CN202315704U - Fluidized reactor and smoke catalytic denitration device with same - Google Patents
Fluidized reactor and smoke catalytic denitration device with same Download PDFInfo
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- CN202315704U CN202315704U CN2011204777228U CN201120477722U CN202315704U CN 202315704 U CN202315704 U CN 202315704U CN 2011204777228 U CN2011204777228 U CN 2011204777228U CN 201120477722 U CN201120477722 U CN 201120477722U CN 202315704 U CN202315704 U CN 202315704U
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Abstract
The utility model relates to a fluidized reactor and a smoke catalytic denitration device with the same. The fluidized reactor comprises a shell, wherein the lower end of the shell is provided with an air inlet, and the upper end of the shell is provided with an air outlet; a catalytic bed is horizontally arranged in the shell; the catalytic bed comprises a catalytic reaction bed and a reaction bed material arranged on the catalytic reaction bed; and the catalytic reaction bed is a guide plate for guiding air flow entering a catalytic unit to the reaction bed material. In the process of using the fluidized reactor disclosed by the utility model, the guide plate can effectively guide air flow to be reacted into the reaction bed material so that the air flow sufficiently contacts and reacts with the reaction bed material, thereby greatly improving the catalytic reaction efficiency of a denitration reactor and solving the problem that the existing denitration reactor is low in denitration efficiency.
Description
Technical field
The utility model relates to smoke pollution control field, especially a kind of smoke catalytic denitration device that is applicable to the fluidizing reactor of garbage power plant, castoff burning power plant and coal-fired plant and uses this reactor.
Background technology
Along with rapid development of economy, the problem that resource-constrained, ecological deterioration and population growth are brought becomes increasingly conspicuous, rationally, clean and utilize Limited resources to become most important efficiently.The burning city domestic garbage technology is a kind of efficient treatment technology, for compost treatment and chemical treatment, but this technology have innoxious thoroughly, subtract the remarkable resource utilization degree advantages of higher of appearanceizations.But; Limitation owing to operating procedure in the burning process very easily causes secondary pollution; Wherein the NOx pollutant in the incineration flue gas is the most direct, influence is remarkable, and this pollutant not only is detrimental to health, and can cause serious secondary pollution to atmosphere, soil and underground water.If effectively do not control and administer, will cause very serious pollution and destruction to environment, destroy human beings'health and existence directly or indirectly.Carry out effective improvement of NOx in this type incineration flue gas, become current environment and administered one of significant problem of being badly in need of solution.
But garbage burning factory is the same with power plants such as fire coal, fuel oils, and the flue gas that enters in the atmospheric environment also can contain a certain amount of soot dust granule thing, HCl, HF, SO2 and atmosphere pollutions such as NOx sour gas and dioxin.To this; House refuse power plant all designs and gas cleaning facilities such as depickling reaction tower, sack cleaner is installed at afterbody, has successfully controlled flue dust, particle and ease of solubility sour gas, but the NOx nitrogen oxide in the flue gas; Because the overwhelming majority is NO; Not soluble in water, can not effectively remove through existing denitrification apparatus, cause the high concentration discharging.
Application number is that 201110121309.2 one Chinese patent application discloses a kind of sinter fume denitrating system without the ammonia reducing agent; This denitrating system comprises heater, Benitration reactor and the deduster that connects successively, is provided with catalytic bed in the described Benitration reactor.In the course of the work, flue gas at first through described heater heating, passes through described Benitration reactor and deduster then successively, thereby accomplishes dedusting and denitration to flue gas.Though above-mentioned sinter fume denitrating system without the ammonia reducing agent has solved the problem of the water-fast nitrogen oxide high concentration discharging in the flue gas to a certain extent, in use still there is following problem in it; 1) in use; Through the flue gas of said heater because flow velocity, apart from the differences such as distance of heater; Therefore the inequality of being heated at the heater place; And temperature is a vital condition of catalytic reaction, so flue gas is preheating the uneven denitration efficiency that has directly reduced Benitration reactor of being heated of place, unit; 2) described Benitration reactor adopts general single-layer type fluidizing reactor, though compare the on-line replacing that has realized the reaction bed material with fixed bed type reactor, in the higher occasion of flue gas discharge capacity; Its operating efficiency is low; Specifically, promptly be arranged at reaction bed stockpile on the fluid bed long-pending blocked up and little with the contact area of flue gas, time of contact short, on the other hand; Pile up blocked up reaction bed stockpile and actively be prone to be worn and react not exclusively, this has then caused the waste to the reaction bed material; 3) because described deduster is located at described Benitration reactor downstream; Benitration reactor in work the time is and the smoke reaction that contains dust, influenced the reaction efficiency of reaction bed material, aggravated the wearing and tearing of reaction bed material simultaneously; Caused the waste of reaction bed material; In addition, the irregular Benitration reactor that flows to of flue gas after said heater heating, the air-flow of irregular distribution has reduced the reaction efficiency of reaction bed material from another point of view; 4) described dust arrester adopts traditional fiber bag precipitator, and it causes the life-span of resistance and operate as normal short to the mobile of flue gas, needs often to change.
Summary of the invention
The purpose of the utility model is to provide a kind of fluidizing reactor, with the low problem of denitration efficiency that solves existing Benitration reactor; The purpose of the utility model also is to provide the smoke catalytic denitration device that uses above-mentioned fluidizing reactor simultaneously.
In order to address the above problem; Said fluidizing reactor adopts following technical scheme: a kind of fluidizing reactor; Comprise housing, the lower end of said housing is provided with air inlet, and the upper end is provided with the gas outlet; Level is provided with catalytic bed in the housing; Said catalytic bed comprises catalytic bed and is located at the reaction bed material on the said catalytic bed, and said catalytic bed is to be used for the air-flow that gets into catalyst unit is caused the deflector on the reaction bed material, and the outer peripheral face of catalytic bed is matched in clearance between the internal face of housing.
Said fluidizing reactor comprises two-layer above-described catalytic bed; Each catalytic bed is parallel interval setting and be equipped with central tube successively from the top down; Said central tube is in tube wall with cooperating of each catalytic bed and is provided with air admission hole, and the upper end of central tube communicates with the gas outlet of said housing.
The cooperation place of said central tube and each catalytic bed is arranged with cylindrical sieve plate.
Said smoke catalytic denitration device adopts following technical scheme: a kind of and smoke catalytic denitration device; Comprise housing; The lower end of said housing is provided with gas approach; The upper end is provided with the clean flue gas outlet, between its gas approach and clean flue gas outlet, is provided with gas channel in the housing, is provided with catalytic reaction unit and particulate matter removing device in the said gas channel from top to bottom successively; Said catalytic reaction unit comprises fluidizing reactor; Said fluidizing reactor comprises horizontally disposed catalytic bed, and said catalytic bed comprises catalytic bed and be located at the reaction bed material on the said catalytic bed that said catalytic bed is to be used for the air-flow that gets into catalyst unit is caused the deflector on the reaction bed material.
The separated screen cloth that is provided with between said catalytic reaction unit and the particulate matter removing device.
Said fluidizing reactor comprises two-layer above-described catalytic bed; Each catalytic bed is parallel interval setting and be equipped with central tube successively from the top down; Said central tube is in tube wall with cooperating of each catalytic bed and is provided with air admission hole; The outlet of the upper end of central tube and the clean flue gas of said housing communicates, and is provided with outer the turning edge that the internal face with housing is sealed and matched on the outside wall surface of central tube in the place, top of fluidizing reactor.
The cooperation place of said central tube and each catalytic bed is arranged with cylindrical sieve plate.
Because the lower end of the housing of the fluidizing reactor of the utility model is provided with air inlet; The upper end is provided with the gas outlet; Level is provided with catalytic bed in the housing; Said catalytic bed comprises catalytic bed and is located at the reaction bed material on the said catalytic bed that said catalytic bed is to be used for the air-flow that gets into catalyst unit is caused the deflector on the reaction bed material; Therefore in use; Deflector can be effectively by setting on air-flow to the described reaction bed material that flows to the guiding question response; Thereby make it and the abundant haptoreaction of reaction bed material; Improve the catalytic reaction efficient of Benitration reactor widely, solved the low problem of denitration efficiency of the Benitration reactor of existing denitration reaction tower.
Description of drawings
Fig. 1 is the structural representation of the embodiment 1 of fluidizing reactor;
Fig. 2 is the structural representation of the embodiment 1 of smoke catalytic denitration device.
The specific embodiment
The embodiment 1 of fluidizing reactor, as shown in Figure 1, have housing 51; Cylindrical and its lower end of housing 51 is the opened type structure; The uncovered structure of housing 51 lower ends forms its air inlet, and the upper end of housing 51 is provided with gas outlet 51-1, has been horizontally disposed with four layers in the housing 51 from top to bottom (certainly; Be in other embodiments more than one deck all can) catalytic bed 52; Adopt the range upon range of mode of multilayer catalytic bed to make flue gas fully contact,, fully improve the utilization rate of reaction bed material guaranteeing to improve rate of catalysis reaction under the uniform prerequisite of catalytic bed 52 internal temperatures with catalytic bed; Avoid reaction bed material accumulation blocked up, prevented the generation that the reaction bed material stops up the problem of catalytic bed; Each catalytic bed 52 includes catalytic bed 52-1 and is located at the reaction bed material 52-2 on the catalytic bed 52-1; Wherein catalytic bed 52-1 is used for the air-flow that gets into catalyst unit is caused the deflector (commercial article) on the reaction bed material 52-2; Described catalytic bed 52-1 is made as deflector structure here; The air-flow that can press direction initialization guiding question response effectively is to described reaction bed material 52-2; Thereby make it abundant haptoreaction, improve the catalytic reaction efficient of Benitration reactor widely with reaction bed material 52-2; Be provided with the central tube 53 that axis extends along the vertical direction in the housing 51; The lower end of central tube 53 is positioned on the reaction bed of the bottom; Its upper end is passed after each catalytic bed the gas outlet conducting with housing 51 successively; Central tube 53 is provided with air admission hole and is arranged with columniform screen cloth 54 with being in tube wall cooperating of each catalytic bed 52, has not only improved the removal efficiency of catalytic denitration through this device, and has simplified system and device; Also, strengthened the utilization rate of catalyst through the temperature of gas-particle heat transfer reaction raising flue gas.
In other embodiment of fluidizing reactor, the catalytic bed of the fluidizing reactor described in the embodiment 1 of fluidizing reactor is all can more than one deck.
The embodiment 1 of smoke catalytic denitration device; As shown in Figure 2; Have housing 1, housing is cylindrical and be divided into two sections of upper semisection and lower semisections, and flange connects between said upper semisection and the lower semisection; The housing 1 of employing two-part can be changed each parts of housing 1 inside easily; Wherein the upper end of upper semisection is provided with the clean flue gas outlet 1-1 that supplies treated clean flue gas to discharge, and the lower end of lower semisection is provided with the gas approach that supplies the interior flue gas of corresponding flue to get into, and between said gas approach and clean flue gas outlet 1-1, is provided with gas channel in the housing 1; The lower end of housing 1 is provided with in its gas approach place and preheats the unit, preheats the unit and is used for the flue gas that gets in the said gas channel is preheated to improve its catalytic reaction efficient, preheats the preheating bed that the unit comprises heater 2 and is located at heater 2 tops; Wherein the preheating bed is located in the said gas channel; Heater 2 adopts coil heaters, and the preheating bed comprises a ventilative up and down preheating bed 3-1 and be located at the preparatory hot bed materials 3-2 on the preheating bed 3-1, in advance hot bed materials 3-2 be used for the flue gas heater via preheat the back through the time reach fluidization and and flue gas heat exchange; Thereby fully mixing the uneven flue gas that is heated at heater 2 places originally makes it reach isothermal; Improve its next step catalytic reaction efficient, among this embodiment, hot bed materials 3-2 adopts quartz sand in advance; Be laid with blast cap 4 on the upper surface of preheating bed 3-1; Blast cap 4 lower ends are provided with air inlet, and preheating bed 3-1 is provided with the through hole that communicates with said air inlet, and blast cap 4 makes preheating bed 3-1 form an air distribution plate; The air-flow that is used for passing through distributes uniformly and changes its flow direction; Thereby make the flue gas that passes through flow with direction initialization, the bottom of preheating bed 3-1 is connected with the bed material delivery line 10 that is used to derive preparatory hot bed materials 3-2, and bed material delivery line 10 is provided with discharge switch valve 11; Be provided with catalytic reaction unit and particulate matter removing device in the gas channel of housing 1 one on the other; Particulate matter removing device is located at and is preheated the top, unit so that the pre-warmed flue gas of process is carried out dedusting; Particulate matter removing device comprises dedusting seat 5 and dust removing tube 6; Dedusting seat 5 is the tubular of open upper end, following end closure, and the whole outline of dust removing tube 6 is Y-shaped, and its upper/lower terminal is hatch frame; The outside wall surface of dust removing tube 6 upper ends and the internal face of housing 1 are sealed and matched; The lower end of dust removing tube 6 is inserted in the dedusting seat 5 and the bottom surface matched in clearance of its lower surface and dedusting seat 5, its be positioned at dedusting seat 5 part outside wall surface all with the internal face matched in clearance of dedusting seat 5, the outside wall surface matched in clearance of the internal face of the upper end of dedusting seat and dust removing tube; Thereby make the flue gas that gets into particulate matter removing device to move at first from bottom to top; Under differential pressure action, be moved into dedusting seat 5 from the top down by beginning behind dust removing tube 6 blocks, and then get into dust removing tube 6 once more from bottom to top from dedusting seat 5 interior flue gases, finally the open upper end exhaust particulate matter from dust removing tube 6 removes device; Flue gas is repeatedly switching-over motion in particulate matter removing device; Combine the effect of gravity to cause the particle 7 that wherein is mingled with to be able to remove and to be deposited in the dedusting seat 5 simultaneously, dedusting seat 5 is provided with particle delivery line 8, and an end of particle delivery line 8 is fixed on the dedusting seat 5 and with the inner chamber of dedusting seat 5 and communicates; The other end overhangs to the housing 1 and is downward-sloping; Particle delivery line 8 is used for the particle 7 that is deposited in the dedusting seat 5 is derived reaction unit, and the part that particle delivery line 8 stretches out housing is provided with row's grain switch valve 9, and row's grain switch valve 9 is used for opening as required or cutting off particle delivery line 8; The separated screen cloth 12 that is provided with between catalytic reaction unit and the particulate matter removing device; This screen cloth 12 adopts metallic sieve; Screen cloth 12 can further carry out dust removal process to flue gas on the one hand, is used on the other hand the flue gas that is about to get in the catalytic reaction unit is carried out uniform distribution; The catalytic reaction unit comprises fluidizing reactor, and in the present embodiment, fluidizing reactor comprises four layers of catalytic bed; Each catalytic bed includes catalytic bed 13 and is located at the reaction bed material 14 on the catalytic bed 13; Catalytic bed 13 is designed to deflector, causes on the reaction bed material 14 and makes reaction bed material 14 reach fluidization with the flue gas that will get into the catalytic reaction unit, thereby make flue gas fully contact with the reaction bed material; Guaranteeing to improve rate of catalysis reaction under the uniform prerequisite of catalytic bed internal temperature; Fully improve the utilization rate of reaction bed material, avoided the accumulation of reaction bed material, prevented the generation that the reaction bed material stops up the problem of catalytic bed; The center of each catalytic bed is equipped with a central tube 15; The upper end of this central tube 15 and the clean flue gas of housing export the 1-1 conducting and are provided with the outer 15-1 that turns edge; Outer the turning edge of central tube 15 cut off the gas channel in the housing on vertical; The cooperation place of central tube 15 and each catalytic bed is respectively equipped with the through hole that the flue gas of confession after catalytic reaction pass through and is arranged with cylindrical sieve plate 18, and cylindrical sieve plate is used to prevent that the reaction bed material from getting into central tube 15 with flue gas; Thereby make and discharge via the clean flue gas outlet of housing with the reacted flue gas formation clean flue gas of each catalytic bed and from central tube 15; Respectively be provided with temperature measuring equipment 16 on particulate matter removing device and the catalytic reaction unit, temperature measuring equipment 16 adopts thermocouple and is connected with controller 17, and controller 17 is used for the Signal Regulation heater according to temperature measuring equipment; In addition; The gas approach place also is provided with flow monitoring device (not shown), and the flow monitoring device is used to monitor the flue gas flow that gets into particulate matter removing device, in the use; Flue gas after described gas approach and the boiler combustion is linked to each other; The exhaust gas volumn that produces in the boiler is by burning wind control, and burning wind is how much controlling of based on fuel amount, through observing the fuel quantity of the control boiler that said flow monitoring device can be in good time; Thereby make the exhaust gas volumn that gets into said gas approach be controlled in the optimum range, give full play to the denitration performance of the flue gas of refuse burning dedusting catalytic denitration reaction unit of the utility model.
In other embodiment of smoke catalytic denitration device, the catalytic bed of the fluidizing reactor described in the embodiment 1 of smoke catalytic denitration device is all can more than one deck.
Claims (7)
1. a fluidizing reactor is characterized in that, comprises housing; The lower end of said housing is provided with air inlet; The upper end is provided with the gas outlet, and level is provided with catalytic bed in the housing, and said catalytic bed comprises catalytic bed and is located at the reaction bed material on the said catalytic bed; Said catalytic bed is to be used for the air-flow that gets into catalyst unit is caused the deflector on the reaction bed material, and the outer peripheral face of catalytic bed is matched in clearance between the internal face of housing.
2. fluidizing reactor according to claim 1; It is characterized in that; Said fluidizing reactor comprises two-layer above-described catalytic bed; Each catalytic bed is parallel interval setting and be equipped with central tube successively from the top down, and said central tube is in tube wall with cooperating of each catalytic bed and is provided with air admission hole, and the upper end of central tube communicates with the gas outlet of said housing.
3. fluidizing reactor according to claim 2 is characterized in that the cooperation place of said central tube and each catalytic bed is arranged with cylindrical sieve plate.
4. a smoke catalytic denitration device comprises housing, and the lower end of said housing is provided with gas approach; The upper end is provided with the clean flue gas outlet; Between its gas approach and clean flue gas outlet, be provided with gas channel in the housing, it is characterized in that, be provided with catalytic reaction unit and particulate matter removing device in the said gas channel from top to bottom successively; Said catalytic reaction unit comprises fluidizing reactor; Said fluidizing reactor comprises horizontally disposed catalytic bed, and said catalytic bed comprises catalytic bed and be located at the reaction bed material on the said catalytic bed that said catalytic bed is to be used for the air-flow that gets into catalyst unit is caused the deflector on the reaction bed material.
5. smoke catalytic denitration device according to claim 4 is characterized in that, the separated screen cloth that is provided with between said catalytic reaction unit and the particulate matter removing device.
6. smoke catalytic denitration device according to claim 4; It is characterized in that; Said fluidizing reactor comprises two-layer above-described catalytic bed; Each catalytic bed is parallel interval setting and be equipped with central tube successively from the top down; Said central tube is in tube wall with cooperating of each catalytic bed and is provided with air admission hole, and the outlet of the upper end of central tube and the clean flue gas of said housing communicates, and is provided with outer the turning edge that the internal face with housing is sealed and matched on the outside wall surface of central tube in the place, top of fluidizing reactor.
7. smoke catalytic denitration device according to claim 6 is characterized in that the cooperation place of said central tube and each catalytic bed is arranged with cylindrical sieve plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204777228U CN202315704U (en) | 2011-11-26 | 2011-11-26 | Fluidized reactor and smoke catalytic denitration device with same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011204777228U CN202315704U (en) | 2011-11-26 | 2011-11-26 | Fluidized reactor and smoke catalytic denitration device with same |
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| Publication Number | Publication Date |
|---|---|
| CN202315704U true CN202315704U (en) | 2012-07-11 |
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| CN2011204777228U Expired - Fee Related CN202315704U (en) | 2011-11-26 | 2011-11-26 | Fluidized reactor and smoke catalytic denitration device with same |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102688731A (en) * | 2011-11-26 | 2012-09-26 | 河南科技大学 | Fluidized reactor and flue gas catalyzing and denitrification device using same |
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2011
- 2011-11-26 CN CN2011204777228U patent/CN202315704U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102688731A (en) * | 2011-11-26 | 2012-09-26 | 河南科技大学 | Fluidized reactor and flue gas catalyzing and denitrification device using same |
| CN102688731B (en) * | 2011-11-26 | 2014-09-24 | 河南科技大学 | Fluidized reactor and flue gas catalyzing and denitrification device using same |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120711 Termination date: 20141126 |
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| EXPY | Termination of patent right or utility model |