CN205090402U - Denitrification device for smoke gas - Google Patents
Denitrification device for smoke gas Download PDFInfo
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- CN205090402U CN205090402U CN201520798215.2U CN201520798215U CN205090402U CN 205090402 U CN205090402 U CN 205090402U CN 201520798215 U CN201520798215 U CN 201520798215U CN 205090402 U CN205090402 U CN 205090402U
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Abstract
The utility model discloses a denitrification device for smoke gas, this denitrification device for smoke gas is including the economizer and the denitration reactor that connect in order, the economizer links to each other with supply line, be equipped with multistage low pressure feed water heater and multistage high pressure feed water heater among the supply line, denitration reactor's parallelly connected medium temperature economizer and the air heater of being provided with in exit, it gets into the heat absorption of medium temperature economizer to locate to take out partial condensate water by low pressure feed water heater, after mixing, supply line export feedwater gets into the economizer with medium temperature economizer export feedwater, through improving the entry gas temperature that the feedwater temperature that gets into the economizer import improves denitration reactor. The utility model discloses a denitrification device for smoke gas can show improvement SCR entry gas temperature, especially when the power plant boiler load is lower, can guarantee that SCR deNOx systems puts into operation into operation, and the row of messenger gas temperature degree keeps preventing low temperature corrosion more than sour dew point simultaneously.
Description
Technical field
The utility model relates to a kind of flue gas processing device, particularly relates to a kind of flue-gas temperature by improving denitrification apparatus entrance, and then improves the equipment for denitrifying flue gas of its denitration efficiency.
Background technology
The mainstream technology controlling NOx emission in coal fired power plant is SCR denitration technology, the exemplary configurations mode of SCR process system is arranged between economizer and air preheater by SCR reactor, the running temperature of SCR process system generally designs between 300 DEG C-400 DEG C, in this temperature range, catalyst can ensure to run under higher activity; In active temperature interval, SCR process system can obtain good effect, and denitration performance raises along with the rising of flue-gas temperature.
But under flue-gas temperature is lower than catalyst activity temperature range in limited time, catalyst activity is lower, it reduces denitration efficiency on the one hand, on the other hand the escaping of ammonia rate is increased, the oxysulfide reaction generation hydrogen sulfate ammonia in the ammonia of escape and flue gas, easily causes the blocking of air preheater.
Especially, when station boiler load is lower, denitrification apparatus entrance flue gas temperature does not reach the temperature that puts into operation of denitrating system, and denitrating system is forced to out of service, and under promoting underload, the inlet flue gas temperature of SCR denitration device is the key addressed this problem.
Summary of the invention
For solving above-mentioned the problems of the prior art, the utility model provides the equipment for denitrifying flue gas that a kind of structure is simple, denitration efficiency is high.
For achieving the above object, the concrete technical scheme of equipment for denitrifying flue gas of the present utility model is as follows:
A kind of equipment for denitrifying flue gas, comprise the economizer and Benitration reactor that connect in turn, economizer is connected with supply line, multistage low-pressure heater and multistage pressure heater is provided with in supply line, the exit of Benitration reactor has been arranged in parallel middle temperature economizer and air preheater, enter middle temperature economizer by low-pressure heater extraction section condensate water to absorb heat, supply line outlet feedwater and middle temperature economizer exit enter economizer after feeding water and mixing, and improve the inlet flue gas temperature of Benitration reactor by improving the feedwater water temperature entering economizer import.
Further, one end of middle temperature economizer is connected with low-pressure heater, and current enter middle temperature economizer after the heating of at least one-level low-pressure heater.
Further, the other end of middle temperature economizer is connected to the outlet of final stage high-pressure heater, current through with final stage high-pressure heater export feed water mix after enter economizer.
Further, the entrance point of air preheater and middle temperature economizer is provided with controllable register, and controllable register is for distributing the exhaust gas volumn entered in air preheater and middle temperature economizer.
Further, the port of export of air preheater and middle temperature economizer is connected with deduster, to remove pollutant further and to prevent blocking.
Further, one end of air preheater is connected with for carrying out preheating warm-air drier to boiler wind speed adjustment, and boiler wind speed adjustment enters boiler, to improve the temperature of boiler wind speed adjustment further after warm-air drier preheating and air preheater heating.
Equipment for denitrifying flue gas of the present utility model can significantly improve SCR inlet flue gas temperature, especially when station boiler load is lower, can ensure that SCR denitration system puts into operation, make exhaust gas temperature remain on more than acid dew point simultaneously, can prevent cold end corrosion.In addition, it is simple that equipment for denitrifying flue gas of the present utility model has structure, the features such as dependability is good, and temperature rise effect is obvious.
Accompanying drawing explanation
Fig. 1 is the structural representation of equipment for denitrifying flue gas of the present utility model.
Detailed description of the invention
In order to understand the purpose of this utility model, structure and function better, below in conjunction with accompanying drawing, further detailed description is done to a kind of equipment for denitrifying flue gas of the present utility model.
As shown in Figure 1, SCR equipment for denitrifying flue gas of the present utility model comprises the economizer 1 and Benitration reactor 2 that connect in turn, and economizer 1 is connected with supply line, is provided with multistage low-pressure heater and multistage pressure heater in supply line.
The exit of Benitration reactor 2 has been arranged in parallel middle temperature economizer 4 and air preheater 5, enter middle temperature economizer 4 by supply line mesolow heater extraction section condensate water to absorb heat, supply line outlet feedwater and middle temperature economizer 4 export feed water mix after enter economizer 1, the feedwater water temperature entering economizer 1 import by raising improves the inlet flue gas temperature of Benitration reactor 2.More specifically, the utility model enters the feedwater water temperature of economizer 1 by improving, and reduces feedwater to the heat absorption of flue gas in economizer 1, and the heat exchange of minimizing flue gas in economizer 1, improves the inlet flue gas temperature of Benitration reactor 2.
One end of middle temperature economizer 4 is connected with low-pressure heater, and current enter middle temperature economizer 4 after the heating of at least one-level low-pressure heater.Particularly, the water lines entrance point of middle temperature economizer 4 exports with the water lines of low-pressure heater 8 and is connected, the water lines port of export of middle temperature economizer 4 is connected with the outlet supply line of final stage high-pressure heater 13, thus supply line final stage high-pressure heater 13 outlet feedwater and middle temperature economizer 4 export feed water mix after enter economizer 1; Reducing the heat absorption of feedwater at economizer place by improving economizer inlet water temperature, improving the inlet flue gas temperature of Benitration reactor 2.
In the present embodiment, multiple stage heater for convenience of explanation, the approximate number n hereinafter used states the multiple of uncertain quantity.
Described multiple stage heater comprises from the top of supply line successively to end, first order low-pressure heater 8, second level low-pressure heater 9, third level low-pressure heater 10, and the n-th-2 grades high-pressure heaters 11, (n-1)th grade of high-pressure heater 12, n-th grade of high-pressure heater 13 (final stage high-pressure heater); One end of middle temperature economizer 4 is connected to (or between second level low-pressure heater 9 and third level low-pressure heater 10) between first order low-pressure heater 8 and second level low-pressure heater 9, thus current are divided into two-way after first order low-pressure heater 8, wherein road current are successively through second level low-pressure heater 9, third level low-pressure heater 10 etc., until the n-th-2 grades high-pressure heaters 11, (n-1)th grade of high-pressure heater 12, and arrive final stage high-pressure heater 13; Another road part feedwater enters middle temperature economizer 4 and heats, and enters economizer 1 and carry out heat exchange with flue gas after the heating of two-way current.
Further, the import department of air preheater 5 and middle temperature economizer 4 is provided with controllable register 3, controllable register 3 for distributing the exhaust gas volumn entered in air preheater 5 and middle temperature economizer 4, to regulate the exhaust gas volumn entered in middle temperature economizer 4 and air preheater 5.In the present embodiment, controllable register 3 is arranged on the import department of middle temperature economizer 4 and air preheater 5, and controllable register 3 is the baffle plates that can pivot.
Further, the port of export of middle temperature economizer 4 and air preheater 5 is connected with deduster 6, and in passing through, the flue gas of warm economizer 4 and air preheater 5 enters dedusting in deduster 6, to remove pollutant further and to prevent blocking.
In addition, one end of air preheater 5 is also connected with the warm-air drier 7 for carrying out preheating to boiler wind speed adjustment, boiler wind speed adjustment enters boiler again after warm-air drier 7 preheating and air preheater 5 are heated, to improve the temperature of boiler wind speed adjustment further, thus can avoid that boiler wind speed adjustment temperature is lower brings harmful effect to boiler combustion efficiency and heat absorption.Such as, utilize warm-air drier 7 by air heat to about 50 DEG C, make exhaust gas temperature remain on more than acid dew point, can cold end corrosion be prevented.
The workflow of equipment for denitrifying flue gas of the present utility model is as follows:
The flue gas produced in boiler enters economizer 1, flue gas enters SCR denitration reactor 2 and reacts in economizer 1 after heat exchange, reacted flue gas is divided into two-way after controllable register 3 regulates, and a road enters middle temperature economizer 4 with pipeline and carries out heat exchange, and another road enters air preheater 5 with pipeline.Above-mentioned two-way flue gas enters in deduster 6 to remove pollutant further after middle temperature economizer 4 and air preheater 5 heat exchange.
On the other hand, the current after first order low-pressure heater 8 heats are divided into two-way, and wherein road current arrive final stage high-pressure heater 13 successively along hot water line after multiple heater; Another low-pressure heater place, road extraction section feedwater enters middle temperature economizer 4 and heats, and two-way current enter economizer 1 and carry out heat exchange with flue gas after the port of export of final stage high-pressure heater 13 converges.
Thus, when keeping bleeder steam and exerting oneself constant, owing to flowing through the discharge reduction of multiple stage heater, recept the caloric constant, make to export from final stage high-pressure heater 13 water flow temperature flowed out to raise, after another road enters the part feedwater heat absorption in middle temperature economizer 4, temperature raises, and causes mixed water flow temperature to raise, thus make the heat absorption that minimizing is fed water at economizer place, indirectly improve the temperature entering the flue gas of SCR denitration reactor 2.
In actual use, when boiler nominal situation runs, utilize of the present utility model comprise the equipment for denitrifying flue gas of middle temperature economizer 4 after (middle temperature economizer flue gas share is set to about 35%), the inlet flue gas temperature of SCR denitration reactor 2 improves about 24 DEG C, has the effect significantly promoting flue-gas temperature.
By specific embodiment, the utility model is further described above; but it should be understood that; here concrete description; should not be construed as the restriction to essence of the present utility model and scope; one of ordinary skilled in the art to the various amendments that above-described embodiment is made, belongs to the scope that the utility model is protected after reading this specification.
Claims (6)
1. an equipment for denitrifying flue gas, comprise the economizer (1) and Benitration reactor (2) that connect in turn, economizer (1) is connected with supply line, multistage low-pressure heater and multistage pressure heater is provided with in supply line, it is characterized in that, the exit of Benitration reactor (2) has been arranged in parallel middle temperature economizer (4) and air preheater (5), the heat absorption of middle temperature economizer (4) is entered by low-pressure heater extraction section condensate water, supply line outlet feedwater and middle temperature economizer (4) export feed water mix after enter economizer (1), the inlet flue gas temperature of Benitration reactor (2) is improved by improving the feedwater water temperature entering economizer (1) import.
2. equipment for denitrifying flue gas according to claim 1, is characterized in that, one end of middle temperature economizer (4) is connected with low-pressure heater, and current enter middle temperature economizer (4) after the heating of at least one-level low-pressure heater.
3. equipment for denitrifying flue gas according to claim 1, it is characterized in that, the other end of middle temperature economizer (4) is connected to final stage high-pressure heater (13) outlet, current through with final stage high-pressure heater (13) export feed water mix after enter economizer (1).
4. equipment for denitrifying flue gas according to claim 1, it is characterized in that, the entrance point of air preheater (5) and middle temperature economizer (4) is provided with controllable register (3), and controllable register (3) is for distributing the exhaust gas volumn entered in air preheater (5) and middle temperature economizer (4).
5. equipment for denitrifying flue gas according to claim 1, is characterized in that, the port of export of air preheater (5) and middle temperature economizer (4) is connected with deduster (6), to remove pollutant further and to prevent blocking.
6. equipment for denitrifying flue gas according to claim 1, it is characterized in that, one end of air preheater (5) is connected with for carrying out preheating warm-air drier (7) to boiler wind speed adjustment, boiler wind speed adjustment enters boiler, to improve the temperature of boiler wind speed adjustment further after warm-air drier (7) preheating and air preheater (5) heating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520798215.2U CN205090402U (en) | 2015-10-15 | 2015-10-15 | Denitrification device for smoke gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520798215.2U CN205090402U (en) | 2015-10-15 | 2015-10-15 | Denitrification device for smoke gas |
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| CN205090402U true CN205090402U (en) | 2016-03-16 |
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| CN201520798215.2U Active CN205090402U (en) | 2015-10-15 | 2015-10-15 | Denitrification device for smoke gas |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107149873A (en) * | 2017-06-27 | 2017-09-12 | 北京国能中电节能环保技术股份有限公司 | A kind of energy-saving full load denitrating system |
| CN107687634A (en) * | 2017-06-23 | 2018-02-13 | 山东泓奥电力科技有限公司 | The denitration of boiler full load couples fume afterheat gradient utilization system |
| CN110141961A (en) * | 2019-05-22 | 2019-08-20 | 上海电力学院 | A kind of coal-burning boiler full load SCR denitration system |
| CN114904415A (en) * | 2022-06-13 | 2022-08-16 | 宁波市第一医院 | Medicine device is spouted in adjustable drug concentration anesthesia |
-
2015
- 2015-10-15 CN CN201520798215.2U patent/CN205090402U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107687634A (en) * | 2017-06-23 | 2018-02-13 | 山东泓奥电力科技有限公司 | The denitration of boiler full load couples fume afterheat gradient utilization system |
| CN107149873A (en) * | 2017-06-27 | 2017-09-12 | 北京国能中电节能环保技术股份有限公司 | A kind of energy-saving full load denitrating system |
| CN107149873B (en) * | 2017-06-27 | 2023-09-01 | 北京国能中电节能环保技术股份有限公司 | Energy-saving full-load denitration system |
| CN110141961A (en) * | 2019-05-22 | 2019-08-20 | 上海电力学院 | A kind of coal-burning boiler full load SCR denitration system |
| CN114904415A (en) * | 2022-06-13 | 2022-08-16 | 宁波市第一医院 | Medicine device is spouted in adjustable drug concentration anesthesia |
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Address after: 100020, AB, 8 floor, ocean Guanghua International Center, No. 10 Jin Tong West Road, Beijing, Chaoyang District Patentee after: Beijing CPCEP Energy Conservation and Environmental Protection Technology Co., Ltd. Address before: 100020, AB, 8 floor, ocean Guanghua International Center, No. 10 Jin Tong West Road, Beijing, Chaoyang District Patentee before: Beijing Guoneng Zhongdian Energy-Saving Environmental Protection Technology Co., Ltd. |