CN201807301U - Smoke denitration equipment - Google Patents
Smoke denitration equipment Download PDFInfo
- Publication number
- CN201807301U CN201807301U CN2010202597090U CN201020259709U CN201807301U CN 201807301 U CN201807301 U CN 201807301U CN 2010202597090 U CN2010202597090 U CN 2010202597090U CN 201020259709 U CN201020259709 U CN 201020259709U CN 201807301 U CN201807301 U CN 201807301U
- Authority
- CN
- 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
- 239000000779 smoke Substances 0.000 title abstract 3
- 230000003197 catalytic effect Effects 0.000 claims abstract description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 55
- 239000003546 flue gas Substances 0.000 claims description 55
- 239000003795 chemical substances by application Substances 0.000 claims description 26
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 11
- 230000006378 damage Effects 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract 2
- 238000010438 heat treatment Methods 0.000 abstract 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 5
- 229910010413 TiO 2 Inorganic materials 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 241000264877 Hippospongia communis Species 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- 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
- 238000001816 cooling Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000007599 discharging Methods 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
- 239000000203 mixture Substances 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000006722 reduction reaction Methods 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
- 239000000126 substance 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 smoke denitration equipment. A novel coal economizer including a heat exchange pipe and a plurality of heat exchange plates is used in the smoke denitration equipment, wherein the heat exchange pipe passes through the heat exchange plates, and the outer wall of the heat exchange pipe is in close contact with the heat exchange plates, so the volume of the coal economizer is reduced while heat exchange efficiency is ensured, and the volume of a flue can be reduced as much as possible; and on the other hand, a header is positioned at the upper part of a catalytic reactor, so that damage to a catalyst bed layer due to non-uniform heating or uneven position can be prevented.
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).
One of gas denitrifying technology of utilization comparative maturity is SCR (SCR) technology at present, the chemical principle of SCR denitrating technique is: under the condition that catalyst exists, in flue gas, spray into denitrfying agent (urea or ammonia), in specific temperature range with flue gas in NO
xCarry out the selective reduction reaction and generate nitrogen (N
2) and steam (H
2O).Because the temperature of SCR denitration is 280-420 ℃, and the temperature of flue gas is generally more than 800 ℃ even 1000 ℃, in order to realize the cooling of flue gas, common way is to set up an economizer (being heat exchanger) before beds at present, and economizer is formed by a plurality of heat exchanger tubes that are connected in series mutually.In order to guarantee that the flue gas after the heat exchange can satisfy the requirement that SCR reacts, the number of heat exchanger tube is very huge, thereby the volume of economizer is very huge.
In order effectively to utilize the high heat of flue gas, flue is surrounded by a plurality of metal tubes (also claiming bag wall superheater) of interior dress demineralized water usually, and the high heat in the flue gas passes to demineralized water in the metal tube by transfer modes such as radiation, thereby obtains superheated steam.A plurality of metal tubes come together in the collection case of bag wall superheater, and beds is usually located at the bottom of flue afterbody and collection case.This setup can cause the beds out-of-flatness on the one hand, on the other hand, also can cause beds inconsistent, thereby whole reaction bed temperature skewness damage easily to beds with collection box foundation position and other position temperature.
The utility model content
The purpose of this utility model is in order to overcome the shortcoming that economizer is bulky and beds destroys easily that existing denitrating flue gas equipment exists, and provides a kind of economizer volume little and be not easy to cause the ruined denitrating flue gas equipment of beds.
The utility model provides a kind of denitrating flue gas equipment, this equipment comprises the flue that is surrounded by bag wall superheater, flow direction along flue gas, be disposed with denitrfying agent feedway and economizer in the flue, wherein, described flue comprises first vertical section, second vertical section and horizontal segment, and the two ends of described horizontal segment are communicated with the top of first vertical section and second vertical section respectively, economizer is positioned at second vertical section, and the collection case of bag wall superheater is positioned at the bottom of second vertical section; This equipment also comprises catalytic reactor, and this catalytic reactor is communicated with the bottom of second vertical section, and described economizer comprises heat exchanger tube and a plurality of heat exchanger fin, and 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), when guaranteeing heat exchange efficiency, reduced the shared volume of economizer, on the other hand, be positioned at the top of described catalytic reactor, can prevent the destruction that beds causes because of be heated inequality or position out-of-flatness beds by making the collection case.
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 is the structural representation of the heat exchanger fin of economizer in the denitrating flue gas equipment in the another kind of embodiment of the present utility model.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is described in detail.
As shown in Figure 1, the denitrating flue gas equipment that the utility model provides comprises the flue 1 that is surrounded by bag wall superheater 8, flow direction along flue gas, be disposed with denitrfying agent feedway 2 and economizer 3 in the 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, economizer 3 is positioned at second vertical section 6, and the collection case 9 of bag wall superheater 8 is positioned at the bottom of second vertical section 6; This equipment also comprises catalytic reactor 10, this catalytic reactor 10 is communicated with the bottom of second vertical section 6, described economizer 3 comprises heat exchanger tube 11 and a plurality of heat exchanger fin 12, and described heat exchanger tube 11 passes described heat exchanger fin 12, and the outer wall of heat exchanger tube 11 closely contacts with heat exchanger fin 12.
Described catalytic reactor 10 can be the various selective-catalytic-reduction denitrified reactors of flue gas that can be used in, specifically can select according to the form of catalyst, for example, described catalytic reactor 10 can have the tank reactor in hole or slit for the bottom, and the sidewall of tank reactor is connected with the bottom sidewall of second vertical section 6 of flue 1.
According to the denitrating flue gas equipment that the utility model provides, in the described catalytic reactor 10 beds 4 can also be housed, the thickness of described beds 4 can in very large range change, and is preferably 1.5-2.0 rice.
Wherein said 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
2Preferred described beds 4 is with 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..
As shown in Figure 2, in a kind of preferred implementation, described a plurality of heat exchanger fins 12 are arranged in parallel, and more than 11 past ground return of described heat exchanger tube passes a plurality of heat exchanger fins that are arranged in parallel 12 successively, forms the parallel multirow and the heat exchanger tube array of multiple row.
In another kind of preferred implementation, described a plurality of heat exchanger fins 12 are arranged in parallel, and described heat exchanger tube 11 is a plurality of, and a plurality of heat exchanger tubes 11 pass a plurality of heat exchanger fins that are arranged in parallel 12 successively, form 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 11 on the described heat exchanger fin 12.
As shown in Figure 4, in another embodiment, each heat exchanger fin 12 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 11 adapts, described heat exchanger tube 11 passes this space and closely contacts with heat exchanger fin 12.
In the utility model, the quantity of heat exchanger fin 12 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 12 can be the 10-20% of single file or single-row heat exchanger tube 11 length, under the preferred situation, the distance of two adjacent heat exchanger fins 12 can be 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 12, and the thickness of each heat exchanger fin 12 can be 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 12.
In the utility model, the size of described heat exchanger fin 12 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 11 of each described heat exchanger fin 12 can account for the 10-50% of these heat exchanger fin 12 single face areas.There is no particular limitation for the size of described heat exchanger tube 11, can select the heat exchanger tube size of various routines for use, and for example, the sectional area of described heat exchanger tube 11 can be the 10-100 square centimeter.
In addition, in described economizer 3, the density that described heat exchanger tube 11 is arranged can in very large range change, and under the preferable case, two adjacent in parallel multirow or the heat exchanger tube of multiple row 11 distances capable or two row heat exchanger tubes 11 can be 5-25 centimetre.
In a kind of preferred implementation of the present utility model, described heat exchanger tube 11 forms integrative-structure with a plurality of heat exchanger fins 12.
In the utility model, the position of denitrfying agent feedway 2 can in very large range be selected, as long as can provide denitrfying agent to realize the selective-catalytic-reduction denitrified of flue gas and to be positioned at economizer 3 before along flue gas flow direction to flue gas.Under the preferable case, the distance A of the bottom of denitrfying agent feedway 2 to first vertical sections 5 and the top of first vertical section 5 to the bottom apart from satisfying A: B=20-28 between the B: 30, more preferably A: B=23-28: 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 are along the axially-aligned of flue 1, 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 °.
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.
In the utility model, described flue 1 is surrounded by bag wall superheater 8, can feed heat exchange medium in the bag wall superheater 8, thereby can make full use of the heat in the flue gas.Under the preferable case, described bag wall superheater 8 for example can be carbon steel pipe, stainless steel tube, copper pipe, titanium pipe or various metal alloy pipes etc.
The using method of denitrating flue gas equipment provided by the utility model comprises, by denitrfying agent feedway 2 denitrfying agent is sent in the flue 1, mix with the flue gas in the flue 1, afterwards with economizer 3 in heat transferring medium carry out heat exchange to the temperature that is fit to the flue gas SCR, carry out catalytic reactor 10, under the selective-catalytic-reduction denitrified condition of flue gas, contact, thereby carry out the flue gas SCR with catalyst in the catalytic reactor 10.
The selective-catalytic-reduction denitrified condition of described flue gas comprises, the condition that described nitrogen oxide is reduced to nitrogen comprises that temperature can be 280-420 ℃, is preferably 300-400 ℃, and the flow velocity of flue gas can be the 4-12 meter per second, be preferably the 5-8 meter per second, NO in the amino of denitrfying agent and the flue gas
xMol ratio (ammonia nitrogen mol ratio) can be 0.5-1.1: 1, be preferably 0.7-1: 1.
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), when guaranteeing heat exchange efficiency, reduced the shared volume of economizer, can make the volume-diminished of flue 1 as best one can, on the other hand, by using the collection case to be positioned at the top of described catalytic reactor, can prevent the destruction that beds causes because of be heated inequality or position out-of-flatness to beds.
Claims (13)
1. denitrating flue gas equipment, this equipment comprises the flue (1) that is surrounded by bag wall superheater (8), flow direction along flue gas, be disposed with denitrfying agent feedway (2) and economizer (3) in the 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, economizer (3) is positioned at second vertical section (6), and the collection case (9) of bag wall superheater (8) is positioned at the bottom of second vertical section (6); This equipment also comprises catalytic reactor (10), this catalytic reactor (10) is communicated with the bottom of second vertical section (6), described economizer (3) comprises heat exchanger tube (11) and a plurality of heat exchanger fin (12), described heat exchanger tube (11) passes described heat exchanger fin (12), and the outer wall of heat exchanger tube (11) closely contacts with heat exchanger fin (12).
2. denitrating flue gas equipment according to claim 1, it is characterized in that, each heat exchanger fin (12) 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 (11) adapts, described heat exchanger tube (11) passes this space and closely contacts with heat exchanger fin (12).
3. denitrating flue gas equipment according to claim 1 and 2, it is characterized in that, described a plurality of heat exchanger fin (12) is arranged in parallel, and described heat exchanger tube (11) repeatedly passes a plurality of heat exchanger fins that are arranged in parallel (12) 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 (11) distances capable or two row heat exchanger tubes (11) 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 fin (12) is arranged in parallel, described heat exchanger tube (11) is a plurality of, a plurality of heat exchanger tubes (11) pass a plurality of heat exchanger fins that are arranged in parallel (12) 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 (11) distances capable or two row heat exchanger tubes (11) 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 (12) is the 10-20% of single file or single-row heat exchanger tube (11) length.
8. denitrating flue gas equipment according to claim 7, it is characterized in that, the distance of adjacent two heat exchanger fins (12) is 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (12), and the thickness of each heat exchanger fin (12) is 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (12).
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 (11) of each described heat exchanger fin (12) accounts for the 10-50% of this heat exchanger fin (12) single face area.
10. denitrating flue gas equipment according to claim 9 is characterized in that, the sectional area of each heat exchanger tube (11) 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=20-28 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, opening on every pipeline that stretches in the flue (1) is a plurality of, described a plurality of pipeline is along the axially-aligned 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).
13. denitrating flue gas equipment according to claim 1 is characterized in that, beds (4) is housed in the described catalytic reactor (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202597090U CN201807301U (en) | 2010-05-21 | 2010-07-13 | Smoke denitration equipment |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020210385 | 2010-05-21 | ||
| CN201020210385.1 | 2010-05-21 | ||
| CN2010202597090U CN201807301U (en) | 2010-05-21 | 2010-07-13 | Smoke denitration equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201807301U true CN201807301U (en) | 2011-04-27 |
Family
ID=43890256
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202599630U Expired - Lifetime CN201807306U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitrification device |
| CN2010202597090U Expired - Lifetime CN201807301U (en) | 2010-05-21 | 2010-07-13 | Smoke denitration equipment |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202599630U Expired - Lifetime CN201807306U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitrification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN201807306U (en) |
-
2010
- 2010-07-13 CN CN2010202599630U patent/CN201807306U/en not_active Expired - Lifetime
- 2010-07-13 CN CN2010202597090U patent/CN201807301U/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN201807306U (en) | 2011-04-27 |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20110427 |
|
| CX01 | Expiry of patent term |