CN112237841A - SCR reactor and nitrogen oxide removal system - Google Patents
SCR reactor and nitrogen oxide removal system Download PDFInfo
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- CN112237841A CN112237841A CN202011276250.XA CN202011276250A CN112237841A CN 112237841 A CN112237841 A CN 112237841A CN 202011276250 A CN202011276250 A CN 202011276250A CN 112237841 A CN112237841 A CN 112237841A
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- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 title claims abstract description 51
- 239000003546 flue gas Substances 0.000 claims abstract description 51
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000003054 catalyst Substances 0.000 claims description 41
- 230000003197 catalytic effect Effects 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 238000010531 catalytic reduction reaction Methods 0.000 abstract description 3
- 238000009827 uniform distribution Methods 0.000 abstract description 3
- 238000010992 reflux Methods 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 description 11
- 238000005299 abrasion Methods 0.000 description 8
- 238000005452 bending Methods 0.000 description 7
- 238000009826 distribution Methods 0.000 description 7
- 239000010881 fly ash Substances 0.000 description 7
- 230000003068 static effect Effects 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 239000002956 ash Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 230000003116 impacting effect Effects 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000001364 causal effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention provides an SCR (selective catalytic reduction) reactor and a nitrogen oxide removal system, and relates to the technical field of nitrogen oxide removal. The SCR reactor provided by the invention effectively avoids the deflection of the flue gas entering the rectifying grating at the side caused by the excessively low height of the rectifying grating at the side close to the flue gas inlet of the reactor, even forms a reflux area, and realizes the uniform distribution of the flue gas in the reactor.
Description
Technical Field
The invention relates to the technical field of nitrogen oxide removal, in particular to an SCR (selective catalytic reduction) reactor and a nitrogen oxide removal system.
Background
Selective Catalytic Reduction (SCR) is the most efficient technology for removing nitrogen oxides, and is widely used in the industries of thermal power, steel and the like. The most core factor of the system is the catalyst, so in order to ensure the efficient, safe and stable operation of the catalyst, the flow field of the SCR system needs to be optimized, so that the flue gas is fully mixed and then uniformly enters the catalyst.
As shown in fig. 1 and 2, fig. 1 is a flow chart of flue gas in a reactor when a rectification grid is arranged at a low position in the prior art; FIG. 2 is a cloud view of the static pressure distribution of flue gas in a reactor when a rectifying grid is arranged at a low position in the prior art. The reactor rectifying grating is arranged in a low position, namely the upper surface of the rectifying grating is lower than the bottom surface of the inlet flue of the reactor. Flue outline, inside guide plate and rectification grid all according to actual size with 1: 1, establishing a proportion, and replacing a catalyst layer with a porous medium model.
As shown in FIG. 2, a low pressure zone exists near the front wall of the reactor 1, and the flue gas is inclined forward by the static pressure difference and even forms a reflux zone. In addition to causing unnecessary pressure loss, problems such as ash deposition and catalyst abrasion are caused. The catalyst inlet flow rate for this configuration was 30.5% relative standard deviation.
The above reactor has the following disadvantages:
1. the deposition of ash is serious:
as shown in fig. 2, the flue gas flow velocity in the area close to the front wall in the reactor arranged at the lower position of the flow-straightening grid 2 is suddenly reduced, the fly ash is very easy to deposit, if the ash viscosity is large or the flue gas is accompanied by large particle ash lumps, the mesh blockage of the filter screen in front of the catalyst corresponding to the area is easily caused, a mountain-peak-shaped ash bag is formed after the blockage is aggravated, and the height of a serious person can exceed one meter.
2. The abrasion is serious:
there is a causal relationship between catalyst plugging and attrition. When part of the catalyst channels are clogged and the total flue gas amount is constant, the flow velocity in the remaining catalyst channels is inevitably increased, and it is generally considered that the abrasion is accelerated when the flow velocity of the flue gas in the channels exceeds 5.5 m/s. Theoretically, the higher the concentration and kinetic energy of the fly ash, the higher the collision frequency with the catalyst, and the higher the abrasion speed of the catalyst. The wear rate can be expressed as:
T∝ημω3τ
t-abrasion loss, g/m 3;
eta-impact rate of fly ash impacting the heated surface;
μ -fly ash concentration, g/m 3;
omega-flue gas flow velocity, m/s;
τ -duration of action.
The abrasion of the catalyst is related to the included angle between the incoming smoke and the catalyst, besides the speed of the fly ash.
The acting force of a large amount of fly ash impacting the surface of the catalyst can be divided into normal component force and tangential component force, and the normal component force increases the internal energy of catalyst molecules, so that fine cracks are generated on the surface of the catalyst; the tangential force component has a cutting effect, the latter being the main contributing factor to wear.
According to the design rule of a denitration system, the included angle between the smoke flow line before entering the first layer of catalyst and the vertical direction is not more than 10 degrees, so that the tangential cutting force is reduced. Whereas the average inclination angle of the flow lines entering the catalyst layer in fig. 1 reached 34 °. Under the dual effects of high flue gas flow velocity and inclined scouring, the original catalyst monomer is worn through in a large area and then collapses.
In summary, the reactor with the rectification grids arranged at the lower position usually causes large-area accumulation of fly ash and severe abrasion of the catalyst due to the structural characteristics, which means that the amount of the catalyst actually participating in the denitration reaction may not meet the design value requirement. However, in order to ensure that the emission value of the chimney outlet does not exceed the standard, the concentration of nitrogen oxides can be reduced only by increasing the ammonia injection amount in many power plants, reducing agent waste is caused, air preheater blockage is caused, dust is hung on an electric bag, the bag is pasted, and the like, so that the operation cost of a unit is increased.
Therefore, how to provide an SCR reactor and a nitrogen oxide removal system that can effectively improve the uniformity of flue gas is one of the technical problems to be solved by those skilled in the art.
Disclosure of Invention
The invention aims to provide an SCR reactor and a nitrogen oxide removal system, which can realize uniform distribution of flue gas in the SCR reactor.
In order to achieve the purpose, the invention provides the following technical scheme:
in a first aspect, the invention provides an SCR reactor, which includes a reactor and a rectifying grid, wherein the reactor sequentially forms an inlet flue, a catalytic flue and an outlet flue from top to bottom, a first flow guide assembly is arranged in the inlet flue, the top surface of the rectifying grid is obliquely arranged in the rectifying grid, one side close to a reactor flue inlet is positioned on the bottom surface of the inlet flue, and one side far away from the reactor flue inlet is lower than the bottom surface of the inlet flue.
Further, the included angle between the top surface of the rectifying grating and the horizontal plane is 3-10 degrees.
Further, the included angle between the top surface of the rectifying grating and the horizontal plane is 5 degrees.
Further, the first flow guide assembly is provided with a plurality of flow guide channels, and the flow guide channels are uniformly distributed on the air inlet surface of the first flow guide assembly.
Further, along the flowing direction of the flue gas, the flow guide channel extends downwards in an inclined mode, and the included angle between the extending direction of the flow guide channel and the horizontal plane is 25-45 degrees.
Furthermore, a second flow guide assembly is arranged in the outlet flue and used for uniformly guiding the smoke in the outlet flue out of the smoke outlet of the outlet flue.
Further, the second guide assembly comprises a first guide plate and a second guide plate which are both arranged in the outlet flue, and the first guide plate and the second guide plate are distributed up and down.
Furthermore, the outlet flue is provided with a bending section, the bending section is positioned between the smoke inlet and the smoke outlet of the outlet flue, the first guide plate is positioned on the bending section, and the second guide plate is positioned at the smoke outlet of the outlet flue.
Furthermore, a first catalyst layer, a second catalyst layer and a third catalyst layer are sequentially arranged in the catalytic flue from top to bottom.
In a second aspect, the invention further provides a nitrogen oxide removal system, which comprises the SCR reactor in the above scheme.
The SCR reactor and the nitrogen oxide removal system provided by the invention can produce the following beneficial effects:
when the SCR reactor is used, flue gas enters the inlet flue from the flue inlet of the reactor, primary steering is realized through the first flow guide assembly, secondary steering is realized through the rectifying grating, and the flue gas is uniformly guided to the catalytic flue and is discharged from the outlet flue.
Compared with the prior art, in the SCR reactor provided by the first aspect of the invention, one side of the top surface of the rectifying grid, which is close to the flue gas inlet of the reactor, is raised, the side is positioned on the bottom surface of the inlet flue, and the side, which is far away from the flue gas inlet of the reactor, is lower than the bottom surface of the inlet flue, so that flue gas, which is originally easy to form a low-pressure area, in the inlet flue can quickly enter the rectifying grid on the bottom surface of the inlet flue, and a large turning direction does not need to be generated between the inlet flue and the catalytic flue, thereby effectively avoiding the deflection of the flue gas entering the rectifying grid on the side, even forming a backflow area, caused by the low.
The nitrogen oxide removal system provided by the second aspect of the present invention has the SCR reactor provided by the first aspect of the present invention, thereby having all the advantages of the SCR reactor provided by the first aspect of the present invention.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a flow diagram of flue gas in a reactor with a rectification grid arranged at a low position in the prior art;
FIG. 2 is a cloud view of static pressure distribution of flue gas in a reactor when a rectification grid is arranged at a low position in the prior art;
FIG. 3 is a flow diagram of flue gas in an SCR reactor according to an embodiment of the present invention;
fig. 4 is a cloud diagram of the static pressure distribution of flue gas in the SCR reactor according to an embodiment of the present invention.
Icon: 1-a reactor; 11-inlet flue; 12-a catalytic flue; 13-an outlet flue; 2-a rectifying grid; 3-a first flow guide assembly; 4-a second flow guide assembly; 41-a first baffle; 42-a second baffle; 5-a first catalyst layer; 6-a second catalyst layer; 7-third catalyst layer.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
FIG. 1 is a flow diagram of flue gas in a reactor with a rectification grid arranged at a low position in the prior art; FIG. 2 is a cloud view of static pressure distribution of flue gas in a reactor when a rectification grid is arranged at a low position in the prior art; FIG. 3 is a flow diagram of flue gas in an SCR reactor according to an embodiment of the present invention; fig. 4 is a cloud diagram of the static pressure distribution of flue gas in the SCR reactor according to an embodiment of the present invention.
An embodiment of the first aspect of the present invention provides an SCR reactor, as shown in fig. 3 and 4, including a reactor 1 and a rectifying grid 2, where the reactor 1 sequentially forms an inlet flue 11, a catalytic flue 12, and an outlet flue 13 from top to bottom, the inlet flue 11 is provided with a first flow guide assembly 3, the top surface of the rectifying grid 2 is obliquely arranged in the rectifying grid 2, and one side close to a flue inlet of the reactor 1 is located at the bottom surface of the inlet flue 11, and one side far away from the flue inlet of the reactor 1 is lower than the bottom surface of the inlet flue 11.
As shown in fig. 3, when the SCR reactor is used, flue gas enters the inlet flue 11 from the flue inlet of the reactor, is turned for the first time by the first flow guide assembly 3, is turned for the second time by the flow guide grid 2, is uniformly guided to the catalytic flue 12, and is discharged from the outlet flue 13.
As shown in fig. 1 and 2, in the prior art, a low pressure region exists near the front wall of the reactor 1, the flue gas inclines forward under the action of static pressure difference, and the included angle between the flue gas flow line before entering the first layer of catalyst and the vertical direction is larger, but in the SCR reactor provided by the first aspect of the invention, as shown in fig. 4, one side of the top surface of the rectifying grid near the flue gas inlet of the reactor is raised, the side is located at the bottom surface of the inlet flue, and the side far away from the flue gas inlet of the reactor is lower than the bottom surface of the inlet flue, so that the flue gas which originally easily forms a low pressure region in the inlet flue can quickly enter the rectifying grid at the bottom surface of the inlet flue, the air pressure is ensured to be stable, a larger steering direction does not need to be generated between the inlet flue and the catalytic flue, the deflection of the flue gas entering the rectifying grid at the side caused by, the uniform distribution of the flue gas in the SCR reactor is realized.
In some embodiments, as shown in fig. 4, the top surface of the straightening grate 2 is angled from 3 ° to 10 ° from the horizontal.
If the included angle between the top surface of the rectifying grating 2 and the horizontal plane is too small, the flow guiding effect is not good, the phenomenon of uneven smoke distribution still easily exists, and if the included angle is too large, the airflow is easily deflected reversely.
Specifically, the angle between the top surface of the straightening grate 2 and the horizontal plane is 3 °, 5 °, 8 ° or 10 °.
In at least one embodiment, the included angle between the top surface of the rectifying grid 2 and the horizontal plane is 5 degrees, so that the distribution of the flue gas in the reactor 1 is more uniform, and the problems of blockage of meshes of a filter screen in front of the catalyst, serious abrasion of the catalyst and the like are effectively relieved.
In some embodiments, the first flow guiding assembly 3 has a plurality of flow guiding channels, which are evenly distributed over the air intake surface of the first flow guiding assembly 3.
After the flue gas gets into entry flue 11, can pass through a plurality of diversion channels and get into rectification grid 2, a plurality of diversion channels have played the effect of a direction to flue gas in the entry flue 11 to because a plurality of diversion channels evenly distributed on the inlet face of first diversion subassembly 3, make the local resistance and the extension resistance unanimous of each interior air current of passageway, avoid the air current to flow to take place to incline by a wide margin.
In some embodiments, as shown in fig. 4, the flow guide channel extends obliquely downwards along the flow direction of the flue gas, and the extending direction of the flow guide channel forms an angle of 25-45 ° with the horizontal plane.
The included angle between the extending direction of the flow guide channel and the horizontal plane is 25-45 degrees, so that the flow direction of the airflow can be effectively and stably guided, the phenomenon that the airflow is unstable due to the fact that the airflow steering angle is too large due to too large inclination angle is avoided, and the phenomenon that the airflow cannot uniformly enter the rectifying grating 2 due to too small inclination angle is also avoided.
Specifically, the included angle between the extending direction of the flow guide channel and the horizontal plane is 25 degrees, 30 degrees, 35 degrees, 40 degrees or 45 degrees.
In some embodiments, as shown in fig. 3, in order to ensure that the outlet air of the reactor 1 is more stable, a second flow guide assembly 4 is disposed in the outlet flue 13, and the second flow guide assembly 4 is used for uniformly guiding the flue gas in the outlet flue 13 out of the flue outlet of the outlet flue 13.
As shown in fig. 3, the second flow guiding assembly 4 includes a first flow guiding plate 41 and a second flow guiding plate 42 both installed in the outlet flue 13, and the first flow guiding plate 41 and the second flow guiding plate 42 are distributed up and down. The two guide plates are arranged, so that the length of the flow guide path can be increased, and the uniform flow of the flue gas in the outlet flue 13 is ensured.
Specifically, as shown in fig. 3, the outlet flue 13 has a bent section, the bent section is located between the smoke inlet and the smoke outlet of the outlet flue 13, the first flow guide plate 41 is located at the bent section, and the second flow guide plate 42 is located at the smoke outlet of the outlet flue 13.
Because at the bending section department, the flow direction of flue gas changes, and first guide plate 41 can play the effect of water conservancy diversion, guarantees that the smooth process bending section of flue gas can not take place violent disturbance, and second guide plate 42 is located the play cigarette mouth department of outlet flue 13 and cooperates first guide plate 41 to use, can guarantee that the exhanst gas of outlet flue exhaust is even, stable.
The first baffle 41 has a plurality of baffle holes, and the extending direction of the baffle holes is the same as the bending direction of the bending section.
In some embodiments, as shown in fig. 3, a first catalyst layer 5, a second catalyst layer 6 and a third catalyst layer 7 are arranged in the catalytic flue 12 from top to bottom.
The flue gas passes through the first catalyst layer 5, the second catalyst layer 6 and the third catalyst layer 7 layer by layer, and each layer of catalyst reacts with the flue gas, so that nitrogen oxides in the flue gas can be effectively removed.
An embodiment of the second aspect of the present invention provides a nitrogen oxide removal system, which includes the SCR reactor.
Embodiments of the second aspect of the present invention provide a nitrogen oxide removal system having the SCR reactor of the first aspect of the present invention, thereby having all the advantages of the SCR reactor of the first aspect of the present invention.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. The utility model provides a SCR reactor, its characterized in that, includes reactor (1) and rectification grid (2), reactor (1) from top to bottom forms entry flue (11), catalytic flue (12) and export flue (13) in proper order, be equipped with first water conservancy diversion subassembly (3) in entry flue (11), the top surface of rectification grid (2) is in the slope sets up in rectification grid (2), and is close to one side that reactor (1) went into the mouth is located the bottom surface of entry flue (11), keeps away from one side that reactor (1) went into the mouth is less than the bottom surface of entry flue (11).
2. SCR reactor according to claim 1, characterized in that the angle between the top surface of the rectifying grid (2) and the horizontal plane is 3 ° -10 °.
3. SCR reactor according to claim 2, characterized in that the angle between the top surface of the rectifying grid (2) and the horizontal plane is 5 °.
4. An SCR reactor as claimed in claim 1, characterised in that the first flow guide assembly (3) has a plurality of flow guide channels which are evenly distributed over the air inlet face of the first flow guide assembly (3).
5. SCR reactor according to claim 4, wherein the flow guiding channels extend obliquely downwards in the flow direction of the flue gases and wherein the angle between the extension direction of the flow guiding channels and the horizontal plane is 25-45 °.
6. SCR reactor according to claim 4, characterized in that a second flow guiding assembly (4) is arranged in the outlet flue (13), and the second flow guiding assembly (4) is used for guiding the flue gas in the outlet flue (13) out of the flue outlet of the outlet flue (13) uniformly.
7. An SCR reactor as claimed in claim 6, wherein the second flow guiding assembly (4) comprises a first flow guiding plate (41) and a second flow guiding plate (42) both mounted in the outlet flue (13), the first flow guiding plate (41) and the second flow guiding plate (42) being distributed above and below.
8. SCR reactor according to claim 7, wherein the outlet flue (13) has a bend between the inlet and outlet of the outlet flue (13), the first baffle (41) being located at the bend and the second baffle (42) being located at the outlet of the outlet flue (13).
9. SCR reactor according to claim 8, characterized in that a first catalyst layer (5), a second catalyst layer (6) and a third catalyst layer (7) are arranged in the catalytic flue (12) from top to bottom in sequence.
10. A nitrogen oxide removal system comprising an SCR reactor according to any one of claims 1 to 9.
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| CN202011276250.XA CN112237841A (en) | 2020-11-16 | 2020-11-16 | SCR reactor and nitrogen oxide removal system |
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| CN205216584U (en) * | 2015-11-30 | 2016-05-11 | 武汉凯迪电力环保有限公司 | SCR (selective catalytic reduction) denitration device |
| CN106178948A (en) * | 2016-08-25 | 2016-12-07 | 国网河南省电力公司电力科学研究院 | A kind of Novel SCR denitrating system based on the escaping of ammonia catalytic eliminating |
| CN106731789A (en) * | 2016-12-05 | 2017-05-31 | 北京工业大学 | A kind of efficient SCR denitration reactor |
| CN107303467A (en) * | 2016-04-22 | 2017-10-31 | 湖北强达环保科技股份有限公司 | A kind of SCR denitration reactor |
| CN214020115U (en) * | 2020-11-16 | 2021-08-24 | 华润电力(唐山曹妃甸)有限公司 | SCR reactor and nitrogen oxide removal system |
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2020
- 2020-11-16 CN CN202011276250.XA patent/CN112237841A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP2420309A1 (en) * | 2010-08-19 | 2012-02-22 | Alstom Technology Ltd | A gas cleaning system having a gas flow rectifier |
| CN102350215A (en) * | 2011-07-15 | 2012-02-15 | 无锡华光新动力环保科技股份有限公司 | Multi-field uniform selective catalytic reduction (SCR) flue gas denitration apparatus |
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