CN201807305U - Flue gas denitration equipment - Google Patents
Flue gas denitration equipment Download PDFInfo
- Publication number
- CN201807305U CN201807305U CN2010202599378U CN201020259937U CN201807305U CN 201807305 U CN201807305 U CN 201807305U CN 2010202599378 U CN2010202599378 U CN 2010202599378U CN 201020259937 U CN201020259937 U CN 201020259937U CN 201807305 U CN201807305 U CN 201807305U
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- China
- Prior art keywords
- heat exchanger
- flue gas
- exchanger tube
- equipment according
- gas equipment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 239000003546 flue gas Substances 0.000 title claims abstract description 57
- 239000003795 chemical substances by application Substances 0.000 claims description 46
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 11
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 8
- 238000010531 catalytic reduction reaction Methods 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 10
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 229910010413 TiO 2 Inorganic materials 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 241000264877 Hippospongia communis Species 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 238000006722 reduction reaction Methods 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model provides flue gas denitration equipment. As the equipment uses a novel coal economizer (which comprises a heat exchange tube and a plurality of heat exchange fins, wherein, the heat exchange tube passes through the heat exchange fins, and the outer wall of the heat exchange tube is in close contact with the heat exchange fins.), the volume of the coal economizer is greatly reduced under the circumstance that the heat exchange efficiency is guaranteed, a space can be saved for arranging a catalyst bed layer, and an SNCR (selective non-catalytic reduction) process and an SCR (selective catalytic reduction) process can be simultaneously achieved; compared with SNCR reaction, the equipment improves the denitration efficiency; and compared with SCR reaction, the equipment reduces the thickness of the catalyst bed layer under the circumstance of guaranteeing the denitration efficiency, thereby reducing the cost.
Description
Technical field
The utility model relates to a kind of denitrating flue gas equipment.
Background technology
Flue gas is one of main emission of steam power plant, by the combustible generation of burning in burner (being boiler).Owing to contain a large amount of nitrogen oxide NO usually in the flue gas
xAs NO, if these nitrogen oxide directly are discharged in the atmosphere, can cause the very strong acid rain of corrosivity, so flue gas must be handled before discharging through denitrogenation (being denitration).
At present, the gas denitrifying technology of utilization comparative maturity mainly contains two kinds: SCR (SCR) technology and SNCR denitration (SNCR) technology.SNCR technology generally sprays into denitrfying agent in the burner hearth of 800-1300 ℃ of boiler, denitrfying agent (urea or ammonia) is contacted with flue gas, makes the NO in denitrfying agent and the flue gas
xCarry out the selective reduction reaction and generate nitrogen (N
2) and steam (H
2And discharge and flue gas after denitrfying agent contacts O).The problem that SNCR technology exists is that the efficient of denitration is low, and the denitration efficiency of general SNCR denitration technology is below 40%.
SCR technology then is that beds is set in flue, under 280-420 ℃ of temperature, carries out the catalytic selectivity reduction reaction under the condition that catalyst exists.The denitration efficiency of SCR technology is higher relatively than SNCR, generally can reach 50-60%.
And although SCR denitration effect good than SNCR technology, as mentioned above, the denitration rate of SCR also only is below 60%, remains further to be improved.Though can improve the denitration rate of SCR a little by the thickness of further raising beds,, can cause cost significantly to improve because catalyst is relatively more expensive.
In addition, as mentioned above, SNCR carries out at 800-1300 ℃, the temperature of flue gas is generally more than 800 ℃ even 1000 ℃ after the denitration, in order to realize the cooling of flue gas, common way is to set up an economizer (being heat exchanger) behind the SNCR of the rear portion of flue at present, and economizer is formed by a plurality of heat exchanger tubes that are connected in series mutually.
Although can reduce the temperature of flue gas behind the SNCR to a certain extent by existing economizer,, the temperature of SNCR flue gas is still up to more than 500 ℃.High like this smog discharge temperature does not meet environmental requirement on the one hand, and on the other hand, flue gas is also taken away a large amount of heats, is unfavorable for the utilization again of the energy.
The utility model content
The purpose of this utility model is lower and be unfavorable for the shortcoming of reusing of energy source in order to overcome denitration efficiency that existing denitrating technique exists, a kind of denitration degree height is provided and is beneficial to the denitrating flue gas equipment of reusing of energy source.
In order to improve the efficient of denitration, inventor of the present utility model attempts the amount by used denitrfying agent among the direct increase SNCR, yet is surprised to find that, though the amount of denitrfying agent obviously increases but the nitrogen oxide NO in the flue gas
xAmount not only do not reduce on the contrary and rise to some extent, this may be because ammonia has been oxidized to NO
x
In order to address the above problem, inventor of the present utility model has carried out a large amount of research, proposes a kind of equipment that SNCR and SCR can be combined, and this equipment can improve to realize SNCR and SCR process simultaneously on the basis of equipment at existing SNCR.
The utility model provides a kind of denitrating flue gas equipment, this equipment comprises flue and is arranged on the interior denitrfying agent feedway of flue, economizer and beds, flow direction along flue gas, described denitrfying agent feedway, economizer and beds are successively set in the described flue, wherein, described flue comprises first vertical section, second vertical section and horizontal segment, the two ends of described horizontal segment are communicated with the top of first vertical section and second vertical section respectively, described denitrfying agent feedway is positioned at first vertical section, economizer and beds are positioned at second vertical section, described economizer comprises heat exchanger tube and a plurality of heat exchanger fin, described heat exchanger tube passes described heat exchanger fin, and the outer wall of heat exchanger tube closely contacts with heat exchanger fin.
The utility model (comprises heat exchanger tube and a plurality of heat exchanger fin by using new economizer, described heat exchanger tube passes described heat exchanger fin, and the outer wall of heat exchanger tube closely contacts with heat exchanger fin), thereby under the situation that guarantees heat exchange efficiency, greatly reduce the volume of economizer, can in the space that saves, beds be set thus, SNCR and SCR process have been realized simultaneously, improved denitration efficiency with SNCR reacting phase ratio, compare under the situation that guarantees denitration efficiency with the SCR reacting phase, reduce the thickness of beds, reduced cost.
Description of drawings
The structural representation of the denitrating flue gas equipment that Fig. 1 provides for the utility model;
Fig. 2 is the structural representation of economizer in the denitrating flue gas equipment in a kind of embodiment of the present utility model;
Fig. 3 is the structural representation of the heat exchanger fin of economizer in the denitrating flue gas equipment in a kind of embodiment of the present utility model;
Fig. 4 be in the another kind of embodiment of the present utility model denitrating flue gas equipment in the structural representation of heat exchanger fin of economizer.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is described in detail.
As shown in Figure 1, a kind of denitrating flue gas equipment, this equipment comprises flue 1 and is arranged on denitrfying agent feedway 2 in the flue 1, economizer 3 and beds 4, flow direction along flue gas, described denitrfying agent feedway 2, economizer 3 and beds 4 are successively set in the described flue 1, it is characterized in that, described flue 1 comprises first vertical section 5, second vertical section 6 and horizontal segment 7, the two ends of described horizontal segment 7 are communicated with the top of first vertical section 5 and second vertical section 6 respectively, described denitrfying agent feedway 2 is positioned at first vertical section 5, economizer 3 and beds 4 are positioned at second vertical section 6, described economizer 3 comprises heat exchanger tube 8 and a plurality of heat exchanger fin 9, described heat exchanger tube 8 passes described heat exchanger fin 9, and the outer wall of heat exchanger tube 8 closely contacts with heat exchanger fin 9.
As shown in Figure 2, in a kind of preferred implementation, described a plurality of heat exchanger fins 9 are arranged in parallel, and more than 8 past ground return of described heat exchanger tube passes a plurality of heat exchanger fins 9 that are arranged in parallel successively, forms the parallel multirow and the heat exchanger tube array of multiple row.
The structure of described heat exchanger fin can change according to the needs of heat exchange and the size of heat exchanger tube, for example, as shown in Figure 3, is formed with the space of mating with the size of described heat exchanger tube 8 on the described heat exchanger fin 9.
As shown in Figure 4, in another embodiment, each heat exchanger fin 9 comprises a plurality of plate bodys, this plate body have in groove and adjacent two plate bodys groove toward each other, the space that the shape of formation and heat exchanger tube 8 adapts, described heat exchanger tube 8 passes this space and closely contacts with heat exchanger fin 9.
In another kind of preferred implementation, described a plurality of heat exchanger fins 9 are arranged in parallel, and described heat exchanger tube 8 is a plurality of, and a plurality of heat exchanger tubes 8 pass a plurality of heat exchanger fins 9 that are arranged in parallel successively, form the parallel multirow and the heat exchanger tube array of multiple row.
In the utility model, the quantity of heat exchanger fin 9 can in very large range change in the described economizer 3, can adjust according to the needs of heat exchange and the needs of size, under the preferable case, the gross thickness of a plurality of heat exchanger fins that are arranged in parallel 9 can be the 10-20% of single file or single-row heat exchanger tube 8 length, under the preferred situation, the distance of two adjacent heat exchanger fins 9 can be 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 9, and the thickness of each heat exchanger fin 9 can be 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 9.
In the utility model, the size of described heat exchanger fin 9 can in very large range change, the needs that can be size according to the needs of heat exchange are adjusted, and under the preferable case, the total sectional area that passes the heat exchanger tube 8 of each described heat exchanger fin 9 can account for the 10-50% of these heat exchanger fin 9 single face areas.There is no particular limitation for the size of described heat exchanger tube 8, can select the heat exchanger tube size of various routines for use, and for example, the sectional area of described heat exchanger tube 8 can be the 10-100 square centimeter.
In addition, in described economizer 3, the density that described heat exchanger tube 8 is arranged can in very large range change, and under the preferable case, two adjacent in parallel multirow or the multiple row heat exchanger tube 8 distances capable or two row heat exchanger tubes 8 can be 5-25 centimetre.
In a kind of preferred implementation of the present utility model, described heat exchanger tube 8 forms integrative-structure with a plurality of heat exchanger fins 9.
According to the utility model, the SNCR that described denitrfying agent feedway 2 is positioned at described flue is the SNCR district.Under the preferable case, the top of the distance A of the bottom of described denitrfying agent feedway 2 to first vertical sections 5 and denitrfying agent feedway 2 and first vertical section 5 to the bottom apart from satisfying A: B=10-25 between the B: 30, preferred A: B=15-23: 30.
According to the utility model, described denitrfying agent feedway 2 can be the various devices that denitrfying agent is provided that can be used in, under the preferable case, described denitrfying agent feedway 2 is a pipeline, this pipeline passes the wall of flue 1, stretches in the flue 1, stretches on the pipeline in the flue 1 to be formed with opening.Under the preferable case, described pipeline can be for a plurality of, and the opening on every pipeline that stretches in the flue 1 can be for a plurality of.
A kind of preferred embodiment in, described a plurality of pipelines along flue 1 axially or circumferential array, under the preferred situation, a plurality of openings on every pipeline that stretches in the flue 1 are along the axial distribution of described pipeline.For denitrfying agent is better contacted with flue gas, the direction of described opening is preferably opposite with the direction of flow of flue gas in the flue 1.
In the utility model, the direction of described opening is opposite with the direction of flow of flue gas in the flue 1 to be not absolute opposite, the direction that comprises described opening down, towards the situation of level or downward-sloping 1-15 °.
According to a kind of embodiment of the present utility model, the cross-sectional area of described flue 1 is 5000-50000 with the ratio of the gross area of the opening of the pipeline of described denitrfying agent feedway 2: 1, be preferably 20000-30000: 1.
In the described denitrfying agent feedway 2, the other end of described pipeline is communicated with the denitrfying agent source.Described denitrfying agent source can be the denitrfying agent storage tank, described denitrfying agent can be various can with NO
xThereby reaction reduces NO in the flue gas
xThe reagent of content for example can be ammonia.Described denitrfying agent preferably uses with the form of its aqueous solution, and the concentration of described solution has been conventionally known to one of skill in the art, the various concentration that can reach for denitrfying agent.In order to reduce the consumption of denitrfying agent, preferred described denitrfying agent uses with the form of its saturated solution.
Described catalyst can be various can catalytic denitration agent and nitrogen oxide NO
xReaction makes nitrogen oxide NO
xBe converted into the catalyst of nitrogen, be preferably metal oxide catalyst.Described metal oxide such as V
2O
5, Fe
2O
3, CuO, Cr
2O
3, Co
3O
4, NiO, CeO
2, La
2O
3, Pr
6O
11, Nd
2O
3, Gd
2O
3, Yb
2O
3In one or more, preferred V
2O
5Further preferred described catalyst is to be dispersed in TiO
2Upward, with V
2O
5Be main active component, WO
3Or MoO
3Be the vanadium titanium system of co-catalyst, i.e. V
2O
5-WO
3/ TiO
2Or V
2O
5-MoO
3/ TiO
2Described beds 4 is preferably above-mentioned V
2O
5-WO
3/ TiO
2Or V
2O
5-MoO
3/ TiO
2Catalyst is fixed on the corrosion resistant plate surface or makes the ceramic honey comb shape, forms the version of stainless steel corrugated plate dst and ceramic honey comb.Above-mentioned catalyst can be commercially available, and for example can change into available from Japanese catalyst, the Cormetech company of Hitachi, Ltd, Germany refined robust and sturdy grand company and the U.S..The thickness of described beds 4 can in very large range change, and is preferably 1.5-2.0 rice.
In the utility model, described flue 1 is surrounded by metal tube, can feed heat exchange medium in the metal tube, thereby can make full use of the heat in the flue gas.Under the preferable case, described metal tube for example can be carbon steel pipe, stainless steel tube, copper pipe, titanium pipe or various metal alloy pipes etc.
In the utility model, the using method of described denitrating flue gas equipment comprises by denitrfying agent feedway 2 provides denitrfying agent in flue 1, make flue gas and denitrfying agent that the SNCR reaction take place in first vertical section 5, promptly carry out the SNCR denitration, flue gas after the SNCR denitration and residual denitrfying agent enter second vertical section 6 after passing described horizontal segment 7, carry out heat exchange with the heat transferring medium in the economizer 3 in second vertical section 6, afterwards by beds 4, nitrogen oxide in the flue gas and residual denitrfying agent further take place selective-catalytic-reduction denitrified under the effect of beds 4, obtain the flue gas that amount of nitrogen oxides further reduces, thereby finish the SNCR and the SCR combined denitration process of described flue gas.
The condition of described flue gas and the reaction of described denitrfying agent generation SNCR comprises that temperature is preferably 800-1300 ℃ more preferably 800-1100 ℃, in the nitrogen element, and NO in nitrogen and the flue gas in the denitrfying agent
xThe mol ratio (be called for short ammonia nitrogen mol ratio) of nitrogen (in NO) can be 0.3-2: 1, be preferably 0.5-1.5: 1, the time that contacts under this temperature is preferably 0.1-2 second, more preferably 0.5-1 second.Thereby said temperature can utilize the temperature of this section flue gas itself to realize by the position of selecting described denitrfying agent to supply with, thereby need not extra heat supply or cooling.The temperature of above-mentioned SNCR needs strict control, and when temperature was higher than 1300 ℃, ammonia just was oxidized to NO
x, following reaction promptly takes place:
And when temperature was lower than 800 ℃, aforementioned SNCR was reflected under the catalyst-free existence and can not takes place.
The selective-catalytic-reduction denitrified condition of flue gas comprises that the condition that described nitrogen oxide is reduced to nitrogen comprises that temperature can be 280-420 ℃, is preferably 300-400 ℃, the flow velocity of flue gas can be the 4-12 meter per second, be preferably the 5-8 meter per second, in the nitrogen element, NO in nitrogen and the flue gas in the denitrfying agent
xThe mol ratio of nitrogen (in NO) can be 0.5-1.1: 1, be preferably 0.7-1: 1.
In preferred embodiment, the denitrfying agent that described denitrfying agent feedway 2 is supplied with is excessive with respect to carrying out that SNCR reacts, to carry out SCR and SNCR reaction better simultaneously.
The utility model (comprises heat exchanger tube and a plurality of heat exchanger fin by using new economizer, described heat exchanger tube passes described heat exchanger fin, and the outer wall of heat exchanger tube closely contacts with heat exchanger fin), thereby under the situation that guarantees heat exchange efficiency, greatly reduce the volume of economizer, thereby can in the space that saves, beds be set, SNCR and SCR process have been realized simultaneously, improved denitration efficiency with SNCR reacting phase ratio, compare under the situation that guarantees denitration efficiency with the SCR reacting phase, reduce the thickness of beds, thereby reduced cost.
Claims (13)
1. denitrating flue gas equipment, this equipment comprises flue (1) and is arranged on the interior denitrfying agent feedway (2) of flue (1), economizer (3) and beds (4), flow direction along flue gas, described denitrfying agent feedway (2), economizer (3) and beds (4) are successively set in the described flue (1), it is characterized in that, described flue (1) comprises first vertical section (5), second vertical section (6) and horizontal segment (7), the two ends of described horizontal segment (7) are communicated with the top of first vertical section (5) and second vertical section (6) respectively, described denitrfying agent feedway (2) is positioned at first vertical section (5), economizer (3) and beds (4) are positioned at second vertical section (6), described economizer (3) comprises heat exchanger tube (8) and a plurality of heat exchanger fin (9), described heat exchanger tube (8) passes described heat exchanger fin (9), and the outer wall of heat exchanger tube (8) closely contacts with heat exchanger fin (9).
2. denitrating flue gas equipment according to claim 1, it is characterized in that, each heat exchanger fin (9) comprises a plurality of plate bodys, this plate body have in groove and adjacent two plate bodys groove toward each other, the space that the shape of formation and heat exchanger tube (8) adapts, described heat exchanger tube (8) passes this space and closely contacts with heat exchanger fin (9).
3. denitrating flue gas equipment according to claim 1 and 2, it is characterized in that, described a plurality of heat exchanger fin (9) is arranged in parallel, and described heat exchanger tube (8) repeatedly passes a plurality of heat exchanger fins that are arranged in parallel (9) successively toward ground return, forms the parallel multirow and the heat exchanger tube array of multiple row.
4. denitrating flue gas equipment according to claim 3 is characterized in that, two adjacent in parallel multirow or the multiple row heat exchanger tube (8) distances capable or two row heat exchanger tubes (8) are 5-25 centimetre.
5. denitrating flue gas equipment according to claim 1 and 2, it is characterized in that described a plurality of heat exchanger fins (9) are arranged in parallel, described heat exchanger tube (8) is a plurality of, a plurality of heat exchanger tubes (8) pass a plurality of heat exchanger fins that are arranged in parallel (9) successively, form the parallel multirow and the heat exchanger tube array of multiple row.
6. denitrating flue gas equipment according to claim 5 is characterized in that, two adjacent in parallel multirow or the multiple row heat exchanger tube (8) distances capable or two row heat exchanger tubes (8) are 5-25 centimetre.
7. denitrating flue gas equipment according to claim 1 and 2 is characterized in that, the gross thickness of a plurality of heat exchanger fins that are arranged in parallel (9) is the 10-20% of single file or single-row heat exchanger tube (8) length.
8. denitrating flue gas equipment according to claim 7, it is characterized in that, the distance of adjacent two heat exchanger fins (9) is 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (9), and the thickness of each heat exchanger fin (9) is 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (9).
9. denitrating flue gas equipment according to claim 1 and 2 is characterized in that, the total sectional area that passes the heat exchanger tube (8) of each described heat exchanger fin (9) accounts for the 10-50% of this heat exchanger fin (9) single face area.
10. denitrating flue gas equipment according to claim 9 is characterized in that, the sectional area of each heat exchanger tube (8) is the 10-100 square centimeter.
11. denitrating flue gas equipment according to claim 1 is characterized in that, denitrfying agent feedway (2) to the top of the distance A of the bottom of first vertical section (5) and first vertical section (5) to the bottom apart from satisfying A: B=10-25 between the B: 30.
12. denitrating flue gas equipment according to claim 1, it is characterized in that, described denitrfying agent feedway (2) is a pipeline, this pipeline passes the wall of flue (1), stretch in the flue (1), stretch on the pipeline in the flue (1) and be formed with opening, described pipeline is a plurality of, and the opening on every pipeline that stretches in the flue (1) is a plurality of.
13. denitrating flue gas equipment according to claim 12, it is characterized in that, described a plurality of pipeline is along the axial or circumferential array of flue (1), a plurality of openings on every pipeline that stretches in the flue (1) are along the axial distribution of described pipeline, and the direction of described opening is opposite with the direction of flow of flue gas in the flue (1).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202599378U CN201807305U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020209790 | 2010-05-21 | ||
| CN201020209790.1 | 2010-05-21 | ||
| CN2010202599378U CN201807305U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201807305U true CN201807305U (en) | 2011-04-27 |
Family
ID=43890257
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202599378U Expired - Lifetime CN201807305U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201807305U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111151131A (en) * | 2020-02-28 | 2020-05-15 | 中国华能集团清洁能源技术研究院有限公司 | Normal-temperature SCR denitration device and process for improving denitration efficiency of boiler |
-
2010
- 2010-07-13 CN CN2010202599378U patent/CN201807305U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111151131A (en) * | 2020-02-28 | 2020-05-15 | 中国华能集团清洁能源技术研究院有限公司 | Normal-temperature SCR denitration device and process for improving denitration efficiency of boiler |
| CN111151131B (en) * | 2020-02-28 | 2024-01-30 | 中国华能集团清洁能源技术研究院有限公司 | Normal-temperature SCR denitration device and technology for improving denitration efficiency of boiler |
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| Date | Code | Title | Description |
|---|---|---|---|
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