CN114367180B - Oxidation reaction device and method for flue gas NOx - Google Patents
Oxidation reaction device and method for flue gas NOx Download PDFInfo
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- CN114367180B CN114367180B CN202111642714.9A CN202111642714A CN114367180B CN 114367180 B CN114367180 B CN 114367180B CN 202111642714 A CN202111642714 A CN 202111642714A CN 114367180 B CN114367180 B CN 114367180B
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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
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
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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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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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
- B01D53/8628—Processes characterised by a specific catalyst
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- 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
Abstract
The invention provides an oxidation reaction device and method for flue gas NOx, wherein the oxidation reaction device comprises a reactor shell and at least one group of NOx oxidation reaction units; the NOx oxidation reaction unit comprises a guide plate and a catalytic oxidation unit; the catalytic oxidation unit comprises two groups of reaction pipelines which are oppositely arranged; the reaction pipeline comprises an oxidant conveying pipeline and a catalyst powder conveying pipeline. When the oxidation reaction device provided by the invention is adopted, the movement stroke of the flue gas is increased through the guide plate, and the contact time of the flue gas and the reaction substances is prolonged; the oxidant and the catalyst are conveyed through the oxidant conveying pipeline and the catalyst powder conveying pipeline, the flue gas, the oxidant and the catalyst are fully mixed, and efficient denitration is achieved.
Description
Technical Field
The invention belongs to the technical field of atmospheric treatment, relates to a flue gas oxidation reaction device, and particularly relates to an oxidation reaction device and method for flue gas NOx.
Background
Industrial boilers are important thermal power plants for power plants. At present, coal is one of the main energy sources, and a large amount of nitrogen oxides (NOx) and sulfur dioxide (SO) are generated in the combustion process of the coal in an industrial boiler 2 ) And dust. Wherein NOx and SO 2 Is a harmful atmospheric environmental pollutant, can cause negative effects on human bodies, animals, plants and the environment, and dust can cause PM2.5 index increase, thereby causing air quality reduction. The contents of nitrogen oxides and sulfur dioxide in the flue gas discharged by a power plant in various places in China have specific requirements, and the flue gas of a boiler needs to be denitrated and desulfurized to reach relevant standards before being discharged.
At present, the denitration method mainly adopts a selective catalytic reduction denitration method (SCR) and a selective non-catalytic reduction denitration method (SNCR). The selective catalytic reduction denitration method is mature in process, high in denitration efficiency and dominant in practical application. The selective catalytic reduction denitration method needs to adopt an SCR catalyst, and the actual service time of the SCR catalyst is usually shorter than the theoretical operation time because of the reasons of alkali metal poisoning, blockage, sintering, abrasion and the like caused by dust in flue gas, so that the cost of the SCR catalyst becomes one of the main components of a denitration system of a power plant.
Through introducing denitration preprocessing device, can reduce catalyst load, extension catalyst live time reduces nitrogen oxide, sulfur dioxide and the dust content in the final emission flue gas simultaneously, improves the environmental protection index of discharging the flue gas. The wet combined desulfurization and denitrification has the advantages of stable operation and simple technology, and can be applied to a denitrification pretreatment device. Because about 95% of NOx in the flue gas is NO with low solubility, the NOx is difficult to absorb and remove directly, and the flue gas, the oxidant and the catalyst need to be fully mixed in the NOx oxidation reactor to oxidize the NO into NO with higher solubility 2 And N 2 O 5 。
CN 105749748A discloses a desulfurization and denitrification integrated device, which comprises a top bin, a shell, an ammonia spraying header pipe, a denitrification chamber, an air inlet, an air outlet, a discharge valve and a support, wherein the shell is divided into an upper denitrification area, a middle buffer area and a lower desulfurization area by an upper annular baffle plate and a lower annular baffle plate, the denitrification area and the sulfur area are divided into different chambers by an inverted truncated hollow cone and a truncated hollow cone, and the denitrification area is sequentially provided with a clean flue gas outlet chamber, a denitrification chamber and a denitrification inlet chamber from outside to inside; the bowl removing area is sequentially provided with a desulfurization inlet chamber, a desulfurization chamber and a bowl removing outlet chamber from outside to inside: the desulfurization chamber is communicated with the denitration chamber through a blanking pipe of the buffer area, and the desulfurization gas outlet chamber is communicated with the denitration gas inlet chamber through a vortex ammonia mixing chamber of the buffer area. Although the activated carbon purification technology has a removal effect on various pollutants, particularly has an obvious effect on removing sulfur dioxide, high denitration rate is difficult to realize, and the purification of flue gas has to be carried out at low space velocity. The process of the active coke is adopted, and the space velocity is usually 300-500h -1 Left and right, make whole equipment huge, equipment investment and operation cost high, the active carbon consumption is big, and the material consumption cost is high, and the denitration rate is difficult to satisfy the requirement.
CN107511064A discloses a desulfurization and denitrification device based on activated carbon and low temperature catalyst, including sack cleaner, smoke chamber, fluidization chamber and the cyclone that communicates in proper order, wherein the bottom of smoke chamber is equipped with the toper ash bucket and communicates ammonia source and high-speed air current source. The carrier of the low-temperature catalyst is activated carbon which is in a fluidized state, so that flue gas is fully contacted with the low-temperature catalyst and the activated carbon, desulfurization and denitrification are realized in one step, and meanwhile, the activated carbon and the activated carbon serving as the carrier of the low-temperature catalyst do not need to be separated in the later stage and can be used as the carrier of the low-temperature catalyst after retreatment. However, the desulfurization and denitrification efficiency of the desulfurization and denitrification apparatus is not high enough.
CN 203803374U discloses a wet catalytic oxidation denitration device, which comprises a catalytic oxidation reaction furnace, a flue gas supply system for feeding treated flue gas into the catalytic oxidation reaction furnace, an oxidant supply system and a reaction product collection system; a carrying plate for placing a catalyst carrier is arranged in the catalytic oxidation reaction furnace, and a catalyst carrier replacing door is arranged on the side wall of the carrying plate; the oxidant supply system comprises an oxidant conveying pipe and a spraying device, wherein the oxidant conveying pipe is used for conveying liquid oxidant into the catalytic oxidation reaction furnace, the spraying device is used for spraying the liquid oxidant onto the catalyst carrier, and the oxidant conveying pipe is provided with a booster pump; the flue gas supply system comprises a flue gas conveying pipeline, and a supercharging device and a heating device are arranged on the flue gas conveying pipeline of the flue gas conveying pipeline; the reaction product collecting system comprises a collecting bottle and a reaction product discharge pipe provided with a temperature reduction device. In the wet catalytic oxidation denitration process, the flue gas, the oxidant and the catalyst are not sufficiently mixed, so that the NO oxidation rate is not high, and the low denitration efficiency of the wet absorption process is caused.
In summary, the objective of increasing the oxidation rate of NO and increasing the denitration efficiency by increasing the mixing degree of the flue gas, the oxidant and the catalyst is provided, which is one of the problems to be solved in the art.
Disclosure of Invention
The invention aims to provide an oxidation reaction device and method for flue gas NOx. When the oxidation reaction device is used, the movement stroke of the flue gas is increased through the guide plate, and the contact time of the flue gas and the reaction substances is increased; the oxidant and the catalyst are conveyed through the oxidant conveying pipeline and the catalyst powder conveying pipeline, the flue gas, the oxidant and the catalyst are fully mixed, and efficient denitration is achieved.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides an oxidation reaction device for flue gas NOx, which includes a reactor housing and at least one group of NOx oxidation reaction units;
the NOx oxidation reaction unit comprises a guide plate and a catalytic oxidation unit;
the catalytic oxidation unit comprises two groups of reaction pipelines which are oppositely arranged;
the reaction pipeline comprises an oxidant conveying pipeline and a catalyst powder conveying pipeline.
According to the invention, the movement stroke of the flue gas is increased through the NOx oxidation reaction unit, the contact time of the flue gas and the reaction substances is increased, the flue gas, the oxidant and the catalyst are fully mixed, and the denitration efficiency is further improved.
Preferably, the baffles comprise a first baffle and a second baffle.
Preferably, the first flow guide plate comprises a first fixing plate, a first flow guide plate and a second flow guide plate.
Preferably, the second flow guide plate comprises a second fixing plate, a third flow guide plate and a fourth flow guide plate.
Preferably, the first fixing plate and the second fixing plate are respectively and independently fixedly arranged on the side wall of the reactor shell.
The first guide plates and the second guide plates are arranged in a staggered mode, and the first guide plates and the second guide plates jointly form an NOx oxidation reaction unit, so that the flowing direction of flue gas is controlled, the moving stroke of the flue gas is further increased, the contact time of the flue gas and reaction substances is prolonged, and efficient denitration of the flue gas is realized.
If two or more groups of NOx oxidation reaction units are arranged in the oxidation reaction device for the NOx in the flue gas, the fixed plate in the front group of the two adjacent groups of NOx oxidation reaction units is used as the fixed plate in the rear group. The structure scheme can save the inner space of the device and control the flue gas circulation path.
Preferably, the angle between the first fixing plate and the side wall of the reactor housing is 50-90 °, for example, 50 °, 55 °, 60 °, 65 °, 70 °, 75 °, 80 °, 85 ° or 90 °, but not limited to the values listed, and other values not listed in the numerical range are also applicable.
Preferably, the angle between the second fixing plate and the side wall of the reactor housing is 50-90 °, for example, 50 °, 55 °, 60 °, 65 °, 70 °, 75 °, 80 °, 85 ° or 90 °, but not limited to the values listed, and other values not listed in the numerical range are also applicable.
The included angle between the fixed plate and the side wall of the reactor shell is specifically the angle formed by the fixed plate and the side wall of the reactor shell after the fixed plate is inclined downwards.
Preferably, the first flow-guiding plate is disposed perpendicular to the ground at an end point of the first fixing plate away from the side wall.
Preferably, the third flow-guiding plate is disposed perpendicular to the ground at an end point of the second fixing plate away from the side wall.
Preferably, the second flow-guide plate is disposed between the first flow-guide plate and the third flow-guide plate perpendicular to the ground.
Preferably, the fourth drainage plate is disposed between the first and second drainage plates perpendicular to the ground.
According to the invention, the first drainage plate and the second drainage plate are fixedly arranged above the first fixing plate, and the third drainage plate and the fourth drainage plate are fixedly arranged below the second fixing plate. The first drainage plate, the second drainage plate, the third drainage plate and the fourth drainage plate are arranged in the same space in a crossed mode to form a flue gas circulation line, and therefore the circulation line of flue gas is controlled.
Preferably, the distance between the two groups of reaction tubes is 20-60cm, for example 20cm, 25cm, 30cm, 35cm, 40cm, 45cm, 50cm, 55cm or 60cm, but is not limited to the values listed, and other values not listed in the range of values are equally applicable.
Preferably, the reaction tubes are arranged parallel to the ground between the first flow-guide plate and the side wall of the reactor shell.
Preferably, the oxidant delivery pipeline is provided with an oxidant atomization nozzle.
Preferably, the catalyst powder conveying pipeline is provided with a catalyst powder nozzle.
Preferably, the number of oxidant atomizer nozzles and catalyst powder nozzles is the same.
Preferably, the oxidant delivery conduits and the catalyst powder delivery conduits are arranged alternately in parallel to the reaction plate.
The NOx oxidation reaction unit provided by the invention is provided with two groups of reaction tubes which are arranged oppositely, and catalyst powder nozzles and oxidant atomizing nozzles arranged on the reaction tubes are arranged oppositely in pairs; catalyst powder spout and two liang of staggered arrangements of oxidant atomizer on same one side reaction tube can make catalyst and oxidant pass through the speed that the velocity direction is opposite totally and spray catalyst powder and oxidant simultaneously, reaches the purpose of catalyst and oxidant intensive mixing, realizes the promotion of denitration efficiency.
Preferably, each interval between the first drainage plate, the second drainage plate, the third drainage plate and the fourth drainage plate and the side wall of the reactor shell meets the following formula:
D1≥D2≥D3≥D4
in the formula, D1 is the distance between the first drainage plate and the side wall of the outer shell of the reactor; d2 is the distance between the first drainage plate and the fourth drainage plate; d3 is the distance between the fourth drainage plate and the second drainage plate; d4 is the distance between the second drainage plate and the third drainage plate.
Preferably, the following formula is satisfied at each interval between the first drainage plate, the second drainage plate, the third drainage plate, the fourth drainage plate, the first fixing plate and the second fixing plate:
L1≥L2≥L3≥L4
in the formula, L1 is the distance between the first drainage plate and the second fixing plate, L2 is the distance between the fourth drainage plate and the first fixing plate, L3 is the distance between the second drainage plate and the second fixing plate, and L4 is the distance between the third drainage plate and the first fixing plate.
The distances between the drainage plates and the side walls and between the drainage plates and the fixing plates are different, so that the section of the flue gas is continuously changed from large to small when the flue gas flows through the guide plates from the catalytic oxidation unit, and the change frequency of the flue gas speed is continuously increased until the next catalytic oxidation unit. The mixing effect is enhanced through the change of the speed size and the speed change frequency, and the denitration efficiency is improved.
In a second aspect, the present invention provides a method performed by using the oxidation reaction device for flue gas NOx provided in the first aspect, the method comprising the steps of:
and after the flue gas containing NOx is pretreated, introducing the flue gas into the oxidation reaction device for the NOx in the flue gas, and simultaneously carrying out oxidation treatment and catalytic treatment for at least one time to obtain the purified flue gas.
Preferably, the pretreatment comprises preheating and electrostatic dust removal which are sequentially carried out;
preferably, the temperature of the preheated flue gas is 120-160 ℃, for example 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃, 155 ℃ or 160 ℃, but is not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, the flow velocity of the flue gas is between 5 and 8m/s, for example 5m/s, 6m/s, 7m/s or 8m/s, but is not limited to the values listed, and other values not listed in the range of values are equally applicable.
Preferably, the catalyst powder used in the catalytic treatment process comprises Fe 2 O 3 、MnO、TiO 2 Or CuO, or a combination of at least two of them, a typical but non-limiting combination including Fe 2 O 3 In combination with MnO, mnO and TiO 2 Combinations of (A) and (B), tiO 2 And CuO, fe 2 O 3 MnO and TiO 2 Combination of MnO and TiO 2 And CuO, or Fe 2 O 3 、MnO、TiO 2 And CuO.
Preferably, the catalyst powder has an average particle size of 60 to 80 μm, for example, 60 μm, 62 μm, 64 μm, 66 μm, 68 μm, 70 μm, 72 μm, 74 μm, 76 μm, 78 μm or 80 μm, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, the catalyst powder is sprayed at a velocity of 10 to 15m/s, for example 10m/s, 11m/s, 12m/s, 13m/s, 14m/s or 15m/s, but not limited to the values listed, and other values not listed in the numerical range are equally applicable.
Preferably, the oxidant liquid used in the oxidation treatment process comprises H 2 O 2 、KMnO 4 NaClO or NaClO 2 Any one or a combination of at least two of the above, typical but not limiting combinations include H 2 O 2 、 KMnO 4 Combination of (1), H 2 O 2 、KMnO 4 And NaClO, KMnO 4 And NaClO, naClO and NaClO 2 Combination of (1), H 2 O 2 And NaClO 2 Combination of (1), H 2 O 2 、KMnO 4 And NaClO 2 A combination of (A) or (H) 2 O 2 、KMnO 4 NaClO and NaClO 2 A combination of (a) and (b).
The oxidant liquid atomizes the oxidant into fog drops with the volume median diameter of 80-100 mu m by the injection of the oxidant atomizing nozzle.
Because the particle sizes of the catalyst powder and the oxidant fog drops are close and the particle size of the oxidant fog drops is slightly larger than that of the catalyst powder, the oxidant fog drops can be better coated on the surface of the catalyst powder in the spraying process, and simultaneously have larger contact specific surface area, thereby being beneficial to promoting the oxidation-reduction reaction.
Preferably, the flow rate of the oxidant liquid is 10-15m/s, and may be, for example, 10m/s, 11m/s, 12m/s, 13m/s, 14m/s or 15m/s, but is not limited to the values recited, and other values not recited within the range of values are equally applicable.
According to the invention, the mixing uniformity among the oxidant, the catalyst powder and the flue gas is optimized by controlling the flow rates of the oxidant, the catalyst powder and the flue gas, and the aim of improving the denitration efficiency is achieved by improving the NO oxidation efficiency.
As a preferred technical solution of the present invention, the method provided by the second aspect of the present invention is performed by using the oxidation reaction device for flue gas NOx provided by the first aspect, and the method includes the following steps:
preheating flue gas containing NOx to 120-160 ℃, introducing the flue gas into the oxidation reaction device for the NOx in the flue gas at a flow speed of 5-8m/s after electrostatic dust collection, and simultaneously carrying out oxidation treatment and catalytic treatment at least once to obtain purified flue gas; the average grain diameter of the catalyst powder adopted in the catalysis process is 60-80 μm; the spraying speed is 10-15m/s; the flow velocity of the oxidant in the oxidation process is 10-15m/s.
The recitation of numerical ranges herein includes not only the above-recited numerical values, but also any numerical values between non-recited numerical ranges, and is not intended to be exhaustive or to limit the invention to the precise numerical values encompassed within the range for brevity and clarity.
Compared with the prior art, the invention has the following beneficial effects:
(1) The oxidation reaction device for the flue gas NOx, which is provided by the invention, has a simple structure, can improve the mixing uniformity of solid catalyst powder, a liquid oxidant and gaseous flue gas, and improve the NO oxidation efficiency, so that the denitration efficiency is improved;
(2) The oxidation reaction device for the flue gas NOx can prolong the service life of the catalyst and reduce the annual average investment cost of the denitration catalyst;
(3) The catalytic oxidation denitration process performed by adopting the oxidation reaction device for the flue gas NOx provided by the invention has good economic benefit and environmental protection benefit.
Drawings
FIG. 1 is a schematic structural diagram of an oxidation reaction device for flue gas NOx provided in embodiment 1 of the present invention;
FIG. 2 is a front view of a reaction channel provided in example 1 of the present invention;
fig. 3 is a schematic size diagram provided in embodiment 1 of the present invention.
The device comprises a reactor shell 1, an oxidant conveying pipeline 2-1, a catalyst powder conveying pipeline 2-2, an oxidant atomizing nozzle 2-3, a catalyst powder nozzle 2-4, a first fixing plate 3-1, a first flow guide plate 3-2, a second flow guide plate 3-3, a second fixing plate 4-1, a third flow guide plate 4-2 and a fourth flow guide plate 4-3, wherein the reactor shell is a reactor shell, the catalyst powder nozzle 2-1, the first flow guide plate 3-1, the third flow guide plate 4-2 and the fourth flow guide plate 4-3.
Detailed Description
The technical solution of the present invention is further described below by way of specific embodiments. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitations of the present invention.
Example 1
The embodiment provides an oxidation reaction device for flue gas NOx as shown in FIG. 1, which comprises a reactor shell 1 and four groups of NOx oxidation reaction units;
the NOx oxidation reaction unit comprises a guide plate and a catalytic oxidation unit; the catalytic oxidation unit comprises two groups of reaction pipelines 2 which are oppositely arranged; the reaction pipeline comprises an oxidant conveying pipeline 2-1 and a catalyst powder conveying pipeline 2-2.
The baffle comprises a first baffle and a second baffle; the first guide plate comprises a first fixing plate 3-1, a first drainage plate 3-2 and a second drainage plate 3-3; the second guide plate comprises a second fixing plate 4-1, a third drainage plate 4-2 and a fourth drainage plate 4-3; the first fixing plate 3-1 and the second fixing plate 4-1 are respectively and independently fixed on the side wall of the reactor shell 1.
The included angle between the first fixing plate 3-1 and the side wall of the reactor shell 1 is 75 degrees; the included angle between the second fixing plate 4-1 and the side wall of the reactor shell 1 is 75 degrees.
The first drainage plate 3-2 is arranged at the end point of the first fixing plate 3-1 far away from the side wall of the reactor shell 1, and is vertical to the ground; the third drainage plate 4-2 is arranged at the end point of the second fixing plate 4-1 far away from the side wall of the reactor shell 1, and is vertical to the ground; the second drainage plate 3-3 is arranged between the first drainage plate 3-2 and the third drainage plate 4-2 and is vertical to the ground; the fourth drainage plate 4-3 is arranged between the first drainage plate 3-2 and the second drainage plate 3-3 and is perpendicular to the ground.
The distance between the two groups of reaction pipelines is 40cm;
the reaction pipeline is arranged between the first drainage plate 3-2 and the side wall of the reactor shell 1 in parallel to the ground; as shown in fig. 2, an oxidant atomization nozzle 2-3 is arranged on the oxidant delivery pipe 2-1; the catalyst powder conveying pipeline 2-2 is provided with a catalyst powder nozzle 2-4; the number of the oxidant atomizing nozzles 2-3 is the same as that of the catalyst powder nozzles 2-4; the oxidant conveying pipelines 2-1 and the catalyst powder conveying pipelines 2-2 are alternately arranged in parallel.
The distances among the first drainage plate 3-2, the second drainage plate 3-3, the third drainage plate 4-2, the fourth drainage plate 4-3 and the side wall of the reactor shell 1 satisfy the following formula:
D1≥D2≥D3≥D4
as shown in FIG. 3, D1 is the distance between the first flow-guiding plate 3-2 and the side wall of the reactor shell 1; d2 is the distance between the first drainage plate 3-2 and the fourth drainage plate 4-3; d3 is the distance between the fourth drainage plate 4-3 and the second drainage plate 3-3; d4 is the distance between the second drainage plate 3-3 and the third drainage plate 4-2.
In addition, in this embodiment, the relationship among D1, D2, D3, and D4 is: D1/D2= D2/D3= D3/D4=1.5.
The distances among the first drainage plate 3-2, the second drainage plate 3-3, the third drainage plate 4-2, the fourth drainage plate 4-3, the first fixing plate 3-1 and the second fixing plate 4-1 satisfy the following formula:
L1≥L2≥L3≥L4
as shown in FIG. 3, in the formula, L1 is the distance between the first drainage plate 3-2 and the second fixing plate 4-1, L2 is the distance between the fourth drainage plate 4-3 and the first fixing plate 3-1, L3 is the distance between the second drainage plate 3-3 and the second fixing plate 4-1, and L4 is the distance between the third drainage plate 4-2 and the first fixing plate 3-1.
In this embodiment, the relationship among L1, L2, L3, and L4 is: L1/L2= L2/L3= L3/L4=1.5.
Example 2
This example provides an oxidation reaction device for flue gas NOx, which differs from example 1 only in that: the present embodiment is provided with a group of NOx oxidation reaction units.
Example 3
This example provides an oxidation reaction apparatus for NOx, which differs from example 1 only in that: in this embodiment, the included angle between the first fixing plate 3-1 and the side wall of the reactor shell 1 is 90 degrees; the included angle between the second fixing plate 4-1 and the side wall of the reactor shell 1 is 90 degrees.
Example 4
This example provides an oxidation reaction apparatus for NOx, which differs from example 1 only in that: in this embodiment, the included angle between the first fixing plate 3-1 and the side wall of the reactor shell 1 is 60 degrees; the included angle between the second fixing plate 4-1 and the side wall of the reactor shell 1 is 60 degrees.
Example 5
This example provides an oxidation reaction apparatus for NOx, which differs from example 1 only in that: in this embodiment, the included angle between the first fixing plate 3-1 and the side wall of the reactor shell 1 is 30 degrees; the included angle between the second fixing plate 4-1 and the side wall of the reactor shell 1 is 30 degrees.
Example 6
This example provides an oxidation reaction apparatus for NOx, which differs from example 1 only in that: the relationship among D1, D2, D3 and D4 is changed as follows: D1/D2= D2/D3= D3/D4=1.2; the relationship among L1, L2, L3 and L4 is changed as follows: L1/L2= L2/L3= L3/L4=1.2.
Example 7
This example provides an oxidation reaction apparatus for NOx, which differs from example 1 only in that: the relationship among D1, D2, D3 and D4 is changed as follows: D1/D2= D2/D3= D3/D4=0.9; the relationship among L1, L2, L3 and L4 is changed as follows: L1/L2= L2/L3= L3/L4=0.9.
Application example 1
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, the method including the steps of:
preheating flue gas containing NOx to 140 ℃, introducing the flue gas into the oxidation reaction device for the flue gas NOx at the flow speed of 6m/s after electrostatic dust collection, and simultaneously carrying out oxidation treatment and catalytic treatment at least once to obtain purified flue gas; the catalyst powder Fe adopted in the catalytic process 2 O 3 Has an average particle diameter of 70 μm; the spraying speed is 12m/s; oxidizing agent H in the oxidation process 2 O 2 The flow velocity of (2) is 12m/s.
Application example 2
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 2, which is the same as application example 1.
Application example 3
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 3, which is the same as application example 1.
Application example 4
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 4, which is the same as application example 1.
Application example 5
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 5, which is the same as application example 1.
Application example 6
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 6, which is the same as application example 1.
Application example 7
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in example 7, which is the same as application example 1.
Application example 8
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, the method including the steps of:
preheating flue gas containing NOx to 120 ℃, introducing the flue gas into the oxidation reaction device for the flue gas NOx at the flow speed of 5m/s after electrostatic dust collection, and simultaneously carrying out oxidation treatment and catalytic treatment at least once to obtain purified flue gas; the catalyst powder TiO adopted in the catalytic process 2 Has an average particle diameter of 60 μm; the spraying speed is 10m/s; the oxidizing agent KMnO in the oxidation process 4 The flow velocity of (2) is 10m/s.
Application example 9
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, the method including the steps of:
preheating the flue gas containing NOx to 160 ℃, introducing the flue gas into the oxidation reaction device for the flue gas NOx at the flow speed of 8m/s after electrostatic dust collection, and simultaneously carrying out oxidation treatment and catalytic treatment at least once to obtain the purified flue gas; the average particle size of catalyst powder CuO adopted in the catalysis process is 80 μm; the spraying speed is 15m/s; the flow rate of the oxidant NaClO in the oxidation process is 15m/s.
Application example 10
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, which differs from application example 1 in that: the temperature of the flue gas preheat containing NOx is changed to 100 ℃.
Application example 11
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, which differs from application example 1 in that: the temperature of the flue gas preheat containing NOx is changed to 200 ℃.
Application example 12
The present application example provides a method performed using the oxidation reaction apparatus for NOx provided in embodiment 1, which differs from application example 1 in that: the flow velocity of the flue gas containing NOx was changed to 10m/s.
The flue gas containing NOx and the treated flue gas provided in application examples 1 to 12 were introduced into a flue gas analyzer, the change in NOx concentration in the flue gas before and after the reaction was measured, and the removal efficiency was calculated, the results of which are shown in table 1.
TABLE 1
In conclusion, when the oxidation reaction device provided by the invention is adopted, the movement stroke of the flue gas is increased through the guide plate, and the contact time of the flue gas and the reaction substances is increased; the oxidant and the catalyst are conveyed through the oxidant conveying pipeline and the catalyst powder conveying pipeline, the flue gas, the oxidant and the catalyst are fully mixed, and efficient denitration is achieved.
The applicant declares that the above description is only a specific embodiment of the present invention, but the scope of the present invention is not limited thereto, and it should be understood by those skilled in the art that any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are within the scope and disclosure of the present invention.
Claims (17)
1. The oxidation reaction device for the NOx in the flue gas is characterized by comprising a reactor shell and at least two groups of NOx oxidation reaction units;
the NOx oxidation reaction unit comprises a guide plate and a catalytic oxidation unit;
the baffles comprise a first baffle and a second baffle;
the first guide plate comprises a first fixed plate, a first drainage plate and a second drainage plate;
the second guide plate comprises a second fixing plate, a third drainage plate and a fourth drainage plate;
the first fixing plate and the second fixing plate are respectively and independently fixedly arranged on the side wall of the reactor shell;
the first drainage plate is arranged at the end point of the first fixing plate far away from the side wall of the reactor shell, and is vertical to the ground;
the third drainage plate is arranged at the end point of the second fixing plate far away from the side wall of the reactor shell, and is vertical to the ground;
the second drainage plate is arranged between the first drainage plate and the third drainage plate and is vertical to the ground;
the fourth drainage plate is arranged between the first drainage plate and the second drainage plate and is vertical to the ground;
the first drainage plate and the second drainage plate are fixedly arranged above the first fixing plate, and the third drainage plate and the fourth drainage plate are fixedly arranged below the second fixing plate; the first drainage plate, the second drainage plate, the third drainage plate and the fourth drainage plate are arranged in the same space in a crossed manner to form a flue gas circulation line;
the second fixed plate in the former group of the two adjacent groups of the NOx oxidation reaction units is used as the first fixed plate in the latter group;
the catalytic oxidation unit comprises two groups of reaction pipelines which are oppositely arranged; the reaction pipeline is arranged between the first drainage plate and the side wall of the reactor shell in parallel to the ground;
the reaction pipeline comprises an oxidant conveying pipeline and a catalyst powder conveying pipeline;
the oxidant conveying pipelines and the catalyst powder conveying pipelines are alternately arranged in parallel.
2. The oxidation reaction device for flue gas NOx as claimed in claim 1, wherein the first retaining plate is angled at 50-90 ° to the side wall of the reactor housing.
3. The oxidation reaction device for flue gas NOx of claim 1, wherein the angle between the second retaining plate and the side wall of the reactor housing is 50-90 °.
4. The oxidation reaction device for flue gas NOx as claimed in claim 1, wherein the spacing between the two sets of reaction tubes is 20-60cm.
5. The oxidation reaction device for flue gas NOx of claim 1, wherein the oxidant delivery conduit is provided with an oxidant atomizer;
and the catalyst powder conveying pipeline is provided with a catalyst powder nozzle.
6. The oxidation reaction device for flue gas NOx of claim 5, wherein the number of oxidant atomizer nozzles and catalyst powder nozzles is the same.
7. The oxidation reaction device for flue gas NOx of claim 1, wherein the respective distances between the first flow guide plate, the second flow guide plate, the third flow guide plate, the fourth flow guide plate and the side wall of the reactor shell satisfy the following formula:
D1≥D2≥D3≥D4
in the formula, D1 is the distance between the first drainage plate and the side wall of the outer shell of the reactor; d2 is the distance between the first drainage plate and the fourth drainage plate; d3 is the distance between the fourth drainage plate and the second drainage plate; d4 is the distance between the second drainage plate and the third drainage plate.
8. The oxidation reaction device for flue gas NOx of claim 1, wherein the respective distances between the first flow guide plate, the second flow guide plate, the third flow guide plate, the fourth flow guide plate, the first fixing plate and the second fixing plate satisfy the following formula:
L1≥L2≥L3≥L4
in the formula, L1 is the distance between the first drainage plate and the second fixing plate, L2 is the distance between the fourth drainage plate and the first fixing plate, L3 is the distance between the second drainage plate and the second fixing plate, and L4 is the distance between the third drainage plate and the first fixing plate.
9. A method carried out with the oxidation reaction device for flue gas NOx according to any one of claims 1 to 8, characterized in that it comprises the following steps:
after the flue gas containing NOx is pretreated, introducing the flue gas into the oxidation reaction device for the flue gas NOx, and simultaneously carrying out oxidation treatment and catalytic treatment to obtain the purified flue gas.
10. The method of claim 9, wherein the pre-treatment comprises a pre-heating and an electrostatic precipitation in sequence.
11. The method of claim 10, wherein the temperature of the preheated flue gas is 120-160 ℃.
12. The method according to claim 9, wherein the flow velocity of the flue gas is 5-8m/s.
13. The method of claim 9, wherein the catalyst powder used in the catalytic treatment process comprises Fe 2 O 3 、MnO、TiO 2 Or CuO, or a combination of at least two thereof.
14. The method of claim 13, wherein the catalyst powder has an average particle size of 60-80 μm.
15. The method according to claim 13, wherein the injection velocity of the catalyst powder is 10-15m/s.
16. The method of claim 9 wherein the oxidizer liquid used in the oxidation process comprises H 2 O 2 、KMnO 4 NaClO or NaClO 2 Any one or a combination of at least two of them.
17. The method according to claim 16, wherein the flow rate of the oxidant liquid is 10-15m/s.
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| CN103463978B (en) * | 2013-09-30 | 2016-03-02 | 南京理工大学 | Based on the device and method of catalytic oxidation of hydrogen peroxide flue gas and desulfurizing and denitrifying |
| CN203803374U (en) * | 2014-01-28 | 2014-09-03 | 西安科技大学 | Catalytic wet air oxidation desulfurization and denitrification device |
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