CN114367192A - Denitration reaction pretreatment device system and pretreatment method - Google Patents

Denitration reaction pretreatment device system and pretreatment method Download PDF

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CN114367192A
CN114367192A CN202111633093.8A CN202111633093A CN114367192A CN 114367192 A CN114367192 A CN 114367192A CN 202111633093 A CN202111633093 A CN 202111633093A CN 114367192 A CN114367192 A CN 114367192A
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flue gas
temperature
denitration
nox
heat exchanger
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谷朋泰
邓志成
汪勇
丁刚
孙猛
方超
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Shanghai Power Equipment Research Institute Co Ltd
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Shanghai Power Equipment Research Institute Co Ltd
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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
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1412—Controlling the absorption process
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1456—Removing acid components
    • 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
    • B01D53/14—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 by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/346—Controlling the process
    • 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
    • B01D53/88—Handling or mounting catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C1/00—Magnetic separation
    • B03C1/02—Magnetic separation acting directly on the substance being separated
    • B03C1/30—Combinations with other devices, not otherwise provided for
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/017—Combinations of electrostatic separation with other processes, not otherwise provided for
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/08—Arrangements of devices for treating smoke or fumes of heaters
    • 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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  • Chemical Kinetics & Catalysis (AREA)
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  • Biomedical Technology (AREA)
  • Treating Waste Gases (AREA)
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Abstract

The invention provides a denitration reaction pretreatment device system and a pretreatment method, wherein the denitration reaction pretreatment device system comprises a heat exchanger, a NOx oxidation reactor, an electrostatic dust collector, a NOx absorption reactor and a first three-way flue gas flow controller which are sequentially connected and arranged according to the flowing direction of high-temperature flue gas; the solid powder outlet of the electrostatic dust collector is connected with the magnetic separator; and a flue gas heat exchange port of the first three-way flue gas flow controller is connected with the heat exchanger. The device system provided by the invention can obviously reduce the concentration of NOx in the flue gas at the inlet of the SCR denitration system, and greatly reduces the load of the denitration catalyst; meanwhile, by reducing the concentration of dust in the flue gas, the failure phenomenon of the catalyst caused by alkali metal poisoning, blockage, sintering, abrasion and the like caused by the dust in the flue gas is relieved, and the service life of the SCR catalyst is prolonged.

Description

Denitration reaction pretreatment device system and pretreatment method
Technical Field
The invention belongs to the technical field of atmospheric treatment, and particularly relates to a denitration reaction pretreatment device system and a pretreatment method.
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 boiler2) And dust. Wherein NOx and SO2Is 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.
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. Wherein, the wet method combined desulfurization and denitrification has the advantages of stable operation and simple technology,can be applied to a denitration 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 solubility2And N2O5。
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 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 space velocity of the adopted active coke is usually 300-500h-1Left 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 SOx/NOx control device based on active carbon and low temperature catalyst, including sack cleaner, smoke chamber, fluidization room and the cyclone that communicates in proper order, wherein the bottom of smoke chamber is equipped with the toper ash bucket and communicates ammonia water 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, wherein a supercharging device and a heating device are arranged on 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.
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 use of selective catalytic reduction denitration requires the use of a catalyst. However, the service life of the catalyst is obviously influenced by the phenomena of alkali metal poisoning, blockage, sintering, abrasion and the like caused by dust in flue gas, and the actual service time is often shorter than the theoretical operation time. Meanwhile, the content of NOx in the flue gas at the inlet of an SCR denitration system of some thermal power plants is high, so that the catalyst is in a heavy-load working state for a long time, and the service life of the SCR denitration catalyst is further influenced. Because SCR denitration catalyst is expensive, account for SCR denitration system cost specific gravity big, it has important meaning to reduce the power plant running cost to improve SCR denitration catalyst life-span.
Disclosure of Invention
The invention aims to provide a denitration reaction pretreatment device system and a pretreatment method, wherein the denitration reaction pretreatment device system greatly reduces the load of a denitration catalyst by remarkably reducing the concentration of NOx in flue gas at the inlet of an SCR denitration system; meanwhile, by reducing the concentration of dust in the flue gas, the failure phenomenon of the catalyst caused by alkali metal poisoning, blockage, sintering, abrasion and the like caused by the dust in the flue gas is relieved, the service life of the SCR catalyst is prolonged, and the annual investment cost of the denitration catalyst of the thermal power plant is reduced. In addition, the pretreatment device system of the denitration reactor provided by the invention ensures that the temperature of the flue gas in the NOx oxidation reactor is in the optimal working temperature range of the catalyst by utilizing the self heat exchange of the flue gas, ensures the denitration efficiency of the system, and avoids extra equipment cost and energy loss caused by introducing external heating or cooling equipment. Has the advantages of environmental protection, energy conservation, high denitration efficiency and good economic benefit.
In order to achieve the purpose, the invention adopts the following technical scheme:
according to a first aspect, the invention provides a denitration reaction pretreatment device system, which comprises a heat exchanger, a NOx oxidation reactor, an electrostatic dust collector, a NOx absorption reactor and a first three-way flue gas flow controller, wherein the heat exchanger, the NOx oxidation reactor, the electrostatic dust collector, the NOx absorption reactor and the first three-way flue gas flow controller are sequentially connected and arranged in the flowing direction of high-temperature flue gas;
the solid powder outlet of the electrostatic dust collector is connected with the magnetic separator;
and a flue gas heat exchange port of the first three-way flue gas flow controller is connected with the heat exchanger.
The denitration reaction pretreatment device system provided by the invention reduces the concentration of NOx in the flue gas at the inlet of the SCR denitration system through oxidation catalytic reaction and denitration and desulfurization reaction, thereby greatly reducing the load of a denitration catalyst.
The electrostatic precipitator is used for capturing catalyst powder and fly ash in flue gas leaving a NOx oxidation reactor; the magnetic separator is used for separating the catalyst powder, removing the fly ash, conveying the separated catalyst solid powder into the catalyst powder storage tank, completing the circulation of the catalyst powder for one time, and preparing to convey the catalyst solid powder into the catalyst powder nozzle for the next catalyst powder circulation. Therefore, the catalyst powder is recycled, and the pretreatment cost is reduced.
Preferably, the high-temperature flue gas inlet of the heat exchanger is connected with a first flue gas flowmeter.
Preferably, a first temperature measuring device is arranged at a high-temperature flue gas inlet of the heat exchanger.
Preferably, the cold flow outlet of the heat exchanger is connected with a second three-way flue gas flow controller.
Preferably, a flue gas mixer is arranged between the heat exchanger and the NOx oxidation reactor.
Preferably, a second temperature measuring device is arranged between the flue gas mixer and the NOx oxidation reactor.
Preferably, a fourth temperature measuring device is arranged at the cold flow outlet of the heat exchanger.
The heat source of the heat exchanger is high-temperature flue gas from an industrial boiler, the cold source is flue gas passing through the NOx absorption reactor, the heat exchanger and the NOx absorption reactor realize primary heat exchange, and the temperature of the high-temperature flue gas at the inlet of the NOx oxidation reactor is reduced to be within the optimal temperature range for the operation of the catalyst. Because the direct heat exchange that the flue gas itself converges in the flue gas blender is utilized, an external heating or cooling device is not needed, the energy loss caused by external heating or cooling is avoided, and an additional device related to external heating or cooling is also avoided.
Preferably, the catalyst powder inlet of the NOx oxidation reactor is connected to a catalyst powder storage tank by a blower.
Preferably, the catalyst powder reservoir is connected to the outlet of the magnetic separator.
Preferably, the oxidant inlet of the NOx oxidation reactor is connected to the oxidant solution storage tank by an oxidant delivery pump.
Preferably, a liquid level detector is arranged inside the oxidant solution storage tank.
The device system of the invention carries out catalytic oxidation reaction on high-temperature flue gas through the NOx oxidation reactor.
Preferably, the flue gas outlet of the second three-way flue gas flow controller is connected with the flue gas mixer through a third flue gas flow meter.
Preferably, a second flue gas flowmeter is arranged between the flue gas heat exchange port of the first three-way flue gas flow controller and the heat exchanger.
Preferably, a third temperature measuring device is arranged at the outlet of the second flue gas flow meter.
The invention realizes secondary heat exchange by converging the flue gas passing through the heat exchanger and the flue gas passing through the NOx absorption reactor in the flue gas mixer, further reduces the temperature of high-temperature flue gas at the inlet of the NOx oxidation reactor, and ensures that the temperature of the high-temperature flue gas is in the optimal temperature range of the operation of the catalyst. Because the direct heat exchange that the flue gas itself converges in the flue gas blender is utilized, an external heating or cooling device is not needed, the energy loss caused by external heating or cooling is avoided, and an additional device related to external heating or cooling is also avoided.
Preferably, the NOx absorption reactor is placed in a thermostatic waterbath apparatus.
Preferably, an electric stirring device is provided inside the NOx absorption reactor.
Preferably, a pH value monitoring device is arranged in the NOx absorption reactor.
The invention promotes the reaction to be carried out efficiently by controlling key parameters such as constant temperature water bath temperature, electric stirring speed, pH value, absorbent concentration and the like.
Preferably, a reaction liquid outlet of the NOx absorption reactor is connected with a circulating standby reaction liquid storage tank;
preferably, the reaction liquid inlet of the NOx absorption reactor is connected with a circulating standby reaction liquid storage tank through a reaction liquid circulating pump.
Preferably, a reaction liquid flow meter is arranged between the reaction liquid inlet of the NOx absorption reactor and the reaction liquid circulating pump.
The circulating standby reaction liquid storage tank is used for providing fresh reaction liquid for the NOx absorption reactor so as to keep the pH value of the reaction liquid in the NOx absorption reactor to be more than or equal to 8. And the size of the supplementary flow is controlled by a flowmeter.
Preferably, a flue gas outlet of the first three-way flue gas flow controller is connected with an SCR denitration system.
Preferably, a flue gas outlet of the second three-way flue gas flow controller is connected with an SCR denitration system.
The flue gas treated by the NOx oxidation reactor and the NOx absorption reactor obviously reduces the concentration of NOx in the inlet flue gas of the SCR denitration system and the concentration of dust in the flue gas.
The first flue gas flowmeter, the second flue gas flowmeter and the third flue gas flowmeter respectively measure the flow m of high-temperature flue gas introduced into the heat exchanger and the flow m of high-temperature flue gas introduced into the heat exchanger after reaction in the NOx absorption reactor1And the flow m directly introduced into the flue gas mixer after the reaction of the NOx absorption reactor2(ii) a The first temperature measuring device, the second temperature measuring device, the third temperature measuring device and the fourth temperature measuring device respectively measure the temperature T of high-temperature flue gas before the high-temperature flue gas is introduced into the heat exchanger1The temperature T of the high-temperature flue gas which is introduced into the heat exchanger and passes through the flue gas mixer2Temperature T after reaction in a NOx absorption reactor3And the temperature T of the reaction product after the reaction in the NOx absorption reactor and passing through the heat exchanger4。
The optimal working temperature range of the high-temperature flue gas passing through the NOx oxidation reactor is 120-:
Figure BDA0003441631930000061
Figure BDA0003441631930000062
in a second aspect, the present invention provides a pretreatment method using the denitration reaction pretreatment apparatus system provided in the first aspect, the pretreatment method including the steps of:
the high-temperature flue gas is treated by a heat exchanger and then is subjected to catalytic oxidation in an NOx oxidation reactor, and then is subjected to desulfurization and denitrification in an NOx absorption reactor to obtain pretreated flue gas.
The method can obviously reduce the content of NOx pollutants in the finally discharged flue gas: finally, the NOx concentration of the discharged flue gas can be reduced to be lower than the original 20%, and the discharged flue gas can reach the NOx discharge standard of 50mg/Nm 3.
Preferably, the temperature of the high temperature flue gas is 160-240 ℃, such as 160 ℃, 170 ℃, 180 ℃, 190 ℃, 200 ℃, 210 ℃, 220 ℃, 230 ℃ or 240 ℃, but 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 high temperature flue gas is 5-8m/s, for example, 5m/s, 5.5m/s, 6m/s, 6.5m/s, 7m/s, 7.5m/s or 8m/s, but is not limited to the values listed, and other values not listed in the numerical range are also applicable.
Preferably, the temperature of the high temperature flue gas after the heat exchanger treatment is 120-160 ℃, for example, 120 ℃, 125 ℃, 130 ℃, 135 ℃, 140 ℃, 145 ℃, 150 ℃, 155 ℃ or 160 ℃, but not limited to the enumerated values, and other unrecited values in the numerical range are also applicable.
Preferably, the catalyst powder used in the catalytic oxidation process comprises Fe2O3、MnO、TiO2Or CuO, or a combination of at least two of them, a typical but non-limiting combination including Fe2O3In combination with MnO, MnO and TiO2Combinations of (A) and (B), TiO2And CuO, Fe2O3MnO and TiO2Combination of MnO and TiO2And CuO, or Fe2O3、MnO、TiO2And 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 oxidant liquid used in the catalytic oxidation process comprises H2O2、KMnO4NaClO or NaClO2Any one or a combination of at least two of the above, typical but not limiting combinations include H2O2And KMnO4KMnO4And NaClO, NaClO and NaClO2Combination of (1), H2O2、KMnO4And NaClO, KMnO4NaClO and NaClO2A combination of (A) or (H)2O2、KMnO4NaClO and NaClO2Combinations of (a) and (b).
Preferably, the droplets of the oxidizer liquid have an average diameter of 80-100 μm, such as 80 μm, 82 μm, 84 μm, 86 μm, 88 μm, 90 μm, 92 μm, 94 μm, 96 μm, 98 μm or 100 μm, but not limited to the values recited, and other values not recited within the range of values are equally applicable.
The particle size of the catalyst powder is close to that of the oxidant liquid fog drops, and the particle size of the oxidant liquid fog drops is slightly larger than that of the catalyst powder, so that the catalyst powder can be better coated on the surface of the oxidant liquid fog drops in the spraying process, and meanwhile, the catalyst powder has larger contact specific surface area, and is favorable for promoting the oxidation-reduction reaction.
Preferably, the temperature of the desulfurization and denitrification process is 40-60 ℃, for example, 40 ℃, 42 ℃, 44 ℃, 46 ℃, 48 ℃, 50 ℃, 52 ℃, 54 ℃, 56 ℃, 58 ℃ or 60 ℃, but not limited to the recited values, and other values not recited in the numerical range are also applicable.
Preferably, the reaction liquid adopted in the desulfurization and denitrification process comprises Na2S、Na2SO3Or NaOH, or a combination of at least two of them, a typical but non-limiting combination including Na2S and Na2SO3Combination of (A) and (B), Na2SO3And NaOH, Na2A combination of S and NaOH, or Na2S、Na2SO3And NaOH.
Preferably, the reaction solution has a pH of 8 or more, for example, 8, 8.1, 8.2, 8.3, 8.4, 8.5, 8.6, 8.7, 8.8, 8.9, or 9.0, but not limited to the values recited, and other values not recited in the numerical ranges are also applicable.
Preferably, the concentration of the reaction solution is 0.02 to 0.05mol/L, and may be, for example, 0.02mol/L, 0.024mol/L, 0.028mol/L, 0.032mol/L, 0.036mol/L, 0.04mol/L, 0.044mol/L, 0.048mol/L, or 0.05mol/L, but is not limited to the values recited, and other values not recited in the range of values are also applicable.
Preferably, the stirring speed in the desulfurization and denitrification process is 300-500rpm, such as 300rpm, 320rpm, 340rpm, 360rpm, 380rpm, 400rpm, 420rpm, 440rpm, 460rpm, 480rpm or 500rpm, but is not limited to the enumerated values, and other unrecited values in the numerical range are also applicable.
As a preferred technical solution of the present invention, the pretreatment method provided by the second aspect of the present invention includes the steps of:
(1) treating the high-temperature flue gas at the temperature of 160-240 ℃ by a heat exchanger at the flow speed of 5-8m/s to obtain the heat-exchanged flue gas at the temperature of 120-160 ℃;
(2) carrying out catalytic oxidation on the heat-exchanged flue gas obtained in the step (1) in an NOx oxidation reactor to obtain oxidized flue gas; the average grain diameter of the catalyst powder used in the catalytic oxidation process is 60-80 μm; the average diameter of the oxidant liquid fog drops used in the catalytic oxidation process is 80-100 mu m;
(3) desulfurizing and denitrating the oxidized flue gas obtained in the step (2) in an NOx absorption reactor to obtain pretreated flue gas; the temperature in the desulfurization and denitrification process is 40-60 ℃, and the stirring speed is 300-500 rpm; the pH value of the reaction liquid adopted in the desulfurization and denitrification process is more than or equal to 8, and the concentration is 0.02-0.05 mol/L.
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 denitration reaction pretreatment device system provided by the invention can prolong the service life of the catalyst and reduce the annual average investment cost of the denitration catalyst;
(2) the denitration reaction pretreatment device system provided by the invention can obviously reduce NOx and SO in flue gas2The concentration of the denitration catalyst greatly reduces the load of the denitration catalyst, relieves the failure phenomenon of the catalyst caused by alkali metal poisoning, blockage, sintering, abrasion and the like due to dust in flue gas, prolongs the service life of the catalyst, and reduces the annual investment cost of the denitration catalyst of a thermal power plant;
(3) the denitration reaction pretreatment device system provided by the invention has the advantages of environmental protection, energy conservation, high denitration efficiency and good economic benefit.
Drawings
Fig. 1 is a schematic view of a denitration reaction pretreatment apparatus system provided in embodiment 1 of the present invention.
Wherein, 1 is a heat exchanger, 2 is a NOx oxidation reactor, 3 is an electrostatic dust collector, 4 is a NOx absorption reactor, 5 is a magnetic separator, 6-1 is a first three-way flue gas flow controller, 6-2 is a second three-way flue gas flow controller, 7-1 is a first flue gas flow meter, 7-2 is a second flue gas flow meter, 7-3 is a third flue gas flow meter, 8-1 is a first temperature measuring device, 8-2 is a second temperature measuring device, 8-3 is a third temperature measuring device, 8-4 is a fourth temperature measuring device, 9 is a flue gas mixer, 10 is a catalyst powder storage tank, 11 is an oxidant solution storage tank, 12 is a liquid level detector, 13 is a constant temperature water bath device, 14 is an electric stirring device, 15 is a pH value monitoring device, 16 is a circulating standby reaction liquid storage tank, 17 is a reaction liquid flow meter, and 18 is an SCR denitration system.
Detailed Description
The technical solution of the present invention is further explained by the following 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 a denitration reaction pretreatment device system as shown in fig. 1, which comprises a heat exchanger 1, a NOx oxidation reactor 2, an electrostatic dust collector 3, a NOx absorption reactor 4 and a first three-way flue gas flow controller 6-1, which are sequentially connected and arranged according to the flow direction of high-temperature flue gas; the solid powder outlet of the electrostatic dust collector 3 is connected with the magnetic separator 5; and the flue gas heat exchange port of the first three-way flue gas flow controller 6-1 is connected with the heat exchanger 1.
A high-temperature flue gas inlet of the heat exchanger 1 is connected with a first flue gas flowmeter 7-1; a first temperature measuring device 8-1 is arranged at a high-temperature flue gas inlet of the heat exchanger 1; a cold flow outlet of the heat exchanger 1 is connected with a second three-way flue gas flow controller 6-2; a flue gas mixer 9 is arranged between the heat exchanger 1 and the NOx oxidation reactor 2; a second temperature measuring device 8-2 is arranged between the flue gas mixer 9 and the NOx oxidation reactor 2; and a cold flow outlet of the heat exchanger 1 is provided with a fourth temperature measuring device 8-4.
The catalyst powder inlet of the NOx oxidation reactor 2 is connected to a catalyst powder storage tank 10 by a blower; the catalyst powder storage tank 10 is connected with the outlet of the magnetic separator 5.
An oxidant inlet of the NOx oxidation reactor 2 is connected with an oxidant solution storage tank 11 through an oxidant delivery pump; the inside of the oxidizer solution tank 11 is provided with a liquid level detector 12.
The flue gas outlet of the second three-way flue gas flow controller 6-2 is connected with a flue gas mixer 9 through a third flue gas flowmeter 7-3; a second flue gas flowmeter 7-2 is arranged between the flue gas heat exchange port of the first three-way flue gas flow controller 6-1 and the heat exchanger 1; and a third temperature measuring device 8-3 is arranged at an outlet of the second flue gas flowmeter 7-2.
The NOx absorption reactor is placed 4 in a constant temperature water bath device 13; an electric stirring device 14 is arranged in the NOx absorption reactor 4; a pH value monitoring device 15 is arranged in the NOx absorption reactor 4.
The reaction liquid outlet of the NOx absorption reactor 4 is connected with a circulating standby reaction liquid storage tank 16; a reaction liquid inlet of the NOx absorption reactor 4 is connected with a circulating standby reaction liquid storage tank 16 through a reaction liquid circulating pump; a reaction liquid flow meter 17 is arranged between the reaction liquid inlet of the NOx absorption reactor 4 and the reaction liquid circulating pump.
The flue gas outlet of the first three-way flue gas flow controller 6-1 is connected with an SCR denitration system 18; and the flue gas outlet of the second three-way flue gas flow controller 6-2 is connected with an SCR denitration system 18.
Example 2
This example provides a denitration reaction pretreatment apparatus system, which is different from example 1 only in that: the thermostatic waterbath device 13 is omitted in this embodiment.
Compared with the embodiment 1, the denitration reaction pretreatment device system of the embodiment can not control the temperature in the reaction process of the NOx absorption reactor, thereby influencing the desulfuration and denitration reaction.
Example 3
This example provides a denitration reaction pretreatment apparatus system, which is different from example 1 only in that: the flue gas mixer 9 is omitted in this embodiment.
Compared with the embodiment 1, the denitration reaction pretreatment device system provided by the embodiment is used, when the temperature of high-temperature flue gas is too high, the heat exchange process only comprises one-time heat exchange, and the flue gas temperature after heat exchange cannot be completely ensured to influence the catalytic oxidation effect within the optimal temperature range of the catalyst work.
Example 4
This example provides a denitration reaction pretreatment apparatus system, which is different from example 1 only in that: this example omits the circulating backup reaction liquid storage tank 16.
Compared with the embodiment 1, the denitration reaction pretreatment device system provided by the embodiment cannot timely provide the reaction liquid for the NOx absorption reactor, cannot control the ph of the reaction liquid in real time, and causes insufficient reaction or even failure in completing denitration and desulfurization.
Comparative example 1
This comparative example provides a denitration reaction pretreatment apparatus system, which differs from example 1 only in that: the present comparative example omits the magnetic separator 5.
Compared with the embodiment 1, the denitration reaction pretreatment device system provided by the comparative example cannot recycle the catalyst used in the catalytic reaction process, and waste of catalyst resources is caused.
Application example 1
This application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, the pretreatment method including the steps of:
(1) treating high-temperature flue gas with the temperature of 220 ℃ by a heat exchanger at the flow speed of 6m/s to obtain heat-exchanged flue gas with the temperature of 140 ℃;
(2) carrying out catalytic oxidation on the heat-exchanged flue gas obtained in the step (1) in an NOx oxidation reactor to obtain oxidized flue gas; the average particle size of the catalyst powder used in the catalytic oxidation process is 70 μm; the average diameter of the oxidant liquid fog drops used in the catalytic oxidation process is 90 micrometers;
(3) desulfurizing and denitrating the oxidized flue gas obtained in the step (2) in an NOx absorption reactor to obtain pretreated flue gas; the temperature in the desulfurization and denitrification process is 50 ℃, and the stirring speed is 400 rpm; the pH value of the reaction liquid adopted in the desulfurization and denitrification process is 8.6, and the concentration is 0.03 mol/L.
Application example 2
The present application example provides a method of performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 2, and the pretreatment method is the same as in application example 1.
Application example 3
The present application example provides a method of performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 3, and the pretreatment method is the same as in application example 1.
Application example 4
The present application example provides a method of performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 4, and the pretreatment method is the same as in application example 1.
Application example 5
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the flue gas after heat exchange in the step (1) is changed to 200 ℃.
Application example 6
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the flue gas after heat exchange in the step (1) is changed to 80 ℃.
Application example 7
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the average particle size of the catalyst powder used in the catalytic oxidation process of the step (2) is 80 μm; the average diameter of the oxidant liquid droplets used in the catalytic oxidation process is 100 μm.
Application example 8
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the average particle size of the catalyst powder used in the catalytic oxidation process of the step (2) is 100 μm; the average diameter of the oxidant liquid droplets used in the catalytic oxidation process was 80 μm.
Application example 9
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the desulfurization and denitrification process in the step (3) is changed to 40 ℃.
Application example 10
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the desulfurization and denitrification process in the step (3) is changed to 60 ℃.
Application example 11
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the desulfurization and denitrification process in the step (3) is changed to 80 ℃.
Application example 12
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: the temperature of the desulfurization and denitrification process in the step (3) is changed to 30 ℃.
Application example 13
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: and (4) changing the pH value of the reaction liquid adopted in the desulfurization and denitrification process in the step (3) to 7.2.
Application example 14
The present application example provides a method for performing pretreatment using the denitration reaction pretreatment apparatus system provided in embodiment 1, and the pretreatment method is different from application example 1 only in that: and (4) changing the pH value of the reaction liquid adopted in the desulfurization and denitrification process in the step (3) to 6.5.
Comparative application example 1
This comparative application example provides a method of performing pretreatment using the denitration reaction pretreatment apparatus system provided in comparative example 1, and the pretreatment method is the same as in application example 1.
The high-temperature flue gas provided in application examples 1 to 14 and comparative application example 1 and the pretreated flue gas were introduced into a flue gas analyzer, the concentration change of NOx in the flue gas before and after treatment was measured, and the removal efficiency was calculated, the results of which are shown in table 1.
TABLE 1
High temperature flue gas (mg/Nm)3) Pretreated flue gas (mg/Nm)3) Removal Rate (%)
Application example 1 526 65 87.6
Application example 2 526 92 82.5
Application example 3 526 86 83.7
Application example 4 526 125 76.2
Application example 5 526 136 74.1
Application example 6 526 162 69.2
Application example 7 526 78 85.2
Application example 8 526 110 79.1
Application example 9 526 81 84.6
Application example 10 526 62 88.2
Application example 11 526 87 83.5
Application example 12 526 97 81.6
Application example 13 526 127 75.9
Application example 14 526 165 68.6
Comparative application example 1 526 75 85.7
In conclusion, the denitration reaction pretreatment device system provided by the invention can obviously reduce the concentration of NOx in the flue gas at the inlet of the SCR denitration system, and greatly reduce the load of a denitration catalyst; meanwhile, by reducing the concentration of dust in the flue gas, the failure phenomenon of the catalyst caused by alkali metal poisoning, blockage, sintering, abrasion and the like caused by the dust in the flue gas is relieved, the service life of the SCR catalyst is prolonged, and the annual investment cost of the denitration catalyst of the thermal power plant is reduced. In addition, the pretreatment device system of the denitration reactor provided by the invention ensures that the temperature of the flue gas in the NOx oxidation reactor is in the optimal working temperature range of the catalyst by utilizing the self heat exchange of the flue gas, ensures the denitration efficiency of the system, and avoids extra equipment cost and energy loss caused by introducing external heating or cooling equipment. Has the advantages of environmental protection, energy conservation, high denitration efficiency and good economic benefit.
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 (10)

1. A denitration reaction pretreatment device system is characterized by comprising a heat exchanger, an NOx oxidation reactor, an electrostatic dust collector, an NOx absorption reactor and a first three-way flue gas flow controller which are sequentially connected and arranged according to the flowing direction of high-temperature flue gas;
the solid powder outlet of the electrostatic dust collector is connected with the magnetic separator;
and a flue gas heat exchange port of the first three-way flue gas flow controller is connected with the heat exchanger.
2. The denitration reaction pretreatment apparatus system of claim 1, wherein a high temperature flue gas inlet of the heat exchanger is connected to a first flue gas flow meter;
preferably, a first temperature measuring device is arranged at a high-temperature flue gas inlet of the heat exchanger;
preferably, a cold flow outlet of the heat exchanger is connected with a second three-way flue gas flow controller;
preferably, a flue gas mixer is arranged between the heat exchanger and the NOx oxidation reactor;
preferably, a second temperature measuring device is arranged between the flue gas mixer and the NOx oxidation reactor;
preferably, a fourth temperature measuring device is arranged at the cold flow outlet of the heat exchanger.
3. The denitration reaction pretreatment apparatus system according to claim 1 or 2, wherein a catalyst powder inlet of the NOx oxidation reactor is connected to a catalyst powder storage tank by a blower;
preferably, the catalyst powder storage tank is connected with an outlet of the magnetic separator;
preferably, the oxidant inlet of the NOx oxidation reactor is connected to an oxidant solution storage tank by an oxidant delivery pump;
preferably, a liquid level detector is arranged inside the oxidant solution storage tank.
4. The denitration reaction pretreatment apparatus system of claim 2, wherein a flue gas outlet of the second three-way flue gas flow controller is connected to the flue gas mixer through a third flue gas flow meter;
preferably, a second flue gas flowmeter is arranged between the flue gas heat exchange port of the first three-way flue gas flow controller and the heat exchanger;
preferably, a third temperature measuring device is arranged at the outlet of the second flue gas flow meter.
5. The denitration reaction pretreatment apparatus system according to any one of claims 1 to 4, wherein the NOx absorption reactor is placed in a constant-temperature water bath apparatus;
preferably, an electric stirring device is arranged inside the NOx absorption reactor;
preferably, a pH value monitoring device is arranged in the NOx absorption reactor.
6. The denitration reaction pretreatment apparatus system according to any one of claims 1 to 5, wherein a reaction liquid outlet of the NOx absorption reactor is connected to a circulating standby reaction liquid storage tank;
preferably, a reaction liquid inlet of the NOx absorption reactor is connected with a circulating standby reaction liquid storage tank through a reaction liquid circulating pump;
preferably, a reaction liquid flow meter is arranged between the reaction liquid inlet of the NOx absorption reactor and the reaction liquid circulating pump.
7. The denitration reaction pretreatment device system according to claim 2 or 4, wherein a flue gas outlet of the first three-way flue gas flow controller is connected with an SCR denitration system;
preferably, a flue gas outlet of the second three-way flue gas flow controller is connected with an SCR denitration system.
8. A pretreatment method for the denitration reaction pretreatment apparatus system according to any one of claims 1 to 7, wherein the pretreatment method comprises the steps of:
the high-temperature flue gas is treated by a heat exchanger and then is subjected to catalytic oxidation in an NOx oxidation reactor, and then is subjected to desulfurization and denitrification in an NOx absorption reactor to obtain pretreated flue gas.
9. The pretreatment method as claimed in claim 8, wherein the temperature of the high-temperature flue gas is 160-240 ℃;
preferably, the flow velocity of the high-temperature flue gas is 5-8 m/s;
preferably, the temperature of the high-temperature flue gas treated by the heat exchanger is 120-160 ℃;
preferably, the catalyst powder used in the catalytic oxidation process comprises Fe2O3、MnO、TiO2Or CuO, or a combination of at least two thereof;
preferably, the catalyst powder has an average particle diameter of 60 to 80 μm;
preferably, the oxidant liquid used in the catalytic oxidation process comprises H2O2、KMnO4NaClO or NaClO2Any one or a combination of at least two of;
preferably, the average diameter of said oxidant liquid droplets is between 80 and 100 μm.
10. The pretreatment method according to claim 8 or 9, wherein the temperature of the desulfurization and denitrification process is 40-60 ℃;
preferably, the reaction liquid adopted in the desulfurization and denitrification process comprises Na2S、Na2SO3Or NaOH, or a combination of at least two of the above;
preferably, the pH of the reaction solution is more than or equal to 8;
preferably, the concentration of the reaction solution is 0.02-0.05 mol/L;
preferably, the stirring speed in the desulfurization and denitrification process is 300-500 rpm.
CN202111633093.8A 2021-12-29 2021-12-29 Denitration reaction pretreatment device system and pretreatment method Pending CN114367192A (en)

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Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103463978A (en) * 2013-09-30 2013-12-25 南京理工大学 Device and method for smoke simultaneous desulfurization and denitrification based on hydrogen peroxide catalytic oxidation
CN105536467A (en) * 2016-01-25 2016-05-04 华北电力大学（保定） Flue gas purification device and method combining photo-catalytic oxidization and double cyclic absorption
CN106861392A (en) * 2017-02-21 2017-06-20 华北电力大学 A kind of nitrogen oxide removal process based on catalytic oxidation of hydrogen peroxide
CN109865425A (en) * 2017-12-01 2019-06-11 河南正达环保科技有限公司 A kind of device and method of catalytic oxidation treatment exhaust gas
CN209393034U (en) * 2019-06-18 2019-09-17 四川恒泰环境技术有限责任公司 A kind of middle low temperature SCR denitration preprocessor and system
CN110523251A (en) * 2019-09-24 2019-12-03 北京中航泰达环保科技股份有限公司 A kind of system for desulfuration and denitration and method of sintering flue gas circulation joint ozone pre-oxidation
CN211913294U (en) * 2020-02-24 2020-11-13 北京科技大学 Cement kiln denitration system
CN212188531U (en) * 2020-04-30 2020-12-22 西安交通大学 Desulfurization and denitrification flue gas comprehensive treatment device with cooperative thermal power generation
AU2021100781A4 (en) * 2021-02-09 2021-04-22 Hangzhou Yuanshuo Environmental Protection Technology Co., Ltd. Ultra-clean treatment system for high-temperature and high-alkali flue gas
CN112844395A (en) * 2019-11-28 2021-05-28 中冶京诚工程技术有限公司 Oxidation denitration catalyst, and flue gas catalytic oxidation denitration method and device
CN112915778A (en) * 2019-12-06 2021-06-08 中国科学院大连化学物理研究所 Catalytic oxidation absorption denitration method and device thereof
CN113750783A (en) * 2021-08-24 2021-12-07 福建华电可门发电有限公司 Method of two-section type SCR reaction device suitable for wide-temperature-zone denitration

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103463978A (en) * 2013-09-30 2013-12-25 南京理工大学 Device and method for smoke simultaneous desulfurization and denitrification based on hydrogen peroxide catalytic oxidation
CN105536467A (en) * 2016-01-25 2016-05-04 华北电力大学（保定） Flue gas purification device and method combining photo-catalytic oxidization and double cyclic absorption
CN106861392A (en) * 2017-02-21 2017-06-20 华北电力大学 A kind of nitrogen oxide removal process based on catalytic oxidation of hydrogen peroxide
CN109865425A (en) * 2017-12-01 2019-06-11 河南正达环保科技有限公司 A kind of device and method of catalytic oxidation treatment exhaust gas
CN209393034U (en) * 2019-06-18 2019-09-17 四川恒泰环境技术有限责任公司 A kind of middle low temperature SCR denitration preprocessor and system
CN110523251A (en) * 2019-09-24 2019-12-03 北京中航泰达环保科技股份有限公司 A kind of system for desulfuration and denitration and method of sintering flue gas circulation joint ozone pre-oxidation
CN112844395A (en) * 2019-11-28 2021-05-28 中冶京诚工程技术有限公司 Oxidation denitration catalyst, and flue gas catalytic oxidation denitration method and device
CN112915778A (en) * 2019-12-06 2021-06-08 中国科学院大连化学物理研究所 Catalytic oxidation absorption denitration method and device thereof
CN211913294U (en) * 2020-02-24 2020-11-13 北京科技大学 Cement kiln denitration system
CN212188531U (en) * 2020-04-30 2020-12-22 西安交通大学 Desulfurization and denitrification flue gas comprehensive treatment device with cooperative thermal power generation
AU2021100781A4 (en) * 2021-02-09 2021-04-22 Hangzhou Yuanshuo Environmental Protection Technology Co., Ltd. Ultra-clean treatment system for high-temperature and high-alkali flue gas
CN113750783A (en) * 2021-08-24 2021-12-07 福建华电可门发电有限公司 Method of two-section type SCR reaction device suitable for wide-temperature-zone denitration

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