CN214051160U - Device for CO-processing CO and NOx - Google Patents
Device for CO-processing CO and NOx Download PDFInfo
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- CN214051160U CN214051160U CN202022850867.XU CN202022850867U CN214051160U CN 214051160 U CN214051160 U CN 214051160U CN 202022850867 U CN202022850867 U CN 202022850867U CN 214051160 U CN214051160 U CN 214051160U
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Abstract
The utility model discloses a device of coprocessing CO and NOx, include: the system comprises a boiler, a flue from the tail of the boiler to an inlet of an SCR reactor, a CO oxidation catalyst, a nitrogen-air mixer and an SCR management and control system, wherein the input end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the tail of the boiler, the output end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the inlet of the SCR reactor, the nitrogen-air mixer is connected with the flue in the front of the SCR reactor, so that an air source required for oxidizing CO into CO2 enters the SCR reactor through the ammonia-air mixer, the CO oxidation catalyst is arranged behind the outlet of the tail of the boiler, and the SCR management and control system is respectively connected with the inlet section and the outlet section of the CO oxidation catalyst so as to monitor the CO amount of. The utility model provides the high flue gas temperature who gets into the SCR reactor has solved start-up, the problem that low-load stage stopped spouting the ammonia, has enlarged the SCR denitration operation interval.
Description
Technical Field
The utility model relates to a flue gas SCR denitration technical field of thermal power factory especially relates to a device of coprocessing CO and NOx in coordination.
Background
In the field of thermal power coal burning, there are three main methods for coal burning NOx control: firstly, denitration of fuel; improving the combustion mode and the production process, and denitrating in the combustion; and thirdly, flue gas denitration, namely a technology for controlling NOx after combustion. Wherein the fuel denitration degree of difficulty is big, and the cost is very high, is difficult to realize in practical application. Therefore, the NOx removal rate is improved by combining an improved combustion mode with flue gas denitration so as to meet the environmental emission standard. The low NOx burner can meet the requirements of fuel ignition and combustion, can inhibit NOx generation to the maximum extent, and plays an important role in denitration during combustion. And secondly, a NOx denitration technology after combustion, which mainly comprises a Selective Catalytic Reduction (SCR) technology and a selective non-catalytic reduction (SNCR) technology, wherein the SCR technology is the most widely applied flue gas denitration technology with the most mature technology at present, and because of the use of the catalyst, a reducing agent (ammonia) is sprayed into a flue to be fully mixed with the flue gas at a lower temperature, so that NOx in the flue gas is reduced into N2 and water.
However, the prior SCR denitration catalyst needs to have enough activity under medium-high temperature (280-420 ℃) to obtain better denitration effect. However, the operation of the thermal power generating unit cannot meet the optimal denitration efficiency at any time, for example, the temperature of the SCR catalyst cannot reach the optimal operation activity of the SCR catalyst in the startup stage and the low-load operation stage, and ammonia injection needs to be stopped at this stage, which causes poor denitration efficiency and denitration time delay. Meanwhile, in the low-load and start-up stages, the content of CO in the boiler is high due to insufficient combustion, so that considerable content of unburned CO enters flue gas, and the atmospheric environment is not affected. In addition, the CO emission concentration of the boiler is 1000-5000 ppm, and the high CO content in the flue gas can be caused by an anoxic environment, so that the heat efficiency of the boiler is reduced.
In recent years, with the rapid development of new energy technology, domestic coal-fired units are saturated, a large number of units are required to be operated in a peak shaving mode frequently, and the low-load operation state is more, so that the effective operation of the SCR catalyst can be ensured and the CO emission can be reduced under the condition, and the method becomes a subject worth being researched in the denitration industry.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information constitutes prior art already known to a person skilled in the art.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a coprocessing device of CO and NOx, it can solve prior art's above-mentioned problem.
To achieve the above object, the present invention provides an apparatus for CO-processing CO and NOx, comprising: the system comprises a boiler, a flue from the tail of the boiler to an inlet of an SCR reactor, a CO oxidation catalyst, a nitrogen-air mixer and an SCR management and control system, wherein the input end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the tail of the boiler, the output end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the inlet of the SCR reactor, the nitrogen-air mixer is connected with the flue in the front of the SCR reactor, so that an air source required for oxidizing CO into CO2 enters the SCR reactor through the nitrogen-air mixer, the CO oxidation catalyst is arranged behind the outlet of the tail of the boiler, and the SCR management and control system is respectively connected with the inlet section and the outlet section of the CO oxidation catalyst so as to monitor the CO amount of the inlet section and the outlet section of the CO oxidation catalyst.
In one or more embodiments, the CO oxidation catalyst is connected in series between the boiler tail and the inlet flue of the SCR reactor and in front of the SCR reactor, and the SCR management and control system is a CO oxidation catalyst full-life-cycle management system, and the CO oxidation catalyst full-life-cycle management systems are respectively connected to monitoring points in the flues on both sides of the CO oxidation catalyst.
In one or more embodiments, the CO oxidation catalyst is disposed above the SCR catalyst in the SCR reactor and is connected to the SCR catalyst into a whole, the SCR management and control system is a CO oxidation catalyst full-life-cycle management system, and the CO oxidation catalyst full-life-cycle management system is respectively connected to a tail monitoring point from a boiler tail to an inlet flue of the SCR reactor and a monitoring point at a bottom output end of the SCR reactor.
In one or more embodiments, the boiler is a low NOx burner boiler.
In one or more embodiments, the CO oxidation catalyst and the SCR catalyst are disposed in an upper middle portion of the SCR reactor.
In one or more embodiments, the SCR reactor employs medium-high temperature SCR denitration technology.
In one or more embodiments, the operating temperature of the SCR reactor ranges from 280 ℃ to 400 ℃.
In one or more embodiments, the pressure drop of the CO oxidation catalyst is < 300 Pa.
In one or more embodiments, the CO oxidation catalyst is used for accelerating the oxidation of CO into CO2, and the temperature of the flue gas after the reaction is increased by 10-20 ℃ through the CO oxidation catalyst.
In one or more embodiments, the nitrogen-air mixer includes an air inlet and a nitrogen inlet, and the air and nitrogen are sufficiently mixed within the nitrogen-air mixer.
Compared with the prior art, the utility model discloses a coprocessing CO and NOx's device has following advantage: (1) the utility model discloses a set up CO oxidation catalyst, utilize the reaction in the process of CO reaction formation CO2 to release heat, improved the flue gas temperature to improve the flue gas temperature who gets into the SCR reactor, solved start, the problem that the low-load stage stops to spout ammonia, enlarged SCR denitration running interval, realize the high-efficient denitration of full operating mode; (2) the utility model can remove over 80% of CO concentration by CO catalyst, improve the thermal efficiency of the boiler, and reduce the pollution of CO emission to the atmospheric environment; (3) the utility model discloses a CO oxidation catalyst can arrange in a flexible way, both can arrange in denitration entry flue, also can arrange and be connected as an organic wholely with former SCR catalyst in the SCR reactor, tears the trade in a flexible way and need not to reform transform, practice thrift the space to current device.
Drawings
Fig. 1 is a block diagram of an apparatus for CO-processing CO and NOx according to an embodiment of the present invention.
Fig. 2 is a block diagram of an apparatus for CO-processing CO and NOx according to another embodiment of the present invention.
Description of the main reference numerals:
the system comprises a boiler 1, a boiler 2, a flue from the tail of the boiler to the inlet of an SCR (selective catalytic reduction) reactor, a CO 3 oxidation catalyst, a SCR 4 management and control system, a nitrogen 5-air mixer, an SCR 6, an SCR catalyst 7, air 8 and nitrogen 9.
Detailed Description
The following detailed description of the present invention is provided in conjunction with the accompanying drawings, but it should be understood that the scope of the present invention is not limited by the following detailed description.
Throughout the specification and claims, unless explicitly stated otherwise, the word "comprise", or variations such as "comprises" or "comprising", will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component.
Example 1:
as shown in fig. 1, the CO-processing apparatus for CO and NOx according to an embodiment of the present invention includes a boiler 1, a boiler tail to SCR reactor inlet flue 2, a CO oxidation catalyst 3, an SCR management and control system 4, a nitrogen-air mixer 5, and an SCR reactor 6. The input end from the tail of the boiler to the inlet flue 2 of the SCR reactor is connected with the tail of the boiler 1, the output end from the tail of the boiler to the inlet flue 2 of the SCR reactor is connected with the inlet of the SCR reactor 6, and the nitrogen-air mixer 5 is connected with the front flue of the SCR reactor, so that the air source required for oxidizing CO into CO2 enters the SCR reactor 6 through the nitrogen-air mixer 5. The CO oxidation catalyst 3 is connected in series between the boiler tail to the SCR reactor inlet flue 2 and before the SCR reactor 6 (ammonia injection device), while the air supply required for CO oxidation to CO2 enters the SCR reactor front flue through the nitrogen air mixer 5. The SCR management and control system 4 is connected to the CO oxidation catalyst inlet section and the CO oxidation catalyst outlet section, respectively, to monitor the CO amount in the CO oxidation catalyst inlet section and the CO amount in the CO oxidation catalyst outlet section, and to determine the effectiveness of the CO oxidation catalyst.
In a preferred embodiment, the SCR management and control system is a CO oxidation catalyst full-life cycle management system, and the CO oxidation catalyst full-life cycle management system is connected to monitoring points in the two side flues of the CO oxidation catalyst respectively. The service life of the CO catalyst is accurately monitored according to the change of CO at the inlet and the outlet of the CO oxidation catalyst, and when the inlet value is close to the outlet value, the CO oxidation oxidant is invalid and the CO oxidation catalyst needs to be replaced in time.
In one or more embodiments, the boiler 1 is a low NOx burner boiler.
In a preferred embodiment, the SCR reactor denitration technology is a medium-high temperature SCR denitration technology in a Selective Catalytic Reduction (SCR) technology, and the operating temperature range of the SCR reactor is 280 to 400 ℃.
In a preferred embodiment, the pressure drop of the CO oxidation catalyst 3 is < 300 Pa.
In a preferred embodiment, the CO oxidation catalyst 3 is used for accelerating the oxidation of CO into CO2, and the temperature of the flue gas after the reaction can be increased by 10-20 ℃ through the CO oxidation catalyst.
In one or more embodiments, the nitrogen-air mixer 5 includes an air inlet and a nitrogen inlet, and the air 8 and nitrogen 9 are sufficiently mixed within the nitrogen-air mixer 5.
Example 2:
as shown in fig. 2, the CO-processing apparatus for CO and NOx according to an embodiment of the present invention includes a boiler 1, a boiler tail to SCR reactor inlet flue 2, a CO oxidation catalyst 3, an SCR management and control system 4, a nitrogen-air mixer 5, and an SCR reactor 6. The input end from the tail of the boiler to the inlet flue 2 of the SCR reactor is connected with the tail of the boiler 1, the output end from the tail of the boiler to the inlet flue 2 of the SCR reactor is connected with the inlet of the SCR reactor 6, and the nitrogen-air mixer 5 is connected with the front flue of the SCR reactor, so that the air source required for oxidizing CO into CO2 enters the SCR reactor 6 through the nitrogen-air mixer 5. The CO oxidation catalyst 3 is disposed in the SCR reactor 6 above the SCR catalyst 7 and is integrally connected to the SCR catalyst 7, while the air supply required for CO oxidation to CO2 enters the SCR reactor 6 through the nitrogen-air mixer 5. The SCR management and control system 4 is a CO oxidation catalyst full-life cycle management system, and the CO oxidation catalyst full-life cycle management system is respectively connected with a tail monitoring point position 10 (monitoring inlet CO amount) from the tail of the boiler to an inlet flue 2 of the SCR reactor and a monitoring point position 11 (monitoring outlet CO amount) of a bottom output end 8 of the SCR reactor 6.
In one or more embodiments, the boiler 1 is a low NOx burner boiler.
In one or more embodiments, the CO oxidation catalyst 3 and the SCR catalyst 7 are disposed in an upper middle portion of the SCR reactor.
In one or more embodiments, the SCR reactor 6 employs medium-high temperature SCR denitration technology. The working temperature range of the SCR reactor is 280-400 ℃.
In one or more embodiments, the pressure drop of the CO oxidation catalyst 3 is < 300 Pa.
In one or more embodiments, the CO oxidation catalyst 5 is used for accelerating the oxidation of CO into CO2, and the temperature of the flue gas after the reaction is increased by 10-20 ℃ by the CO oxidation catalyst.
In one or more embodiments, the nitrogen-air mixer 5 includes an air inlet and a nitrogen inlet, and the air 8 and nitrogen 9 are sufficiently mixed within the nitrogen-air mixer 5.
The utility model discloses a device can solve the denitration in catalyst start-up stage, low-load stage and can not throw the problem, has enlarged SCR denitration operation interval, maintains SCR entry flue-gas temperature and moves in the optimum period of SCR denitration catalyst activity, realizes the high-efficient denitration of full operating mode.
The foregoing descriptions of specific exemplary embodiments of the present invention have been presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents.
Claims (10)
1. An apparatus for CO-processing CO and NOx, the apparatus comprising: the system comprises a boiler, a flue from the tail of the boiler to an inlet of an SCR (selective catalytic reduction) reactor, an SCR reactor, a CO oxidation catalyst, a nitrogen-air mixer and an SCR management and control system, wherein the input end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the tail of the boiler, the output end from the tail of the boiler to the flue from the inlet of the SCR reactor is connected with the inlet of the SCR reactor, and the nitrogen-air mixer is connected with the flue at the front of the SCR reactor so as to oxidize CO into CO2The required air source enters the SCR reactor through the nitrogen-air mixer, the CO oxidation catalyst is arranged behind the outlet of the tail part of the boiler, and the SCR management and control system is respectively connected with the inlet section and the outlet section of the CO oxidation catalyst so as to monitor the CO amount of the inlet section and the outlet section of the CO oxidation catalyst.
2. The apparatus for CO-processing CO and NOx as claimed in claim 1, wherein the CO oxidation catalyst is connected in series between the boiler tail and the inlet flue of the SCR reactor and before the SCR reactor, and the SCR management and control system is a CO oxidation catalyst full-life-cycle management system, and the CO oxidation catalyst full-life-cycle management system is connected with monitoring points in the two side flues of the CO oxidation catalyst respectively.
3. The device for CO-processing and NOx as claimed in claim 1, wherein the CO oxidation catalyst is disposed above the SCR catalyst in the SCR reactor and is connected with the SCR catalyst into a whole, the SCR management and control system is a CO oxidation catalyst full-life-cycle management system, and the CO oxidation catalyst full-life-cycle management system is respectively connected with a tail monitoring point from the tail of the boiler to the inlet flue of the SCR reactor and a monitoring point at the bottom output end of the SCR reactor.
4. An apparatus for CO-processing and NOx as claimed in claim 2 or 3, wherein the boiler is a low NOx burner boiler.
5. The apparatus for CO-processing and NOx as claimed in claim 3, wherein the CO oxidation catalyst and the SCR catalyst are disposed at an upper middle portion of the SCR reactor.
6. The device for CO-processing and NOx as claimed in claim 4, wherein the SCR reactor employs medium-high temperature SCR denitration technology.
7. The device for CO-processing and NOx as claimed in claim 6, wherein the operating temperature of the SCR reactor is in the range of 280-400 ℃.
8. The apparatus for CO-processing of CO and NOx as claimed in claim 1, wherein the CO oxidation catalyst has a pressure drop of < 300 Pa.
9. The apparatus for CO-processing CO and NOx of claim 8, wherein the CO oxidation catalystAgents for accelerating the oxidation of CO to CO2And raising the temperature of the flue gas after reaction by 10-20 ℃ through the CO oxidation catalyst.
10. The apparatus for CO-processing and NOx as claimed in claim 7, wherein the nitrogen-air mixer includes an air inlet and a nitrogen inlet, and air and nitrogen are sufficiently mixed in the nitrogen-air mixer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022850867.XU CN214051160U (en) | 2020-12-02 | 2020-12-02 | Device for CO-processing CO and NOx |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022850867.XU CN214051160U (en) | 2020-12-02 | 2020-12-02 | Device for CO-processing CO and NOx |
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| Publication Number | Publication Date |
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| CN214051160U true CN214051160U (en) | 2021-08-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202022850867.XU Active CN214051160U (en) | 2020-12-02 | 2020-12-02 | Device for CO-processing CO and NOx |
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| CN (1) | CN214051160U (en) |
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Effective date of registration: 20211210 Address after: 100039 room 901, 9 / F, building 1, yard 16, West Fourth Ring Middle Road, Haidian District, Beijing Patentee after: Guoneng Longyuan environmental protection Co.,Ltd. Patentee after: Guoneng Longyuan environmental protection Taizhou Co., Ltd Address before: 100039 room 901, 9 / F, building 1, yard 16, West Fourth Ring Middle Road, Haidian District, Beijing Patentee before: Guoneng Longyuan environmental protection Co.,Ltd. |