CN204485652U - A kind of low-temperature denitration reactor - Google Patents
A kind of low-temperature denitration reactor Download PDFInfo
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- CN204485652U CN204485652U CN201520073050.2U CN201520073050U CN204485652U CN 204485652 U CN204485652 U CN 204485652U CN 201520073050 U CN201520073050 U CN 201520073050U CN 204485652 U CN204485652 U CN 204485652U
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Abstract
The utility model relates to a kind of low-temperature denitration reactor, belongs to off-gas cleaning equipment field, to recover the activity of reactor inner catalyst.A kind of low-temperature denitration reactor, comprise reactor, described reactor is connected with air inlet pipe and escape pipe, described air inlet pipe is provided with the primary heater for heating gas in described air inlet pipe, described air inlet pipe is connected with bypass air inlet pipe, described bypass air inlet pipe is provided with secondary heater for heating gas in described bypass air inlet pipe and air blast, and the heated air in described bypass air inlet pipe, under the blowing of described air blast, is entered in described reactor by described air inlet pipe.
Description
Technical field
The utility model relates to a kind of low-temperature denitration reactor, belongs to off-gas cleaning equipment field.
Background technology
The upper clear stipulaties of fossil-fuel power plant atmospheric pollutant emission standard (GB13223-2011) that national environmental protection portion issued in July, 2011: from 1 day July in 2014, the discharged nitrous oxides standard of coal-burning power plant was 100mg/m
3, the emission standards for sulfur dioxide of newly-built coal-burning power plant is 100mg/m
3, the emission standards for sulfur dioxide of existing coal-burning power plant is 200mg/m
3.
For meeting this standard, the boiler smoke pipeline of glass factory, cement plant thermal power plant and garbage burning factory installing desulfurization reactor, and in desulfurization reactor, desulphurization catalyst is installed, to meet fossil-fuel power plant atmospheric pollutant emission standard.Wherein, existing desulfurization reactor mainly designs for middle temperature catalyst denitration, and its serviceability temperature is 320 DEG C-420 DEG C.
Boiler is in low-temperature denitration process, and the temperature in Benitration reactor is lower than 270 DEG C.At this temperature, oxidizing sulfur dioxide is sulfur trioxide by the catalyst in Benitration reactor, sulfur trioxide and ammonia react rapidly and generate ammonium sulfate and ammonium hydrogen sulfate (sulfur trioxide is oxidizing gas, ammonia is reducibility gas, will there is redox reaction in the two), ammonium sulfate and ammonium hydrogen sulfate can cover the micropore place generating catalyst in Benitration reactor, cause rapid catalyst deactivation.
Summary of the invention
Problem to be solved in the utility model is just to provide a kind of low-temperature denitration reactor, to recover the activity of reactor inner catalyst.
For solving the problem, the utility model adopts following technical scheme:
A kind of low-temperature denitration reactor, comprise reactor, described reactor is connected with air inlet pipe and escape pipe, described air inlet pipe is provided with the primary heater for heating gas in described air inlet pipe, described air inlet pipe is connected with bypass air inlet pipe, described bypass air inlet pipe is provided with secondary heater for heating gas in described bypass air inlet pipe and air blast, and the heated air in described bypass air inlet pipe, under the blowing of described air blast, is entered in described reactor by described air inlet pipe.
Further, described bypass air inlet pipe is positioned at the one end connecting described air inlet pipe and is provided with the first deflector.
Further, described air inlet pipe is positioned at the one end connecting described reactor and is provided with the second deflector.
Further, described air inlet pipe is provided with the first switch valve, and described escape pipe is provided with second switch valve.
Further, described bypass air inlet pipe is provided with the 3rd switch valve.
Further, described escape pipe is connected with bypass escape pipe, described bypass escape pipe is provided with emission-control equipment.
Further, described emission-control equipment comprises for the first absorption tower of sulfur dioxide absorption and the second absorption tower for absorbing ammonia.
Further, described bypass escape pipe is provided with the 4th switch valve.
Further, flow straightening grid is provided with in described reactor.
The beneficial effects of the utility model:
In the utility model, after gas in air inlet pipe is heated by primary heater, gas temperature reaches predetermined value, and (described predetermined value is avoid the temperature value of catalysqt deactivation, namely in reactor, the temperature value of gas is greater than 370 DEG C), that is, after primary heater can avoid gas to enter reactor, the catalysqt deactivation in reactor.Secondary heater and air blast are arranged in bypass air inlet pipe, bypass air inlet pipe is connected in air inlet pipe, after gas temperature in bypass heating tube is raised by secondary heater, after heated air in bypass heating tube is blown into air inlet pipe by air blast, and enter in reactor by air inlet pipe, maintain predetermined value with the constant temperature in realization response still.
Accompanying drawing explanation
Fig. 1 is the structural representation of a kind of low-temperature denitration reactor in the utility model.
Detailed description of the invention
With reference to Fig. 1, a kind of low-temperature denitration reactor, comprise reactor 1, reactor 1 is connected with air inlet pipe 2 and escape pipe 5, temperature enters in reactor 1 lower than the gaseous effluent of 280 DEG C by air inlet pipe, and with the catalyst reaction in reactor 1 generate gas (described gas be slough part sulfur dioxide, ammonia after gaseous effluent), ammonium sulfate and ammonium hydrogen sulfate, ammonium sulfate and ammonium hydrogen sulfate can cover the micropore place generating catalyst in reactor 1, thus cause rapid catalyst deactivation.Catalysqt deactivation will cause sulfur dioxide and ammonia cannot continue reaction generation ammonium sulfate and ammonium hydrogen sulfate, for avoiding the generation of catalysqt deactivation situation, air inlet pipe 2 is provided with primary heater 21, temperature can reach 370 DEG C lower than the gaseous effluent of 280 DEG C through primary heater 21 temperature after heating, after the gaseous effluent of 370 DEG C enters reactor 1, ammonium sulfate and ammonium hydrogen sulfate will decomposes.
With reference to Fig. 1, the existence of thermal source is not had in reactor 1, and ammonium sulfate and ammonium hydrogen sulfate can absorb heat in decomposable process, this just means, even if the temperature of gaseous effluent when entering reactor 1 is 370 DEG C, but, after a period of time, the temperature of gaseous effluent can reduce gradually, thus causes ammonium sulfate and ammonium hydrogen sulfate cannot decomposes.For avoiding the generation of this situation, in the present embodiment, air inlet pipe 2 is connected with bypass air inlet pipe 3, bypass air inlet pipe 3 is provided with air blast 31 and secondary heater 32, wherein, secondary heater 32 than air blast 31 closer to bypass air inlet pipe 3 junction with air inlet pipe 2.In air blast 31 and secondary heater 32 course of work, secondary heater 32 is for adding the gas in thermal bypass air inlet pipe 3, air blast 31 is blown in reactor 1 by continual for the gas after heating by air inlet pipe 2, maintains more than 370 DEG C with the gas temperature in realization response still 1.
With reference to Fig. 1, in the present embodiment, air inlet pipe 2 is provided with the first switch valve 23, bypass air inlet pipe 3 is provided with second switch valve 33, escape pipe 5 is provided with the 3rd switch valve 51.
With reference to Fig. 1, the operation principle of reactor in the present embodiment: first, is communicated with the circuit of primary heater 21, opens the valve of the first switch valve 23 and the 3rd switch valve 51 successively, passes in air inlet pipe 2 by temperature lower than the gaseous effluent of 280 DEG C; Then, gaseous effluent heats at primary heater 21 place and makes its temperature more than 370 DEG C, and the gaseous effluent of temperature more than 370 DEG C enters in reactor 1 by air inlet pipe 2; Finally, the catalyst in reactor 1 and gaseous effluent fully react, and reacted gas drains into outside reactor 1 from escape pipe 5.
With reference to Fig. 1, in the reactor course of work, technical staff is by the temperature in temperature gauge detection reaction still 1, when the temperature in reactor 1 lower than or near 370 DEG C time, technical staff can be communicated with secondary heater 32, start air blast 31 and open second switch valve 33, to realize raising the temperature in reactor 1.
With reference to Fig. 1, gas outlet air inlet pipe 2 having the air inlet be connected with Boiler flue pipe and is connected with reactor 1, heated air in bypass air inlet pipe 3 is when without restriction, can flow in Boiler flue pipe, this can cause the waste of heated air, for improving the utilization rate of heated air in bypass air inlet pipe 3, bypass air inlet pipe 3 and air inlet pipe 2 junction are provided with the first deflector 34, described first deflector 34 is made up of some arcs, arc guides the heated air in bypass air inlet pipe 3 to flow in reactor 1, to realize the utilization rate improving heated air in bypass air inlet pipe 3.
With reference to Fig. 1, in like manner, air inlet pipe 2 and the junction of reactor 1 are provided with the second deflector 22, and described second deflector 22 is made up of some arcs, flows in reactor 1 to guide the heated air in air inlet pipe 1.
Because ammonium sulfate and ammonium hydrogen sulfate decomposes can produce sulfur dioxide and ammonia, this just means, stops, after air inlet pipe conveying gas, will leaving certain sulfur dioxide and ammonia in reactor 1 at Boiler flue pipe.
With reference to Fig. 1, the present embodiment is avoid sulfur dioxide remaining in reactor 1 and ammonia emission in air, escape pipe 5 is connected with bypass escape pipe 4, bypass escape pipe 4 is provided with the 4th switch valve 43 and emission-control equipment, wherein, emission-control equipment comprises for the first absorption tower 41 of sulfur dioxide absorption and the second absorption tower 42 for absorbing ammonia.After Boiler flue pipe stops carrying gas to air inlet pipe 2, technical staff can close the first switch valve 23 and the 3rd switch valve 51, if now, second switch valve 33 is opened, air blast 31 and secondary heater 32 in running order, so, technical staff only need open the 4th switch valve 43, the gas got final product in realization response still 1 is blown in the first absorption tower 41 and second absorption tower 42, so that the first absorption tower 41 absorbs the sulfur dioxide in gas, second absorption tower 42 absorbs the ammonia in gas.If now, second switch valve 33 cuts out, air blast 31 and secondary heater 32 are in off-position, so, technical staff needs first to start air blast 31 and secondary heater 32, and opens second switch valve 33 and the 4th switch valve 43, thus the gas in realization response still 1 is blown in the first absorption tower 41 and second absorption tower 42, so that the first absorption tower 41 absorbs the sulfur dioxide in gas, second absorption tower 42 absorbs the ammonia in gas.
With reference to Fig. 1, for improving the catalyst effect in reactor 1 further, in reactor 1, arrange flow straightening grid 11, described flow straightening grid 11 can be made up of some flow-guiding channels, and gaseous effluent enters the catalyst micropore canals of reactor 1 inside uniformly by flow straightening grid 11.
The above, be only detailed description of the invention of the present utility model, but protection domain of the present utility model is not limited thereto, and those of ordinary skill in the art should be understood that the content that the utility model includes but not limited to accompanying drawing and describes in detailed description of the invention above.Any amendment not departing from function and structure principle of the present utility model all will comprise within the scope of the appended claims.
Claims (9)
1. a low-temperature denitration reactor, it is characterized in that: comprise reactor, described reactor is connected with air inlet pipe and escape pipe, described air inlet pipe is provided with the primary heater for heating gas in described air inlet pipe, described air inlet pipe is connected with bypass air inlet pipe, described bypass air inlet pipe is provided with secondary heater for heating gas in described bypass air inlet pipe and air blast, heated air in described bypass air inlet pipe, under the blowing of described air blast, is entered in described reactor by described air inlet pipe.
2. low-temperature denitration reactor as claimed in claim 1, is characterized in that: described bypass air inlet pipe is positioned at the one end connecting described air inlet pipe and is provided with the first deflector.
3. low-temperature denitration reactor as claimed in claim 1, is characterized in that: described air inlet pipe is positioned at the one end connecting described reactor and is provided with the second deflector.
4. low-temperature denitration reactor as claimed in claim 1, it is characterized in that: described air inlet pipe is provided with the first switch valve, described escape pipe is provided with second switch valve.
5. low-temperature denitration reactor as claimed in claim 4, is characterized in that: described bypass air inlet pipe is provided with the 3rd switch valve.
6. the low-temperature denitration reactor as described in one of claim 1 to 5, is characterized in that: described escape pipe is connected with bypass escape pipe, and described bypass escape pipe is provided with emission-control equipment.
7. low-temperature denitration reactor as claimed in claim 6, is characterized in that: described emission-control equipment comprises for the first absorption tower of sulfur dioxide absorption and the second absorption tower for absorbing ammonia.
8. low-temperature denitration reactor as claimed in claim 6, is characterized in that: described bypass escape pipe is provided with the 4th switch valve.
9. the low-temperature denitration reactor as described in one of claim 1 to 5, is characterized in that: be provided with flow straightening grid in described reactor.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520073050.2U CN204485652U (en) | 2015-02-02 | 2015-02-02 | A kind of low-temperature denitration reactor |
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| CN201520073050.2U CN204485652U (en) | 2015-02-02 | 2015-02-02 | A kind of low-temperature denitration reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106823792A (en) * | 2017-03-31 | 2017-06-13 | 华能国际电力股份有限公司玉环电厂 | Full load SCR flue gas denitrification systems |
| CN108069440A (en) * | 2018-01-23 | 2018-05-25 | 华北电力大学（保定） | A kind of ammonium hydrogen sulfate reaction generating means based on high temperature process furnances |
-
2015
- 2015-02-02 CN CN201520073050.2U patent/CN204485652U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106823792A (en) * | 2017-03-31 | 2017-06-13 | 华能国际电力股份有限公司玉环电厂 | Full load SCR flue gas denitrification systems |
| CN106823792B (en) * | 2017-03-31 | 2023-09-26 | 华能国际电力股份有限公司玉环电厂 | Full-load SCR flue gas denitration system |
| CN108069440A (en) * | 2018-01-23 | 2018-05-25 | 华北电力大学（保定） | A kind of ammonium hydrogen sulfate reaction generating means based on high temperature process furnances |
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