CN203002215U - SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite - Google Patents
SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite Download PDFInfo
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- CN203002215U CN203002215U CN 201220732450 CN201220732450U CN203002215U CN 203002215 U CN203002215 U CN 203002215U CN 201220732450 CN201220732450 CN 201220732450 CN 201220732450 U CN201220732450 U CN 201220732450U CN 203002215 U CN203002215 U CN 203002215U
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Abstract
The utility model discloses an SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite. According to the system, flue gas from a furnace hearth firstly passes through a horizontal flue, an economizer and a high-temperature air preheater, is fully mixed with reducing agent i.e. ammonia water injected by an ammonia injection grid, enters an SCR reactor, is subjected to the SCR reaction under the action of catalyst and finally enters a low-temperature air preheater after the reaction. The system disclosed by the utility model has the advantages that during the lignite burning, high-temperature flue gas entering the SCR reactor can be cooled to 320-400 DEG C which is needed by the denitration catalyst by utilizing air, conveyed from a fan to the furnace hearth, in the high-temperature air preheater through adjusting the air flow in an air bypass pipeline, so that the denitration catalyst has no risk of sintering; and the air provided to the furnace hearth by the fan is preheated by the low-temperature air preheater and heated to above 400 DEG C which is required by lignite or lignite blending combustion by high-temperature flue gas in the high-temperature air preheater.
Description
Technical field
The utility model relates to SCR flue gas denitrification system after a kind of boiler of mixing burning for brown coal or brown coal, specifically, relate to a kind of employing low temperature and high temperature two-stage air preheater, the SCR reactor is arranged between the two-stage air preheater, guarantee when the burning brown coal, in the SCR reactor, flue-gas temperature satisfies the reactivity temperature of denitrating catalyst, avoids the SCR flue gas denitrification system of the sintering risk of denitrating catalyst.
Background technology
The out of stock system of traditional flue gas such as Fig. 2: coal dust generates high-temperature flue gas in burner hearth 1 internal combustion, and high-temperature flue gas passes through horizontal flue 2, economizer 3 successively; SCR reactor 8 is connected with economizer 3 by flue gas access tube 4, arranges successively deflector 5, ammonia-spraying grid 6, static mixer 7 in flue gas access tube 4, and denitrating catalyst 9 is arranged in SCR reactor 8; SCR reactor 8 bottoms are connected with electrostatic precipitator 24 by flue gas efferent duct 23, are provided with air preheater 22 in the flue gas efferent duct 23 between electrostatic precipitator 24 and SCR reactor, gas baffle 19; The air input pipe 20 of described burner hearth 1 is connected through air preheater 22 with blower fan 21; Unload ammonia compressor 15 with the liquefied ammonia step-down and be saved in storage ammonia tank 13, ammonia evaporator 12 will store up the interior ammoniacal liquor evaporation of ammonia tank 13, utilize ammonia fairlead 11 to enter ammonia/air mixer 10; Pressure fan 16 is connected with ammonia/air mixer 10 by air efferent duct 17; Ammonia/air mixer 10 is connected with ammonia-spraying grid 6.The nozzle of ammonia-spraying grid 7 is consistent with the flow of flue gas direction; In the SCR reactor, NO in flue gas
xWith the ammonia of ammonia-spraying grid ejection under the effect of catalyst, selective catalytic reduction reaction occurs, NO
xBe reduced into N
2And H
2O。After after purifying, flue gas enters air preheater 22, electrostatic precipitator 24, FGD desulphurization plant 26 successively, by smoke stack emission.
In traditional SCR denitrating technique, due to the active reaction temperature of denitrating catalyst at 320-400 ℃, and brown coal or when mixing burning brown coal, because brown coal moisture is higher, need to use the temperature of air preheater outlet air to reach more than 400 ℃, and denitrating catalyst is arranged between air preheater and economizer, and the flue-gas temperature that this moment should the interval can be over 400 ℃.High like this flue-gas temperature is not suitable for denitrating catalyst; usually can cause the denitrating catalyst sintering; make the denitrating catalyst active part or completely lose; so carry out the SCR denitrating flue gas at the boiler of mixing burning brown coal or burning brown coal; if according to traditional SCR denitrating technique; between economizer and air preheater, denitrating catalyst has very high sintering risk with the SCR catalyst arrangement.
Therefore, how to solve when the boiler of mixing burning brown coal or burning brown coal carries out the SCR denitrating flue gas, guarantee that flue-gas temperature satisfies the reactivity temperature of denitrating catalyst, prevent that the sintering of denitrating catalyst from just seeming quite important.
Summary of the invention
The purpose that the utility model proposes is for the deficiencies in the prior art, and a kind of SCR flue gas denitrification system for the burning brown coal is provided.
The purpose of this utility model is achieved through the following technical solutions: a kind of SCR flue gas denitrification system for the burning brown coal, and it comprises: flue gas access tube, deflector, ammonia-spraying grid, static mixer, SCR reactor, ammonia/air mixer, ammonia evaporator, storage ammonia tank, unload ammonia compressor, pressure fan, slag-blowing equipmemt, gas baffle, hot air duct, blower fan, air preheater, electrostatic precipitator, air-introduced machine, high-temperature air preheater, bypass air pipeline, air register; Wherein, described furnace outlet is connected with economizer with horizontal flue successively.The entrance of SCR reactor is connected with economizer by the flue gas access tube, arranges successively deflector, high-temperature air preheater, ammonia-spraying grid, static mixer in the flue gas access tube; Described SCR reactor lower part is connected with electrostatic precipitator by the flue gas efferent duct, and electrostatic precipitator is connected by the flue gas efferent duct with the outlet of SCR reactor, arranges successively gas baffle and air preheater in the flue gas efferent duct; Blower fan is connected with burner hearth by the air duct of air preheater, the air duct of high-temperature air preheater successively; Draw the bypass air pipeline after air preheater, walk around high-temperature air preheater, directly be connected with burner hearth; In the bypass air pipeline, air register is set; Unload ammonia compressor and be connected with the entrance of storage ammonia tank, ammonia evaporator is connected with storage ammonia tank, is used for ammoniacal liquor in evaporation storage ammonia tank; The outlet of storage ammonia tank is connected with the ammonia entrance of ammonia/air mixer by the ammonia fairlead; Pressure fan is connected with the air intake of ammonia/air mixer by the air efferent duct; The outlet of ammonia/air mixer is connected with the nozzle of ammonia-spraying grid, and the nozzle of ammonia-spraying grid is consistent with the flow of flue gas direction; Electrostatic precipitator is connected with air-introduced machine.
The beneficial effects of the utility model are, the utility model adopts high temperature and low temperature two-stage air preheater, denitration device is arranged between the two-stage air preheater, by increasing the air bypass pipeline, by changing the air register aperture, suitably regulate entering the SCR temperature of reactor.When flue-gas temperature is too high, reduce the air register aperture, reduce air mass flow in the bypass air pipeline, increase the heat exchange between air and flue gas, fully reduce flue-gas temperature; During near the required active reaction temperature of denitrating catalyst, improve the air register aperture when flue-gas temperature, suitably increase air mass flow in the bypass air pipeline, reduce the heat exchange between air and flue gas, suitably reduce flue-gas temperature.Guarantee that the flue-gas temperature that enters the SCR reactor can satisfy the active reaction temperature of the required 320-400 of denitrating catalyst ℃, reduce the risk of denitrating catalyst sintering.Simultaneously, guarantee through after high-temperature air preheater heating, the air themperature that enters burner hearth reaches brown coal or brown coal and mixes and burn necessary temperature range more than 400 ℃.
Description of drawings
Fig. 1 is the utility model be used to burn structural representation of SCR flue gas denitrification system of brown coal;
Fig. 2 is the structural representation of traditional SCR flue gas denitrification system;
in figure: burner hearth 1, horizontal flue 2, economizer 3, flue gas access tube 4, deflector 5, ammonia-spraying grid 6, static mixer 7, SCR reactor 8, catalyst 9, ammonia/air mixer 10, ammonia fairlead 11, ammonia evaporator 12, storage ammonia tank 13, liquefied ammonia tank vehicle 14, unload ammonia compressor 15, pressure fan 16, air efferent duct 17, slag-blowing equipmemt 18, gas baffle 19, hot air duct 20, blower fan 21, air preheater 22, flue gas efferent duct 23, electrostatic precipitator 24, air-introduced machine 25, FGD desulphurization plant 26, high-temperature air preheater 27, bypass air pipeline 28, air register 29.
The specific embodiment
Below in conjunction with accompanying drawing, the utility model is further described, it is more obvious that the purpose of this utility model and effect will become.
As shown in Figure 1, the utility model SCR flue gas denitrification system of being used for the burning brown coal comprises: flue gas access tube 4, deflector 5, ammonia-spraying grid 6, static mixer 7, SCR reactor 8, ammonia/air mixer 10, ammonia evaporator 12, storage ammonia tank 13, unload ammonia compressor 15, pressure fan 16, slag-blowing equipmemt 18, gas baffle 19, hot air duct 20, blower fan 21, air preheater 22, electrostatic precipitator 24, air-introduced machine 25, high-temperature air preheater 27, bypass air pipeline 28 and air register 29.
Burner hearth 1 exports to be connected with economizer with horizontal flue 2 successively and is connected.The entrance of SCR reactor 8 is connected with economizer 3 by flue gas access tube 4, arranges successively deflector 5, high-temperature air preheater 27, ammonia-spraying grid 6, static mixer 7 in flue gas access tube 4; Described SCR reactor 8 bottoms are connected with electrostatic precipitator 24 by flue gas efferent duct 23, and electrostatic precipitator 24 is connected by flue gas efferent duct 23 with the outlet of SCR reactor 8, arranges successively gas baffle 19 and air preheater 22 in flue gas efferent duct 23; Blower fan 21 is connected with burner hearth 1 by the air duct of air preheater 22, the air duct of high-temperature air preheater 27 successively; Draw bypass air pipeline 28 after air preheater 22, walk around high-temperature air preheater 27, directly be connected with burner hearth 1; Air register 29 is set in bypass air pipeline 28; Unload ammonia compressor 15 and be connected with the entrance of storage ammonia tank 13, ammonia evaporator 12 is connected with storage ammonia tank 13, is used for evaporation storage ammonia tank 13 interior ammoniacal liquor; The outlet of storage ammonia tank 13 is connected with the ammonia entrance of ammonia/air mixer 10 by ammonia fairlead 11; Pressure fan 16 is connected with the air intake of ammonia/air mixer 10 by air efferent duct 17; The outlet of ammonia/air mixer 10 is connected with the nozzle of ammonia-spraying grid 6, and the nozzle of ammonia-spraying grid 6 is consistent with the flow of flue gas direction; Electrostatic precipitator 24 is connected with air-introduced machine 25.
The course of work of the present utility model is as follows: after boiler operatiopn, burner hearth 1 produces high-temperature flue gas and enters static mixer 7 by horizontal flue 2, economizer 3, high-temperature air preheater 27, ammonia-spraying grid 6 successively; After the ammonia steam that ammonia evaporator 13 produces entered ammonia/air mixer 10, the air of sending here with pressure fan 16 mixed, and forms certain density ammonia, and is sprayed in flue gas by ammonia-spraying grid 6; High-temperature flue gas and ammonia enter SCR reactor 8 after mixing in static mixer 7; In SCR reactor 8, NO in flue gas
xWith the ammonia of ammonia-spraying grid 6 ejections under the effect of catalyst 9, selective catalytic reduction reaction occurs, NO
xBe reduced into N
2And H
2O。After purifying, flue gas enters low-temperature air preheater 22, electrostatic precipitator 24 successively, then sends into follow-up FGD desulphurization plant 26 by air-introduced machine 25 and carry out the desulfurization processing, goes out by smoke stack emission at last.In SCR reactor 8, high-temperature flue gas is undertaken cooling by the air that blower fan 21 is delivered to burner hearth 1 in high-temperature air preheater 27.When flue-gas temperature is too high, by reducing air register 29 apertures, reduce bypass air pipeline 28 interior air mass flows, increase the heat exchange between air and flue gas, fully reduce flue-gas temperature; During near the required active reaction temperature of denitrating catalyst, by increasing air register 29 apertures, suitably increase the interior air mass flow of bypass air pipeline 28 when flue-gas temperature, reduce the heat exchange between air and flue gas, suitably reduce flue-gas temperature.By the adjusting to air register 29, after guaranteeing that high-temperature flue gas is cooling through air, reach the required 320-400 of denitrating catalyst ℃ (as 350 ℃), this moment, denitrating catalyst was without the risk of sintering.And the air that blower fan 21 offers burner hearth 1 is by after air preheater 22 preheatings of low temperature, then is heated to brown coal or brown coal by high-temperature flue gas mixes and burn necessary temperature range more than 400 ℃ in high-temperature air preheater 27.
Claims (1)
1. SCR flue gas denitrification system that is used for the burning brown coal, burner hearth (1) outlet is connected 3 with horizontal flue (2) with economizer successively) be connected; It is characterized in that, it comprises: flue gas access tube (4), deflector (5), ammonia-spraying grid (6), static mixer (7), SCR reactor (8), ammonia/air mixer (10), ammonia evaporator (12), storage ammonia tank (13), unload ammonia compressor (15), pressure fan (16), slag-blowing equipmemt (18), gas baffle (19), hot air duct (20), blower fan (21), air preheater (22), electrostatic precipitator (24), air-introduced machine (25), high-temperature air preheater (27) and bypass air pipeline (28); Wherein the entrance of SCR reactor (8) is connected with economizer (3) by flue gas access tube (4), arranges successively deflector (5), high-temperature air preheater (27), ammonia-spraying grid (6), static mixer (7) in flue gas access tube (4); Described SCR reactor (8) bottom is connected with electrostatic precipitator (24) by flue gas efferent duct (23), arranges successively gas baffle (19) and air preheater (22) in flue gas efferent duct (23); Blower fan (21) is connected with burner hearth (1) by the air duct of air preheater (22), the air duct of high-temperature air preheater (27) successively; Air preheater (22) directly is connected with burner hearth (1) by bypass air pipeline (28), and air register (29) is set in bypass air pipeline (28); Unload ammonia compressor (15) and be connected with the entrance of storage ammonia tank (13), ammonia evaporator (12) is connected with storage ammonia tank (13), is used for the interior ammoniacal liquor of evaporation storage ammonia tank (13); The outlet of storage ammonia tank (13) is connected with the ammonia entrance of ammonia/air mixer (10) by ammonia fairlead (11); Pressure fan (16) is connected with the air intake of ammonia/air mixer (10) by air efferent duct (17); The outlet of ammonia/air mixer (10) is connected with the nozzle of ammonia-spraying grid (6), and the nozzle of ammonia-spraying grid (6) is consistent with the flow of flue gas direction; Electrostatic precipitator (24) is connected with air-introduced machine (25).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220732450 CN203002215U (en) | 2012-12-27 | 2012-12-27 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220732450 CN203002215U (en) | 2012-12-27 | 2012-12-27 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
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| CN203002215U true CN203002215U (en) | 2013-06-19 |
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| CN 201220732450 Withdrawn - After Issue CN203002215U (en) | 2012-12-27 | 2012-12-27 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103041703A (en) * | 2012-12-27 | 2013-04-17 | 浙江信耳科技有限公司 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
| CN103486566A (en) * | 2013-09-17 | 2014-01-01 | 西安西热锅炉环保工程有限公司 | Waste heat utilization system capable of guaranteeing lignite boiler dry output and SCR safe flue gas temperature |
| CN103822220A (en) * | 2014-02-26 | 2014-05-28 | 章礼道 | Hot air heating system shared by electric precipitator ash hopper and selective catalytic reduction (SCR) |
| CN104307322A (en) * | 2014-10-16 | 2015-01-28 | 无锡雪浪环境科技股份有限公司 | Flue gas cleaning system for preventing NOx and dioxin from reflowing and method thereof |
| CN110856800A (en) * | 2018-08-22 | 2020-03-03 | 江苏凯亚环保科技有限公司 | High-temperature denitration system for selective catalytic reduction |
-
2012
- 2012-12-27 CN CN 201220732450 patent/CN203002215U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103041703A (en) * | 2012-12-27 | 2013-04-17 | 浙江信耳科技有限公司 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
| CN103041703B (en) * | 2012-12-27 | 2014-12-10 | 杭州玺清环保科技有限公司 | SCR (Selective Catalytic Reduction) flue gas denitration system for burning lignite |
| CN103486566A (en) * | 2013-09-17 | 2014-01-01 | 西安西热锅炉环保工程有限公司 | Waste heat utilization system capable of guaranteeing lignite boiler dry output and SCR safe flue gas temperature |
| CN103822220A (en) * | 2014-02-26 | 2014-05-28 | 章礼道 | Hot air heating system shared by electric precipitator ash hopper and selective catalytic reduction (SCR) |
| CN104307322A (en) * | 2014-10-16 | 2015-01-28 | 无锡雪浪环境科技股份有限公司 | Flue gas cleaning system for preventing NOx and dioxin from reflowing and method thereof |
| CN110856800A (en) * | 2018-08-22 | 2020-03-03 | 江苏凯亚环保科技有限公司 | High-temperature denitration system for selective catalytic reduction |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: HANGZHOU SEEKING ENVIRONMENTAL PROTECTION TECHONLO Free format text: FORMER OWNER: ZHEJIANG XINER SCIENCE + TECHNOLOGY CO., LTD. Effective date: 20140129 |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 310014 HANGZHOU, ZHEJIANG PROVINCE TO: 310012 HANGZHOU, ZHEJIANG PROVINCE |
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| TR01 | Transfer of patent right |
Effective date of registration: 20140129 Address after: 310012, room 1506, C, Zijin Plaza, 701 Pier Road, Hangzhou, Zhejiang, Xihu District Patentee after: Hangzhou Seeking Environmental Protection Techonlogy Co., Ltd. Address before: 310014 room 2, 1606 New Youth Plaza, Hangzhou, Zhejiang, Gongshu District Patentee before: Zhejiang Xiner Technology Co., Ltd. |
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| TR01 | Transfer of patent right | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20130619 Effective date of abandoning: 20141210 |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20130619 Effective date of abandoning: 20141210 |
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| RGAV | Abandon patent right to avoid regrant |