WO2005065805A1 - Procede pour traiter des gaz d'echappement et dispositif utilise a cet effet - Google Patents

Procede pour traiter des gaz d'echappement et dispositif utilise a cet effet Download PDF

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Publication number
WO2005065805A1
WO2005065805A1 PCT/JP2004/017049 JP2004017049W WO2005065805A1 WO 2005065805 A1 WO2005065805 A1 WO 2005065805A1 JP 2004017049 W JP2004017049 W JP 2004017049W WO 2005065805 A1 WO2005065805 A1 WO 2005065805A1
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Prior art keywords
exhaust gas
gas
discharge system
reactor
reaction zone
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PCT/JP2004/017049
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English (en)
Japanese (ja)
Inventor
Masaaki Okubo
Toshiaki Yamamoto
Tomoyuki Kuroki
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Osaka Industrial Promotion Organization
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Priority to JP2005516807A priority Critical patent/JP4472638B2/ja
Publication of WO2005065805A1 publication Critical patent/WO2005065805A1/fr

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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
    • B01D53/79—Injecting reactants
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/10—Gas phase, e.g. by using aerosols
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Definitions

  • the present invention relates to a method and apparatus for treating exhaust gas, and a reaction by-product in exhaust gas.
  • the present invention relates to a method and apparatus for cleaning.
  • nitrogen acids such as nitrogen monoxide (NO) and nitrogen dioxide (NO 2).
  • Nitrogen oxides discharged into the environment are the cause of photochemical smog, etc., and measures are being considered as an important issue of environmental problems in large cities.
  • one acid, two nitrogen (NO) is also attracting attention as a cause of global warming gas, which has become a problem in recent years.
  • Patent Document 1 Japanese Patent Application Laid-Open No. 2000-117049
  • Patent Document 2 Japanese Patent Application Laid-Open No. 2000-51653
  • Patent Document 3 Japanese Patent Application Laid-Open No. 2001-300257
  • the exhaust gas to be treated is flowed directly into the reactor, and the non-thermal plasma is used to acidify NO NO to NO and the two-step method of treating with a chemical scrubber.
  • the non-thermal direct plasma method has been proposed with relatively low energy efficiency. Since the high temperature gas flows into the plasma reactor, the processing efficiency is reduced. In addition, since the corrosive exhaust gas is allowed to flow into the plasma reactor, there is a problem such as corrosion of electrodes and the like.
  • the present invention can suppress reaction by-products (eg, NO, HNO, HNO, NO-, CO) in exhaust gas and can process exhaust gas efficiently.
  • reaction by-products eg, NO, HNO, HNO, NO-, CO
  • the method for treating exhaust gas according to the present invention is a method for purifying an exhaust gas containing nitrogen oxide, wherein air is supplied to an atmospheric pressure low temperature non-equilibrium plasma reactor to generate a radical gas,
  • the nitrogen oxide in the exhaust gas can be supplied by supplying a gas to the acid reaction region and supplying the exhaust gas to a line force separate from the radical gas generation line. Oxidize to NO containing oxidizing gas by radical gas, then
  • NO is reduced to nitrogen gas (N 2) by bringing the acid gas into contact with the reducing agent solution.
  • the exhaust gas treatment apparatus of the present invention is an apparatus for purifying an exhaust gas containing nitrogen oxide, which comprises an atmospheric pressure low-temperature non-equilibrium plasma reactor for converting air into a radical gas, and the radical gas.
  • a line for supplying an acid reaction region, a line for supplying the exhaust gas to the oxidation reaction region from a line separate from the radical gas generation line, and nitrogen oxides in the exhaust gas are included in the radical To acidify NO-containing oxidizing gas by gas By contacting the oxidation reaction region and the oxidizing gas with a reducing agent solution, NO can be nitrogenated.
  • reaction area is directly connected.
  • FIG. 1 is a schematic view of an apparatus in which a nonthermal remote plasma method of the present invention and a wet reactor are connected in one embodiment of the present invention.
  • FIG. 2 The same, a schematic cross sectional view of a non-thermal plasma reactor.
  • FIG. 4 The schematic of the experiment apparatus of the direct plasma method of a comparative example.
  • FIG. 5 is a graph showing the concentration change in the direct plasma processing method of the comparative example.
  • FIG. 6A is a graph showing the change in concentration in the comparative example
  • FIG. 6B is a graph showing the change in concentration in the treatment method in which the non-thermal remote plasma method and the wet reactor are directly linked in one example of the present invention.
  • FIG. 7] AB is a graph which shows the density
  • FIG. 8A is a graph showing the change in concentration in the comparative example
  • FIG. 8B is a graph showing the change in concentration in the treatment method in which the non-thermal remote plasma method and the wet reactor are directly linked in one example of the present invention.
  • FIG. 9 is a graph showing the same voltage and current waveforms.
  • FIG. 10 A graph showing the plasma consumption energy per unit processing gas volume and the removal efficiency of nitrogen oxides.
  • FIG. 11 is a schematic view of an apparatus in which boiler exhaust gas in Example 4 of the present invention is treated using the non-thermal remote plasma method of the present invention and a wet reactor.
  • the method and apparatus of the present invention comprises: air radicalized with atmospheric pressure low temperature non-equilibrium plasma;
  • the exhaust gas is supplied to the oxidation reaction area, the nitrogen oxides in the exhaust gas are oxidized by the radical gas to the oxidation gas containing NO, and then the oxidation gas is brought into contact with the reducing agent solution about
  • the present invention refers to air as atmospheric pressure low temperature non-equilibrium plasma (hereinafter referred to as “low temperature non-equilibrium plasma”!).
  • radical gas which is supplied to the oxidation reaction zone, reacted with separately supplied exhaust gas, and nitrogen oxides in the exhaust gas contain NO by the radical gas.
  • the present invention feeds air into a plasma reactor, mixes the radical gas of the air component excited by the low temperature non-equilibrium plasma with the exhaust gas at the bottom of the wet reactor, and oxidizes NO to NO
  • non-thermal remote plasma-chemical nod method remove by reduction with a chemical scrubber (wet reactor).
  • a chemical scrubber wet reactor
  • the low-temperature non-equilibrium plasma used in the present invention means that the gas temperature is considerably lower than the combustion temperature (about 700-1000 ° C.) of a normal gas, and the plasma in the ionizing state is usually 300 ° C. or less I say plasma.
  • the lower limit temperature may be, for example, 200 ° C.
  • More preferable conditions are temperature: 100 ° C. or less, particularly preferably normal temperature (0-40 ° C.).
  • Other preferable conditions are: pressure: about atmospheric pressure, relative humidity: 60% or less, applied voltage: 10-100 kV, peak current 1 1 100 A, frequency: 250 Hz-1000 Hz.
  • the oxidation reaction zone and the reduction reaction zone are preferably present in one wet reactor.
  • the wet reactor be a column or column reactor
  • the oxidation reaction zone be present at the lower part of the wet reactor
  • the reduction reaction zone be present at the upper part of the wet reactor. ,. This will make the device smaller.
  • the reducing agent solution is selected from Na 2 SO 4, Na 2 S, NaOH, Na 2 S 2 O, and Ca (OH).
  • aqueous solution containing at least one compound is preferable that it is an aqueous solution containing at least one compound.
  • Aqueous solutions containing these compounds can be recycled with high reducibility.
  • the exhaust gas that can be treated by the present invention is combustion exhaust gas, and the components to be treated are: soot, soot
  • At least one selected from dyestuff, hydrocarbon, CO, CO and steam (H 0) is preferred .
  • nitrogen oxides (NO 2) such as soot, soot, soot, soot, etc. are reduced to nitrogen gas (soot), SO 2, SO 3
  • Volatilization of sulfur oxides such as 2 2 2 5 x 2 2 3 etc., hydrocarbons, CO, CO, toluene, benzene, xylene, etc.
  • Environmental pollutants such as volatile organic compounds (VOCs), dioxins, halogenated aromatics, and highly condensed aromatic hydrocarbons can be decomposed or converted into harmless substances or substances with low environmental impact.
  • VOCs volatile organic compounds
  • dioxins dioxins
  • halogenated aromatics halogenated aromatics
  • highly condensed aromatic hydrocarbons can be decomposed or converted into harmless substances or substances with low environmental impact.
  • high temperature exhaust gas of 300 ° C. or more can be efficiently oxidized to NO by low temperature remote plasma at room temperature (27 ° C.).
  • One embodiment of the present invention relates to a method and apparatus for treating exhaust gas, which uses a reducing agent solution for radical gas formed by low-temperature non-equilibrium plasma at atmospheric pressure installed separately from the exhaust gas line.
  • Reaction by-products N 0
  • a low temperature non-thermal plasma reactor installed outside the exhaust gas flow path and a wet chemical scrubber (wet reactor) into which activated radicals are injected are directly connected.
  • a wet chemical scrubber wet reactor
  • the type of low temperature non-thermal plasma reactor and the type of plasma to be generated are not particularly limited.
  • V can be exemplified as a preferred example of the non-equilibrium plasma reactor described in the following examples.
  • a pulse discharge method by alternating current or direct current voltage no Voice discharge method, corona discharge method, creeping discharge method, barrier discharge method, honeycomb discharge method, pellet packed bed discharge method, arc discharge method, inductively coupled discharge method, capacitively coupled discharge method, microwave excitation discharge method, laser induced A discharge method, an electron beam induced discharge method, a particle beam induced discharge method, or a combination of these can be used. That is, the plasma reactor used in the present invention can adopt various conceivable methods suitable for each method of applying plasma. It is particularly convenient to use the non-equilibrium plasma generated by the non-equilibrium plasma force pulse corona discharge.
  • the type of wet chemical scrubber is also not particularly limited, and the ability to use various types of scrubbers.
  • a typical chemical scrubber of the Raschig ring filling type described in Example 1 below is a preferred example.
  • a bubble scrubbing type chemical scrubber in a liquid phase can be mentioned as a suitable example.
  • the purpose is to remove air pollutants such as nitrogen oxides, NOx and the like emitted from diesel engines and thermal power plants by the hybrid process combining non-equilibrium plasma process and wet chemical reaction process.
  • the chemical reaction of this process is a combination of the following two reactions.
  • Plasma process NO + 0 * (oxygen radical) + M (third body object) ⁇ NO + M (1)
  • reaction (1) accounts for the majority of the exhaust gas NO is oxidized to NO at low cost
  • a drug such as Na 2 S 2, 2 3 2 3 3 (eg, Na 2 S, NaOH, Na 2 S 2 O 3, Ca (OH), etc.) may be used.
  • non-thermal remote method is to flow air or a small amount of additive (hydrocarbon, ammonia, etc.) into the plasma reactor, inject excited radical gas into the exhaust gas flow path, and oxidize NO to NO. Name it (indirect) plasma method.
  • FIG. 1 An outline of an experimental apparatus 50 using the non-thermal remote plasma method of the present invention is shown in FIG.
  • Compressed air is supplied from the compressor 32 to a dryer 33 equipped with an air filter to produce dry air, and this dry air is supplied to the non-thermal plasma reactor 1 at a predetermined flow rate by a mass flow controller 35.
  • the non-thermal plasma reactor 1 is applied with a high-speed rising short width pulse high voltage generated by an IGBT pulse power supply (PPCP Pulsar SMC-30 / 1000, manufactured by Masuda Laboratories) 21.
  • IGBT pulse power supply PPCP Pulsar SMC-30 / 1000, manufactured by Masuda Laboratories
  • the applied voltage, current, and power consumption of the non-thermal plasma reactor 1 are measured with an oscilloscope (Yokogawa DL1740) 37, a high voltage probe, and a current probe (SonyTektronix, P6015A and P6021), and the integrated value of instantaneous power I asked for power consumption.
  • the activated gas thus obtained is directly injected into the chemical scrubber 11 of the wet reactor.
  • NO gas which is a model gas of exhaust gas
  • a mass flow controller 34 supplied at a predetermined flow rate from an air supply line 51 by a mass flow controller 52.
  • the simulated exhaust gas air-diluted NOx, concentration 300 ppm in which NO is adjusted to a predetermined concentration is directly injected into the chemical scrubber 11 by mixing with NO.
  • the reaction (1) takes place in the lower acid reaction zone 10 of the chemical scrubber 11 and the reaction
  • the non-thermal plasma reactor 1 has a cylindrical reaction tube which has a 1.5 mm diameter stainless steel discharge wire electrode 3 passing through an inner space of a Pyrex (registered trademark) glass (quartz glass) cylinder 2 with an inner diameter of 20 mm and an outer diameter of 24 mm.
  • a copper mesh (effective length: 260 mm) was placed on the outer wall of 2 to form a ground electrode 4.
  • a pulsed high voltage power supply 21 was connected between the discharge wire electrode 3 and the ground electrode 4.
  • the lower and upper hollow portions of the cylinder 2 were sealed by silicone rubber stoppers 5 and 6.
  • 7 is a porous plate made of polytetrafluoroethylene
  • 8 is a gas supply port
  • 9 Indicates a gas outlet
  • a and b indicate gas flows.
  • the reaction (1) is realized by this plasma reactor.
  • FIG. 1 A schematic cross-sectional view of a chemical scrubber (packed column) 11 which is a wet reactor is shown in FIG.
  • the gas to be treated is made to flow from the lower part to the upper part of the stainless steel tube 12 with an inner diameter of 55.5 mm and an outer diameter of 60.5 mm, and the Na 2 SO 4 aqueous solution 14 is sprayed from the upper part by a spray nozzle 13
  • the wet chemical reaction (2) is carried out.
  • the inside is filled with Raschig ring (made of cylindrical glass, inner diameter 5 mm, outer diameter 7 mm, width 7.2 mm) 15 in order to accelerate the reaction.
  • the reference numeral 15a is an enlarged shape of the lashing.
  • the filling height of the Raschig ring 15 is 160 mm
  • the height of the liquid spray nozzle 13 is from the gas inlet 16 to 340 mm
  • the difference in height from the gas inlet 16 to the Raschig start point is 100 mm.
  • 17 shows a gas outlet
  • c and d show gas flows.
  • the numeral 18 is a manometer for measuring the height of the liquid
  • 19 is a valve
  • 20 is a liquid (drain) outlet
  • e is the flow of the discharged liquid.
  • FIG. 2% NO gas cylinder 31 Force et al. NO gas is supplied by a mass flow controller 34 at a predetermined flow rate.
  • compressed air is supplied from the compressor 32 to a dryer 33 equipped with an air filter to produce dry air, and this dry air is supplied by a mass flow controller 35 at a predetermined flow rate.
  • the plasma reactor 1 is supplied with a simulated exhaust gas (air diluted NOx, concentration 300 ppm) in which NO is adjusted to a predetermined concentration by mixing with NO.
  • the plasma reactor 1 is applied with a high-speed rising short width pulse high voltage generated by an IGBT pulse power supply (PPCP Pulsar SMC-30 / 1000, manufactured by Masuda Laboratory) 21. This causes the reaction (1) to occur, and then the reduction treatment reaction (2) is performed in the chemical scrubber 11. Next, let it pass through the ozone removal heater 38, gas analyzer (HORIBA's PG-235 and VIA-510) 39 and NO, NO CO, N 0, CO,
  • IGBT pulse power supply PPCP Pulsar SMC-30 / 1000, manufactured by Masuda Laboratory
  • the power consumption was determined from the integrated value of instantaneous power by measuring with a scope (Yokogawa Electric Corporation DL 1740) 37, a high voltage probe, and a current probe (P6015A and P6021 manufactured by Sony Tektronix).
  • 40 is a gas outlet
  • 41 is a Na 2 SO 4 aqueous solution tank.
  • Example Comparative Example 1 1 uses the apparatus shown in FIG. 1, Comparative Example 1 deals with the direct plasma processing apparatus 30 of FIG. 4 only, and Comparative Example 2 deals with the direct plasma apparatus 30 and wet reactor 11 shown in FIG. In Comparative Example 3, only the non-thermal remote plasma apparatus 50 shown in FIG. 1 was used, and the removal experiment of NO was performed when the flow rate of the simulated gas was 5.0 L / min.
  • the flow rate of the simulated exhaust gas was 5.0 L / min
  • the flow rate of the radical gas at remote was 0.5 L / min
  • the initial concentration of NO was 300 ppm.
  • the flow rate of the reducing agent aqueous solution to be flowed to the packed column is 0.20 L / min
  • the concentration of Na 2 SO 4 is 2.0 g / L.
  • IGBT pulse power IGBT pulse power
  • the source frequency was set to 420 Hz.
  • the residence time in the plasma reactor at this time was 0.84 s for the direct method and 8.4 s for the remote method.
  • FIGS. 5A-B and 6A-B The above results are shown in FIGS. 5A-B and 6A-B.
  • Fig. 5A shows the direct plasma method only (Comparative Example 1)
  • Fig. 5B shows the process in which the direct plasma method and the wet reactor are directly connected
  • Fig. 6A shows the non-thermal remote plasma method only (Comparative Example 3)
  • 6B is data of a process in which a nonthermal remote plasma method and a wet reactor are directly connected (Example 1).
  • FIGS. 5A-B and 6A-B Comparing FIGS. 5A-B and 6A-B, the non-thermal remote plasma method (FIGS. 6A-B) consumes less reactor power than the direct plasma method (FIGS. 5A-B). It can be seen that the reduction in NOx is also large. In addition, comparing Figs. 6A-B, it can be seen that the reduction amount of NO and NOx in which the power consumption of the reactor is smaller is larger in Fig. 6B. Forces that concern about the generation of N 0 and CO as harmful by-products when the plasma is applied As shown in FIG.
  • CO was less than 7 ppm.
  • concentration of CO is around 360 ppm, several ppm
  • Example 2 uses the apparatus shown in FIG. 1, Comparative Example 4 deals with the direct plasma processing apparatus 30 of FIG. 4 only, and Comparative Example 5 deals with the direct plasma apparatus 30 and wet reactor 11 shown in FIG. In Comparative Example 6, only the non-thermal remote plasma apparatus 50 shown in FIG. 1 was used, and NO removal experiments were conducted when the flow rate of the simulated gas was 7.0 L / min.
  • the flow rate of the simulated exhaust gas was 7.0 L / min
  • the radical gas at the remote was 0.7 L / min
  • the initial concentration of NO was 300 ppm.
  • the flow rate of the reducing agent aqueous solution to be flowed to the packed column was 0.20 L / min
  • the concentration of Na 2 SO was 2.0 g / L.
  • the frequency was set to 420 Hz.
  • the residence time in the plasma reactor at this time was 0.6 s for the direct method and 6.0 s for the remote method.
  • FIGS. 7A-B and 8A-B The results are shown in FIGS. 7A-B and 8A-B.
  • Fig. 7A shows the direct plasma method only (Comparative Example 4)
  • Fig. 7B shows the process in which the direct plasma method and the wet reactor are directly connected
  • Fig. 8A shows the non-thermal remote plasma method only
  • FIGS. 7A-B and 8A-B Comparing FIGS. 7A-B and 8A-B, as in the cases of FIGS. 5A-B and 6A-B, the non-thermal remote plasma method (FIGS. 8A-B) consumes less reactor power.
  • Fig. 8B also shows that the reduction amount of NO and NOx, where the reactor power consumption is smaller, is larger.
  • NO was about 10 ppm and CO was 7 ppm or less.
  • the concentration of CO was around 370 ppm, with a few ppm decrease.
  • FIGS. 9A-B show examples of voltage and current waveforms corresponding to FIGS. 8A-B, respectively.
  • Unit treatment gas volume for the treatment in which the nonthermal remote plasma method shown in FIG. 1 and the wet reactor are directly connected (Example 3) and the treatment in which the direct plasma method and the wet reactor shown in FIG.
  • SED per unit plasma consumption energy
  • the plasma-chemical nanolibritt process using the non-thermal remote plasma method of the present example shows a significant improvement in energy efficiency, and it is approximately compared to the case where the direct plasma method is used. It was confirmed that NOx was reduced and removed with energy per unit flow rate of 30%.
  • the energy consumption can be further reduced by lowering the plasma consumption energy per unit flow rate.
  • Example 4 a pilot test using an actual boiler was conducted to demonstrate the remote non-thermal plasma 'chemical no-e-blit process technology of the present invention.
  • FIG. 1 An experimental device diagram is shown in FIG. The same reference numerals are given to the devices common to FIG. 1 and the description is omitted.
  • a small-sized smoke pipe type small boiler 60 using A fuel oil as fuel was used as a boiler.
  • the exhaust gas from the boiler 60 was supplied from the exhaust gas supply line 23 to the oxidation reaction zone 10 in the lower part of the chemical scrubber 11.
  • a non-thermal plasma reactor 1 was a pulse discharge reactor. 21 high voltage power supply.
  • the chemical scrubber 11 is filled with a filler as shown in FIG. 3 to promote gas-liquid contact reaction. Also, the Na 2 SO 4 aqueous solution is
  • the chemical scrubber 11 was supplied from the top of the 2 3 4 tank 41 to the spray 42 to be sprayed, collected at the bottom, and pumped back to the top.
  • the radical gas generated by the non-thermal plasma reactor 1 by sucking the outside air is carried by the fan 61 rotated by the motor, injected into the exhaust gas flue, and oxidized in the lower part of the chemical scrubber 11.
  • NO in exhaust gas is oxidized to NO by radicals such as ozone, and in the chemical scrubber 11, NO is reduced and removed to Na by Na 2 SO 4,
  • Figure 12 shows the relationship between plasma consumption energy per unit process gas volume and NO, NOx removal efficiency when changing to 0-180 Nm 3 Zh. From Fig. 12, it can be confirmed that NO and NOx can be removed efficiently even with high temperature exhaust gas.
  • the exhaust gas treatment method and apparatus of the present invention are a diesel engine, a boiler, a gaster It can be connected to combustion systems such as bottles and incinerators.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treating Waste Gases (AREA)
  • Exhaust Gas After Treatment (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un procédé pour purifier des gaz d'échappement contenant des oxydes d'azote, et un dispositif utilisé à cet effet. Le dispositif comprend un réacteur à plasma non équilibré à basse température et à pression atmosphérique (1) qui sert à convertir de l'air en gaz radical; une conduite (22) pour alimenter une zone de réaction d'oxydation (10) en gaz radical; une conduite (23) pour alimenter en gaz d'échappement la zone de réaction d'oxydation (10) séparément de la conduite de formation de gaz radical; la zone de réaction d'oxydation (10) qui sert à oxyder les oxydes d'azote contenus dans les gaz d'échappement avec le gaz radical, pour donner un gaz oxydé contenant NO2; et une zone de réaction de réduction (11) qui sert à mettre en contact le gaz oxydé avec une solution d'agent réducteur pour produire une réaction de réduction de NO2 en azote gazeux (N2), la zone de réaction d'oxydation (10) et la zone de réaction de réduction (11) étant reliées directement entre elles. Ainsi, l'invention concerne un dispositif de traitement de gaz d'échappement et un procédé de traitement qui permettent de supprimer l'apparition de sous-produits réactionnels (par exemple N2O, HNO2, HNO3, NO3 et CO) dans les gaz d'échappement, avec un rendement élevé.
PCT/JP2004/017049 2004-01-07 2004-11-17 Procede pour traiter des gaz d'echappement et dispositif utilise a cet effet WO2005065805A1 (fr)

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WO2008102708A1 (fr) * 2007-02-21 2008-08-28 Osaka Prefecture University Public Corporation Procédé et appareil pour le traitement d'un gaz d'échappement
JP2010061938A (ja) * 2008-09-03 2010-03-18 Akitoshi Okino プラズマ温度制御装置及びプラズマ温度制御方法
JP2011529430A (ja) * 2008-07-29 2011-12-08 ユニオン、エンジニアリング、アクティーゼルスカブ 高純度二酸化炭素の回収方法
KR101408337B1 (ko) 2012-08-07 2014-06-17 엠엔테크(주) 재활용시스템용 배출가스 저감장치
US10940471B1 (en) 2019-10-30 2021-03-09 W. L. Gore & Associates, Inc. Catalytic efficiency of flue gas filtration
US11071947B2 (en) 2019-10-30 2021-07-27 W. L. Gore & Associates, Inc. Catalytic efficiency of flue gas filtration
US11448409B2 (en) 2020-01-28 2022-09-20 Samsung Electronics Co., Ltd. Device and method for purifying air purification device and method

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CN104772014A (zh) * 2015-04-10 2015-07-15 无锡华光新动力环保科技股份有限公司 一种水泥回转窑炉烟气联合脱硝装置及其脱硝工艺

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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101110667B1 (ko) 2007-02-21 2012-02-17 도꾸리쯔교세이호징 가가꾸 기쥬쯔 신꼬 기꼬 배기 가스의 처리 방법 및 처리 장치
US8574506B2 (en) 2007-02-21 2013-11-05 Osaka Prefecture University Public Corporation Method and apparatus for processing exhaust gas
WO2008102708A1 (fr) * 2007-02-21 2008-08-28 Osaka Prefecture University Public Corporation Procédé et appareil pour le traitement d'un gaz d'échappement
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