CN201807306U - Flue gas denitrification device - Google Patents
Flue gas denitrification device Download PDFInfo
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- CN201807306U CN201807306U CN2010202599630U CN201020259963U CN201807306U CN 201807306 U CN201807306 U CN 201807306U CN 2010202599630 U CN2010202599630 U CN 2010202599630U CN 201020259963 U CN201020259963 U CN 201020259963U CN 201807306 U CN201807306 U CN 201807306U
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- heat exchanger
- flue gas
- vertical section
- exchanger tube
- gas equipment
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 239000003546 flue gas Substances 0.000 title claims abstract description 67
- 230000003197 catalytic effect Effects 0.000 claims abstract description 15
- 239000003795 chemical substances by application Substances 0.000 claims description 45
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 239000003054 catalyst Substances 0.000 abstract description 16
- 238000000034 method Methods 0.000 abstract description 8
- 238000010531 catalytic reduction reaction Methods 0.000 abstract description 4
- 238000006722 reduction reaction Methods 0.000 abstract description 4
- 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 18
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 10
- 238000005516 engineering process Methods 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- 229910010413 TiO 2 Inorganic materials 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002184 metal Substances 0.000 description 4
- 239000010935 stainless steel Substances 0.000 description 3
- 229910001220 stainless steel Inorganic materials 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 241000264877 Hippospongia communis Species 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 239000004202 carbamide Substances 0.000 description 2
- 239000000919 ceramic Substances 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
- 230000000694 effects Effects 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000004706 metal oxides Chemical class 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 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
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000010962 carbon steel 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
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 229910001092 metal group alloy Inorganic materials 0.000 description 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000012047 saturated solution Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000126 substance 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
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model provides a flue gas denitrification device, which is characterized in that the distance from a header (10) of a wall enclosure superheater (9) to the top of an economizer (3) is 85-100% a distance from the header (10) of the wall enclosure superheater (9) to the top of a baffle plate (8). Space below the economizer (3) is enlarged as far as possible, while the side of the economizer (3) is not directly flushed by flue gas, a catalytic reactor (11) is connected to the bottom of a second vertical section (6) of a flue (1), thereby a selective non-catalyst reduction (SNCR) process and a selective catalytic reduction (SCR) process are carried out simultaneously, the denitrification efficiency is increased as compared with the SNCR, and compared with the SCR, consumption of catalyst is reduced and cost is reduced, while the denitrification efficiency is guaranteed.
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
xAs 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 before discharging through denitrogenation (being denitration).
At present, the gas denitrifying technology of utilization comparative maturity mainly contains two kinds: SCR (SCR) technology and SNCR denitration (SNCR) technology.The chemical principle of SCR and SNCR denitrating technique all is the same, all be in flue gas, to spray into denitrfying agent (urea or ammonia), in specific temperature range with flue gas in NO
xCarry out the selective reduction reaction and generate nitrogen (N
2) and steam (H
2O).
SNCR technology generally sprays into denitrfying agent in the burner hearth of 800-1300 ℃ of boiler, denitrfying agent (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
2And discharge and flue gas after denitrfying agent contacts O).The problem that SNCR technology exists is that the efficient of denitration is low, and the denitration efficiency of general SNCR denitration technology is below 40%.
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.The denitration efficiency of SCR technology is higher relatively than SNCR, generally can reach 50-60%.
And although SCR denitration effect good than SNCR technology, as mentioned above, the denitration rate of SCR also only is below 60%, remains further to be improved.Though can improve the denitration rate of SCR a little by the thickness of further raising beds,, can cause cost significantly to improve because catalyst is relatively more expensive.
In addition, as mentioned above, SNCR carries out at 800-1300 ℃, the temperature of flue gas is generally more than 800 ℃ even 1000 ℃ after the denitration, in order to realize the cooling of flue gas, at present common way is that flue is surrounded by a plurality of metal tubes (also claiming bag wall superheater) of interior dress demineralized water, and the 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, and beds is usually located at the bottom of flue afterbody and collection case.Set up an economizer (being heat exchanger) on the other hand behind the SNCR of the rear portion of flue, economizer is formed by a plurality of heat exchanger tubes that are connected in series mutually.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.
Although can reduce the temperature of flue gas behind the SNCR to a certain extent by metal tube and existing economizer,, the temperature of SNCR flue gas is still up to more than 500 ℃.High like this smog discharge temperature does not meet environmental requirement on the one hand, and on the other hand, flue gas is also taken away a large amount of heats, is unfavorable for the utilization again of the energy.And this setup that beds is arranged on collection case bottom not only can be caused the beds out-of-flatness, also can cause beds inconsistent with collection box foundation position and other position temperature, thereby whole reaction bed temperature skewness damages beds easily.
The utility model content
The purpose of this utility model is in order to overcome the shortcoming that the denitration rate is low, economizer is bulky and beds destroys easily that existing denitrating flue gas equipment exists, a kind of denitration rate height to be provided, the economizer volume is little and is not easy to cause the ruined denitrating flue gas equipment of beds.
In order to improve the efficient of denitration, inventor of the present utility model attempts the amount by used denitrfying agent among the direct increase SNCR, yet is surprised to find that, though the amount of denitrfying agent obviously increases but the nitrogen oxide NO in the flue gas
xAmount not only do not reduce on the contrary and rise to some extent, this may be because ammonia has been oxidized to NO
x
In order to address the above problem, inventor of the present utility model has carried out a large amount of research, proposes a kind of equipment that SNCR and SCR can be combined, and this equipment can improve to realize SNCR and SCR process simultaneously on the basis of equipment at existing SNCR.
The utility model provides a kind of denitrating flue gas equipment, this equipment comprises the flue that is surrounded by bag wall superheater, flow direction along flue gas, be disposed with denitrfying agent feedway and economizer in the flue, wherein, described 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, described denitrfying agent feedway is positioned at first vertical section, economizer is 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 baffle plate top to the distance at the top of described economizer; This equipment also comprises catalytic reactor, and this catalytic reactor is communicated with the bottom of second vertical section.
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, and pass through to connect catalytic reactor in the bottom of flue second vertical section, thereby SNCR and SCR process have been realized simultaneously, improved denitration efficiency with SNCR reacting phase ratio, compare under the situation that guarantees denitration efficiency with the SCR reacting phase, reduce catalyst consumption, reduced cost.
Description of drawings
The structural representation of the denitrating flue gas equipment that Fig. 1 provides for the utility model;
Fig. 2 is the structural representation of economizer in the denitrating flue gas equipment in a kind of embodiment of the present utility model;
Fig. 3 is the structural representation of the heat exchanger fin of economizer in the denitrating flue gas equipment in a kind of embodiment of the present utility model;
Fig. 4 is the structural representation of the heat exchanger fin of economizer in the denitrating flue gas equipment in the another kind of embodiment of the present utility model.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is described in detail.
As shown in Figure 1, the utility model provides a kind of denitrating flue gas equipment, this equipment comprises the flue 1 that is surrounded by bag wall superheater 9, flow direction along flue gas, be disposed with denitrfying agent feedway 2 and economizer 3 in the flue, wherein, described flue 1 comprises first vertical section 5, second vertical section 6 and horizontal segment 7, the two ends of described horizontal segment 7 are communicated with the top of first vertical section 5 and second vertical section 6 respectively, described denitrfying agent feedway 2 is positioned at first vertical section 5, economizer 3 is positioned at second vertical section 6, the collection case 10 of bag wall superheater 9 is positioned at the bottom of second vertical section 6, be provided with baffle plate 8 between second vertical section 6 and the horizontal segment 7, the collection case 10 of described bag wall superheater is the 85-100% of the collection case 10 of described bag wall superheater to the distance at baffle plate 8 tops to the distance at the top of described economizer 3; This equipment also comprises catalytic reactor 11, and this catalytic reactor 11 is communicated with the bottom of second vertical section 6.
According to the denitrating flue gas equipment that the utility model provides, the lower end of the baffle plate 8 that is provided with between second vertical section 6 and the horizontal segment 7 preferably closely contacts with the bottom of described horizontal segment 7.Described baffle plate 8 can be made by stainless steel, copper or various alloy.
Described catalytic reactor 11 can be the various selective-catalytic-reduction denitrified reactors of flue gas that can be used in, specifically can select according to the form of catalyst, for example, when described catalyst uses with the beds form, described catalytic reactor 11 can have the tank reactor in hole or slit for the bottom, the sidewall of tank reactor is connected with the bottom sidewall of second vertical section 6 of flue 1, and beds 4 places the bottom of catalytic reactor 1.The thickness of described beds 4 can in very large range change, and is preferably 1.5-2.0 rice.
Wherein said 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.Described metal oxide such as 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, preferred V
2O
5Further 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
2Preferred described beds 4 is with above-mentioned V
2O
5-WO
3/ TiO
2Or V
2O
5-MoO
3/ TiO
2Catalyst is fixed on the corrosion resistant plate surface or makes the ceramic honey comb shape, forms the version of stainless steel corrugated plate dst and ceramic honey comb.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..
In a kind of preferred implementation, the collection case 10 of described bag wall superheater is that the collection case 10 of described bag wall superheater is to 100% of the distance at baffle plate 8 tops to the distance at the top of described economizer 3, be that the top of economizer 3 and the top of baffle plate 8 maintain an equal level, can make the volume maximization under the economizer 3 like this, so that use.
Described economizer 3 can be the various heat exchangers that can be used in heat exchange, in order under the situation that guarantees heat exchange efficiency, further to dwindle the volume of economizer 3, under the preferable case, described economizer 3 comprises heat exchanger tube 12 and a plurality of heat exchanger fin 13, described heat exchanger tube 12 passes described heat exchanger fin 13, and the outer wall of heat exchanger tube 12 closely contacts with heat exchanger fin 13.
The structure of described heat exchanger fin can change according to the needs of heat exchange and the size of heat exchanger tube, for example, as shown in Figure 3, is formed with the space of mating with the size of described heat exchanger tube 12 on the described heat exchanger fin 13.
As shown in Figure 4, in another embodiment, each heat exchanger fin 13 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 12 adapts, described heat exchanger tube 12 passes this space and closely contacts with heat exchanger fin 13.
As shown in Figure 2, in a kind of preferred implementation, described a plurality of heat exchanger fins 13 are arranged in parallel, and more than 12 past ground return of described heat exchanger tube passes a plurality of heat exchanger fins that are arranged in parallel 13 successively, forms the parallel multirow and the heat exchanger tube array of multiple row.
In another kind of preferred implementation, described a plurality of heat exchanger fins 13 are arranged in parallel, and described heat exchanger tube 12 is a plurality of, and a plurality of heat exchanger tubes 12 pass a plurality of heat exchanger fins that are arranged in parallel 13 successively, form the parallel multirow and the heat exchanger tube array of multiple row.
In the utility model, the quantity of heat exchanger fin 13 can in very large range change in the described economizer 3, 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 13 can be the 10-20% of single file or single-row heat exchanger tube 12 length, under the preferred situation, the distance of two adjacent heat exchanger fins 13 can be 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 13, and the thickness of each heat exchanger fin 13 can be 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel 13.
In the utility model, the size of described heat exchanger fin 13 can in very large range change, the needs that can be size according to the needs of heat exchange are adjusted, and under the preferable case, the total sectional area that passes the heat exchanger tube 12 of each described heat exchanger fin 13 can account for the 10-50% of these heat exchanger fin 13 single face areas.There is no particular limitation for the size of described heat exchanger tube 12, can select the heat exchanger tube size of various routines for use, and for example, the sectional area of described heat exchanger tube 12 can be the 10-100 square centimeter.
In addition, in described economizer 3, the density that described heat exchanger tube 12 is arranged can in very large range change, and under the preferable case, two adjacent in parallel multirow or the heat exchanger tube of multiple row 12 distances capable or two heat exchanger tubes 12 that are listed as can be 5-25 centimetre.
In a kind of preferred implementation of the present utility model, described heat exchanger tube 12 forms integrative-structure with a plurality of heat exchanger fins 13.
According to the utility model, the SNCR that described denitrfying agent feedway 2 is positioned at described flue is the SNCR district.Under the preferable case, the top of the distance A of the bottom of described denitrfying agent feedway 2 to first vertical sections 5 and denitrfying agent feedway 2 and first vertical section 5 to the bottom apart from satisfying A: B=10-25 between the B: 30, preferred A: B=15-23: 30.
According to the utility model, described denitrfying agent feedway 2 can be the various devices that denitrfying agent is provided that can be used in, under the preferable case, described denitrfying agent feedway 2 is a pipeline, this pipeline passes the wall of flue 1, stretches in the flue 1, stretches on the pipeline in the flue 1 to be formed with opening.Under the preferable case, described pipeline can be for a plurality of, and the opening on every pipeline that stretches in the flue 1 can be for a plurality of.
A kind of preferred embodiment in, described a plurality of pipelines along flue 1 axially or circumferential array, under the preferred situation, a plurality of openings on every pipeline that stretches in the flue 1 are along the axial distribution of described pipeline.For denitrfying agent is better contacted with flue gas, the direction of described opening is preferably opposite with the direction of flow of flue gas in the flue 1.
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.
In the described denitrfying agent feedway 2, the other end of described pipeline is communicated with the denitrfying agent source.Described denitrfying agent source can be the denitrfying agent storage tank, 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.Described 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.
In the utility model, described flue 1 is surrounded by bag wall superheater 9, can feed heat exchange medium in the bag wall superheater 9, thereby can make full use of the heat in the flue gas.Under the preferable case, described bag wall superheater 9 for example can be carbon steel pipe, stainless steel tube, copper pipe, titanium pipe or various metal alloy pipes etc.
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 first vertical section 5, promptly carry out the SNCR denitration, flue gas after the SNCR denitration and residual denitrfying agent enter second vertical section 6 after passing described horizontal segment 7, carry out heat exchange with the heat transferring medium in the economizer 3 in second vertical section 6, afterwards by the beds 4 in the hydrogen-catalyst reactor 11, nitrogen oxide in the flue gas and residual denitrfying agent further take place selective-catalytic-reduction denitrified under the effect of 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 0.3-2: 1, be preferably 0.5-1.5: 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, 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) can be 0.5-1.1: 1, be preferably 0.7-1: 1.
In preferred embodiment, the denitrfying agent that described denitrfying agent feedway 2 is supplied with is excessive with respect to carrying out that SNCR reacts, to carry out SCR and SNCR reaction better simultaneously.
The collection case 10 of the utility model by making bag wall superheater 9 is the 85-100% that the collection case 10 of described bag wall superheater 9 arrives the distance at baffle plate 8 tops to the distance at the top of described economizer 3, guaranteeing under the situation that economizer 3 sides are not directly washed away by flue gas, can make the space of economizer 3 belows big as far as possible, and pass through to connect catalytic reactor 11 in the bottom of flue 1 second vertical section 6, thereby SNCR and SCR process have been realized simultaneously, improved denitration efficiency with SNCR reacting phase ratio, compare under the situation that guarantees denitration efficiency with the SCR reacting phase, reduce catalyst consumption, reduced cost.
Claims (14)
1. denitrating flue gas equipment, this equipment comprises the flue (1) that is surrounded by bag wall superheater (9), flow direction along flue gas, be disposed with denitrfying agent feedway (2) and economizer (3) in the flue, it is characterized in that, described flue (1) comprises first vertical section (5), second vertical section (6) and horizontal segment (7), the two ends of described horizontal segment (7) are communicated with the top of first vertical section (5) and second vertical section (6) respectively, described denitrfying agent feedway (2) is positioned at first vertical section (5), economizer (3) is positioned at second vertical section (6), the collection case (10) of bag wall superheater (9) is positioned at the bottom of second vertical section (6), be provided with baffle plate (8) between second vertical section (6) and the horizontal segment (7), the collection case (10) of described bag wall superheater is the 85-100% of the collection case (10) of described bag wall superheater to the distance at baffle plate (8) top to the distance at the top of described economizer (3); This equipment also comprises catalytic reactor (11), and this catalytic reactor (11) is communicated with the bottom of second vertical section (6).
2. denitrating flue gas equipment according to claim 1, it is characterized in that, described economizer (3) comprises heat exchanger tube (12) and a plurality of heat exchanger fin (13), and described heat exchanger tube (12) passes described heat exchanger fin (13), and the outer wall of heat exchanger tube (12) closely contacts with heat exchanger fin (13).
3. denitrating flue gas equipment according to claim 2, it is characterized in that, each heat exchanger fin (13) 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 (12) adapts, described heat exchanger tube (12) passes this space and closely contacts with heat exchanger fin (13).
4. according to claim 2 or 3 described denitrating flue gas equipment, it is characterized in that, described a plurality of heat exchanger fin (13) is arranged in parallel, and described heat exchanger tube (12) repeatedly passes a plurality of heat exchanger fins that are arranged in parallel (13) successively toward ground return, forms the parallel multirow and the heat exchanger tube array of multiple row.
5. denitrating flue gas equipment according to claim 4 is characterized in that, two adjacent in parallel multirow or the multiple row heat exchanger tube (11) distances capable or two row heat exchanger tubes (11) are 5-25 centimetre.
6. according to claim 2 or 3 described denitrating flue gas equipment, it is characterized in that, described a plurality of heat exchanger fin (13) is arranged in parallel, described heat exchanger tube (12) is a plurality of, a plurality of heat exchanger tubes (12) pass a plurality of heat exchanger fins that are arranged in parallel (13) successively, form the parallel multirow and the heat exchanger tube array of multiple row.
7. denitrating flue gas equipment according to claim 6 is characterized in that, two adjacent in parallel multirow or the multiple row heat exchanger tube (11) distances capable or two row heat exchanger tubes (11) are 5-25 centimetre.
8. according to claim 2 or 3 described denitrating flue gas equipment, it is characterized in that the gross thickness of a plurality of heat exchanger fins that are arranged in parallel (13) is the 10-20% of single file or single-row heat exchanger tube length.
9. denitrating flue gas equipment according to claim 8, it is characterized in that, the distance of two adjacent heat exchanger fins is 1-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (13), and the thickness of each heat exchanger fin is 0.5-5 centimetre in a plurality of heat exchanger fins that are arranged in parallel (13).
10. according to claim 2 or 3 described denitrating flue gas equipment, it is characterized in that the total sectional area that passes the heat exchanger tube (12) of each described heat exchanger fin (13) accounts for the 10-50% of this heat exchanger fin single face area.
11. denitrating flue gas equipment according to claim 10 is characterized in that, the sectional area of each heat exchanger tube (12) is the 10-100 square centimeter.
12. denitrating flue gas equipment according to claim 1 is characterized in that, denitrfying agent feedway (2) to the top of the distance A of the bottom of first vertical section (5) and first vertical section (5) to the bottom apart from satisfying A: B=10-25 between the B: 30.
13. denitrating flue gas equipment according to claim 1 is characterized in that, described denitrfying agent feedway (2) is a pipeline, and this pipeline passes the wall of flue (1), stretches in the flue, stretches on the pipeline in the flue to be formed with opening; Described pipeline is a plurality of, and the opening on every pipeline that stretches in the flue (1) is a plurality of, described a plurality of pipelines along flue (1) axially or circumferential array; A plurality of openings on every pipeline that stretches in the flue (1) are along the axial distribution of described pipeline, and the direction of described opening is opposite with the direction of flow of flue gas in the flue.
14. denitrating flue gas equipment according to claim 1 is characterized in that, beds (4) is housed in the described catalytic reactor (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202599630U CN201807306U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitrification device |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201020210385 | 2010-05-21 | ||
| CN201020210385.1 | 2010-05-21 | ||
| CN2010202599630U CN201807306U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitrification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201807306U true CN201807306U (en) | 2011-04-27 |
Family
ID=43890256
Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202599630U Expired - Lifetime CN201807306U (en) | 2010-05-21 | 2010-07-13 | Flue gas denitrification device |
| CN2010202597090U Expired - Lifetime CN201807301U (en) | 2010-05-21 | 2010-07-13 | Smoke denitration equipment |
Family Applications After (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010202597090U Expired - Lifetime CN201807301U (en) | 2010-05-21 | 2010-07-13 | Smoke denitration equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (2) | CN201807306U (en) |
-
2010
- 2010-07-13 CN CN2010202599630U patent/CN201807306U/en not_active Expired - Lifetime
- 2010-07-13 CN CN2010202597090U patent/CN201807301U/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CN201807301U (en) | 2011-04-27 |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20110427 |