble in water, and the sulfur dioxide complete oxidation generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
The invention has the beneficial effects as follows: the present invention is based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; In flue gas (or chemical gases), add gaseous hydrogen peroxide; Lower valency nitrogen oxide, sulfur dioxide and carbon monoxide in the flue gas carry out oxidation, can make flue gas reach the desulfurization degree more than the denitration rate and 95% more than 85%, and this cover system cost of investment is cheap; It is low and easy to use that energy consumes, be SCR method and ozone oxidation method denitration method can not compare.
Description of drawings
Fig. 1 is the structural representation to the flue gas and desulfurizing and denitrifying system that the present invention is based on the hydrogen peroxide effect;
Fig. 2 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 1 that the present invention is based on the hydrogen peroxide effect;
Fig. 3 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 2 that the present invention is based on the hydrogen peroxide effect;
Fig. 4 is the front view of reaction warehouse of the present invention;
Fig. 5 is the side view of reaction warehouse of the present invention;
Fig. 6 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 3 that the present invention is based on the hydrogen peroxide effect;
Fig. 7 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 4 that the present invention is based on the hydrogen peroxide effect;
Fig. 8 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 5 that the present invention is based on the hydrogen peroxide effect;
Fig. 9 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 6 that the present invention is based on the hydrogen peroxide effect;
Figure 10 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 7 that the present invention is based on the hydrogen peroxide effect;
Figure 11 is the structural representation to flue gas and desulfurizing and denitrifying system embodiment 8 that the present invention is based on the hydrogen peroxide effect.
The specific embodiment
Below in conjunction with accompanying drawing principle of the present invention and characteristic are described, institute gives an actual example and only is used to explain the present invention, is not to be used to limit scope of the present invention.
In the nitrogen oxide of fire coal boiler fume, nitric oxide accounts for more than 90%, other be nitrogen dioxide etc.; Nitric oxide is one of more unmanageable polluter, when it is oxidized to the nitrogen dioxide of high valence state, nitrogen trioxide; Can generate nitric acid and nitrous acid with the water reaction behind the dinitrogen pentoxide, very easily removed, through in flue, adding the hydrogen peroxide of steam state by the wet absorption device; Hydrogen peroxide and nitric oxide production mol ratio can be high valence state nitrogen oxide with oxidation of nitric oxide greater than 0.5, remove with the wet absorption tower; Part sulfur dioxide also can be oxidized to sulfur trioxide simultaneously; And sulfur trioxide is more water-soluble more easily than sulfur dioxide, and therefore the afterbody behind the steam state hydrogen peroxide oxidation cooperates the wet absorption device, just can realize desulphurization denitration simultaneously.Denitration efficiency is relevant with the steam state amount of hydrogen peroxide that sprays into, and for the system that is equipped with wet desulphurization device (or water dust scrubber), then can carry out appropriate reconstruction to it, and is supporting with method of the present invention, practices thrift cost of investment.Absorption liquid is an alkali lye; Recycle; The sulfate of enrichment and nitrate through dedusting, concentrate, crystallization can be sold or further handle; The present invention and existing organic catalysis method (being the mixture that uses alkaline solution and organic catalyst in the absorption tower) combine, more can prevent in decomposition and the ammonia process of inferior sulfate radical and nitrite anions and after the escaping of ammonia.
As shown in Figure 1; Saidly the flue gas and desulfurizing and denitrifying system is comprised flue gas generation device 1, the deduster 3 that links to each other with said flue gas generation device 1 through flue, the absorption tower 4 that links to each other with said deduster 3 through flue based on the hydrogen peroxide effect; The top on said absorption tower 4 is connected with chimney 5; The bottom on said absorption tower 4 is connected with oxidation fan 9 and liquid dust arrester 6, is connected with saline solution concentration and crystallization device 7 on the said liquid dust arrester 6, is connected with finished product packing device 8 on the said saline solution concentration and crystallization device 7; Be connected with hydrogen peroxide carburetion system 100 on the said flue, said hydrogen peroxide carburetion system 100 is used to provide hydrogen peroxide gas.Said oxidation fan 9 helps not oxidized SO
3 2-And NO
2 -Forced oxidation.4 tops, said absorption tower are provided with demister, and the bottom is provided with reservoir, is provided with alkaline solution in the said reservoir, and the bottom on said absorption tower 4 is connected with the circulation absorption pump, are connected with a plurality of solution shower nozzles on the said circulation absorption pump.Said alkaline solution is NaOH, KOH, Ca (OH)
2, CaO, MgO, CaCO
3, NH
3H
2O, NH
4HCO
3With one or more the mixture in the seawater.Said flue is provided with reaction warehouse 2, and said hydrogen peroxide carburetion system 100 comprises first air inlet, second air inlet, the 3rd air inlet and gas outlet; Said first air inlet is connected on the flue between flue gas generation device 1 and the deduster 3 through first pipeline, and said first pipeline is provided with first control valve; Said second air inlet is connected on the flue between deduster 3 and the absorption tower 4 through second pipeline, and said second pipeline is provided with second control valve; Said the 3rd air inlet is through the external outside air of the 3rd pipeline, and said the 3rd pipeline is provided with the 3rd control valve; Said gas outlet is connected on the flue between flue gas generation device 1 and the deduster 3 through the 4th pipeline, perhaps is connected on the flue between deduster 3 and the absorption tower 4.
As shown in Figure 2, in the present embodiment, said flue gas generation device 1 is a boiler, and said hydrogen peroxide carburetion system comprises filter 11, blower fan 12, heater 13 and hydrogen peroxide storage tank 10; One end of said filter 11 links to each other with first pipeline, second pipeline and the 3rd pipeline respectively, and the other end links to each other with blower fan 12; The other end of said blower fan 12 links to each other with heater 13, and the other end of said heater 13 is connected with the 5th pipeline, and an end of said the 5th pipeline and the 4th pipeline links to each other, and the other end of said the 4th pipeline is connected with distribution device in gas-fluid; Be provided with atomizer in said the 5th pipeline, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with hydrogen peroxide storage tank 10 on the said supply pump.Said distribution device in gas-fluid is arranged in the flue between flue gas generation device 1 and the deduster 3.
When the system of use embodiment 1 carried out the desulphurization denitration operation, wherein, the molal quantity of hydrogen peroxide gas straying quatity was 1.1 times of nitric oxide molal quantity; Oxidization time 0.5 second, in the present embodiment, second control valve and the 3rd control valve are closed; First control valve is opened, and makes that the interior flue gas of flue gets into heater between boiler and the deduster, and the temperature of flue gas is 175 ℃ in the flue between boiler and the deduster; The temperature of the gas that comes out from heater is 200 ℃; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:326 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 813mg/ m
3, the absorption tower exports detected NOx:15 mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 95.40%, desulfuration efficiency is 100%.
Wet method ammonia process technology is joined on the absorption tower, and absorption liquid is NH
3H
2O recycles; After flue gas is absorbed washing, send into chimney, saline solution ammonium sulfate after the absorption and ammonium nitrate enrichment after dedusting, concentrate, crystallization, dehydration be the finished product chemical fertilizer; Nitrogen content is about 25%, and the absorbent of this instance also can be seawater, NaOH, KOH, Ca (OH)
2, CaO, CaCO
3, NH
3H
2O, NH
4HCO
3Deng wherein one or more.
Embodiment 2
As shown in Figure 3; Be with embodiment 1 difference; Flue between said distribution device in gas-fluid and the deduster 3 is provided with reaction warehouse 2; Shown in Fig. 4 and 5, said reaction warehouse comprises first hollow cylinder 14 and second hollow cylinder 15 that is set in said first hollow cylinder 14, and the length of said second hollow cylinder 15 is less than the length 14 of first hollow cylinder; One end of one end of said first hollow cylinder 14 and second hollow cylinder 15 is connected to the two ends of a hollow round platform sidewall 16, and the other end of the other end of said first hollow cylinder 14 and second hollow cylinder 15 is connected to the two ends of another hollow round platform 17 sidewalls.
When the system of use embodiment 2 carried out the desulphurization denitration operation, wherein, the molal quantity of hydrogen peroxide gas straying quatity was 0.8 times of nitric oxide molal quantity; Oxidization time 0.5 second, in the present embodiment, second control valve and the 3rd control valve are closed; First control valve is opened, and makes that the interior flue gas of flue gets into heater between boiler and the deduster, and the temperature of flue gas is 169 ℃ in the flue between boiler and the deduster; The temperature of the gas that comes out from heater is 180 ℃; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:318 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 821mg/ m
3, the absorption tower exports detected NOx:7 mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 97.80%, desulfuration efficiency is 100%.
Wet method ammonia process technology is joined on the absorption tower, and absorption liquid is NH
3H
2O recycles; After flue gas is absorbed washing, send into chimney, saline solution ammonium sulfate after the absorption and ammonium nitrate enrichment after dedusting, concentrate, crystallization, dehydration be the finished product chemical fertilizer; Nitrogen content is about 25%, and the absorbent of this instance also can be seawater, NaOH, KOH, Ca (OH)
2, CaO, CaCO
3, NH
3H
2O, NH
4HCO
3Deng wherein one or more; After this embodiment uses reaction warehouse, though than embodiment 1 under lower temperature, the denitration desulfuration efficiency does not use the situation of reaction warehouse apparently higher than embodiment 1; This is because this reaction warehouse can make reactant fully mix in moment; And increase exponentially reaction power, and be not only applicable to the gas-solid/liquid/gas reactions occasion in the chemical process, also be applicable to the gas-liquid reaction occasion in the chemical process.
As shown in Figure 6 and embodiment 1 difference is that said distribution device in gas-fluid is arranged on the flue between deduster 3 and the absorption tower 4.
When the system of use embodiment 3 carried out the desulphurization denitration operation, wherein, the molal quantity of hydrogen peroxide gas straying quatity was 1.8 times of nitric oxide molal quantity; Oxidization time 0.5 second, in the present embodiment, first control valve and the 3rd control valve are closed; Second control valve is opened, and makes that the interior flue gas of flue gets into heater between deduster and the absorption tower, and the temperature of flue gas is 110 ℃ in the flue between deduster and the absorption tower; The temperature of the gas that comes out from heater is 250 ℃; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:322 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 815mg/ m
3, the absorption tower exports detected NOx:22 mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 93.17%, desulfuration efficiency is 100%.
Wet method ammonia process technology is joined on the absorption tower, and absorption liquid is NH
3H
2O recycles; After flue gas is absorbed washing, send into chimney, saline solution ammonium sulfate after the absorption and ammonium nitrate enrichment after dedusting, concentrate, crystallization, dehydration be the finished product chemical fertilizer; Nitrogen content is about 25%, and the absorbent of this instance also can be seawater, NaOH, KOH, Ca (OH)
2, CaO, CaCO
3, NH
3H
2O, NH
4HCO
3Deng wherein one or more.
As shown in Figure 7 and embodiment 3 differences are that the flue between said distribution device in gas-fluid and the absorption tower 4 is provided with reaction warehouse 2, and the structure of this reaction warehouse 2 is the same with reaction warehouse structure among the embodiment 2.
When the system of use embodiment 4 carried out the desulphurization denitration operation, wherein, the molal quantity of hydrogen peroxide gas straying quatity was 1.5 times of nitric oxide molal quantity; Oxidization time 0.5 second, in the present embodiment, first control valve and the 3rd control valve are closed; Second control valve is opened, and makes that the interior flue gas of flue gets into heater between deduster and the absorption tower, and the temperature of flue gas is 105 ℃ in the flue between deduster and the absorption tower; The temperature of the gas that comes out from heater is 200 ℃; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:315 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 799mg/ m
3, the absorption tower exports detected NOx:15 mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 95.24%, desulfuration efficiency is 100%.
Wet method ammonia process technology is joined on the absorption tower, and absorption liquid is NH
3H
2O recycles; After flue gas is absorbed washing, send into chimney, saline solution ammonium sulfate after the absorption and ammonium nitrate enrichment after dedusting, concentrate, crystallization, dehydration be the finished product chemical fertilizer; Nitrogen content is about 25%, and the absorbent of this instance also can be seawater, NaOH, KOH, Ca (OH)
2, CaO, CaCO
3, NH
3H
2O, NH
4HCO
3Deng wherein one or more, after this embodiment uses reaction warehouse, though than embodiment 3 under lower temperature, the denitration desulfuration efficiency does not use the situation of reaction warehouse apparently higher than embodiment 3.
As shown in Figure 8, in the present embodiment, said flue gas generation device 1 is a boiler, and said hydrogen peroxide carburetion system comprises vapourizing unit 18 and hydrogen peroxide storage tank 10; Said vapourizing unit 18 links to each other with hydrogen peroxide storage tank 10, and said vapourizing unit 18 is connected with distribution device in gas-fluid through the 4th pipeline; Be provided with atomizer in the said vapourizing unit, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with hydrogen peroxide storage tank 10 on the said supply pump.Said distribution device in gas-fluid is arranged in the flue between flue gas generation device 1 and the deduster 3.Said vapourizing unit 18 is oil bath heating vaporized hydrogen peroxide device.
When the system of use embodiment 5 carries out the desulphurization denitration operation; Wherein, the molal quantity of hydrogen peroxide gas straying quatity is 2.0 times of nitric oxide molal quantity, oxidization time 0.5 second; The temperature of flue gas is 300 ℃ in the flue between boiler and the deduster; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:316 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 659mg/ m
3, the absorption tower exports detected NOx:27mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 91.45%, desulfuration efficiency is 100%.
Wet method ammonia process technology is joined on the absorption tower, and absorption liquid is NH
3H
2O recycles; After flue gas is absorbed washing, send into chimney, saline solution ammonium sulfate after the absorption and ammonium nitrate enrichment after dedusting, concentrate, crystallization, dehydration be the finished product chemical fertilizer; Nitrogen content is about 25%, and the absorbent of this instance also can be seawater, NaOH, KOH, Ca (OH)
2, CaO, CaCO
3, NH
3H
2O, NH
4HCO
3Deng wherein one or more.
As shown in Figure 9 and embodiment 5 differences are that the flue between said distribution device in gas-fluid and the deduster 3 is provided with reaction warehouse 2, and the structure of this reaction warehouse 2 is the same with reaction warehouse structure among the embodiment 2.Said vapourizing unit 18 is a ultrasonic wave vaporized hydrogen peroxide device.
When the system of use embodiment 6 carries out the desulphurization denitration operation; Wherein, the molal quantity of hydrogen peroxide gas straying quatity is 2.0 times of nitric oxide molal quantity, oxidization time 0.5 second; The temperature of flue gas is 300 ℃ in the flue between boiler and the deduster; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:328 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 668mg/ m
3, the absorption tower exports detected NOx:13mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 96.03%, desulfuration efficiency is 100%.
Shown in figure 10 and embodiment 5 differences are that said distribution device in gas-fluid is arranged on the flue between deduster 3 and the absorption tower 4.Said vapourizing unit 18 is electrical heating vaporized hydrogen peroxide device.
When the system of use embodiment 7 carries out the desulphurization denitration operation; Wherein, the molal quantity of hydrogen peroxide gas straying quatity is 2.0 times of nitric oxide molal quantity, oxidization time 0.5 second; The temperature of flue gas is 110 ℃ in the flue between boiler and the deduster; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:321 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 652mg/ m
3, the absorption tower exports detected NOx:36mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 88.7%, desulfuration efficiency is 100%.
Shown in figure 11 and embodiment 7 differences are that the flue between said distribution device in gas-fluid and the absorption tower 4 is provided with reaction warehouse 2, and the structure of this reaction warehouse 2 is the same with reaction warehouse structure among the embodiment 2.Said vapourizing unit 18 is electrical heating vaporized hydrogen peroxide device.
When the system of use embodiment 8 carries out the desulphurization denitration operation; Wherein, the molal quantity of hydrogen peroxide gas straying quatity is 2.0 times of nitric oxide molal quantity, oxidization time 0.5 second; The temperature of flue gas is 108 ℃ in the flue between boiler and the deduster; Wherein, the detecting instrument that nitrogen oxide in the flue gas and sulfur dioxide adopt is: NOVA2000, NOx:318 mg/ m in the flue gas that the flue gas generation device produces
3SO
2: 656mg/ m
3, the absorption tower exports detected NOx:29mg/ m
3SO
2: 0mg/ m
3, denitration efficiency is 90.88%, desulfuration efficiency is 100%.
The above is merely preferred embodiment of the present invention, and is in order to restriction the present invention, not all within spirit of the present invention and principle, any modification of being done, is equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (14)
- One kind based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, comprise the flue gas generation device, the deduster that links to each other with said flue gas generation device through flue; The absorption tower that links to each other with said deduster through flue; The top on said absorption tower is connected with chimney, and the bottom on said absorption tower is connected with oxidation fan and liquid dust arrester, is connected with the saline solution concentration and crystallization device on the said liquid dust arrester; Be connected with the finished product packing device on the said saline solution concentration and crystallization device; It is characterized in that, be connected with the hydrogen peroxide carburetion system on the said flue, said hydrogen peroxide carburetion system is used to provide hydrogen peroxide gas.
- 2. according to claim 1 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, it is characterized in that be provided with alkaline solution in the said absorption tower, the bottom on said absorption tower is connected with supply pump, be connected with a plurality of solution shower nozzles on the said supply pump; Said alkaline solution is NaOH, KOH, Ca (OH) 2, CaO, MgO, CaCO 3, NH 3H 2O, NH 4HCO 3With one or more the mixture in the seawater.
- 3. according to claim 1 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, it is characterized in that being provided with weight ratio in the said absorption tower is the alkaline solution of 1:1 and the mixture of organic catalyst; Said organic catalyst is the product LEXFINE that Israel Lextran company produces, and said alkaline solution is NaOH, KOH, Ca (OH) 2, CaO, MgO, CaCO 3, NH 3H 2O, NH 4HCO 3With one or more the mixture in the seawater.
- 4. according to claim 1 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; It is characterized in that; Said flue is provided with reaction warehouse; Said reaction warehouse comprises first hollow cylinder and second hollow cylinder that is set in said first hollow cylinder; The length of said second hollow cylinder is less than the length of first hollow cylinder, and an end of said first hollow cylinder and an end of second hollow cylinder are connected to the two ends of a hollow round platform sidewall, and the other end of the other end of said first hollow cylinder and second hollow cylinder is connected to the two ends of another hollow round platform sidewall; Said hydrogen peroxide carburetion system comprises first air inlet, second air inlet, the 3rd air inlet and gas outlet; Said first air inlet is connected on the flue between flue gas generation device and the deduster through first pipeline, and said first pipeline is provided with first control valve; Said second air inlet is connected on the flue between deduster and the absorption tower through second pipeline, and said second pipeline is provided with second control valve; Said the 3rd air inlet is through the external outside air of the 3rd pipeline, and said the 3rd pipeline is provided with the 3rd control valve; Said gas outlet is connected on the flue between flue gas generation device and the deduster through the 4th pipeline, perhaps is connected on the flue between deduster and the absorption tower.
- 5. according to claim 4 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, it is characterized in that said hydrogen peroxide carburetion system comprises filter, blower fan, heater and hydrogen peroxide storage tank; One end of said filter links to each other with first pipeline, second pipeline and the 3rd pipeline respectively, and the other end links to each other with blower fan; The other end of said blower fan links to each other with heater, and the other end of said heater is connected with the 5th pipeline, and an end of said the 5th pipeline and the 4th pipeline links to each other, and the other end of said the 4th pipeline is connected with distribution device in gas-fluid; Be provided with atomizer in said the 5th pipeline, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with the hydrogen peroxide storage tank on the said supply pump.
- 6. according to claim 5 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; It is characterized in that; Said distribution device in gas-fluid is arranged in the flue between flue gas generation device and the deduster, and said reaction warehouse is arranged between distribution device in gas-fluid and the deduster.
- 7. according to claim 5 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; It is characterized in that; Said distribution device in gas-fluid is arranged in the flue between deduster and the absorption tower, and said reaction warehouse is arranged between distribution device in gas-fluid and the absorption tower.
- 8. according to claim 4 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, it is characterized in that said hydrogen peroxide carburetion system comprises vapourizing unit and hydrogen peroxide storage tank; Said vapourizing unit links to each other with the hydrogen peroxide storage tank, and said vapourizing unit is connected with distribution device in gas-fluid through the 4th pipeline; Be provided with atomizer in the said vapourizing unit, be connected with the 4th control valve on the said atomizer, be connected with check valve on said the 4th control valve, be connected with supply pump on the said check valve, be connected with the hydrogen peroxide storage tank on the said supply pump.
- 9. according to claim 8 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; It is characterized in that; Said distribution device in gas-fluid is arranged in the flue between flue gas generation device and the deduster, and said reaction warehouse is arranged between distribution device in gas-fluid and the deduster.
- 10. according to claim 8 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system; It is characterized in that; Said distribution device in gas-fluid is arranged in the flue between deduster and the absorption tower, and said reaction warehouse is arranged between distribution device in gas-fluid and the absorption tower.
- 11. according to claim 8 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying system, it is characterized in that said vapourizing unit is ultrasonic wave vaporized hydrogen peroxide device, electrical heating vaporized hydrogen peroxide device or oil bath heating vaporized hydrogen peroxide device.
- 12. one kind based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying method; It is characterized in that; Said method comprising the steps of: at first, hydrogen peroxide gas that the hydrogen peroxide carburetion system is provided sprays in the flue; The lower valency nitrogen oxide that the flue gas generation device is produced and get in the interior flue gas of flue is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
- 13. according to claim 12 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying method; It is characterized in that, said method comprising the steps of: at first, a gas or a plurality of gases in the flue gas in the flue between the flue gas with in the flue between outside air, flue generation device and the deduster, deduster and the absorption tower introduce filter; Then, the gas after filtering through filter gets into heater through blower fan and is heated to after temperature is greater than or equal to 170 ℃, gets into the 5th pipeline; Then; Hydrogenperoxide steam generator in the hydrogen peroxide storage tank extracts the back and sprays in the 5th pipeline through atomizer; Make that vaporization forms hydrogen peroxide gas under the effect of its gas that is greater than or equal to 170 ℃ in temperature; Hydrogen peroxide gas gets into the 4th pipeline again and sprays in the flue between flue gas generation device and the deduster through distribution device in gas-fluid, thereby the flue gas middle or low price attitude nitrogen oxide that the flue gas generation device produces is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Hydrogen peroxide gas that wherein sprays into and the nitrogen oxide mol ratio in the flue gas>0.5, reaction time >=0.3 second; Then, flue gas and hydrogen peroxide gas get into reaction warehouse simultaneously and carry out further oxidation, thereby guarantee that the lower valency nitrogen oxide in the flue gas is completely oxidized to high valence state nitrogen oxide soluble in water, and the sulfur dioxide complete oxidation generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower after getting into the deduster dedusting again, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
- 14. according to claim 12 based on the hydrogen peroxide effect to the flue gas and desulfurizing and denitrifying method, it is characterized in that, said method comprising the steps of: at first, the flue gas that produces of flue gas generation device gets into deduster and carry out dedusting; Then, a gas in the flue gas in the flue between the flue gas in the flue between outside air, flue generation device and the deduster, deduster and the absorption tower or a plurality of gas are introduced filter; Then, the gas after filtering through filter gets into heater through blower fan and is heated to after temperature is greater than or equal to 170 ℃, gets into the 5th pipeline; Then; Hydrogenperoxide steam generator in the hydrogen peroxide storage tank extracts the back and sprays in the 5th pipeline through atomizer; Make that vaporization forms hydrogen peroxide gas under the effect of its gas that is greater than or equal to 170 ℃ in temperature; Hydrogen peroxide gas gets into the 4th pipeline again through in the flue between distribution device in gas-fluid deduster and the absorption tower, thereby the flue gas middle or low price attitude nitrogen oxide that the flue gas generation device produces is oxidized to high valence state nitrogen oxide soluble in water, and oxidizing sulfur dioxide generates sulfur trioxide; Hydrogen peroxide gas that wherein sprays into and the nitrogen oxide mol ratio in the flue gas>0.5, reaction time >=0.3 second; Then; Flue gas after the dedusting and hydrogen peroxide gas get into reaction warehouse simultaneously and carry out further oxidation; Thereby the lower valency nitrogen oxide in the flue gas after the assurance dedusting is completely oxidized to high valence state nitrogen oxide soluble in water, and the sulfur dioxide complete oxidation generates sulfur trioxide; Then, the flue gas after oxidized gets into the absorption tower, washs absorption by alkaline solution in the tower, absorbs nitrogen oxide and oxysulfide behind oxidized in the flue gas simultaneously after chimney enters atmosphere; At last, the inner absorption liquid in absorption tower absorbs through circulating repeatedly, and after the weight percent concentration of the salinity in the absorption liquid reached 35%～40%, come out to carry out successively from the bottom, absorption tower liquid dedusting, condensing crystallizing and drying were packed or dumped.
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| CN2011102264797A CN102274681A (en) | 2011-08-09 | 2011-08-09 | Hydrogen-hydroxide-based flue gas synchronous desulfuration and denitration system and method |
| CN2011103547702A CN102500206A (en) | 2011-08-09 | 2011-11-10 | System and method for desulfurizing and denitrating smoke based on action of hydrogen peroxide |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101352644A (en) * | 2008-08-29 | 2009-01-28 | 浙江大学 | Wet flue gas denitration technique for nitrite recovery |
| CN100496675C (en) * | 2007-04-30 | 2009-06-10 | 武汉凯迪电力环保有限公司 | Simultaneous desulfurization and denitration wet ammonia flue gas cleaning technology and system thereof |
| CN202427336U (en) * | 2011-08-09 | 2012-09-12 | 中悦浦利莱环保科技有限公司 | Hydrogen peroxide-action-based system for conducting desulfurization and denitration on smoke simultaneously |
-
2011
- 2011-08-09 CN CN2011102264797A patent/CN102274681A/en active Pending
- 2011-11-10 CN CN2011103547702A patent/CN102500206A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100496675C (en) * | 2007-04-30 | 2009-06-10 | 武汉凯迪电力环保有限公司 | Simultaneous desulfurization and denitration wet ammonia flue gas cleaning technology and system thereof |
| CN101352644A (en) * | 2008-08-29 | 2009-01-28 | 浙江大学 | Wet flue gas denitration technique for nitrite recovery |
| CN202427336U (en) * | 2011-08-09 | 2012-09-12 | 中悦浦利莱环保科技有限公司 | Hydrogen peroxide-action-based system for conducting desulfurization and denitration on smoke simultaneously |
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| CN103463978A (en) * | 2013-09-30 | 2013-12-25 | 南京理工大学 | Device and method for smoke simultaneous desulfurization and denitrification based on hydrogen peroxide catalytic oxidation |
| CN103463978B (en) * | 2013-09-30 | 2016-03-02 | 南京理工大学 | Based on the device and method of catalytic oxidation of hydrogen peroxide flue gas and desulfurizing and denitrifying |
| CN105344214A (en) * | 2014-08-21 | 2016-02-24 | 山西易通环保技术有限公司 | Liquid-state catalyst flue gas purification integration system and liquid-state catalyst flue gas purification integration process |
| CN106853328A (en) * | 2016-03-11 | 2017-06-16 | 济南大学 | A kind of hydrogen peroxide Efficient utilization method and device for low-temperature flue gas desulphurization denitration |
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| CN106378145B (en) * | 2016-11-18 | 2019-06-11 | 济南大学 | A kind of gaseous state hydrogen peroxide catalyst and its application |
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