CN204824173U - Nitrogen oxide system nitric acid system in flue gas - Google Patents
Nitrogen oxide system nitric acid system in flue gas Download PDFInfo
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- CN204824173U CN204824173U CN201520343475.0U CN201520343475U CN204824173U CN 204824173 U CN204824173 U CN 204824173U CN 201520343475 U CN201520343475 U CN 201520343475U CN 204824173 U CN204824173 U CN 204824173U
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- flue gas
- nox
- adsorption bed
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- oxidation
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Abstract
The utility model relates to a nitrogen oxide system nitric acid system in flue gas comprises NOx adsorption bed, NOx desorption system, NOx oxidative system and NOx absorption system, the NOx oxidative system is passed through the pipeline series connection by oxidation reactor and ozone generator and is constituteed, the NOx adsorption bed is constituteed by more than two sets of or two sets of side by side, pack the heteropoly acid adsorbent in the adsorption bed, income antilinear three - way valve connection to the NOx desorption system and the flue gas input pipeline of every group adsorption bed, the export is through three - way valve connection to fume emission mouth and oxidation reactor entry, the oxidation reactor export is through pipeline and NOx absorption system entry linkage, the pipeline is imported through pipe -line transportation to flue gas to the NO tail gas that contains that the NOx absorption process is produced. The utility model discloses used various raw materials low price, flue gas denitration is with low costs and can realize the waste gas resourceization, and manufacturing equipment is simple, easily operates convenient to popularize and use.
Description
Technical field
The utility model relates to a kind of nitrogen oxides in effluent nitric acid system.
Background technology
Oxynitride (NO
x) be one of principal pollutant in air, wherein coal-fired plant flue gas is NO
xprimary discharge source.Power-plant flue gas has that volume is large, NO
xconcentration is low, NO
xthe feature that total amount is large, therefore denitrating flue gas is a thorny difficult problem.In order to reduce gas cleaning cost, improve denitration efficiency, realize NO
xresource utilization, has carried out extensive research both at home and abroad in denitrating flue gas.Wherein, ZL200810120645.3 is to flue gas direct oxidation and with the NO after alkali liquor absorption oxidation
xmake nitrite, although the method can realize NO
xresource utilization, but with ozone or hydrogen peroxide to the direct oxidation of large discharge flue gas, oxygenant consumption is large and efficiency is low.ZL200810120647.2 is with the ozone O after UV-activated
3or oxydol H
2o
2in oxygenant, the nitrogen protoxide NO in flue gas is oxidized to NO
2, then use alkali lye washing flue gas to remove NO
xalthough the oxidation efficiency oxidation object that the method improves oxygenant is still large discharge flue gas, and therefore operation energy consumption is too high.ZL200610039814.1 will containing NO
xwaste gas and air mixed after, by plural serial stage absorb nitric acid processed, achieve commercial run NO
xthe improvement of waste gas and resource utilization, although this technology technique is simple, absorption equipment is too huge, inapplicable to the power-plant flue gas of lower concentration large discharge.
In sum, NO in flue gas is perplexed
xthe main reason of resource utilization is that its concentration is too low, for solving NO in flue gas
xthe too low problem of concentration, to NO in flue gas
xcarry out adsorption and enrichment, then by the NO after concentrated
xcarry out desorption and be oxidized, after oxidation, absorbing nitric acid processed with the aqueous solution.This technique is simple, running cost is low, and can realize NO in flue gas
xrecycling, have a good application prospect.
Summary of the invention
In order to overcome the few problem of nitrogen oxides in effluent recycling approach, the utility model provides NO in a kind of flue gas
xnitric acid system processed.General plotting of the present utility model is: in order to overcome NO in flue gas
xthe problem that concentration is low, the present invention uses heteropolyacid to NO in flue gas
xadsorption and enrichment, then to the NO of absorption
xcarry out desorption to realize NO
xconcentrated; In order to solve NO
xmiddle NO
2the problem of the follow-up nitric acid efficiency processed of the too low impact of content, adopts the mode of ozone oxidation to NO
xbe oxidized, to improve NO
2at NO
xin proportion; NO is absorbed for the aqueous solution
xnitric acid processed can produce this practical work of NO, and nitric acid tail gas processed is back to the import of heteropolyacid adsorber again, makes circulation of tail gas carry out adsorption-desorption-oxidation-nitric acid operation processed, to realize the zero release of relieving haperacidity tail gas.
The utility model is achieved through the following technical solutions:
A kind of nitrogen oxides in effluent nitric acid system, by NO
xadsorption bed, NO
xdesorption system, NO
xoxidation system and NO
xabsorption system forms; NO
xoxidation system consists of placed in series oxidation reactor and ozonizer, NO
xadsorption bed is made up of side by side two groups or more, and fill heteropolyacid sorbent material in adsorption bed, the entrance often organizing adsorption bed is connected to NO through T-valve
xdesorption system and flue gas input channel, export and be connected to fume emission mouth and oxidation reactor entrance through T-valve, and oxidation reactor outlet is by pipeline and NO
xabsorption system entrance connects, NO
xwhat absorption process produced contains NO tail gas through Cemented filling to flue gas input channel; NO
xdesorption system desorbing agent used is water vapour; NO
xoxidation system oxygenant used is ozone, is produced by ozonizer; NO
xabsorption system is bubble tower, and absorption agent used is dust technology.
Aforesaid nitrogen oxides in effluent nitric acid system, described heteropolyacid sorbent material comprises phospho-wolframic acid H
3pW
12o
40, germanotungstic acid H
4geW
12o
40, silicotungstic acid H
3siW
12o
40, phospho-molybdic acid H
3pMo
12o
40, adsorption temp is 105 ~ 200 DEG C, and flue gas air speed is 500 ~ 10000h
-1.
Aforesaid nitrogen oxides in effluent nitric acid system, described water vapor is produced by steam generator, and vapour content is 3.1 ~ 83.4vol.%, and desorption temperature is 25 ~ 95 DEG C, and air speed is 50 ~ 1000h
-1.
Aforesaid nitrogen oxides in effluent nitric acid system, described ozone concn is 10 ~ 120mg/L.
Aforesaid nitrogen oxides in effluent nitric acid system, described dust technology concentration is 2 ~ 10%.
The utility model processing unit is simple to operation, various low in raw material price used, and denitrating flue gas cost is low and can realize exhaust-gas resource, is convenient to promote the use of.
Accompanying drawing explanation
Accompanying drawing 1 is structural representation of the present utility model.
Wherein, 1, flue gas input channel; 2-1, T-valve; 2-2, T-valve; 2-3, T-valve; 2-4, T-valve; 2-5, T-valve; 2-6, T-valve; 3-1, adsorption bed; 3-2, adsorption bed; 4, steam generator; 5, oxidation reactor; 6, ozonizer; 7, absorption tower; 8, relieving haperacidity exhaust pipe; 9, check valve; 10, fume emission mouth.
Embodiment
Below in conjunction with embodiment, the present invention is described in further detail.
Embodiment 1:
Fig. 1 is structural representation of the present utility model, and as shown in Figure 1, the flue gas after desulfurization and dedusting enters adsorption bed 3-1 through inlet duct 1 by T-valve 2-1, and the flue gas after purification is discharged by discharge outlet 10 through T-valve 2-4.NO
xwhen penetrating adsorption bed 3-1, switch three-way valve 2-1 makes flue gas enter adsorption bed 3-2 to carry out adsorption cleaning, and the flue gas after purification is discharged by discharge outlet 10 through T-valve 2-5.Start steam generator 4, make water vapour enter adsorption bed 3-1 desorption NO by T-valve 2-2
x.NO after desorption
xgas mixture enters oxidation reactor 5, NO by T-valve 2-4,2-6
xby the ozone oxidation that ozonizer 6 produces.NO after oxidation
xgas mixture enters adsorption tower 7, NO
xabsorbed by dust technology and produce nitric acid, what produce returns smoke inlet pipeline 1 through piping 8 by check valve 9 containing NO tail gas simultaneously.The nitric acid produced is discharged through discharge outlet 11.
In this embodiment, exhaust gas volumn is 500ml/min, NO
xconcentration is 1000ppm, and sorbent material used in adsorption bed 3-1 is phosphorus heteropoly tungstic acid H
3pW
12o
40, adsorption temp is 150 DEG C, air speed is 5000h
-1.The water vapour content that steam generator 4 produces is 8%, and desorption temperature is 50 DEG C, air speed is 500h
-1.It is 60mg/L that ozonizer 6 produces ozone concn.Absorption tower 7 absorption liquid used is 5% dust technology 100ml, and after running 2h, concentration of nitric acid becomes 6.2%.
Embodiment 2-6 is different from the processing parameter of sorbent material that embodiment 1 adopts and each step, and all the other conditions are with embodiment 1.Embodiment 2-6 processing parameter and Performance Assessment are in table 1:
Wherein, adopt the Chinese of sorbent material to be expressed as follows: H
4geW
12o
40: germanotungstic acid; H
3siW
12o40: silicotungstic acid; H
3pMo
12o
40: phospho-molybdic acid; H
3pW
12o
40: phospho-wolframic acid.
Table 1
Claims (1)
1. a nitrogen oxides in effluent nitric acid system, is characterized in that by NO
xadsorption bed, NO
xdesorption system, NO
xoxidation system and NO
xabsorption system forms; NO
xoxidation system consists of placed in series oxidation reactor and ozonizer, NO
xadsorption bed is made up of side by side two groups or more, and fill heteropolyacid sorbent material in adsorption bed, the entrance often organizing adsorption bed is connected to NO through T-valve
xdesorption system and flue gas input channel, export and be connected to fume emission mouth and oxidation reactor entrance through T-valve, and oxidation reactor outlet is by pipeline and NO
xabsorption system entrance connects, NO
xwhat absorption process produced contains NO tail gas through Cemented filling to flue gas input channel; NO
xdesorption system desorbing agent used is water vapour; NO
xoxidation system oxygenant used is ozone, is produced by ozonizer; NO
xabsorption system is bubble tower, and absorption agent used is dust technology.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520343475.0U CN204824173U (en) | 2015-05-26 | 2015-05-26 | Nitrogen oxide system nitric acid system in flue gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520343475.0U CN204824173U (en) | 2015-05-26 | 2015-05-26 | Nitrogen oxide system nitric acid system in flue gas |
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| Publication Number | Publication Date |
|---|---|
| CN204824173U true CN204824173U (en) | 2015-12-02 |
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ID=54681795
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|---|---|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107215854A (en) * | 2017-03-22 | 2017-09-29 | 傅国琳 | A kind of devices and methods therefor for producing nitric acid |
| CN111229006A (en) * | 2020-03-11 | 2020-06-05 | 山东师范大学 | Method for denitration by using chlorine dioxide-containing liquid |
| CN112423861A (en) * | 2018-07-17 | 2021-02-26 | 奥迪股份公司 | Utilization of nitrogen oxides from ambient air |
| CN113509820A (en) * | 2021-07-29 | 2021-10-19 | 南通斐腾新材料科技有限公司 | Method for preparing acid by concentrating nitrogen oxide by zeolite rotating wheel and washing and absorbing nitrogen oxide |
-
2015
- 2015-05-26 CN CN201520343475.0U patent/CN204824173U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107215854A (en) * | 2017-03-22 | 2017-09-29 | 傅国琳 | A kind of devices and methods therefor for producing nitric acid |
| CN112423861A (en) * | 2018-07-17 | 2021-02-26 | 奥迪股份公司 | Utilization of nitrogen oxides from ambient air |
| US11826693B2 (en) | 2018-07-17 | 2023-11-28 | Audi Ag | Utilization of nitrogen oxides from ambient air |
| CN111229006A (en) * | 2020-03-11 | 2020-06-05 | 山东师范大学 | Method for denitration by using chlorine dioxide-containing liquid |
| CN113509820A (en) * | 2021-07-29 | 2021-10-19 | 南通斐腾新材料科技有限公司 | Method for preparing acid by concentrating nitrogen oxide by zeolite rotating wheel and washing and absorbing nitrogen oxide |
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|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20151202 Termination date: 20160526 |