CN201997246U - Smoke gas denitration equipment - Google Patents
Smoke gas denitration equipment Download PDFInfo
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- CN201997246U CN201997246U CN2011200602614U CN201120060261U CN201997246U CN 201997246 U CN201997246 U CN 201997246U CN 2011200602614 U CN2011200602614 U CN 2011200602614U CN 201120060261 U CN201120060261 U CN 201120060261U CN 201997246 U CN201997246 U CN 201997246U
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- flue gas
- heat exchanger
- flue
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- tube
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- 239000000779 smoke Substances 0.000 title abstract 4
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 75
- 238000010531 catalytic reduction reaction Methods 0.000 claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 120
- 239000003546 flue gas Substances 0.000 claims description 120
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 22
- 239000003245 coal Substances 0.000 abstract 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 19
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 14
- 239000000203 mixture Substances 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 229910021529 ammonia Inorganic materials 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 229910044991 metal oxide Inorganic materials 0.000 description 5
- 150000004706 metal oxides Chemical class 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 238000006722 reduction reaction Methods 0.000 description 4
- 229910010413 TiO 2 Inorganic materials 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances 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
- 230000008901 benefit Effects 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 241000264877 Hippospongia communis Species 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
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- 238000005859 coupling reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
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- 229910001092 metal group alloy Inorganic materials 0.000 description 1
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- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
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- 239000012047 saturated solution Substances 0.000 description 1
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- GFNGCDBZVSLSFT-UHFFFAOYSA-N titanium vanadium Chemical compound [Ti].[V] GFNGCDBZVSLSFT-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model relates to smoke gas denitration equipment, which comprises a flue (1) defined by a wall covering overheater (8), wherein a denitration agent supply device (2), a perturbation device (12), a coal economizer (5) and a catalyst bed layer (4) are sequentially arranged in the flue (1) in the smoke gas flowing direction, the distance from a collection box (9) of the wall covering overheater (8) to the top of the coal economizer (5) is 85 to 100 percent of the distance from the collection box (9) of the wall covering overheater (8) to the top of a baffle plate (11), and a ratio of the distance A from the denitration agent supply device (2) to the bottom of a first vertical section (a) to the distance B from the bottom of the first vertical section (a) to the top is 10 to 25/30. The smoke gas denitration equipment according to the utility model realizes the selective non-catalytic reduction (SNCR) and selective catalytic reduction (SCR) combined denitration, so the denitration efficiency is improved.
Description
Technical field
The utility model relates to a kind of denitrating flue gas equipment.
Background technology
Flue gas is one of main emission of steam power plant, by the combustible generation of burning in burner (being boiler).Owing to contain a large amount of nitrogen oxide NO usually in the flue gas
x(as NO) if these nitrogen oxide directly are discharged in the atmosphere, can cause the very strong acid rain of corrosivity, so flue gas must be handled through denitrogenation (that is denitration) before discharging.
At present, the gas denitrifying technology of utilization comparative maturity mainly contains two kinds: selective-catalytic-reduction denitrified (SCR) technology and SNCR denitration (SNCR) technology.The chemical principle of SCR and SNCR denitrating technique all is the same, all is denitrfying agent (for example: urea or ammonia) is contacted with flue gas, makes the NO in denitrfying agent and the flue gas
xCarry out the selective reduction reaction and generate nitrogen (N
2) and steam (H
2O).SNCR technology is generally carried out the selective reduction reaction in the burner hearth of 800-1250 ℃ of boiler.SCR technology then is that beds is set in flue, under 280-420 ℃ of temperature, carries out the catalytic selectivity reduction reaction under the condition that catalyst exists.
SNCR and SCR cut both ways, and the advantage of SNCR is not need expensive catalyst bed, and shortcoming is that denitration effect is relatively poor, and the denitration rate generally is no more than 40%.The shortcoming of SCR then is need to use expensive catalyst bed, and needs enough spaces catalyst bed is set, and advantage then is that denitration effect is good than SNCR, and the denitration rate is generally below 60%.
Therefore, the nitrogen oxide that how to remove efficiently in the flue gas remains a technical problem that needs to be resolved hurrily.
And, because the temperature of SCR denitration is 280-420 ℃, and the temperature of flue gas is generally more than 800 ℃ even 1000 ℃, for cooling that realizes flue gas and the high heat that effectively utilizes flue gas, common way is that flue is surrounded by a plurality of metal tubes (also claiming bag wall superheater) of interior dress demineralized water at present, high heat in the flue gas passes to demineralized water in the metal tube by transfer modes such as radiation, thereby obtains superheated steam.A plurality of metal tubes come together in the collection case of bag wall superheater.Be to set up an economizer (being heat exchanger) before beds on the other hand, economizer is formed by a plurality of heat exchanger tubes that are connected in series mutually.In order to guarantee that the flue gas after the heat exchange can satisfy the requirement that SCR reacts, the number of heat exchanger tube is very huge, thereby the volume of economizer is very huge.For the π type flue that comprises two vertical sections and a horizontal segment, economizer is arranged in the vertical section at collection case place of bag wall superheater usually, the collection case that promptly wraps the wall superheater to the distance at the top of described economizer less than the collection case of described bag wall superheater distance to horizontal segment and vertical section position adjacent.
The utility model content
The purpose of this utility model is in order to overcome the lower shortcoming of denitration rate that existing flue-gas denitration process exists, to provide a kind of denitration rate higher denitrating flue gas equipment.
The utility model provides a kind of denitrating flue gas equipment, and this equipment comprises the flue that is surrounded by bag wall superheater, wherein, along the flow direction of flue gas, is disposed with denitrfying agent feedway, disturbance device, economizer and beds in the flue; Flue comprises first vertical section, second vertical section and horizontal segment, the two ends of described horizontal segment are communicated with the top of first vertical section and second vertical section respectively, the denitrfying agent feedway is positioned at first vertical section, economizer and beds are positioned at second vertical section, the collection case of bag wall superheater is positioned at the bottom of second vertical section, be provided with baffle plate between second vertical section and the horizontal segment, the collection case of described bag wall superheater is the 85-100% of the collection case of described bag wall superheater to the distance at the top of described baffle plate to the distance at the top of described economizer; The ratio apart from B to the top is 10-25 to described denitrfying agent feedway to the bottom of the distance A of the bottom of first vertical section and described first vertical section: 30.
The collection case of the utility model by making bag wall superheater is the 85-100% of the collection case of described bag wall superheater to the distance at baffle plate top to the distance at the top of described economizer, guaranteeing under the situation that the economizer side is not directly washed away by flue gas, can make the space of flue of economizer below big as far as possible, thereby can in existing flue, set up beds, make simultaneously and realized the associating of flue gas SNCR reaction, improved the denitration efficiency of flue gas with the flue gas selective catalytic reduction reaction according to denitrating flue gas equipment of the present utility model.In addition, between described denitrfying agent feedway and beds, disturbance device is set according to denitrating flue gas equipment of the present utility model, described disturbance device is used for flue gas is carried out disturbance, flue gas and denitrfying agent are mixed, thereby both avoided the excessive problem that local beds inefficacy is quickened and local amount of ammonia slip exceeds standard that causes of local ammonia concentration, also avoided the problem of the too small denitration efficiency that does not reach design that causes of local ammonia concentration simultaneously.
Description of drawings
Fig. 1 is the structural representation of a kind of embodiment of denitrating flue gas equipment of the present utility model;
Fig. 2 is the partial structurtes schematic diagram of disturbance device position in the used denitrating flue gas equipment of a kind of embodiment that shows denitration method for flue gas provided by the invention;
Fig. 3 is when disturbance device is tube in the used denitrating flue gas equipment of a kind of embodiment that shows denitration method for flue gas provided by the invention, and tube is arranged in the schematic diagram towards the angle α of Y and flow of flue gas direction X of the port of flue;
Fig. 4 is a kind of structural representation of embodiment of the heat exchanger of denitrating flue gas equipment of the present utility model;
Fig. 5 is a kind of structural representation of embodiment of heat exchanger fin of the heat exchanger of denitrating flue gas equipment of the present utility model;
Fig. 6 is the structural representation of the another kind of embodiment of the heat exchanger fin of economizer in the denitrating flue gas equipment of the present utility model.
The specific embodiment
Below in conjunction with accompanying drawing denitrating flue gas equipment of the present utility model is described in detail.
As shown in Figure 1, the utility model provides a kind of denitrating flue gas equipment, and this equipment comprises the flue 1 that is surrounded by bag wall superheater 8, wherein, along the flow direction of flue gas, be disposed with denitrfying agent feedway 2, disturbance device 12, economizer 5 and beds 4 in the flue 1; Flue 1 comprises the first vertical section a, the second vertical section c and horizontal segment b, the two ends of described horizontal segment b are communicated with the top of the first vertical section a and the second vertical section b respectively, denitrfying agent feedway 2 is positioned at the first vertical section a, economizer 5 and beds 4 are positioned at the second vertical section c, the collection case 9 of bag wall superheater 8 is positioned at the bottom of the second vertical section c, be provided with baffle plate 11 between the second vertical section c and the horizontal segment b, the collection case 9 of described bag wall superheater 8 is the 85-100% of the collection case 9 of described bag wall superheater 8 to the distance at the top of described baffle plate 11 to the distance at the top of described economizer 5; The distance A of the bottom of described denitrfying agent feedway 2 to first vertical section a and the bottom of the described first vertical section a are 10-25 to the ratio apart from B at top: 30.
In the preferred case, the bottom of the distance A of the bottom of described denitrfying agent feedway 2 to first vertical section a and the described first vertical section a is 15-23 to the ratio apart from B at top: 30.
In the preferred case, the collection case 9 of described bag wall superheater 8 is the 90-100% of the collection case 9 of described bag wall superheater 8 to the distance at the top of described baffle plate 11 to the distance at the top of described economizer 5, most preferably is 100%.
According to the denitrating flue gas equipment that the utility model provides, described flue 1 is used to guide flue gas to flow according to predetermined direction on the one hand; On the other hand, described flue 1 can also be as flue gas being carried out the place that denitration is handled.According to denitrating flue gas equipment of the present utility model, described flue 1 comprises the first vertical section a, horizontal segment b and the second vertical section c, both can reduce the height of flue 1, improve the security of flue, be convenient in flue, install simultaneously denitrfying agent feedway 2 and beds 4 again, thereby realize the coupling of flue gas selective catalytic reduction reaction and flue gas SNCR reaction, and then improve denitrating flue gas efficient.
Ratio between the height of the length of the height of the described first vertical section a, horizontal segment b and the second vertical section c can carry out suitable selection according to concrete use occasion.
For the reaction of flue gas SNCR, whether the flue gas selective catalytic reduction reaction is evenly more responsive for the distribution of denitrfying agent in the flue gas.The skewness of denitrfying agent in flue gas not only will cause in the beds local denitrfying agent denitration efficiency low, also will make catalyst failure quicken and/or local denitrfying agent escape amount exceeds standard.Therefore, also comprise disturbance device 12 according to denitrating flue gas equipment of the present utility model, in the preferred case, described disturbance device 12 is positioned at horizontal segment b, be used for flue gas is carried out disturbance, thereby before flue gas and denitrfying agent enter described beds 4, flue gas and denitrfying agent are mixed, avoid owing to the denitrfying agent catalyst failure that skewness causes in flue gas quickens, local denitrfying agent denitration efficiency is low and regional area dust stratification blocking problem.
Although the various disturbance devices of disturbance function of can realizing all can be realized the purpose of this utility model, for example, described disturbance device 12 can be for fixed current equalizer, as homogenizing plate.But, thereby need organize homogenizing plates, thereby space that need be bigger because this fixed current equalizer need could realize making denitrfying agent to mix with the even of flue gas by current-sharing repeatedly more.Inventor of the present utility model finds in practice, by to the flue gas jet as the disturbance medium, can produce disturbance effect to flue gas, improve the uniformity that denitrfying agent distributes in flue gas.
As shown in Figure 2, according to the utility model, described disturbance device 12 is a tube, and this tube passes the wall of flue 1, and an end port is arranged in flue 1.Under the preferable case, in order better to obtain the disturbance effect, as shown in Figure 3, the angle α towards Y and flow of flue gas direction X that tube is arranged in the port of flue 1 is 70-90 ° of angle.
In order to make denitrfying agent fully mix with flue gas before entering beds 4, under the preferable case, the port that described tube is arranged in flue 1 is positioned at the first vertical section a or horizontal segment b or the first vertical section a and horizontal segment b adjoiner.
Described tube can be preferably 3-10 for one or more.Further preferred described a plurality of tubes radially or circumferentially distribute along flue 1.
Under the preferable case, describedly be 5-10 times of being described catalyst bed layer thickness of port and the distance described beds 4 between of tube in flue 1, wherein, port and the distance described beds between of described tube in flue refer in the selective-catalytic-reduction denitrified course of reaction of flue gas, and the port that flue gas is arranged in flue from described tube marches to the surperficial actual distance of passing by of beds.
Take all factors into consideration the disturbance effect and to the equipment requirement of disturbance device 12, the cross-sectional area of the preferred described flue 1 of the utility model is 5000-50000 with the ratio of the gross area of the port that is arranged in flue 1 of described tube: 1.Further the cross-sectional area of preferred described flue 1 is 20000-30000 with the ratio of the gross area of the port that is arranged in flue 1 of described tube: 1.
According to a kind of embodiment of the present utility model, this equipment also comprises disturbance medium generator (not shown in figure 1), and disturbance medium generator provides the disturbance medium for disturbance device 12.Described disturbance medium generator can be the various devices that the disturbance medium can be provided, as high-pressure cylinder or pump.One end port of described disturbance device 12 is communicated with disturbance medium generator, and other end port then passes the wall of described flue 1 and stretches in the described flue 1.
According to a kind of embodiment of the present utility model, described disturbance medium be not with the inert media of flue gas and denitrfying agent reaction, determine according to field condition and cost accounting, one or more in the group 0 element in steam, air, nitrogen and the periodic table of elements preferably, thereby can not introduce new impurity to flue gas because of disturbance, the flue gas after the denitration can directly discharge.
According to another kind of embodiment of the present utility model, described disturbance medium is the mixture of flue gas or denitrfying agent and flue gas.Described flue gas as the disturbance medium can be the flue gas that passes through the denitration processing or handle without denitration.When using the flue gas handled without denitration as the disturbance medium, need not the extraneous disturbance medium of supplying with on the one hand, can also make the flue gas of handling without denitration after playing perturbation action, also can obtain denitration effect on the other hand.And when using the mixture of denitrfying agent and flue gas, particularly be the mixture that contains denitrfying agent and flue gas during as the disturbance medium that meets denitration reaction with the ammonia nitrogen mol ratio, the feeding of disturbance medium also can not cause the significantly reduction of denitrfying agent concentration in the mixture of flue gas and denitrfying agent.Therefore the preferred described disturbance medium of the present invention is without the flue gas of denitration processing or the mixture of denitrfying agent and flue gas, the mixture that especially preferred described disturbance medium is denitrfying agent and flue gas, and more preferably in the nitrogen element, NO in nitrogen and the flue gas in the denitrfying agent
xThe mol ratio (be called for short ammonia nitrogen mol ratio) of nitrogen (in NO) be 0.5-1.1: 1 the denitrfying agent and the mixture of flue gas.
According to the denitrating flue gas equipment that provides of the present utility model, described economizer 5 comes down to a kind of heat exchanger, can be the various heat exchangers that can make flue gas and heat transferring medium carry out heat exchange commonly used.From volume that further reduces flue 1 and the angle that improves heat exchange efficiency, described economizer 5 is preferably the heat exchanger with heat exchanger tube 6 and a plurality of heat exchanger fin 7, wherein, described heat exchanger tube 6 passes described heat exchanger fin 7, and the outer wall of heat exchanger tube 6 closely contacts with heat exchanger fin 7, the heat transferring medium that is used for heat-obtaining is housed in the heat exchanger tube 6, and described heat transferring medium for example can be a demineralized water.As long as the temperature of heat transferring medium is lower than the temperature of the mixture of non-catalytic reduction denitration product or non-catalytic reduction denitration product and disturbance medium, for example can be 40-200 ℃.
In the denitrating flue gas equipment that the utility model provides, under the preferable case, as shown in Figure 4, described economizer 5 comprises heat exchanger tube 6 and a plurality of heat exchanger fin 7, and described heat exchanger tube 6 passes described heat exchanger fin 7, and the outer wall of heat exchanger tube 6 closely contacts with heat exchanger fin 7.
According at a kind of embodiment of the present utility model, as shown in Figure 5, described heat exchanger fin 7 has a plurality of spaces that adapt with shape heat exchanger tube 6, and the space that the shape a plurality of and heat exchanger tube 6 in this heat exchanger fin 7 adapts forms the parallel multirow and the array of multiple row, thereby described heat exchanger tube 6 can repeatedly pass this heat exchanger fin 7 toward ground return successively, and described heat exchanger tube 6 forms the array corresponding with the above-mentioned array of heat exchanger fin 7.
According to another kind of embodiment of the present utility model, as shown in Figure 6, each heat exchanger fin 7 comprises a plurality of plate bodys, this plate body have in groove and adjacent two plate bodys groove toward each other, the space that the shape of formation and heat exchanger tube 6 adapts, described heat exchanger tube 6 passes this space and closely contacts with heat exchanger fin 7.
According in a kind of preferred implementation of the present utility model, described a plurality of heat exchanger fins 7 are arranged in parallel, and described heat exchanger tube more than 6 time passes a plurality of heat exchanger fins that are arranged in parallel 7 successively toward ground return, forms the parallel multirow and the heat exchanger tube array of multiple row.
According in another kind of preferred implementation of the present utility model, described a plurality of heat exchanger fins 7 are arranged in parallel, and described heat exchanger tube 6 can be for a plurality of, and a plurality of heat exchanger tubes 6 pass a plurality of heat exchanger fins that are arranged in parallel 7 successively, form the parallel multirow and the heat exchanger tube array of multiple row.
The quantity of heat exchanger fin 7 can in very large range change in the described economizer 5, can adjust according to the needs of heat exchange and the needs of size, under the preferable case, the gross thickness of a plurality of heat exchanger fins that are arranged in parallel 7 can be the 10-20% of single file or single-row heat exchanger tube length.
Under the preferred situation, the distance of two adjacent heat exchanger fins can be 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 7, and the thickness of each heat exchanger fin can be 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 7.
The size of described heat exchanger fin 7 can in very large range change, the needs that can be size according to the needs of heat exchange are adjusted, under the preferable case, the total sectional area that passes the heat exchanger tube 6 of each described heat exchanger fin 7 can account for the 10-50% of these heat exchanger fin 7 single face areas.
There is no particular limitation for the size of described heat exchanger tube 6, can select the heat exchanger tube size of various routines for use, and for example, the sectional area of described heat exchanger tube 6 can be the 10-100 square centimeter.
In addition, in described economizer 5, the density that described heat exchanger tube 6 is arranged can in very large range change, and under the preferable case, two adjacent in parallel multirow or multiple row heat exchanger tube distances capable or two row heat exchanger tubes can be 5-25 centimetre.
The denitrating flue gas equipment that provides according to the utility model, although the various devices that can be used to provide denitrfying agent all can be made described denitrfying agent feedway 2, but under the preferable case, described denitrfying agent feedway 2 is a pipeline, this pipeline passes the wall of flue 1, stretch in the flue 1, stretch on the pipeline in the flue 1 and be formed with opening.Denitrfying agent enters in the flue by this opening.
Further under the preferable case, described pipeline is many, for example is the 3-10 root.
Further under the preferable case, described many pipelines are along the axial or circumferential array of flue 1.
Further under the preferable case, described many pipelines are along the axially-aligned of flue 1 and radially evenly distributing along flue 1.
Further under the preferable case, the opening on every pipeline that stretches in the flue 1 is a plurality of, as 2-20.
Further under the preferable case, a plurality of openings on every pipeline that stretches in the flue 1 are along the axial distribution of described pipeline.
In order to make described denitrfying agent more abundant with contacting of flue gas, the direction of described opening is opposite with the direction of flow of flue gas in the flue 1, thus flue gas with contact in the same way from the described denitrfying agent of described denitrfying agent feedway 2 is non-, can better obtain denitration effect.
In the utility model, the direction of described opening is opposite with the direction of flow of flue gas in the flue 1 to be not absolute opposite, the direction that comprises described opening down, towards the situation of level or downward-sloping 1-15 °.
According to a kind of embodiment of the present utility model, the cross-sectional area of described flue 1 is 5000-50000 with the ratio of the gross area of the opening of the pipeline of described denitrfying agent feedway 2: 1, be preferably 20000-30000: 1.
According to another kind of embodiment of the present utility model, described denitrating flue gas equipment also comprises denitrfying agent source (not shown), for denitrfying agent feedway 2 provides denitrfying agent.Described denitrfying agent source for example can be denitrfying agent storage tank or pump.One end port of described denitrfying agent feedway 2 is communicated with the denitrfying agent source, and other end port then passes the wall of described flue 1 and stretches in the described flue 1.Denitrfying agent feedway 2 can a shared denitrfying agent source, also can be separately be communicated with different denitrfying agent source, provides denitrfying agent by different denitrfying agent sources.Described denitrfying agent can be various can with NO
xThereby reaction reduces NO in the flue gas
xThe reagent of content for example can be ammonia or the various material that can produce ammonia under the denitrating flue gas condition, as urea.Above-mentioned denitrfying agent preferably uses with the form of its aqueous solution, and the concentration of described solution has been conventionally known to one of skill in the art, the various concentration that can reach for denitrfying agent.In order to reduce the consumption of denitrfying agent, preferred described denitrfying agent uses with the form of its saturated solution.
According to the denitrating flue gas equipment that the utility model provides, described beds 4 is the catalyst bed that is formed by catalyst, and there is no particular limitation for the thickness of described beds 4, and under the preferable case, the thickness of described beds 4 can be 1.5-2 rice.Described catalyst can be various can catalytic denitration agent and nitrogen oxide NO
xReaction makes nitrogen oxide NO
xBe converted into the catalyst of nitrogen, be preferably metal oxide catalyst.For example, described metal oxide can be V
2O
5, Fe
2O
3, CuO, Cr
2O
3, Co
3O
4, NiO, CeO
2, La
2O
3, Pr
6O
11, Nd
2O
3, Gd
2O
3, Yb
2O
3In one or more, preferably contain V at least
2O
5The mixture of metal oxide.Further preferred described catalyst is to be dispersed in TiO
2Upward, with V
2O
5Be main active component, WO
3Or MoO
3Be the vanadium titanium system of co-catalyst, i.e. V
2O
5-WO
3/ TiO
2Or V
2O
5-MoO
3/ TiO
2Can be by above-mentioned metal oxide being fixed on the corrosion resistant plate surface or making the ceramic honey comb shape, form board-like catalyst or honeycombed catalyst and make described beds 4, and in described board-like catalyst or honeycombed catalyst, gross weight with described catalyst is a benchmark, and the content of described metal oxide is preferably 1-5 weight %.Above-mentioned catalyst can be commercially available, and for example can change into available from Japanese catalyst, the Cormetech company of Hitachi, Ltd, Germany refined robust and sturdy grand company and the U.S..
According to the denitrating flue gas equipment that the utility model provides, the lower end of the baffle plate 11 between the described horizontal segment b and the second vertical section c preferably closely contacts with the bottom of described horizontal segment b.Described baffle plate 11 can be made by stainless steel, copper or various alloy.
According to the denitrating flue gas equipment that the utility model provides, described bag wall superheater 8 is formed by metal tube.Described metal tube for example can be carbon steel pipe, stainless steel tube, copper pipe, titanium pipe or various metal alloy pipes etc.
The cross section of described flue 1 can be circle, ellipse, rectangle, square or various irregularly shaped.
In the utility model, the using method of described denitrating flue gas equipment comprises by denitrfying agent feedway 2 provides denitrfying agent in flue 1, make flue gas and denitrfying agent that the SNCR reaction take place in the first vertical section a, promptly carry out the SNCR denitration, flue gas after the SNCR denitration and unreacted denitrfying agent enter the second vertical section c after passing described horizontal segment b, after carrying out disturbance evenly by disturbance device 12, carry out heat exchange with the heat transferring medium in the economizer 5 in the second vertical section c, afterwards by beds 4, nitrogen oxide in the flue gas and unreacted denitrfying agent take place selective-catalytic-reduction denitrified in beds 4, obtain the flue gas that amount of nitrogen oxides further reduces, thereby finish the SNCR and the SCR combined denitration process of described flue gas.
The condition of described flue gas and the reaction of described denitrfying agent generation SNCR comprises that temperature is preferably 800-1300 ℃ more preferably 800-1100 ℃, is good with amino denitrfying agent, in the nitrogen element, and NO in nitrogen and the flue gas in the denitrfying agent
xThe mol ratio (be called for short ammonia nitrogen mol ratio) of nitrogen (in NO) can be 0.5-2: 1, be preferably 0.8-1.5: 1, the time that contacts under this temperature is preferably 0.1-2 second, more preferably 0.5-1 second.Thereby said temperature can utilize the temperature of this section flue gas itself to realize by the position of selecting described denitrfying agent to supply with, thereby need not extra heat supply or cooling.The temperature of above-mentioned SNCR needs strict control, and when temperature was higher than 1300 ℃, ammonia just was oxidized to NO
x, following reaction promptly takes place:
And when temperature was lower than 800 ℃, aforementioned SNCR was reflected under the catalyst-free existence and can not takes place.
The selective-catalytic-reduction denitrified condition of flue gas comprises that the condition that described nitrogen oxide is reduced to nitrogen comprises that temperature can be 280-420 ℃, is preferably 300-400 ℃, and the volume space velocity of flue gas can be 200-20000 hour
-1, be preferably 1000-10000 hour
-1
Obviously, by controlling denitrfying agent that described denitrfying agent feedway 2 supplies with respect to carry out SNCR reacting is excessive, can carry out SCR and SNCR reaction better simultaneously, therefore, improved the denitration rate with SNCR reacting phase ratio, compare under the situation that guarantees the denitration rate with the SCR reacting phase, reduced catalyst consumption, reduced cost.
Claims (13)
1. denitrating flue gas equipment, this equipment comprises the flue (1) that is surrounded by bag wall superheater (8), it is characterized in that,, be disposed with denitrfying agent feedway (2), disturbance device (12), economizer (5) and beds (4) in the flue (1) along the flow direction of flue gas; Flue (1) comprises first vertical section (a), second vertical section (c) and horizontal segment (b), the two ends of described horizontal segment (b) are communicated with the top of first vertical section (a) and second vertical section (b) respectively, denitrfying agent feedway (2) is positioned at first vertical section (a), economizer (5) and beds (4) are positioned at second vertical section (c), the collection case (9) of bag wall superheater (8) is positioned at the bottom of second vertical section (c), be provided with baffle plate (11) between second vertical section (c) and the horizontal segment (b), the collection case (9) of described bag wall superheater (8) is the 85-100% of the collection case (9) of described bag wall superheater (8) to the distance at the top of described baffle plate (11) to the distance at the top of described economizer (5); The ratio apart from B to the top is 10-25 to described denitrfying agent feedway (2) to the bottom of the distance A of the bottom of first vertical section (a) and described first vertical section (a): 30.
2. denitrating flue gas equipment according to claim 1 is characterized in that, described disturbance device (12) is positioned at described first vertical section (a) or horizontal segment (b).
3. denitrating flue gas equipment according to claim 2 is characterized in that, described disturbance device (12) is a tube, and this tube passes the wall of flue (1), and an end port is arranged in flue (10).
4. denitrating flue gas equipment according to claim 3 is characterized in that, described tube be arranged in flue (1) port towards becoming 70-90 ° with the flow of flue gas direction.
5. denitrating flue gas equipment according to claim 3, it is characterized in that, described 5-10 times of being arranged in the port of flue (1) and the thickness that the distance between the described beds (4) is described beds (4) for tube, wherein, port and the distance between the described beds (4) that described tube is arranged in flue (1) refer in the selective-catalytic-reduction denitrified course of reaction of flue gas, and the port that flue gas is arranged in flue (1) from described tube marches to the surperficial actual distance of passing by of beds (4).
6. according to claim 4 or 5 described denitrating flue gas equipment, it is characterized in that described tube is a plurality of.
7. denitrating flue gas equipment according to claim 6 is characterized in that, described a plurality of tubes are along the arranged radially of flue (1).
8. denitrating flue gas equipment according to claim 7 is characterized in that, the ratio of the gross area of the port that is arranged in flue (1) of the cross-sectional area of described flue (1) and described tube is 5000-50000: 1.
9. denitrating flue gas equipment according to claim 1 is characterized in that, this equipment also comprises disturbance medium generator, and disturbance medium generator is that disturbance device (1) provides the disturbance medium.
10. denitrating flue gas equipment according to claim 1, it is characterized in that, described economizer (5) comprises heat exchanger tube (6) and a plurality of heat exchanger fin (7), and described heat exchanger tube (6) passes described heat exchanger fin (7), and the outer wall of heat exchanger tube (6) closely contacts with heat exchanger fin (7).
11. denitrating flue gas equipment according to claim 10, it is characterized in that, each heat exchanger fin (7) comprises a plurality of plate bodys, this plate body have in groove and adjacent two plate bodys groove toward each other, the space that the shape of formation and heat exchanger tube (6) adapts, described heat exchanger tube (6) passes this space and closely contacts with heat exchanger fin (7).
12. according to claim 10 or 11 described denitrating flue gas equipment, it is characterized in that, a plurality of heat exchanger fins are arranged in parallel, and described heat exchanger tube (5) repeatedly passes a plurality of heat exchanger fins that are arranged in parallel (6) successively toward ground return, forms parallel multirow and parallel multiple row heat exchanger tube array.
13. according to claim 10 or 11 described denitrating flue gas equipment, it is characterized in that a plurality of heat exchanger fins (6) are arranged in parallel, described heat exchanger tube (5) is a plurality of, a plurality of heat exchanger tubes (5) pass a plurality of heat exchanger fins that are arranged in parallel (6) successively, form parallel multirow and parallel multiple row heat exchanger tube array.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011200602614U CN201997246U (en) | 2010-05-21 | 2011-03-09 | Smoke gas denitration equipment |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020206697 | 2010-05-21 | ||
| CN201020206697.5 | 2010-05-21 | ||
| CN2011200602614U CN201997246U (en) | 2010-05-21 | 2011-03-09 | Smoke gas denitration equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201997246U true CN201997246U (en) | 2011-10-05 |
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ID=43890254
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202597067U Expired - Lifetime CN201807299U (en) | 2010-05-21 | 2010-07-13 | Flue gas selective catalytic reduction denitrification equipment |
| CN2011200602614U Expired - Lifetime CN201997246U (en) | 2010-05-21 | 2011-03-09 | Smoke gas denitration equipment |
Family Applications Before (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202597067U Expired - Lifetime CN201807299U (en) | 2010-05-21 | 2010-07-13 | Flue gas selective catalytic reduction denitrification equipment |
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| Country | Link |
|---|---|
| CN (2) | CN201807299U (en) |
-
2010
- 2010-07-13 CN CN2010202597067U patent/CN201807299U/en not_active Expired - Lifetime
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- 2011-03-09 CN CN2011200602614U patent/CN201997246U/en not_active Expired - Lifetime
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| CN201807299U (en) | 2011-04-27 |
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