CN102806010B - Variable-flow-direction flue gas catalytic-reduction denitration reactor and denitration method - Google Patents
Variable-flow-direction flue gas catalytic-reduction denitration reactor and denitration method Download PDFInfo
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- CN102806010B CN102806010B CN201210281676.3A CN201210281676A CN102806010B CN 102806010 B CN102806010 B CN 102806010B CN 201210281676 A CN201210281676 A CN 201210281676A CN 102806010 B CN102806010 B CN 102806010B
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Abstract
The invention relates to a variable-flow-direction flue gas catalytic-reduction denitration reactor and a denitration method. The reactor consists of a gas inlet passage, flow-direction control passages, a front catalytic-reduction reactor, an inversing area, a dust capturing and auxiliary reducing agent adding area and a back catalytic-reduction reactor, and comprises a first catalyst bed layer, a second catalyst bed layer and a third catalyst bed layer. The flow-direction control passages are arranged on the first catalyst bed layer and the second catalyst bed layer and used for controlling flow direction of gas by regulating two switches synchronously, and the fluid inversing area and the dust capturing and auxiliary reducing agent adding area are combined with the flow-direction control passages. The reactor adopts a sectional fixed bed, temperature distribution within a reaction period is improved by changing flow direction of flue gas at an inlet of the reactor, and components of the low-concentration flue gas can be in catalytic reduction reaction at a uniform and high reduction temperature, catalytic activity of the different catalyst bed layers can be functioned effectively, and flue gas denitration efficiency can be improved.
Description
Technical field
The present invention relates to the field of Environment Protection of air pollution treatment, be particularly useful for the improvement of coal conversion and petroleum refining equal energy source field vapor phase contaminants.
Background technology
Nitrogen oxide (being called for short NOx) is one of air major pollutants, and the chief culprit with oxysulfide formation acid rain, not only endangers natural environment, and have a strong impact on the mankind's health.Their improvement is included in gradually in the environmental protection plans of various countries.
Various coal-burning boilers, catalytic cracking unit etc. produce and with the NOx of fume emission, can reach every year tens million of tons.If do not administered, will bring great disaster to the earth.
Generally, denitrating flue gas is divided into wet method and the large class of dry method two, and except physical absorption, all the other are all the method for chemical conversion.Therefore, reactor just seems very important.Denitrating technique can also be subdivided into: selective catalytic reduction (SCR), SNCR method, optical, electrical catalytic oxidation, red-hot carbon reduction method, wet type Absorption via Chemical Complexation, plasma method and bioanalysis etc.Wherein, selective catalytic reduction is efficient with it, the technical advantage of low energy consumption, has occupied important position in commercialization market.
SCR technology is with various reducing agents, as ammonia, carbon monoxide, hydrogen or hydrocarbon compound, under middle cryogenic conditions, NOx SCR is become to nitrogen.Ammonia process SCR denitrating technique, in the mid-50 in last century, has been invented by Englehard Corporation company; After approximately 20 years, Japan develops has highly active titanium base vanadic anhydride SCR catalyst, and obtains business application; So far, SCR gas denitrifying technology extensively adopts in developed country.
Taking the first denitration of ammonia process SCR as example, can there is exothermic reaction as shown in Figure 1 at reactor with NOx and SOx in the ammonia of injection.Under the condition of adiabatic operation, beds will produce 10 DEG C of above temperature rises.Concrete temperature rise numerical value is looked NOx and SOx content, and conversion ratio and determining.Centering low-temperature denitration process, utilizes temperature rise to add fast response, is the effective means that reduces equipment investment and reduce operating cost.
In order to improve the efficiency of denitrating flue gas, in the time of reactor design, should consider following factor:
1, the temperature of beds and gas flow rate distribute even as far as possible;
2, reducing agent is abundant as far as possible with mixing of flue gas;
3, the conversion ratio of NOx is high as far as possible;
4, the Pressure Drop of denitrification apparatus is as far as possible little;
5, the escape amount of NH3 is the least possible;
6, the cycle of operation is long as far as possible.
Only taken into account foregoing, just can prevent ammonia operation in blast limit, solution dust and sulphur ammonia are attached to catalysqt deactivation that catalyst surface causes and the problem of regeneration.
The main Types of SCR Benitration reactor is divided into fixed bed and fluid bed.Wherein, CN100348301C has designed suspension type fixed bed reactors, is convenient to the dismounting of decaying catalyst; WO2007040308A1 has adopted all-in-one-piece catalyst pattern, and it is the main flow type of fixed bde catalyst; US6146605, US7943097B2, CN201772471U provides the connected mode of Benitration reactor and flue; US2011194986A1, CN101219329B, CN202212106U, CN201572607U, CN202212104U is provided with the parts of removing particle in flue gas in or beyond reactor; CN100425325C, CN201543395U, CN201244436Y, CN201454414U, CN201543370U, CN202212105U, CN102068904A, CN201807307U, CN201596465U, CN201669060U, CN102309920A has designed the conventional structure unit of reactor; CN202036922U has constructed the mounting structure of catalyst; CN101574624B has proposed the reactor of heat accumulating type, and CN102120129A has provided injection and the mixing arrangement of ammonia; CN102389838A has described the on-line cleaning device for catalyst regeneration.And CN1201852C, CN102233232A, CN102026703A, CN102068906A has designed fluidized bed denitration reactor.Relevant patent is too numerous to enumerate.
People (the Experimental investigation of the SCR of NOx in a simulated moving bed reactor.AIChE Journal such as Davide Fissore, 2006,52 (9): 3146-3154) experimental study the SCR denitration reaction in simulation moving-bed.Result shows, the simulation moving-bed uniformity of temperature profile making in reactor, and denitration effect obviously improves.CN2757903Y has designed the heat accumulating type SCR Benitration reactor that can change the flow direction, and wherein thermal storage ceramic part and beds divide and be arranged, and make beds maintain relatively high temperature.CN201899983U has designed the structure of reactor of " C " type rotary current, and for realizing, catalyst cleans and the object of dedusting.
Summary of the invention
The present invention is combining on the basis of above-mentioned paper and patent thought, beds is only set, to reduce pressure drop, and design switching regulator adjustment doors (abbreviation switch gate) at inside reactor, manipulated by external drive structure, unsteady flow by fixed bed reactors is to cycleoperation, realizes in beds Temperature Distribution more uniformly.This design is different from simulation moving-bed three stage structure, is more suitable for high-throughout denitrating flue gas reaction.
Unsteady flow of the present invention is as follows to fuel gas catalytic reduction denitration reactor technology scheme:
A kind of unsteady flow, to fuel gas catalytic reduction denitration reactor 1000, respectively by inlet channel 100, flows to control channel 200, preposition catalytic reactor 300, swing to district 400, dust arrestment and reducing agent are auxiliary adds district 500, and rearmounted catalytic reactor 600 6 part compositions.Reactor 1000 comprises three sections of beds, respectively first paragraph beds 7, second segment beds 12 and the 3rd section of beds 18, it is characterized in that being provided with and flowing to control channel 200 on first paragraph beds 7 and second segment beds 12, by the adjusted in concert of two switch gates 3 and 13, control gas flow; Meanwhile, combine fluid and swung to the auxiliary district 500 that adds in district 400 and dust arrestment and reducing agent.
Wherein, flow to control channel 200 by vertical switch door 3, transversal switch door 13, right channel 4 and left channel 15 form.Vertical switch door 3 is controlled two feeder connections that flow to control channel 200 tops, and transversal switch door 13 is controlled two channel outlet 5 and 14 that flow to control channel 200 front portions.
Described vertical switch door 3 and transversal switch door 13 are to be made up of or shutter whole plate.
In described catalytic reactor 300, be provided with first paragraph beds 7 and second segment beds 12 side by side, above two beds, be provided with soot blower 6.
Described swinging to is provided with hydraulic barrier 9 in district 400; The line of demarcation of hydraulic barrier and first paragraph beds 7 and second segment beds 12 at grade.
The auxiliary district 500 that adds of described dust arrestment and reducing agent is for trapezoidal shape, in it, be provided with two control of dust baffle plates 10, between two control of dust baffle plates 10, be provided with the auxiliary entrance 11 that adds of reducing agent, simultaneously the auxiliary center that adds entrance 11 and be arranged on trapezoidal shape bottom of reducing agent.
In said rearmounted catalytic reactor 600, be provided with end rectification space 16 and the 3rd section of beds 18, and end rectification space 16 is connected with outlet 14 with the outlet 5 that flows to control channel 200.
Utilizing reactor of the present invention to carry out unsteady flow is that the adjusted in concert of the channel vertical switch gate 3 above right channel 4 and the transversal switch door 13 in left channel 15 fronts, realizes flowing to and control to fuel gas catalytic reduction denitration method; In the time that vertical switch door 3 is closed the top of right channel 4, the front portion of transversal switch door 13 close synchronously left channel 15, flue gas enters left channel 15; When vertical switch door 3 is closed the top of left channel 15, the front portion of transversal switch door 13 close synchronously right channel 4, flue gas will enter right channel 4.
The distribution of fluid completes in rectification passage everywhere respectively, comprises right channel 4, swings to district 400, end rectification space 16 and left channel 15; Be accumulated in first paragraph beds 7, the inorganic salts that form after the dust of second segment beds 12 and the 3rd section of beds 18 and reaction, regularly realize dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one is in flue 1, and second it assisted and added entrance 11 by reducing agent.
When vertical switch door 3 is swung to the top of right channel 4, and when transversal switch door 13 close synchronously left channel 15 anterior, flue gas enters left channel 15; Under the guide effect of left channel 15, complete to flow to and adjust, and directly enter the second segment beds 12 in preposition catalytic reactor 300 from top to bottom; Through this section of reacted flue gas, flow into and swing to district 400, subsequently, turn back and enter the first paragraph beds 7 in preposition catalytic reactor 300, then flow into end rectification space 16 by outlet 5; Now, fluid changes the main body direction of motion again, enters the 3rd section of beds 18 in rearmounted catalytic reactor 600, finally by exit passageway 17 outflow reactors 1000;
When vertical switch door 3 is swung to the top of left channel 15, the front portion of transversal switch door 13 close synchronously right channel 4, flue gas will enter right channel 4; Through behind the guide portion of right channel 4 interior settings, enter first paragraph beds 7, reacted flue gas flows into and swings to district 400, turns back and enters second segment beds 12, then flow into end rectification space 16 by outlet 14; Subsequently, fluid changes the main body direction of motion again, enters the 3rd section of beds 18, finally by exit passageway 17 outflow reactors 1000.
A kind of unsteady flow that is suitable for denitrating flue gas is to SCR (SCR) reactor 1000, and its agent structure as shown in Figure 2.By inlet channel 100, flow to control channel 200 respectively, preposition catalytic reactor 300, swings to district 400, and dust arrestment and reducing agent are auxiliary adds district 500, and rearmounted catalytic reactor 600 6 parts assemble.
Fig. 3 has provided the structure chart separately after taking apart of six parts shown in agent structure Fig. 2.Inlet channel 100 comprises flue 1 and expanding reach 2; Flow to control channel 200 by vertical switch door 3, transversal switch door 13, right channel 4, left channel 15, and control Push And Release by vertical switch door 3, be placed in two feeder connections at 200 tops, with controlled Push And Release by transversal switch door 13, be placed in two channel outlet compositions of 200 front portions; Preposition catalytic reactor 300 contains first paragraph beds 7 and second segment beds 12, and side's placed on it soot blower 6; Swing to and in district 400, be provided with hydraulic barrier 9; The auxiliary district 500 that adds of dust arrestment and reducing agent, for trapezoidal shape, inside establishes the auxiliary entrance 11 that adds of control of dust baffle plate 10 and reducing agent; In rearmounted catalytic reactor 600, comprise end rectification space 16 and the 3rd section of beds 18, and with flow to control channel 200 and be connected.Reactor 1000 can be divided into again by function: three sections of beds are for SCR reaction, respectively first paragraph beds 7, second segment beds 12 and the 3rd section of beds 18, the wherein structure of 7 and 12 two-stage catalytic agent beds and measure-alike, and be arranged in parallel after being separated by dividing plate 8; Flow to control by right channel 4 channel vertical switch gate 3 above, and the transversal switch door 13 in left channel 15 fronts, adjusted in concert is realized; The distribution of fluid completes in rectification passage everywhere respectively, comprises right channel 4, swings to district 400, end rectification space 16 and left channel 15; Be accumulated in the dust in catalyst duct and react the inorganic salts that form, regularly realizing dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one is in flue 1, and second it assisted and added entrance 11 by reducing agent.It is characterized in that: by the synchronization action of two channel switch doors, realize the cycle unsteady flow of beds 8 and 17 to operation.
Operation instruction:
In Fig. 3, beds is divided into three sections, wherein first paragraph beds 7 and second segment beds 12 side by side, and by dividing plate baffle plate 8 separately.Be derived from the flue gas that comprises reducing agent of inlet channel 100, before inflow flows to control channel 200, can have two choice of flow directions, and handled respectively by vertical switch door 3 and transversal switch door 13.When vertical switch door 3 is swung to the top of right channel 4, and when transversal switch door 13 close synchronously left channel 15 anterior, flue gas can only enter left channel 15.Under the guide effect of left channel 15, complete to flow to and adjust, and directly enter the second segment beds 12 in preposition catalytic reactor 300 by filled arrows direction.Through this section of reacted flue gas, flow into and swing to district 400, subsequently, turn back and enter the first paragraph beds 7 in preposition catalytic reactor 300, then flow into end rectification space 16 by outlet 5.Now, fluid changes the main body direction of motion again, enters the 3rd section of beds 18 in rearmounted catalytic reactor 600, finally flows out SCR reactor 1000 by exit passageway 17.Another one is selected contrary with the flue gas flow direction in previously described first and second sections of beds, flows according to the sensing of Fig. 3 hollow core arrow.Now, vertical switch door 3 is swung to the top of left channel 15, and the front portion of transversal switch door 13 close synchronously right channel 4, and flue gas will enter right channel 4.Through behind the guide portion of right channel 4 interior settings, enter first paragraph beds 7.Reacted flue gas flows into and swings to district 400, turns back and enters second segment beds 12, then flow into end rectification space 16 by outlet 14.Subsequently, fluid changes the main body direction of motion again, enters the 3rd section of beds 18, finally by exit passageway 17 outflow reactors 1000.The cycle that flows to switching can be adjusted according to reactor outlet denitration result.
Swing to that the top in district 400 and dust arrestment and reducing agent are auxiliary adds the bottom in district 500 to be respectively equipped with hydraulic barrier 9 and control of dust baffle plate 10, the object of disperseing to meet rectification and ammonia.
Reducing agent ammonia is divided into two parts, is entered in reactor 1000 respectively by the auxiliary inlet 11 of ammonia of flue 1 and setting separately.Wherein, the ammonia injection rate of the auxiliary inlet 11 of ammonia and reactor outlet 17 on-line monitoring NOx content form regulating loop, to adjust in time denitration effect, control the escape amount of ammonia.
For the covering of cleaning catalyst surface, spy is provided with soot blower 6 above first paragraph beds 7 and second segment beds 12, for dedusting and the regeneration of catalyst.
The transmission mechanism of master cock door is by motor shaft 21, and driving gear 19 and driven gear 20 form, and the structure of its amplification is illustrated as Fig. 4.In order to prevent intermetallic shock and to ensure the sealing effectiveness of switch gate, be equipped with nonmetal sealing ring 22 in vertical switch door 3 and transversal switch door 13 and the right channel 4 coordinating with it and upper end and the front of left channel 15.
The object of the invention is to design a kind of unsteady flow for first denitration before flue gas desulfurization to scr reactor.Adopt the type of reactor of segmentation fixed bed, by changing the flow direction of reactor inlet flue gas, thereby improve the Temperature Distribution in reactor, make the flue gas composition of low concentration carry out catalytic reaction under more even and higher reduction temperature.Can not only make the catalytic activity of each section of beds be given full play to, can also improve the efficiency of denitrating flue gas.
Compared with the fixed bed reactors of the present invention and the existing single flow direction, because bed temperature is even, reaction rate improves, and catalyst amount can reduce.Meanwhile, unsteady flow, to the structure and the design that has increased the auxiliary inlet of reducing agent of reactor, simplifies dedusting and soot-blowing mode, and the response time shortening automatically regulating.Meet better the basic demand of denitrating flue gas.
Brief description of the drawings
Fig. 1: reaction and enthalpy change figure;
Fig. 2: reactor body structure chart;
The structure chart of the corresponding reactor each several part of Fig. 3: Fig. 2;
Fig. 4: the partial enlarged drawing of transmission mechanism I in Fig. 3.
Detailed description of the invention
The present invention is described in further detail with reference to the accompanying drawings:
A kind of unsteady flow that is suitable for denitrating flue gas is to SCR (SCR) reactor, its agent structure as shown in Figure 2, respectively by inlet channel 100, flow to control channel 200, preposition catalytic reactor 300, swing to district 400, dust arrestment and reducing agent are auxiliary adds district 500, and rearmounted catalytic reactor 600 6 parts assemble.
Fig. 3 has provided the structure chart separately after taking apart of six parts shown in agent structure Fig. 2.Inlet channel 100 comprises flue 1 and expanding reach 2; Flow to control channel 200 by vertical switch door 3, transversal switch door 13, right channel 4, left channel 15, and control Push And Release by vertical switch door 3, be placed in two feeder connections at 200 tops, with controlled Push And Release by transversal switch door 13, be placed in two channel outlet compositions of 200 front portions; Preposition catalytic reactor 300 contains first paragraph beds 7, second segment beds 12 and dividing plate between the two 8, and side's placed on it soot blower 6; Swing to and in district 400, be provided with hydraulic barrier 9; The auxiliary district 500 that adds of dust arrestment and reducing agent, for trapezoidal shape, inside establishes the auxiliary entrance 11 that adds of control of dust baffle plate 10 and reducing agent; In rearmounted catalytic reactor 600, comprise end rectification space 16 and the 3rd section of beds 18, and with flow to control channel 200 and be connected.Can be divided into again by function: three sections of beds are for SCR reaction, respectively first paragraph beds 7, second segment beds 12 and the 3rd section of beds 18, the wherein structure of 7 and 12 two-stage catalytic agent beds and measure-alike, and be arranged in parallel after being separated by dividing plate 8; Flow to control by right channel 4 channel vertical switch gate 3 above, and the transversal switch door 13 in left channel 15 fronts, adjusted in concert is realized; The distribution of fluid completes in rectification passage everywhere respectively, comprises right channel 4, swings to district 400, end rectification space 16 and left channel 15; Be accumulated in the dust in catalyst duct and react the inorganic salts that form, regularly carrying out dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one is in flue 1, and second it assisted and added entrance 11 by reducing agent.By the synchronization action of two channel switch doors, realize the cycle unsteady flow of beds 7 and 12 to operation.
Operation instruction:
In Fig. 3, beds is divided into three sections, wherein first paragraph beds 7 and second segment beds 12 side by side, and by dividing plate baffle plate 8 separately.Be derived from the flue gas that comprises reducing agent of inlet channel 100, before inflow flows to control channel 200, can have two choice of flow directions, and handled respectively by vertical switch door 3 and transversal switch door 13.When vertical switch door 3 is swung to the top of right channel 4, and when transversal switch door 13 close synchronously left channel 15 anterior, flue gas can only enter left channel 15.Under the guide effect of left channel 15, complete to flow to and adjust, and directly enter the second segment beds 12 in preposition catalytic reactor 300 by filled arrows indication direction from top to bottom.Through this section of reacted flue gas, flow into and swing to district 400, subsequently, turn back and enter the first paragraph beds 7 in preposition catalytic reactor 300, then flow into last rectification space 16 by outlet 5.Now, fluid changes the main body direction of motion again, enters the 3rd section of beds 18 in rearmounted catalytic reactor 600, finally flows out SCR reactor 1000 by exit passageway 17.
Another one is selected contrary with the flue gas flow direction in previously described first and second sections of beds, flows according to the sensing of Fig. 3 hollow core arrow.Now, vertical switch door 3 is swung to the top of left channel 15, and the front portion of transversal switch door 13 close synchronously right channel 4, and flue gas will enter right channel 4.Through behind the guide portion of right channel 4 interior settings, enter first paragraph beds 7.Reacted flue gas flows into and swings to district 400, turns back and enters second segment beds 12, then flow into end rectification space 16 by outlet 14.Subsequently, fluid changes the main body direction of motion again, enters the 3rd section of beds 18, finally by exit passageway 17 outflow reactors 1000.The cycle that flows to switching can be adjusted according to reactor outlet denitration result.
Swing to that the top in district 400 and dust arrestment and reducing agent are auxiliary adds the bottom in district 500 to be respectively equipped with hydraulic barrier 9 and control of dust baffle plate 10, the object of disperseing to meet rectification and ammonia.
Reducing agent ammonia is divided into two parts, is entered in reactor 1000 respectively by the auxiliary inlet 11 of reducing agent of flue 1 and setting separately.Wherein, the ammonia injection rate of the auxiliary inlet 11 of reducing agent and reactor outlet 17 on-line monitoring NOx content form regulating loop, to adjust in time denitration effect, control the escape amount of ammonia.
For the covering of cleaning catalyst surface, spy is provided with soot blower 6 above first paragraph beds 7 and second segment beds 12, for dedusting and the regeneration of catalyst.
The transmission mechanism of master cock door is by motor shaft 21, and driving gear 19 and driven gear 20 form, and Fig. 4 is shown in the structure signal of its amplification.In order to prevent intermetallic shock and to ensure the sealing effectiveness of switch gate, be equipped with nonmetal sealing ring 22 in vertical switch door 3 and transversal switch door 13 and the right channel 4 coordinating with it and upper end and the front of left channel 15.
The present invention adopt unsteady flow to cycleoperation, compared with the fixed bed reactors of the single flow direction, the Temperature Distribution of beds is more even; Owing to being provided with rectification passage everywhere, reducing agent is more abundant with mixing of flue gas; Thereby realize under same catalyst consumption the target that NOx conversion ratio is higher; The segmentation of reducing agent adds, and has not only improved the sensitivity of automatic control, and has reduced NH
3escape amount; Soot blower be provided with the long-term operation that is beneficial to reactor.Therefore the reactor that, the present invention designs has reached the requirement of selective-catalytic-reduction-based flue gas denitrifying.
Claims (8)
1. a unsteady flow is to fuel gas catalytic reduction denitration reactor, catalytic-reduction denitrified reactor (1000) is respectively by inlet channel (100), flow to control channel (200), preposition catalytic reactor (300), swing to district (400), dust arrestment and reducing agent are auxiliary adds district (500), and rearmounted catalytic reactor (600) six part compositions; Catalytic-reduction denitrified reactor (1000) comprises three sections of beds, respectively first paragraph beds (7), second segment beds (12) and the 3rd section of beds (18), it is characterized in that being provided with on first paragraph beds and second segment beds and flow to control channel (200), control channel (200) is by two switch gate adjusted in concert, controls gas flow; Meanwhile, combine fluid and swung to the auxiliary district (500) that adds in district (400) and dust arrestment and reducing agent; Flow to control channel (200) by vertical switch door (3), transversal switch door (13), right channel (4) and left channel (15) composition, selected to flow to two feeder connections at control channel (200) top by vertical switch door, select to flow to two anterior channel outlet of control channel (200) by transversal switch door, thereby limit the direction of motion of fluid; In preposition catalytic reactor (300), be provided with first paragraph beds (7) and second segment beds (12) side by side, and dividing plate (8) between two-stage catalytic agent bed; Above two-stage catalytic agent bed, be provided with soot blower (6).
2. reactor as claimed in claim 1, is characterized in that described vertical switch door (3) and transversal switch door (13) are to be made up of or shutter whole plate.
3. reactor as claimed in claim 1, is characterized in that swinging to and in district (400), is provided with hydraulic barrier (9); The line of demarcation of hydraulic barrier and first paragraph beds (7) and second segment beds (12) at grade.
4. reactor as claimed in claim 1, is characterized in that the auxiliary district (500) that adds of dust arrestment and reducing agent, for trapezoidal shape, is inside provided with two control of dust baffle plates (10), is provided with the auxiliary entrance (11) that adds of reducing agent between two control of dust baffle plates.
5. reactor as claimed in claim 1, it is characterized in that being provided with in rearmounted catalytic reactor (600) end rectification space (16) and the 3rd section of beds (18), and end rectification space is connected with outlet (14) with the outlet (5) that flows to control channel (200).
6. claim 1～5 any one unsteady flow is to the method for denitration of fuel gas catalytic reduction denitration reactor, the distribution that it is characterized in that fluid completes in rectification passage everywhere respectively, comprises right channel (4), swings to district (400), end rectification space (16) and left channel (15); Be accumulated in first paragraph beds (7), the inorganic salts that form after the dust of second segment beds (12) and the 3rd section of beds (18) and reaction, regularly realize dedusting and catalyst regeneration by soot blower (6); Reducing agent divides two parts to inject, and one is in flue (1), and second it assisted and added entrance (11) by reducing agent.
7. method as claimed in claim 6, is characterized in that realizing the adjusted in concert of the transversal switch door (13) in channel vertical switch gate (3) above of right channel (4) and left channel (15) front flowing to and control; In the time that vertical switch door (3) is closed the top of right channel (4), the front portion of transversal switch door (13) close synchronously left channel (15), flue gas enters left channel (15); When vertical switch door (3) is closed the top of left channel (15), the front portion of transversal switch door (13) close synchronously right channel (4), flue gas will enter right channel (4).
8. method as claimed in claim 6, is characterized in that swinging to the top of right channel (4) when vertical switch door (3), and the front portion of transversal switch door (13) close synchronously left channel (15), and flue gas enters left channel (15); Under the guide effect of left channel, complete to flow to and adjust, and directly enter the second segment beds (12) in preposition catalytic reactor (300) from top to bottom; Through this section of reacted flue gas, flow into and swing to district (400), subsequently, turn back and enter the first paragraph beds (7) in preposition catalytic reactor (300), then flow into end rectification space (16) by outlet (5); Now, fluid changes the main body direction of motion again, enters the 3rd section of beds (18) in rearmounted catalytic reactor (600), finally flows out catalytic-reduction denitrified reactor (1000) by exit passageway (17); When vertical switch door (3) is swung to the top of left channel (15), and the front portion of transversal switch door (13) close synchronously right channel (4), flue gas will enter right channel (4); Behind the guide portion arranging in right channel, enter first paragraph beds (7), reacted flue gas flows into and swings to district (400), turns back and enters second segment beds (12), then flow into end rectification space (16) by outlet (14); Subsequently, fluid changes the main body direction of motion again, enters the 3rd section of beds (18), finally flows out catalytic-reduction denitrified reactor (1000) by exit passageway (17).
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| JP2000279751A (en) * | 1999-03-29 | 2000-10-10 | Electric Power Dev Co Ltd | Method and device for denitrating pressure fluidized bed boiler |
| CN101721903A (en) * | 2010-01-22 | 2010-06-09 | 中电投远达环保工程有限公司 | Flue gas mixing element and flue gas denitration system using flue gas mixing element |
| CN201899983U (en) * | 2010-12-18 | 2011-07-20 | 李勇成 | SCR denitration reactor |
| CN102614758A (en) * | 2012-04-20 | 2012-08-01 | 湖南安普诺环保科技有限公司 | Urea-solution-based SCR (selective catalytic reduction) flue gas denitration process and device |
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Patent Citations (4)
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|---|---|---|---|---|
| JP2000279751A (en) * | 1999-03-29 | 2000-10-10 | Electric Power Dev Co Ltd | Method and device for denitrating pressure fluidized bed boiler |
| CN101721903A (en) * | 2010-01-22 | 2010-06-09 | 中电投远达环保工程有限公司 | Flue gas mixing element and flue gas denitration system using flue gas mixing element |
| CN201899983U (en) * | 2010-12-18 | 2011-07-20 | 李勇成 | SCR denitration reactor |
| CN102614758A (en) * | 2012-04-20 | 2012-08-01 | 湖南安普诺环保科技有限公司 | Urea-solution-based SCR (selective catalytic reduction) flue gas denitration process and device |
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