CN102806010A - 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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- CN102806010A CN102806010A CN2012102816763A CN201210281676A CN102806010A CN 102806010 A CN102806010 A CN 102806010A CN 2012102816763 A CN2012102816763 A CN 2012102816763A CN 201210281676 A CN201210281676 A CN 201210281676A CN 102806010 A CN102806010 A CN 102806010A
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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 environmental protection field 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 has a strong impact on human beings'health.Improvement to them is included in the environmental protection plans of various countries gradually.
Various coal-burning boilers, catalytic cracking unit etc. produce and with the NOx of fume emission, can reach tens million of tons every year.If do not administer, will bring great disaster to the earth.
Generally, denitrating flue gas is divided into wet method and dry method two big classes, and except that 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, light, catalytic oxidation method, red-hot carbon reduction method, wet type complexed absorption method, plasma method and bioanalysis etc.Wherein, selective catalytic reduction is efficient with it, the technical advantage of low energy consumption, in commercialization market, has occupied important position.
The SCR technology is with various reducing agents, like ammonia, carbon monoxide, hydrogen or hydrocarbon compound, under middle cryogenic conditions, the NOx SCR is become nitrogen.Ammonia process SCR denitrating technique has been invented in the mid-50 in last century by Englehard Corporation company; After about 20 years, Japan develops has highly active titanium base vanadic anhydride SCR catalyst, and obtains commercial application; So far, the SCR gas denitrifying technology extensively adopts in developed country.
With the denitration of ammonia process SCR elder generation is example, and the ammonia of injection with NOx and SOx exothermic reaction as shown in Figure 1 can take place at reactor.Under the condition of adiabatic operation, beds will produce the temperature rise more than 10 ℃.Concrete temperature rise numerical value is looked NOx and SOx content, reaches conversion ratio and decides.Centering low-temperature denitration process utilizes temperature rise to add fast response, is to reduce equipment investment and the effective means that reduces operating cost.
In order to improve the efficient of denitrating flue gas, when reactor design, the following factor of considered:
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 of denitrification apparatus falls 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, the catalysqt deactivation that solution dust and sulphur ammonia cause attached to catalyst surface and the problem of regeneration.
The main type of SCR Benitration reactor is divided into fixed bed and fluid bed.Wherein, CN100348301C has designed the 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 provide the connected mode of Benitration reactor and flue; US2011194986A1, CN101219329B, CN202212106U, CN201572607U, CN202212104U in reactor or outside be provided with the parts of removing particle in the flue gas; CN100425325C, CN201543395U, CN201244436Y, CN201454414U; CN201543370U, CN202212105U, CN102068904A, CN201807307U; CN201596465U, CN201669060U, CN102309920A have 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 the injection and the mixing arrangement of ammonia; CN102389838A has described the on-line cleaning device that is used for catalyst regeneration.And CN1201852C, CN102233232A, CN102026703A, CN102068906A have then designed the fluidized bed denitration reactor.Relevant patent is too numerous to enumerate.
People (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.The result shows, the simulation moving-bed uniformity of temperature profile that makes in the reactor, and denitration effect obviously improves.CN2757903Y has designed the heat accumulating type SCR Benitration reactor that can change the flow direction, and wherein the thermal storage ceramic part is arranged with the beds branch, makes beds keep higher relatively temperature.CN201899983U has designed the structure of reactor of " C " type rotary current, is used to realize that catalyst cleans and the purpose of dedusting.
Summary of the invention
The present invention is on the basis that combines above-mentioned paper and patent thought; Beds only is set; Reducing pressure drop, and designed switching regulator adjustment doors (being called for short the switch door), controlled by the external drive structure at inside reactor; Unsteady flow through fixed bed reactors is to cycleoperation, realizes in the beds that even temperature distributes more.This design is different from simulation moving-bed three stage structure, more is applicable to high-throughout denitrating flue gas reaction.
Unsteady flow of the present invention is following to fuel gas catalytic reduction denitration reactor technology scheme:
A kind of unsteady flow respectively by inlet channel 100, flows to control channel 200 to fuel gas catalytic reduction denitration reactor 1000; Preposition catalytic reactor 300; Swing to district 400, dust arrestment and reducing agent are auxiliary to add district 500, and rearmounted catalytic reactor 600 6 parts are formed.Reactor 1000 comprises three sections beds; Be respectively first section beds 7, second section beds 12 and the 3rd section beds 18; It is characterized in that first section beds 7 and second section beds 12 are provided with flows to control channel 200; Through the adjusted in concert of two switch doors 3 and 13, the control gas flow; Simultaneously, make up fluid and swung to district 400 and dust arrestment and the auxiliary district 500 that adds of reducing agent.
Wherein, flow to control channel 200 by vertical switch door 3, transversal switch door 13, right channel 4 is formed with left channel 15.Vertical switch door 3 control flows to two feeder connections at control channel 200 tops, and 13 controls of transversal switch door flow to two anterior channel outlet 5 of control channel 200 and 14.
Described vertical switch door 3 is to be made up of or shutter whole plate with transversal switch door 13.
Be provided with side by side first section beds 7 and second section beds 12 in the described catalytic reactor 300, above two beds, be provided with soot blower 6.
Described swinging in the district 400 is provided with hydraulic barrier 9; The line of demarcation of hydraulic barrier and first section beds 7 and second section beds 12 at grade.
The auxiliary adding of described dust arrestment and reducing agent district 500 is a trapezoidal shape; Be provided with two control of dust baffle plates 10 in it; Be provided with the auxiliary inlet 11 that adds of reducing agent between two control of dust baffle plates 10, reducing agent is assisted and is added the center that inlet 11 is arranged on the trapezoidal shape bottom simultaneously.
Be provided with terminal rectification space 16 and the 3rd section beds 18 in the said rearmounted catalytic reactor 600, and terminal rectification space 16 links to each other with outlet 14 with the outlet that flows to control channel 200 5.
Utilizing reactor of the present invention to carry out unsteady flow is that the adjusted in concert of the channel vertical switch door 3 above the right channel 4 and the transversal switch door 13 in left channel 15 the place aheads realizes flowing to control to the fuel gas catalytic reduction denitration method; When 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 gets into 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 get into right channel 4.
Fluid distribution is accomplished in the rectification passage everywhere respectively, comprises right channel 4, swings to district 400, terminal rectification space 16 and left channel 15; Be accumulated in the dust and the inorganic salts that the reaction back forms of 7, the second sections beds 12 of first section beds and the 3rd section beds 18, regularly realize dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one of which is in flue 1, and it is second through the auxiliary inlet 11 that adds of reducing agent.
When vertical switch door 3 is swung to the top of right channel 4, and during transversal switch door 13 close synchronously left channel 15 anterior, flue gas gets into left channel 15; Under the guide effect of left channel 15, accomplish flowing to adjustment, and directly get into second section beds 12 in the preposition catalytic reactor 300 from top to bottom; Through this section reacted flue gas, flow into and swing to district 400, subsequently, turning back gets into first section beds 7 in the preposition catalytic reactor 300, flows into terminal rectification space 16 by outlet 5 again; At this moment, fluid changes the main body direction of motion once more, gets into the 3rd section beds 18 in the 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 get into right channel 4; After passing the guide portion that is provided with in the right channel 4, get into first section beds 7, reacted flue gas flows into swings to district 400, and turning back gets into second section beds 12, flows into terminal rectification space 16 by outlet 14 again; Subsequently, fluid changes the main body direction of motion once more, gets into the 3rd section 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 is as shown in Figure 2.By inlet channel 100, flow to control channel 200 respectively, preposition catalytic reactor 300 is swung to district 400, and dust arrestment and reducing agent are auxiliary to add district 500, and rearmounted catalytic reactor 600 6 parts assemble.
Fig. 3 has provided after six parts are taken apart shown in agent structure Fig. 2 structure chart separately.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 by vertical switch door 3 control Push And Releases, place two feeder connections at 200 tops; With by transversal switch door 13 control Push And Releases, place 200 two anterior channel outlet to form; Preposition catalytic reactor 300 contains first section beds 7 and second section beds 12, and side's placed on it soot blower 6; Swing in the district 400 and be provided with hydraulic barrier 9; Dust arrestment and reducing agent be auxiliary, and to add district 500 be trapezoidal shape, in establish control of dust baffle plate 10 and enter the mouth 11 with reducing agent auxiliary adding; Comprise terminal rectification space 16 and the 3rd section beds 18 in the rearmounted catalytic reactor 600, and with flow to control channel 200 and link to each other.Can reactor 1000 be divided into again by function: three sections beds are used for the SCR reaction; Be respectively first section beds 7, second section beds 12 and the 3rd section beds 18; The structure of 7 and 12 two-stage catalytic agent beds and measure-alike wherein, and be arranged in parallel after opening in 8 minutes by dividing plate; Flow to control then by the channel vertical switch door 3 above the right channel 4 and the transversal switch door 13 in left channel 15 the place aheads, adjusted in concert realizes; Fluid distribution is accomplished in the rectification passage everywhere respectively, comprises right channel 4, swings to district 400, terminal rectification space 16 and left channel 15; Be accumulated in dust and the inorganic salts that reaction forms in the catalyst duct, regularly realize dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one of which is in flue 1, and it is second through the auxiliary inlet 11 that adds of reducing agent.It is characterized in that: through the synchronization action of two channel switch doors, the cycle unsteady flow that realizes beds 8 and 17 is to operation.
Operation instruction:
Among Fig. 3, beds is divided into three sections, and wherein first section beds 7 and second section beds 12 and were opened by the dividing plate baffle plate side by side in 8 minutes.Be derived from the flue gas that comprises reducing agent of inlet channel 100, before inflow flows to control channel 200, can have two to flow to selection, and handle 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 during transversal switch door 13 close synchronously left channel 15 anterior, flue gas can only get into left channel 15.Under the guide effect of left channel 15, accomplish flowing to adjustment, and directly get into second section beds 12 in the preposition catalytic reactor 300 by the filled arrows direction.Through this section reacted flue gas, flow into and swing to district 400, subsequently, turning back gets into first section beds 7 in the preposition catalytic reactor 300, flows into terminal rectification space 16 by outlet 5 again.At this moment, fluid changes the main body direction of motion once more, gets into the 3rd section beds 18 in the rearmounted catalytic reactor 600, finally flows out SCR reactor 1000 by exit passageway 17.Flue gas flow direction in first and second sections beds that another one is selected then to describe with the front is opposite, promptly flows according to the sensing of Fig. 3 hollow core arrow.At this moment, 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 get into right channel 4.After passing the guide portion that is provided with in the right channel 4, get into first section beds 7.Reacted flue gas flows into swings to district 400, and turning back gets into second section beds 12, flows into terminal rectification space 16 by outlet 14 again.Subsequently, fluid changes the main body direction of motion once more, gets into the 3rd section 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 the top in district 400 and the bottom in dust arrestment and the auxiliary adding of reducing agent district 500 and be respectively equipped with hydraulic barrier 9 and control of dust baffle plate 10, to satisfy the purpose that rectification and ammonia disperse.
The reducing agent ammonia is divided into two parts, is got in the reactor 1000 by the auxiliary inlet 11 of flue 1 and the ammonia that is provided with separately respectively.Wherein, the ammonia injection rate and the reactor outlet 17 on-line monitoring NOx content of the auxiliary inlet 11 of ammonia constitute regulating loop, so that in time adjust denitration effect, and the escape amount of control ammonia.
Be the covering of cleaning catalyst surface, the spy is provided with soot blower 6 above first section beds 7 and second section beds 12, be used for the dedusting and the regeneration of catalyst.
The transmission mechanism of master cock door is by motor shaft 21, and driving gear 19 constitutes with driven gear 20, and the structure signal of its amplification is like Fig. 4.In order to prevent the sealing effectiveness of intermetallic bump and assurance switch door, be equipped with nonmetal sealing ring 22 in the upper end and the front of vertical switch door 3 and transversal switch door 13 and right channel 4 that cooperates with it and left channel 15.
The objective of the invention is to design a kind of unsteady flow that is used for first denitration before the flue gas desulfurization to scr reactor.Adopt the reactor pattern of segmentation fixed bed,, thereby improve the Temperature Distribution in the reactor, make the flue gas composition of low concentration under more even and higher reduction temperature, carry out catalytic reaction through the flow direction of change reactor inlet flue gas.Can not only make the catalytic activity of each section beds be able to give full play to, can also improve the efficient of denitrating flue gas.
The present invention compares with the fixed bed reactors of the existing single flow direction, because bed temperature is even, reaction rate improves, and catalyst amount can reduce.Meanwhile, unsteady flow is to the structure of reactor and the design that has increased the auxiliary inlet of reducing agent, and make dedusting and blow grey mode and simplify, and the shortening of self-regulating response time.Satisfied the basic demand of denitrating flue gas better.
Description of drawings
Fig. 1: reaction and enthalpy change figure;
Fig. 2: reactor body structure chart;
The structure chart of the pairing reactor each several part of Fig. 3: Fig. 2;
Fig. 4: the partial enlarged drawing of transmission mechanism I among Fig. 3.
The specific embodiment
According to accompanying drawing the present invention is done further detailed description:
A kind of unsteady flow that is suitable for denitrating flue gas is to SCR (SCR) reactor; Its agent structure is as shown in Figure 2, 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 to add district 500, and rearmounted catalytic reactor 600 6 parts assemble.
Fig. 3 has provided after six parts are taken apart shown in agent structure Fig. 2 structure chart separately.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 by vertical switch door 3 control Push And Releases, place two feeder connections at 200 tops; With by transversal switch door 13 control Push And Releases, place 200 two anterior channel outlet to form; Preposition catalytic reactor 300 contains 7, the second sections beds 12 of first section beds and dividing plate between the two 8, and side's placed on it soot blower 6; Swing in the district 400 and be provided with hydraulic barrier 9; Dust arrestment and reducing agent be auxiliary, and to add district 500 be trapezoidal shape, in establish control of dust baffle plate 10 and enter the mouth 11 with reducing agent auxiliary adding; Comprise terminal rectification space 16 and the 3rd section beds 18 in the rearmounted catalytic reactor 600, and with flow to control channel 200 and link to each other.Can be divided into again by function: three sections beds are used for the SCR reaction; Be respectively first section beds 7, second section beds 12 and the 3rd section beds 18; The structure of 7 and 12 two-stage catalytic agent beds and measure-alike wherein, and be arranged in parallel after opening in 8 minutes by dividing plate; Flow to control then by the channel vertical switch door 3 above the right channel 4 and the transversal switch door 13 in left channel 15 the place aheads, adjusted in concert realizes; Fluid distribution is accomplished in the rectification passage everywhere respectively, comprises right channel 4, swings to district 400, terminal rectification space 16 and left channel 15; Be accumulated in dust and the inorganic salts that reaction forms in the catalyst duct, regularly carry out dedusting and catalyst regeneration by soot blower 6; Reducing agent divides two parts to inject, and one of which is in flue 1, and it is second through the auxiliary inlet 11 that adds of reducing agent.Through the synchronization action of two channel switch doors, the cycle unsteady flow that realizes beds 7 and 12 is to operation.
Operation instruction:
Among Fig. 3, beds is divided into three sections, and wherein first section beds 7 and second section beds 12 and were opened by the dividing plate baffle plate side by side in 8 minutes.Be derived from the flue gas that comprises reducing agent of inlet channel 100, before inflow flows to control channel 200, can have two to flow to selection, and handle 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 during transversal switch door 13 close synchronously left channel 15 anterior, flue gas can only get into left channel 15.Under the guide effect of left channel 15, accomplish flowing to adjustment, and directly get into second section beds 12 in the preposition catalytic reactor 300 by filled arrows indication direction from top to bottom.Through this section reacted flue gas, flow into and swing to district 400, subsequently, turning back gets into first section beds 7 in the preposition catalytic reactor 300, flows into last rectification space 16 by outlet 5 again.At this moment, fluid changes the main body direction of motion once more, gets into the 3rd section beds 18 in the rearmounted catalytic reactor 600, finally flows out SCR reactor 1000 by exit passageway 17.
Flue gas flow direction in first and second sections beds that another one is selected then to describe with the front is opposite, promptly flows according to the sensing of Fig. 3 hollow core arrow.At this moment, 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 get into right channel 4.After passing the guide portion that is provided with in the right channel 4, get into first section beds 7.Reacted flue gas flows into swings to district 400, and turning back gets into second section beds 12, flows into terminal rectification space 16 by outlet 14 again.Subsequently, fluid changes the main body direction of motion once more, gets into the 3rd section 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 the top in district 400 and the bottom in dust arrestment and the auxiliary adding of reducing agent district 500 and be respectively equipped with hydraulic barrier 9 and control of dust baffle plate 10, to satisfy the purpose that rectification and ammonia disperse.
The reducing agent ammonia is divided into two parts, is got in the reactor 1000 by the auxiliary inlet 11 of flue 1 and the reducing agent that is provided with separately respectively.Wherein, the ammonia injection rate and the reactor outlet 17 on-line monitoring NOx content of the auxiliary inlet 11 of reducing agent constitute regulating loop, so that in time adjust denitration effect, and the escape amount of control ammonia.
Be the covering of cleaning catalyst surface, the spy is provided with soot blower 6 above first section beds 7 and second section beds 12, be used for the dedusting and the regeneration of catalyst.
The transmission mechanism of master cock door is by motor shaft 21, and driving gear 19 constitutes with driven gear 20, and Fig. 4 is seen in the structure signal of its amplification.In order to prevent the sealing effectiveness of intermetallic bump and assurance switch door, be equipped with nonmetal sealing ring 22 in the upper end and the front of vertical switch door 3 and transversal switch door 13 and right channel 4 that cooperates with it and left channel 15.
The present invention adopt unsteady flow to cycleoperation, compare with the fixed bed reactors of the single flow direction, the Temperature Distribution of beds is more even; Owing to be provided with rectification passage everywhere, reducing agent is more abundant with mixing of flue gas; Thereby realized under the same catalyst consumption target that the 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
3The escape amount; Soot blower be provided with the long-term operation that is beneficial to reactor.Therefore, the reactor designed of the present invention has reached the selective-catalytic-reduction denitrified requirement of flue gas.
Claims (10)
1. a unsteady flow is to the fuel gas catalytic reduction denitration reactor, and reactor flows to control channel 200 respectively by inlet channel 100; Preposition catalytic reactor 300; Swing to district 400, dust arrestment and reducing agent are auxiliary to add district 500, and rearmounted catalytic reactor 600 6 parts are formed; Reactor comprises three sections beds; Be respectively first section beds (7), second section beds (12) and the 3rd section beds (18); It is characterized in that first section beds and second section beds are provided with flows to control channel 200; Control channel 200 is through two switch door adjusted in concert, the control gas flow; Simultaneously, make up fluid and swung to district 400 and dust arrestment and the auxiliary district 500 that adds of reducing agent.
2. reactor as claimed in claim 1; It is characterized in that flowing to control channel 200 by vertical switch door (3); Transversal switch door (13), right channel (4) and left channel (15) are formed, and are selected to flow to two feeder connections at control channel 200 tops by the vertical switch door; Select to flow to two channel outlet of control channel 200 front portions by the transversal switch door, thereby limit the direction of motion of fluid.
3. reactor as claimed in claim 2 is characterized in that described vertical switch door (3) and transversal switch door (13) are to be made up of or shutter whole plate.
4. reactor as claimed in claim 1 is characterized in that being provided with in the preposition catalytic reactor 300 side by side first section beds (7) and second section beds (12), and the dividing plate (8) between two-stage catalytic agent bed; Above two-stage catalytic agent bed, be provided with soot blower (6).
5. reactor as claimed in claim 1 is characterized in that swinging to the district and is provided with hydraulic barrier 9 in 400; The line of demarcation of hydraulic barrier and first section beds (7) and second section beds (12) at grade.
6. reactor as claimed in claim 1 is characterized in that the auxiliary district 500 that adds of dust arrestment and reducing agent is trapezoidal shape, in be provided with two control of dust baffle plates (10), be provided with the auxiliary inlet (11) that adds of reducing agent between two control of dust baffle plates.
7. reactor as claimed in claim 1; It is characterized in that being provided with terminal rectification space (16) and the 3rd section beds (18) in the rearmounted catalytic reactor 600, and terminal rectification space links to each other with outlet (14) with the outlet that flows to control channel 200 (5).
8. any unsteady flow of claim 1～7 is to the fuel gas catalytic reduction denitration method, it is characterized in that fluid distribution accomplishes in the rectification passage everywhere respectively, comprises right channel (4), swings to district 400, terminal rectification space (16) and left channel (15); Be accumulated in first section beds (7), the dust of second section beds (12) and the 3rd section beds (18) and the inorganic salts that the reaction back forms are regularly realized dedusting and catalyst regeneration by soot blower (6); Reducing agent divides two parts to inject, and one of which is in flue (1), and it is second through the auxiliary inlet (11) that adds of reducing agent.
9. method as claimed in claim 8 is characterized in that realizing the adjusted in concert of the transversal switch door 13 in channel vertical switch door (3) and left channel (15) the place ahead above the right channel (4) flowing to and control; When 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 gets into 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 get into right channel (4).
10. method as claimed in claim 8 is characterized in that working as the top that vertical switch door (3) is swung to right channel (4), and the front portion of transversal switch door (13) close synchronously left channel (15), and flue gas gets into left channel (15); Under the guide effect of left channel, accomplish flowing to adjustment, and directly get into the second section beds (12) in the preposition catalytic reactor 300 from top to bottom; Through this section reacted flue gas, flow into and swing to district 400, subsequently, turning back gets into first section beds 7 in the preposition catalytic reactor 300, flows into terminal rectification space (16) by outlet (5) again; At this moment, fluid changes the main body direction of motion once more, gets into the 3rd section beds (18) in the rearmounted catalytic reactor 600, finally by exit passageway (17) outflow reactor 1000; 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 get into right channel (4); After passing the guide portion that is provided with in the right channel, get into first section beds 7, reacted flue gas flows into swings to district 400, and turning back gets into second section beds (12), flows into terminal rectification space (16) by outlet (14) again; Subsequently, fluid changes the main body direction of motion once more, gets into the 3rd section beds (18), finally by exit passageway 17 outflow reactors 1000.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108310972A (en) * | 2018-03-21 | 2018-07-24 | 中冶京诚工程技术有限公司 | Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof |
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| CN108310972A (en) * | 2018-03-21 | 2018-07-24 | 中冶京诚工程技术有限公司 | Multifunctional catalytic reactor for coupling CO catalytic oxidation and SCR denitration and application thereof |
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