CN201807304U - Flue gas denitration equipment - Google Patents
Flue gas denitration equipment Download PDFInfo
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- CN201807304U CN201807304U CN2010202598445U CN201020259844U CN201807304U CN 201807304 U CN201807304 U CN 201807304U CN 2010202598445 U CN2010202598445 U CN 2010202598445U CN 201020259844 U CN201020259844 U CN 201020259844U CN 201807304 U CN201807304 U CN 201807304U
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- Prior art keywords
- flue gas
- flue
- catalyst bed
- heat exchange
- denitration
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- 239000003546 flue gas Substances 0.000 title claims abstract description 103
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 239000003054 catalyst Substances 0.000 claims abstract description 72
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 48
- 239000004071 soot Substances 0.000 claims abstract description 18
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 13
- 239000003245 coal Substances 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000007789 gas Substances 0.000 claims description 6
- 230000005855 radiation Effects 0.000 claims description 6
- 238000010408 sweeping Methods 0.000 claims description 2
- 238000003491 array Methods 0.000 claims 1
- 239000000428 dust Substances 0.000 abstract description 6
- 239000011148 porous material Substances 0.000 abstract description 3
- 230000008021 deposition Effects 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 15
- 238000000034 method Methods 0.000 description 10
- 229910021529 ammonia Inorganic materials 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 230000000694 effects Effects 0.000 description 6
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 239000010935 stainless steel Substances 0.000 description 4
- 229910001220 stainless steel Inorganic materials 0.000 description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Inorganic materials O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000012047 saturated solution Substances 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 229910002637 Pr6O11 Inorganic materials 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 description 1
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 description 1
- UBEWDCMIDFGDOO-UHFFFAOYSA-N cobalt(II,III) oxide Inorganic materials [O-2].[O-2].[O-2].[O-2].[Co+2].[Co+3].[Co+3] UBEWDCMIDFGDOO-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- CMIHHWBVHJVIGI-UHFFFAOYSA-N gadolinium(III) oxide Inorganic materials [O-2].[O-2].[O-2].[Gd+3].[Gd+3] CMIHHWBVHJVIGI-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- MRELNEQAGSRDBK-UHFFFAOYSA-N lanthanum oxide Inorganic materials [O-2].[O-2].[O-2].[La+3].[La+3] MRELNEQAGSRDBK-UHFFFAOYSA-N 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- PLDDOISOJJCEMH-UHFFFAOYSA-N neodymium oxide Inorganic materials [O-2].[O-2].[O-2].[Nd+3].[Nd+3] PLDDOISOJJCEMH-UHFFFAOYSA-N 0.000 description 1
- KTUFCUMIWABKDW-UHFFFAOYSA-N oxo(oxolanthaniooxy)lanthanum Chemical compound O=[La]O[La]=O KTUFCUMIWABKDW-UHFFFAOYSA-N 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
- FIXNOXLJNSSSLJ-UHFFFAOYSA-N ytterbium(III) oxide Inorganic materials O=[Yb]O[Yb]=O FIXNOXLJNSSSLJ-UHFFFAOYSA-N 0.000 description 1
Images
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Chimneys And Flues (AREA)
Abstract
The utility model provides flue gas denitration equipment. By adopting the structure that a denitrating agent feeder (2) is positioned in a specified position in the flue gas denitration equipment, and a catalyst bed (5) is arranged in a flue (1), the flue gas denitration equipment achieves the selective non-catalytic reduction (SNCR) and the selective catalytic reduction (SCR) in the flue (1), and reduces the consumption of catalyst, so as to reduce cost. On the other side, the distance between the header of a wall super-heater (8) and the top of a coal economizer (4) ranges from 85% to 100% of that between the header of the wall super-heater (8) and the top of a baffle plate (10), so that the space below the coal economizer (4) is increased to the greatest extent on the promise that the side surface of the coal-saving device (4) is not directly purged by the flue gas; and a sonic soot blower is arranged between the catalyst bed (5) and the coal-saving device (4), so that the dust deposition on the catalyst bed (5) is carried away by the flue gas through the pores of the catalyst bed (5), resulting in the increase of the denitration efficiency.
Description
Technical Field
The utility model relates to a flue gas denitration equipment.
Background
Flue gas is one of the main emissions from thermal power plants and is produced by the combustion of combustibles in burners (i.e. boilers). Because the flue gas usually contains a large amount of nitrogen oxide NOxSuch as NO, these nitrogen oxides, if discharged directly into the atmosphere, can lead to highly corrosive acid rain, and so the flue gas must be denitrified (i.e., denitrated) prior to discharge.
At present, the application of the relatively mature flue gas denitration technology mainly has two kinds: selective Catalytic Reduction (SCR) processes and selective non-catalytic reduction denitration (SNCR) processes. The chemical reaction principle of SCR and SNCR denitration processes is the same, and denitration agents (urea or ammonia) are sprayed into flue gas and react with NO in the flue gas within a specific temperature rangexPerforming selective reduction reaction to generate nitrogen (N)2) And water vapor (H)2O)。
The SNCR process generally sprays a denitrifier into a hearth of an 800-plus-1300 ℃ boiler, and the denitrifier (urea or ammonia) is contacted with flue gas to ensure that the denitrifier and NO in the flue gasxPerforming selective reduction reaction to generate nitrogen (N)2) And water vapor (H)2O) in parallelAnd discharging the flue gas after the flue gas is contacted with the denitrifying agent. The SNCR technology has the problem of low denitration efficiency, and the denitration efficiency of the general SNCR denitration technology is below 40%.
The SCR process is to arrange a catalyst bed layer in a flue and carry out catalytic selective reduction reaction at the temperature of 280-420 ℃ in the presence of a catalyst. The denitration efficiency of the SCR process is relatively higher than that of SNCR, and can generally reach 50-60%.
In addition, although the SCR denitration effect is better than that of the SNCR process, the denitration rate of SCR is only 60% or less as described above, and needs to be further improved. Although the denitration rate of SCR can be slightly increased by further increasing the thickness of the catalyst bed, the catalyst is relatively expensive, which leads to a significant increase in cost. In addition, since a large amount of dust is present in the flue gas, the dust is deposited on the catalyst bed while passing through the flue, thereby decreasing the denitration efficiency.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a denitration is with low costs and efficient flue gas denitration equipment with low costs and efficient in order to overcome the shortcoming that denitration that current flue gas denitration equipment exists.
The utility model provides a flue gas denitration device, which comprises a flue, a denitration agent supply device, an economizer and a catalyst bed layer which are sequentially arranged in the flue along the flow direction of the flue gas, and is characterized in that the device also comprises a disturbance device and a sound wave soot blower which are arranged in the flue, wherein the disturbance device is positioned between the denitration agent supply device and the catalyst bed layer, the sound wave soot blower is positioned between the catalyst bed layer and the economizer and is used for sweeping the catalyst bed layer, the flue comprises a first vertical section, a horizontal section and a second vertical section along the flow direction of the flue gas, two ends of the horizontal section are respectively communicated with the upper parts of the first vertical section and the second vertical section, the denitration agent supply device is positioned in the first vertical section, the distance A from the denitration agent supply device to the bottom of the first vertical section and the distance B from the top of the first vertical section to the bottom satisfy A: B of 10-25: 30, the coal economizer and the catalyst bed layer are positioned in the second vertical section, a baffle is arranged between the second vertical section and the horizontal section, and the minimum distance from the catalyst bed layer to the top of the coal economizer is 85-100% of the minimum distance from the catalyst bed layer to the top of the baffle.
The utility model has the advantages that the denitration agent supply device is positioned at the specific position in the flue gas denitration device, and the catalyst bed layer is arranged in the flue, so that SNCR and SCR reactions are realized in the flue, the usage amount of the catalyst is reduced, and the cost is reduced; on the other hand, the distance from the collecting box of the wall-wrapping superheater to the top of the economizer is 85-100% of the distance from the collecting box of the wall-wrapping superheater to the top of the baffle plate, so that the space below the economizer is as large as possible under the condition that the side surface of the economizer is not directly washed by flue gas, and the sound wave soot blower is arranged between the catalyst bed layer and the economizer, so that dust deposited on the catalyst bed layer can pass through the pores of the catalyst bed layer and is taken away by the flue gas, and the denitration efficiency is improved; moreover, the flue gas is disturbed by the disturbing device, and the flue gas and the denitrifying agent are uniformly mixed, so that the problems of failure acceleration of a local catalyst bed layer and over-standard escape amount of local ammonia caused by overlarge local ammonia concentration are solved, and the problem that the designed denitrifying efficiency cannot be achieved due to the over-small local ammonia concentration is also solved.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of a flue gas denitration apparatus of the present invention;
fig. 2 is a schematic view showing a partial structure of a position of a disturbance device in an embodiment of a flue gas denitration apparatus provided by the present invention;
fig. 3 is a schematic view showing an included angle α between the direction Y of a port of the tubular object located in the flue and the flow direction X of the flue gas when the disturbance device is the tubular object according to an embodiment of the flue gas denitration apparatus provided by the present invention;
fig. 4 is a schematic structural diagram of an embodiment of a heat exchanger of a flue gas denitration device of the present invention;
fig. 5 is a schematic structural diagram of one embodiment of a heat exchange fin of a heat exchanger of a flue gas denitration device according to the present invention;
fig. 6 is a schematic structural diagram of another embodiment of the heat exchanger fin of the economizer in the flue gas denitration device of the present invention.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
As shown in fig. 1, the flue gas denitration device provided by the present invention comprises a flue 1 and a denitration agent supply device 2 disposed in the flue 1, and is characterized in that the device further comprises a disturbance device 3, an economizer 4, an acoustic soot blower 9 and a catalyst bed layer 5, wherein the denitration agent supply device 2, the disturbance device 3, the economizer 4, the acoustic soot blower 9 and the catalyst bed layer 5 are sequentially disposed in the flue 1 along the flow direction of flue gas, the acoustic soot blower 9 is used for blowing the catalyst bed layer 5, the flue 1 comprises a first vertical section a, a horizontal section B and a second vertical section c, two ends of the horizontal section B are respectively communicated with the upper portions of the first vertical section a and the second vertical section c, the denitration agent supply device 2 is disposed in the first vertical section a, the distance a from the denitration vertical agent supply device 2 to the bottom of the first vertical section a and the distance B from the top to the bottom of the first vertical section a satisfy a: B of 10-25: 30, the economizer 4 and the catalyst bed layer 5 are positioned in the second vertical section c, a baffle plate 10 is arranged between the second vertical section c and the horizontal section b, the minimum distance from the catalyst bed layer 5 to the top of the economizer 4 is 85-100%, most preferably 100% of the minimum distance from the catalyst bed layer 5 to the top of the baffle plate 10, namely the top of the economizer 4 is equal to the top of the baffle plate 10, so that the volume below the economizer 4 can be maximized, and the catalyst bed layer 5 can be conveniently arranged.
According to the utility model provides a flue gas denitration device, the lower extreme of baffle between horizontal segment b and the second vertical section c is preferred with horizontal segment b's bottom in close contact with. The baffle may be made of stainless steel, copper, or various alloys.
The utility model discloses in, denitration agent feeding device 2 satisfies A: B between the distance A of the bottom of first vertical section a and the top of first vertical section a to the distance B of bottom 10-25: 30, preferably A: B15-23: 30, and at this moment denitration agent that denitration agent supply device 2 supplied gets into when the position of flue 1 corresponds to when using the temperature of flue 1 is 800 and 1250 ℃ prefers 1000 and 1250 ℃ the region about and be the non-catalytic reduction denitration region of flue gas to denitration agent carries out SNCR denitration reaction at first this region with the flue gas, later carries out the SCR reaction again, realizes SNCR and SCR's combined denitration from this. In general, when the height of the first vertical section a of the flue is 30 m, the width is 10 m, and the depth is 10 m, the denitration agent supply device 2 is located at a position of 10-25 m, preferably 15-23 m, of the first vertical section a.
According to the utility model discloses, denitration agent feeding device 2 can be the various devices that can be used for providing the denitration agent, under the preferred condition, denitration agent feeding device 2 is the pipeline, and this pipeline passes the wall of flue 1, stretches into in flue 1, is formed with the opening on stretching into the pipeline in flue 1. Preferably, the duct may be a plurality of ducts, and each duct extending into the flue 1 may have a plurality of openings.
In a preferred embodiment, the plurality of ducts are arranged in the axial or circumferential direction of the flue 1, and more preferably, the plurality of openings of each duct extending into the flue 1 are distributed along the axial direction of the duct. For better contact of the denitrifier with the flue gases, the direction of the openings is preferably opposite to the direction of flow of the flue gases in the flue 1.
The utility model discloses in, the opposite direction of flue gas flow is not absolute opposite in open-ended direction and flue 1, include open-ended direction down, towards the condition of level or downward sloping 1-15.
According to an embodiment of the present invention, the ratio of the cross-sectional area of the flue 1 to the total area of the opening of the duct of the denitrating agent supply device 2 is 5000-.
In the denitration agent supply device 2, the other end of the pipe is communicated with a denitration agent source. The denitrifier source can be a denitrifier storage tank, and the denitrifier can be various types capable of reacting with NOxReact to reduce NO in the flue gasxThe reagent may be ammonia, for example. The denitrifier is preferably used in the form of an aqueous solution thereof, the concentration of which is known to those skilled in the art and can be varied to the extent that the denitrifier can achieve the desired concentration. In order to reduce the amount of the denitration agent, it is preferable that the denitration agent is used in the form of a saturated solution thereof.
Although the various disturbing devices that can realize the disturbing function can all realize the object of the present invention, for example, the disturbing device 3 can be a fixed flow equalizing device, such as a flow equalizing plate. However, the fixed flow equalizing device can realize uniform mixing of the denitration agent and the flue gas through multiple flow equalization, so that a plurality of groups of flow equalizing plates are required, and a larger space is required. The inventor of the utility model finds in practice that the flue is sprayed with gas as a disturbance medium, so that a disturbance effect can be generated on the flue gas, and the distribution uniformity of the denitrifying agent in the flue gas is improved.
The position of the disturbing device 3 in the flue is only required to be between the denitrating agent supply device 2 and the catalytic reactor 5, preferably, the disturbing device 3 is between the denitrating agent supply device 2 and the economizer 4, more preferably, the disturbing device 3 is between the first vertical section a and/or the horizontal section b of the flue 1, and most preferably, the disturbing device 3 is in the first vertical section a of the flue.
According to the present invention, preferably, as shown in fig. 2, the disturbing device 3 is a tube which passes through the wall of the flue 1, and one end of the disturbing device is located in the flue 1. Preferably, for better disturbance effect, the ports of the tube in the flue 1 are oriented at an angle α of 70-90 ° to the flow direction X of the flue gas, as shown in fig. 3.
In order to make the denitrifier and the flue gas fully and uniformly mixed before entering the catalyst bed 3, the end of the tube in the flue 1 is preferably positioned in or adjacent to the first vertical section a.
The number of the tubes may be one or more, preferably 3 to 10. It is further preferred that the plurality of tubes are distributed in a radial or circumferential direction of the flue 1.
Preferably, the distance between the port of the tube-shaped object in the flue 1 and the catalyst bed 3 is 5-10 times the thickness of the catalyst bed 5, wherein the distance between the port of the tube-shaped object in the flue 1 and the catalyst bed 5 refers to the actual distance traveled by the flue gas from the port of the tube-shaped object in the flue 1 to the surface of the catalyst bed 5 in the selective catalytic reduction denitration reaction process of the flue gas.
Considering the disturbance effect and the requirement of the disturbance device 3, the present invention preferably selects the ratio of the cross-sectional area of the flue 1 to the total area of the end opening of the tubular object located in the flue 1 to be 5000-50000: 1. It is further preferred that the ratio of the cross-sectional area of the flue 1 to the total area of the ports of the tubes in the flue 1 is 20000-30000: 1.
According to an embodiment of the present invention, the apparatus further comprises a disturbing medium providing device (not shown in fig. 1) which provides the disturbing medium to the disturbing device 3. The perturbation medium supply device can be various devices capable of supplying perturbation medium, such as a high-pressure steel cylinder or a pump. One end port of the disturbance device 3 is communicated with a disturbance medium supply device, and the other end port penetrates through the wall of the flue 1 and extends into the flue 1.
The disturbance medium can be an inert medium which does not react with the flue gas and the denitration agent, is determined according to field conditions and cost accounting, and is preferably one or more of water vapor, air, nitrogen and a group zero element in the periodic table of elements, so that new impurities cannot be introduced into the flue gas due to disturbance, and the denitrated flue gas can be directly discharged.
The disturbing medium can also be flue gas or a mixture of a denitrifying agent and flue gas. The flue gas used as the disturbance medium can be flue gas subjected to denitration treatment or flue gas not subjected to denitration treatment. When the flue gas which is not subjected to denitration treatment is used as a disturbance medium, the disturbance medium is not required to be supplied from the outside, and the denitration effect of the flue gas which is not subjected to denitration treatment can be obtained after the disturbance effect is achieved. When the mixture of the denitrifier and the flue gas is used, particularly when the mixture containing the denitrifier and the flue gas, the ammonia nitrogen molar ratio of which accords with the denitration reaction, is used as a disturbing medium, the disturbing medium is introduced without causing the concentration of the denitrifier in the mixture of the flue gas and the denitrifier to be greatly reduced.
The utility model discloses in, the kind of sound wave soot blower 9 does not have special restriction, as long as can sweep and do not harm catalyst bed 5 to catalyst bed 5 can, for example, sound wave soot blower 9 can be including radiation loudspeaker, radiation loudspeaker's opening direction and the angle alpha of flue gas flow direction can be 80-90, the distance between sound wave soot blower 9 and the catalyst bed 5 can change in a very large range, under the preferred condition, radiation loudspeaker's lower edge extremely the distance of the upper surface of catalyst bed 5 can be 5-50 centimetres. The utility model discloses in, flue gas denitration equipment still includes compressed gas provides the device, and this compressed gas provides the device and is used for providing compressed gas for sound wave soot blower 9.
The economizer 4 can be various heat exchangers capable of exchanging heat, in order to further reduce the size of the economizer 4 while ensuring the heat exchange efficiency, preferably, as shown in fig. 4-6, the economizer 4 comprises a heat exchange tube 6 and a plurality of heat exchange fins 7, the heat exchange tube 6 penetrates through the heat exchange fins 7, and the outer wall of the heat exchange tube 6 is in close contact with the heat exchange fins 7. By using the economizer, the SNCR process can be realized simultaneously by improving the existing SNCR equipment.
The structure of the heat exchange fin can be changed according to the heat exchange requirement and the size of the heat exchange tube, for example, as shown in fig. 5, a space matched with the size of the heat exchange tube 6 is formed on the heat exchange fin 7.
As shown in fig. 6, in another embodiment, each fin 7 comprises a plurality of plate bodies having grooves and the grooves of two adjacent plate bodies are opposite to each other to form a space adapted to the shape of the heat exchange tube 6, through which the heat exchange tube 6 is in close contact with the fin 7.
In a preferred embodiment, the plurality of heat exchange fins 7 are arranged in parallel, and the heat exchange tube 6 passes through the plurality of heat exchange fins 7 arranged in parallel in sequence for multiple times, so as to form a parallel multi-row and multi-column heat exchange tube array.
In another preferred embodiment, the plurality of heat exchange fins 7 are arranged in parallel, the number of the heat exchange tubes 6 is multiple, and the plurality of heat exchange tubes 6 sequentially penetrate through the plurality of heat exchange fins 7 arranged in parallel to form a parallel multi-row and multi-column heat exchange tube array.
The utility model discloses in, the quantity of heat exchanger fin 7 can change in economizer 4 in a large scale, can adjust according to the needs of heat transfer and the needs of size, and under the preferred condition, the gross thickness of a plurality of parallel arrangement's heat exchanger fin 7 can be 10-20% of the heat exchange tube 6 length of single file or single row, and under the more preferred condition, the distance of two adjacent heat exchanger fins 7 can be 1-5 centimetres in a plurality of parallel arrangement's heat exchanger fin 7, and the thickness of every heat exchanger fin 7 can be 0.5-5 centimetres in a plurality of parallel arrangement's heat exchanger fin 7.
The utility model discloses in, the size of heat exchanger fin 7 can change in a large scale, can adjust according to the needs of heat transfer that the needs of size are promptly, and under the preferred condition, pass every the total sectional area of the heat exchange tube 6 of heat exchanger fin 7 can account for 10-50% of this heat exchanger fin 7 single face area. The size of the heat exchange tube 6 is not particularly limited, and various conventional heat exchange tube sizes may be selected, for example, the cross-sectional area of the heat exchange tube 6 may be 10 to 100 square centimeters.
In addition, in the economizer 4, the density of the arrangement of the heat exchange tubes 6 can be changed in a wide range, and preferably, the distance between two adjacent rows or two columns of the parallel rows or columns of the heat exchange tubes 6 can be 5-25 cm.
In a preferred embodiment of the present invention, the heat exchange tube 6 and the plurality of heat exchanging fins 7 form an integral structure.
The utility model discloses in, the collection case of package wall over heater 8 is located the bottom of second vertical section c, is provided with baffle 10 between second vertical section c and the horizontal segment b, under the preferred condition, package wall over heater 8's collection case arrives the distance at economizer 4's top can do package wall over heater 8's collection case is to 85-100% of the distance at baffle 10 top, and most preferred is 100%, and economizer 4's top and baffle 10's top are the same level promptly, can make the volume maximize under economizer 4 like this to in order to set up catalyst bed 5.
The utility model discloses in, flue 1 is enclosed by package wall over heater 8, can let in heat exchange medium in the package wall over heater 8 to heat in can the make full use of flue gas. The wall-covered superheater 8 may be, for example, a carbon steel pipe, a stainless steel pipe, a copper pipe, a titanium pipe, or various metal alloy pipes.
According to the utility model discloses, denitration agent feeding device 2 can be the various devices that can be used for providing the denitration agent, under the preferred condition, denitration agent feeding device 2 is the pipeline, and this pipeline passes the wall of flue 1, stretches into in flue 1, is formed with the opening on stretching into the pipeline in flue 1. Preferably, the duct may be a plurality of ducts, and each duct extending into the flue 1 may have a plurality of openings.
In a preferred embodiment, the plurality of ducts are arranged along the axial direction of the flue 1, and more preferably, the plurality of openings of each duct extending into the flue 1 are distributed along the axial direction of the duct. For better contact of the denitrifier with the flue gases, the direction of the openings is preferably opposite to the direction of flow of the flue gases in the flue 1.
The utility model discloses in, the opposite direction of flue gas flow is not absolute opposite in open-ended direction and flue 1, include open-ended direction down, towards the condition of level or downward sloping 1-15.
According to an embodiment of the present invention, the ratio of the cross-sectional area of the flue 1 to the total area of the opening of the duct of the denitrating agent supply device 2 is 5000-.
In the denitration agent supply device 2, the other end of the pipe is communicated with a denitration agent source. The denitrifier source can be a denitrifier storage tank, and the denitrifier can be various types capable of reacting with NOxReact to reduce NO in the flue gasxThe reagent may be ammonia, for example. The denitrifier is preferably used in the form of an aqueous solution thereof, the concentration of which is known to those skilled in the art and can be varied to the extent that the denitrifier can achieve the desired concentration. In order to reduce the amount of the denitration agent, it is preferable that the denitration agent is used in the form of a saturated solution thereof.
The catalyst can be various catalysts capable of catalyzing the denitration agent and the nitrogen oxide NOxReact to make nitrogen oxide NOxThe catalyst for conversion to nitrogen is preferably a metal oxide catalyst. Said metal oxide is such as V2O5、Fe2O3、CuO、Cr2O3、Co3O4、NiO、CeO2、La2O3、Pr6O11、Nd2O3、Gd2O3、Yb2O3Preferably V2O5. It is further preferred that the catalyst is dispersed in TiO2Up to and with V2O5As the main active component, WO3Or MoO3Vanadium-titanium systems as promoters, i.e. V2O5-WO3/TiO2Or V2O5-MoO3/TiO2. The catalyst bed layer 5 is formed by mixing the above V2O5-WO3/TiO2Or V2O5-MoO3/TiO2The catalyst is fixed on the surface of a stainless steel plate or made into a honeycomb ceramic shape to form the structural forms of a stainless steel corrugated plate type and a honeycomb ceramic. The above catalysts are commercially available, for example, from Japanese catalytic Synthesis, Hitachi, Ya robust and sturdy Longne, Germany, and Cormetech, USA. The catalyst is present in the form of a catalyst bed 5, the thickness of the catalyst bed 5 being able to vary within wide limits, preferably from 1.5 to 2 meters.
The utility model provides a flue gas denitration equipment's application method includes, send into flue 1 with the denitrifier through denitrifier feeding device 2, mixes with the flue gas in flue 1, carries out the SNCR reaction to carry out the heat transfer through the even back of disturbance device 3 disturbance and the heat transfer medium in the economizer 4 to be fit for behind the temperature of flue gas selective catalytic reduction, with catalyst bed 5 contact, thereby carry out flue gas selective catalytic reduction. And in the denitration process, the acoustic wave soot blower 9 is used for blowing the catalyst bed layer 5, so that the dust on the surface of the catalyst bed layer 5 is removed in time, and the contact between the denitration agent and the flue gas and the catalyst bed layer 5 is facilitated.
The conditions of the selective non-catalytic reduction reaction between the flue gas and the denitrifier include that the temperature is preferably 800-1300 ℃, more preferably 800-1100 ℃, and the nitrogen in the denitrifier and the NO in the flue gas are calculated by the nitrogen elementxThe nitrogen (in terms of NO) may be present in a molar ratio (ammonia nitrogen molar ratio for short) of from 0.3 to 2: 1, preferably from 0.5 to 1.5: 1, and the contact time at this temperature is preferably from 0.1 to 2 seconds, more preferably from 0.5 to 1 second. The above temperature can be achieved by selecting the location where the denitrifier is supplied, thereby utilizing the temperature of the flue gas itself in this temperature section, and thus no additional heat supply or temperature reduction is required. The temperature of the above-mentioned selective non-catalytic reduction needs to be strictly controlled, and when the temperature is higher than 1300 deg.CThe ammonia is oxidized to NOxNamely, the following reaction occurs:
when the temperature is less than 800 ℃, the aforementioned selective non-catalytic reduction reaction cannot occur in the absence of a catalyst.
The conditions for selective catalytic reduction denitration of the flue gas comprise that the temperature of the nitrogen oxide reduced into nitrogen can be 280-420 ℃, preferably 300-400 ℃, the flow speed of the flue gas can be 4-12 m/s, preferably 5-8 m/s, the amino of the denitration agent and NO in the flue gasxThe molar ratio of (ammonia nitrogen molar ratio) may be 0.5-1.1: 1, preferably 0.7-1: 1.
The utility model has the advantages that the denitration agent supply device 2 is positioned at a specific position in the flue gas denitration device, and the catalyst bed layer 5 is arranged in the flue 1, so that two reactions of SNCR and SCR are realized in the flue, the usage amount of the catalyst is reduced, and the cost is reduced; on the other hand, the sound wave soot blower 9 is arranged between the catalyst bed layer 5 and the coal economizer 4, so that dust deposited on the catalyst bed layer 5 can pass through the pores of the catalyst bed layer 5 and be taken away by flue gas, and the denitration efficiency is improved.
Claims (13)
1. A flue gas denitration device comprises a flue and a denitration agent supply device arranged in the flue, and is characterized by further comprising a disturbance device, an economizer, an acoustic wave soot blower and a catalyst bed layer, wherein the denitration agent supply device, the disturbance device, the economizer, the acoustic wave soot blower and the catalyst bed layer are sequentially arranged in the flue along the flow direction of flue gas, the acoustic wave soot blower is used for sweeping the catalyst bed layer, the flue comprises a first vertical section, a horizontal section and a second vertical section, two ends of the horizontal section are respectively communicated with the upper parts of the first vertical section and the second vertical section, the denitration agent supply device is positioned in the first vertical section, the distance A from the denitration agent supply device to the bottom of the first vertical section and the distance B from the top to the bottom of the first vertical section meet the condition that A: B is 10-25: 30, the coal economizer and the catalyst bed layer are positioned in the second vertical section, a baffle is arranged between the second vertical section and the horizontal section, and the minimum distance from the catalyst bed layer to the top of the coal economizer is 85-100% of the minimum distance from the catalyst bed layer to the top of the baffle.
2. The flue gas denitration apparatus of claim 1, wherein the disturbance device is a tube that passes through a wall of a flue so that an end port is located within the flue.
3. The flue gas denitration apparatus of claim 2, wherein the port of the tube in the flue is oriented at an angle of 70-90 ° to the flow direction of flue gas.
4. The flue gas denitration apparatus of claim 2, wherein a distance between the port of the tubular object in the flue and the catalyst bed is 5-10 times a thickness of the catalyst bed, wherein the distance between the port of the tubular object in the flue and the catalyst bed is a distance actually traveled by the flue gas from the port of the tubular object in the flue to a surface of the catalyst bed during the flue gas selective catalytic reduction denitration reaction.
5. The flue gas denitration apparatus according to any one of claims 2 to 4, wherein the tubular object is plural.
6. The flue gas denitration apparatus of claim 5, wherein the plurality of tubes are arranged in a radial direction of the flue.
7. The flue gas denitration apparatus of claim 5, wherein the ratio of the cross-sectional area of the flue to the total area of the ports of the tubular object located in the flue is 5000-50000: 1.
8. The flue gas denitration apparatus according to claim 1 or 2, further comprising a disturbing medium supply device which supplies a disturbing medium to the disturbing device.
9. The flue gas denitration apparatus of claim 1, wherein the economizer comprises a heat exchange tube and a plurality of heat exchanger fins, the heat exchange tube passes through the heat exchanger fins, and an outer wall of the heat exchange tube is in close contact with the heat exchanger fins.
10. The flue gas denitration apparatus of claim 9, wherein each heat exchanger plate comprises a plurality of plate bodies having grooves, and the grooves of two adjacent plate bodies are opposite to each other to form a space adapted to the shape of a heat exchange pipe passing through the space to be in close contact with the heat exchanger plate.
11. The flue gas denitration device of claim 9 or 10, wherein a plurality of heat exchange fins are arranged in parallel, and the heat exchange tube passes through the plurality of heat exchange fins arranged in parallel repeatedly and repeatedly in turn to form a parallel multi-row and parallel multi-column heat exchange tube array; or,
the heat exchange tubes are arranged in parallel, and penetrate through the heat exchange fins in parallel to form a plurality of parallel rows and a plurality of parallel columns of heat exchange tube arrays.
12. The flue gas denitration device of claim 1, wherein the acoustic wave soot blower comprises a radiation horn, the angle beta between the opening direction of the radiation horn and the flue gas flowing direction is 80-90 degrees, and the distance between the lower edge of the radiation horn and the upper surface of the catalyst bed layer is 5-50 centimeters.
13. The flue gas denitration apparatus of claim 1, further comprising a compressed gas supply device for supplying compressed gas to the acoustic wave soot blower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202598445U CN201807304U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020206661.7 | 2010-05-21 | ||
| CN201020206661 | 2010-05-21 | ||
| CN2010202598445U CN201807304U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
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| Publication Number | Publication Date |
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| CN201807304U true CN201807304U (en) | 2011-04-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2010202598445U Expired - Lifetime CN201807304U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitration equipment |
| CN2010202596933U Expired - Lifetime CN201807297U (en) | 2010-05-21 | 2010-07-13 | Equipment for selective catalytic reduction denitrification of flue gas |
| CN2011200602826U Expired - Lifetime CN201969481U (en) | 2010-05-21 | 2011-03-09 | Selective-catalytic-reduction-based flue gas denitrifying equipment |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2010202596933U Expired - Lifetime CN201807297U (en) | 2010-05-21 | 2010-07-13 | Equipment for selective catalytic reduction denitrification of flue gas |
| CN2011200602826U Expired - Lifetime CN201969481U (en) | 2010-05-21 | 2011-03-09 | Selective-catalytic-reduction-based flue gas denitrifying equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874280A (en) * | 2015-05-29 | 2015-09-02 | 孙永宏 | SNCR denitration device outside grate-fired furnace |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102927577B (en) * | 2012-11-20 | 2015-02-18 | 上海锅炉厂有限公司 | Flue distribution manner applied to negative omnidistance load commissioning of denitration equipment |
-
2010
- 2010-07-13 CN CN2010202598445U patent/CN201807304U/en not_active Expired - Lifetime
- 2010-07-13 CN CN2010202596933U patent/CN201807297U/en not_active Expired - Lifetime
-
2011
- 2011-03-09 CN CN2011200602826U patent/CN201969481U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104874280A (en) * | 2015-05-29 | 2015-09-02 | 孙永宏 | SNCR denitration device outside grate-fired furnace |
Also Published As
| Publication number | Publication date |
|---|---|
| CN201807297U (en) | 2011-04-27 |
| CN201969481U (en) | 2011-09-14 |
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Granted publication date: 20110427 |