WO2020083198A1 - 排气处理系统及方法 - Google Patents

排气处理系统及方法 Download PDF

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Publication number
WO2020083198A1
WO2020083198A1 PCT/CN2019/112256 CN2019112256W WO2020083198A1 WO 2020083198 A1 WO2020083198 A1 WO 2020083198A1 CN 2019112256 W CN2019112256 W CN 2019112256W WO 2020083198 A1 WO2020083198 A1 WO 2020083198A1
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WIPO (PCT)
Prior art keywords
electric field
exhaust gas
ozone
present
dust
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PCT/CN2019/112256
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English (en)
French (fr)
Inventor
唐万福
段志军
王大祥
邹永安
奚勇
Original Assignee
上海必修福企业管理有限公司
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Application filed by 上海必修福企业管理有限公司 filed Critical 上海必修福企业管理有限公司
Priority to JP2021523033A priority Critical patent/JP2022505945A/ja
Priority to BR112021007637-9A priority patent/BR112021007637A2/pt
Priority to CN201980069619.9A priority patent/CN113474075A/zh
Priority to EP19876827.7A priority patent/EP3871756A4/en
Priority to US17/287,932 priority patent/US20210372308A1/en
Publication of WO2020083198A1 publication Critical patent/WO2020083198A1/zh

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    • B01D2257/708—Volatile organic compounds V.O.C.'s
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/80—Employing electric, magnetic, electromagnetic or wave energy, or particle radiation
    • B01D2259/804—UV light
    • 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
    • B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
    • B01D53/8675—Ozone
    • 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
    • B03C2201/00—Details of magnetic or electrostatic separation
    • B03C2201/08—Ionising electrode being a rod
    • 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
    • B03C2201/00—Details of magnetic or electrostatic separation
    • B03C2201/30—Details of magnetic or electrostatic separation for use in or with vehicles
    • 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
    • B03C2201/00—Details of magnetic or electrostatic separation
    • B03C2201/32—Checking the quality of the result or the well-functioning of the device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2240/00—Combination or association of two or more different exhaust treating devices, or of at least one such device with an auxiliary device, not covered by indexing codes F01N2230/00 or F01N2250/00, one of the devices being
    • F01N2240/04—Combination or association of two or more different exhaust treating devices, or of at least one such device with an auxiliary device, not covered by indexing codes F01N2230/00 or F01N2250/00, one of the devices being an electric, e.g. electrostatic, device other than a heater
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2240/00—Combination or association of two or more different exhaust treating devices, or of at least one such device with an auxiliary device, not covered by indexing codes F01N2230/00 or F01N2250/00, one of the devices being
    • F01N2240/38—Combination or association of two or more different exhaust treating devices, or of at least one such device with an auxiliary device, not covered by indexing codes F01N2230/00 or F01N2250/00, one of the devices being an ozone (O3) generator, e.g. for adding ozone after generation of ozone from air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2250/00—Combinations of different methods of purification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2250/00—Combinations of different methods of purification
    • F01N2250/10—Combinations of different methods of purification cooling and filtering
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2560/00—Exhaust systems with means for detecting or measuring exhaust gas components or characteristics
    • F01N2560/02—Exhaust systems with means for detecting or measuring exhaust gas components or characteristics the means being an exhaust gas sensor
    • F01N2560/026—Exhaust systems with means for detecting or measuring exhaust gas components or characteristics the means being an exhaust gas sensor for measuring or detecting NOx
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2570/00—Exhaust treating apparatus eliminating, absorbing or adsorbing specific elements or compounds
    • F01N2570/14—Nitrogen oxides
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2610/00—Adding substances to exhaust gases
    • F01N2610/02—Adding substances to exhaust gases the substance being ammonia or urea
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2610/00—Adding substances to exhaust gases
    • F01N2610/06—Adding substances to exhaust gases the substance being in the gaseous form
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N2900/00—Details of electrical control or of the monitoring of the exhaust gas treating apparatus
    • F01N2900/04—Methods of control or diagnosing
    • F01N2900/0416—Methods of control or diagnosing using the state of a sensor, e.g. of an exhaust gas sensor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/005—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for draining or otherwise eliminating condensates or moisture accumulating in the apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL COMBUSTION ENGINES
    • F01N3/00—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust
    • F01N3/02—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for cooling, or for removing solid constituents of, exhaust
    • F01N3/0205—Exhaust or silencing apparatus having means for purifying, rendering innocuous, or otherwise treating exhaust for cooling, or for removing solid constituents of, exhaust using heat exchangers
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y02A50/2351—Atmospheric particulate matter [PM], e.g. carbon smoke microparticles, smog, aerosol particles, dust
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention belongs to the field of environmental protection and relates to an exhaust gas treatment system and method.
  • the exhaust gas formed by combustion usually contains a large amount of pollutants, and the direct discharge of the exhaust gas into the atmosphere will cause serious pollution to the environment. Therefore, the exhaust gas needs to be purified before being discharged.
  • the conventional technical route is to use the oxidation catalyst DOC to remove hydrocarbons THC and CO, while oxidizing low-valent NO to high-valent NO 2 ; after the DOC, the diesel particulate trap DPF is used to particulate PM Filtering; urea is injected after the diesel particulate trap DPF, urea is decomposed into ammonia gas NH 3 in the exhaust gas, and NH 3 undergoes a selective catalytic reduction reaction with NO 2 on the selective catalyst SCR afterwards to generate nitrogen N 2 and water. At the end, excess NH 3 is oxidized to N 2 and water on the ammonia gas oxidation catalyst ASC.
  • a large amount of urea needs to be added for the purification of exhaust gas, and the purification effect is general.
  • particulate filtering is usually performed by a particulate filter.
  • the DPF works in a combustion mode, that is, it uses carbon deposits in the porous structure to be fully blocked and then heated up to the ignition point to burn in a natural or combustion-supporting manner.
  • the working principle of DPF is as follows: the intake air with particulate matter enters the honeycomb carrier of the DPF, the particulate matter is intercepted in the honeycomb loading body, and most of the particulate matter has been filtered out when the exhaust gas flows out of the DPF.
  • the carrier materials of DPF are mainly cordierite, silicon carbide, aluminum titanate, etc., which can be selected and used according to the actual situation.
  • the above method stores the following defects:
  • Electrostatic dust removal is a gas dust removal method, usually used in metallurgy, chemical and other industrial fields to purify gas or recover useful dust particles.
  • gas dust removal method usually used in metallurgy, chemical and other industrial fields to purify gas or recover useful dust particles.
  • problems such as large occupied space, complicated system structure, and poor dust removal effect, etc.
  • an object of the present invention is to provide an exhaust gas treatment system with a better effect on exhaust gas purification treatment.
  • the present invention discovered new problems in the existing ionization dust removal technology through research, and solved it through a series of technical means, for example, when the exhaust temperature is lower than a certain temperature, the exhaust may contain liquid water, the present invention Install a water removal device in front of the electric field device to remove the liquid water in the exhaust gas to improve the ionization and dust removal effect; under high temperature conditions, by controlling the ratio of the dust collection area of the anode of the electric field device to the discharge area of the cathode, the length of the cathode / anode, The pole spacing and the setting of auxiliary electric field, etc., effectively reduce the electric field coupling, and make the electric field device still have high efficiency dust collection capacity under high temperature impact. Therefore, the present invention is suitable for operating under harsh conditions and guarantees dust removal efficiency.
  • Example 1 provided by the present invention: an emission treatment system.
  • Example 2 includes the above example 1, including a dust removal system, the dust removal system includes a dust removal system inlet, a dust removal system outlet, and a dust removal electric field device.
  • Example 3 provided by the present invention: including the above example 2, wherein the dust removal electric field device includes a dust removal electric field device inlet, a dust removal electric field device outlet, a dust removal electric field cathode and a dust removal electric field anode, the dust removal electric field cathode and the dust removal electric field electrode
  • the anode is used to generate an electric field for ionization and dust removal.
  • Example 4 provided by the present invention includes the above example 3, wherein the dust-removing electric field anode includes a first anode portion and a second anode portion, the first anode portion is close to the dust-removing electric field device inlet, and the second anode portion is close to the dust-removing At the exit of the electric field device, at least one cathode support plate is provided between the first anode portion and the second anode portion.
  • Example 5 provided by the present invention includes the above example 4, wherein the dust-removing electric field device further includes an insulating mechanism for achieving insulation between the cathode support plate and the dust-removing electric field anode.
  • Example 6 provided by the present invention includes the above example 5, wherein an electric field flow path is formed between the dust removal electric field anode and the dust removal electric field cathode, and the insulation mechanism is provided outside the electric field flow path.
  • Example 7 provided by the present invention includes the above example 5 or 6, wherein the insulating mechanism includes an insulating portion and a heat insulating portion; the material of the insulating portion is a ceramic material or a glass material.
  • Example 8 provided by the present invention includes the above example 7, wherein the insulating part is an umbrella-shaped string ceramic column, an umbrella-shaped string glass column, a column-shaped string ceramic column or a column-shaped glass column, and the glaze is hung on the inside or outside of the umbrella.
  • the insulating part is an umbrella-shaped string ceramic column, an umbrella-shaped string glass column, a column-shaped string ceramic column or a column-shaped glass column, and the glaze is hung on the inside or outside of the umbrella.
  • Example 9 provided by the present invention includes the above example 8, wherein the distance between the outer edge of the umbrella-shaped string ceramic column or the umbrella-shaped string glass column and the anode of the dust-removing electric field is greater than 1.4 times the electric field distance, and the umbrella-shaped string ceramic column or The total length of the umbrella flanges of the umbrella-shaped string glass column is 1.4 times greater than the insulation spacing of the umbrella-shaped string ceramic column or umbrella-shaped string glass column, and the total inner depth of the umbrella edge of the umbrella-shaped string ceramic column or umbrella-shaped string glass column is greater than that of the umbrella-shaped string The insulation distance of the ceramic column or glass string with umbrella-shaped string is 1.4 times.
  • Example 10 provided by the present invention: including any one of the above examples 4 to 9, wherein the length of the first anode portion is 1/10 to 1/4, 1/4 of the length of the anode of the dust removal electric field To 1/3, 1/3 to 1/2, 1/2 to 2/3, 2/3 to 3/4, or 3/4 to 9/10.
  • Example 11 provided by the present invention: including any one of the above examples 4 to 10, wherein the length of the first anode portion is long enough to remove part of dust and reduce accumulation in the insulating mechanism and the Describe the dust on the cathode support plate to reduce the electrical breakdown caused by the dust.
  • Example 12 provided by the present invention: including any one of the above examples 4 to 11, wherein the second anode portion includes a dust accumulation section and a reserved dust accumulation section.
  • Example 13 provided by the present invention: including any one of the above examples 3 to 12, wherein the dust-removing electric field cathode includes at least one electrode rod.
  • Example 14 provided by the present invention includes the above example 13, wherein the diameter of the electrode rod is not greater than 3 mm.
  • Example 15 provided by the present invention includes the above example 13 or 14, wherein the electrode rod has a needle shape, a polygonal shape, a burr shape, a threaded rod shape or a column shape.
  • Example 16 provided by the present invention: including any one of the above examples 3 to 15, wherein the dust-removing electric field anode is composed of a hollow tube bundle.
  • Example 17 provided by the present invention includes the above Example 16, wherein the hollow cross section of the anode tube bundle of the dust removal electric field adopts a circle or a polygon.
  • Example 18 provided by the present invention: including the above Example 17, wherein the polygon is a hexagon.
  • Example 19 provided by the present invention includes any one of the above examples 16 to 18, wherein the tube bundle of the anode of the dust-removing electric field has a honeycomb shape.
  • Example 20 provided by the present invention includes any one of the above examples 3 to 19, wherein the dedusting electric field cathode penetrates into the dedusting electric field anode.
  • Example 21 provided by the present invention includes any one of the above examples 3 to 20, wherein the dust removal electric field device performs carbon black removal treatment when the electric field accumulates dust to a certain degree.
  • Example 22 provided by the present invention includes the above example 21, wherein the dust removal electric field device detects the electric field current to determine whether the dust accumulation has reached a certain level, and carbon black removal treatment is required.
  • Example 23 provided by the present invention includes the above example 21 or 22, wherein the dust removal electric field device increases the electric field voltage to perform the carbon black removal process.
  • Example 24 provided by the present invention includes the above-mentioned Example 21 or 22, wherein the dust-removing electric field device performs a carbon black removal process using an electric field back-corona discharge phenomenon.
  • Example 25 provided by the present invention includes the above example 21 or 22, wherein the dust-removing electric field device utilizes the phenomenon of electric field back-corona discharge to increase the voltage and limit the injection current to cause the rapid discharge occurring at the position of the anode carbon deposit Plasma, which deeply oxidizes the organic components of carbon black, breaks the polymer bonds, and forms small-molecule carbon dioxide and water for carbon black removal treatment.
  • the dust-removing electric field device utilizes the phenomenon of electric field back-corona discharge to increase the voltage and limit the injection current to cause the rapid discharge occurring at the position of the anode carbon deposit Plasma, which deeply oxidizes the organic components of carbon black, breaks the polymer bonds, and forms small-molecule carbon dioxide and water for carbon black removal treatment.
  • Example 26 provided by the present invention: including any one of the above examples 3 to 25, wherein the length of the anode of the dust-removing electric field is 10-90 mm, and the length of the cathode of the dust-removing electric field is 10-90 mm.
  • Example 27 provided by the present invention includes the above example 26, wherein when the electric field temperature is 200 ° C, the corresponding dust collection efficiency is 99.9%.
  • Example 28 provided by the present invention includes the above example 26 or 27, wherein when the electric field temperature is 400 ° C., the corresponding dust collection efficiency is 90%.
  • Example 29 provided by the present invention: including any one of the above examples 26 to 28, wherein when the electric field temperature is 500 ° C., the corresponding dust collection efficiency is 50%.
  • Example 30 provided by the present invention includes any one of the above examples 3 to 29, wherein the dust removal electric field device further includes an auxiliary electric field unit for generating an auxiliary electric field that is not parallel to the ionized dust removal electric field.
  • Example 31 provided by the present invention includes any one of the above examples 3 to 29, wherein the dust removal electric field device further includes an auxiliary electric field unit, the ionized dust removal electric field includes a flow channel, and the auxiliary electric field unit is used for An auxiliary electric field that is not perpendicular to the flow channel is generated.
  • Example 32 provided by the present invention includes the above example 30 or 31, wherein the auxiliary electric field unit includes a first electrode, and the first electrode of the auxiliary electric field unit is disposed at or near the inlet of the ionization and dust removal electric field.
  • Example 33 provided by the present invention: including the above example 32, wherein the first electrode is a cathode.
  • Example 34 provided by the present invention: including the above example 32 or 33, wherein the first electrode of the auxiliary electric field unit is an extension of the cathode of the dust removal electric field.
  • Example 36 provided by the present invention: including any one of the above examples 30 to 35, wherein the auxiliary electric field unit includes a second electrode, and the second electrode of the auxiliary electric field unit is disposed at or near the ionization dust removal The exit of the electric field.
  • Example 37 provided by the present invention: including the above example 36, wherein the second electrode is an anode.
  • Example 38 provided by the present invention includes the above example 36 or 37, wherein the second electrode of the auxiliary electric field unit is an extension of the anode of the dust removal electric field.
  • Example 40 provided by the present invention includes any one of the above examples 30 to 33, 36 and 37, wherein the electrode of the auxiliary electric field and the electrode of the ionization and dust removal electric field are provided independently.
  • Example 41 provided by the present invention includes any one of the above Examples 3 to 40, wherein the ratio of the dust accumulation area of the dust removal electric field anode to the discharge area of the dust removal electric field cathode is 1.667: 1-1680: 1.
  • Example 42 provided by the present invention: including any one of the above Examples 3 to 40, wherein the ratio of the dust accumulation area of the dedusting electric field anode to the discharge area of the dedusting electric field cathode is 6.67: 1-56.67: 1.
  • Example 43 provided by the present invention: including any one of the above examples 3 to 42, wherein the diameter of the dust-removing electric field cathode is 1-3 mm, and the pole spacing between the dust-removing electric field anode and the dust-removing electric field cathode is 2.5-139.9 mm; the ratio of the dust accumulation area of the dust-removing electric field anode to the discharge area of the dust-removing electric field cathode is 1.667: 1-1680: 1.
  • Example 44 provided by the present invention: including any one of the above examples 3 to 42, wherein the electrode separation between the dust removal electric field anode and the dust removal electric field cathode is less than 150 mm.
  • Example 45 provided by the present invention: including any one of the above Examples 3 to 42, wherein the electrode separation between the anode of the dust removal electric field and the cathode of the dust removal electric field is 2.5-139.9 mm.
  • Example 46 provided by the present invention: including any one of the above examples 3 to 42, wherein the electrode separation between the anode of the dust removal electric field and the cathode of the dust removal electric field is 5-100 mm.
  • Example 47 provided by the present invention includes any one of the above examples 3 to 46, wherein the length of the anode of the dust-removing electric field is 10-180 mm.
  • Example 48 provided by the present invention: including any one of the above examples 3 to 46, wherein the length of the dust-removing electric field anode is 60-180 mm.
  • Example 49 provided by the present invention includes any one of the above examples 3 to 48, wherein the length of the dust-removing electric field cathode is 30-180 mm.
  • Example 50 provided by the present invention includes any one of the above Examples 3 to 48, wherein the length of the dust-removing electric field cathode is 54-176 mm.
  • Example 51 provided by the present invention: includes any one of the above examples 41 to 50, wherein, during operation, the number of couplings of the ionizing dust removal electric field is ⁇ 3.
  • Example 52 provided by the present invention: includes any one of the above examples 30 to 50, wherein, during operation, the number of couplings of the ionization and dust removal electric field is ⁇ 3.
  • Example 53 provided by the present invention includes any one of the above examples 3 to 52, wherein the value range of the electric field voltage of the ionization and dust removal is 1kv-50kv.
  • Example 54 provided by the present invention includes any one of the above examples 3 to 53, wherein the dust-removing electric field device further includes several connection housings, and the series electric field stages are connected through the connection housings.
  • Example 55 provided by the present invention includes the above example 54, wherein the distance between adjacent electric field levels is greater than 1.4 times the pole pitch.
  • Example 56 provided by the present invention includes any one of the above Examples 3 to 55, wherein the dust removal electric field device further includes a front electrode, and the front electrode is connected to the dust removal at the entrance of the dust removal electric field device Between the electric field anode and the ionization and dust removal electric field formed by the dust removal electric field cathode.
  • Example 57 provided by the present invention includes the above example 56, wherein the front electrode is dot-shaped, linear, mesh-shaped, orifice-shaped, plate-shaped, needle-rod-shaped, ball cage-shaped, box-shaped, tubular, Material natural form, or material processing form.
  • Example 58 provided by the present invention includes the above example 56 or 57, wherein the front electrode is provided with a through hole.
  • Example 59 provided by the present invention includes the above example 58, wherein the through hole is polygonal, circular, elliptical, square, rectangular, trapezoidal, or rhombic.
  • Example 60 provided by the present invention includes the above example 58 or 59, wherein the size of the through hole is 0.1-3 mm.
  • Example 61 provided by the present invention: including any one of the above examples 56 to 60, wherein the front electrode is a combination of one or more forms of solid, liquid, gas molecular cluster, or plasma .
  • Example 62 provided by the present invention includes any one of the above examples 56 to 61, wherein the front electrode is a conductive mixed-state substance, a biological natural mixed conductive substance, or an object is artificially processed to form a conductive substance.
  • Example 63 provided by the present invention: including any one of the above examples 56 to 62, wherein the front electrode is 304 steel or graphite.
  • Example 64 provided by the present invention: including any one of the above examples 56 to 62, wherein the front electrode is an ion-containing conductive liquid.
  • Example 65 provided by the present invention: including any one of the above examples 56 to 64, wherein, during operation, before the gas carrying pollutants enters the ionization and dedusting electric field formed by the dedusting electric field cathode and the dedusting electric field anode, And when the gas with pollutants passes through the front electrode, the front electrode charges the pollutants in the gas.
  • Example 66 provided by the present invention includes the above example 65, wherein, when the gas carrying pollutants enters the ionization dust removal electric field, the anode of the dust removal electric field exerts an attractive force on the charged pollutants, causing the pollutants to the The anode of the dedusting electric field moves until pollutants adhere to the anode of the dedusting electric field.
  • Example 67 provided by the present invention: includes the above example 65 or 66, wherein the front electrode introduces electrons into pollutants, and the electrons are between the pollutants between the front electrode and the anode of the dust removal electric field Transfer it to make more pollutants electrified.
  • Example 68 provided by the present invention includes any one of the above examples 64 to 66, wherein between the front electrode and the anode of the dust-removing electric field, electrons are conducted through pollutants and an electric current is formed.
  • Example 69 provided by the present invention: including any one of the above examples 65 to 68, wherein the front electrode charges the pollutant by contact with the pollutant.
  • Example 70 provided by the present invention includes any one of the above examples 65 to 69, wherein the front electrode charges the pollutants by means of energy fluctuation.
  • Example 71 provided by the present invention: including any one of the above examples 65 to 70, wherein the front electrode is provided with a through hole.
  • Example 72 provided by the present invention includes any one of the above examples 56 to 71, wherein the front electrode is linear and the dust-removing electric field anode is planar.
  • Example 73 provided by the present invention: including any one of the above examples 56 to 72, wherein the front electrode is perpendicular to the dust removal electric field anode.
  • Example 74 provided by the present invention includes any one of the above examples 56 to 73, wherein the front electrode is parallel to the dust removal electric field anode.
  • Example 75 provided by the present invention includes any one of the above examples 56 to 74, wherein the front electrode is curved or arc-shaped.
  • Example 76 provided by the present invention: including any one of the above examples 56 to 75, wherein the front electrode uses a wire mesh.
  • Example 77 provided by the present invention includes any one of the above examples 56 to 76, wherein the voltage between the front electrode and the anode of the dust removal electric field is different from the cathode of the dust removal electric field and the dust removal electric field The voltage between the anodes.
  • Example 78 provided by the present invention includes any one of the above examples 56 to 77, wherein the voltage between the front electrode and the anode of the dust removal electric field is less than the initial halo voltage.
  • Example 79 provided by the present invention includes any one of the above examples 56 to 78, wherein the voltage between the front electrode and the anode of the dedusting electric field is 0.1 kv-2 kv / mm.
  • Example 80 provided by the present invention includes any one of the above examples 56 to 79, wherein the dust removal electric field device includes an exhaust gas flow path, and the front electrode is located in the exhaust gas flow path; the front The ratio of the cross-sectional area of the placed electrode to the cross-sectional area of the exhaust runner is 99% -10%, or 90-10%, or 80-20%, or 70-30%, or 60-40%, or 50%.
  • Example 81 provided by the present invention includes any one of the above examples 3 to 80, wherein the dust removal electric field device includes an electret element.
  • Example 82 provided by the present invention includes the above example 81, in which the electret element is in the ionization dust removal electric field when the anode of the dust removal electric field and the cathode of the dust removal electric field are powered on.
  • Example 83 provided by the present invention includes the above example 81 or 82, wherein the electret element is close to the outlet of the dust removal electric field device, or the electret element is provided at the outlet of the dust removal electric field device.
  • Example 84 provided by the present invention includes any one of the above examples 81 to 83, wherein the dedusting electric field anode and the dedusting electric field cathode form an exhaust gas flow path, and the electret element is provided in the In the exhaust runner.
  • Example 85 provided by the present invention includes the above example 84, wherein the exhaust runner includes an exhaust runner outlet, the electret element is close to the exhaust runner outlet, or, the electret The body element is provided at the outlet of the exhaust runner.
  • Example 86 provided by the present invention includes the above example 84 or 85, wherein the cross-section of the electret element in the exhaust flow passage accounts for 5% -100% of the cross-section of the exhaust flow passage.
  • Example 87 provided by the present invention: including the above example 86, wherein the cross-section of the electret element in the exhaust runner accounts for 10% -90%, 20% -80% of the cross section of the exhaust runner , Or 40% -60%.
  • Example 88 provided by the present invention includes any one of the above examples 81 to 87, wherein the ionization and dust removal electric field charges the electret element.
  • Example 89 provided by the present invention: includes any one of the above examples 81 to 88, wherein the electret element has a porous structure.
  • Example 90 provided by the present invention: includes any one of the above examples 81 to 89, wherein the electret element is a fabric.
  • Example 91 provided by the present invention: including any one of the above examples 81 to 90, wherein the anode of the dust-removing electric field is tubular, the exterior of the electret element is tubular, and the exterior of the electret element Set inside the anode of the dust removal electric field.
  • Example 92 provided by the present invention: including any one of the above examples 81 to 91, wherein the electret element and the dust-removing electric field anode are detachably connected.
  • Example 93 provided by the present invention: including any one of the above examples 81 to 92, wherein the material of the electret element includes an inorganic compound having electret properties.
  • Example 94 provided by the present invention includes the above Example 93, wherein the inorganic compound is selected from one or more combinations of oxygen-containing compounds, nitrogen-containing compounds, or glass fibers.
  • Example 95 provided by the present invention includes the above Example 94, wherein the oxygen-containing compound is selected from one or more combinations of metal-based oxides, oxygen-containing complexes, and oxygen-containing inorganic heteropoly acid salts.
  • Example 96 provided by the present invention: including the above Example 95, wherein the metal-based oxide is selected from aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, lead oxide, tin oxide One or more combinations.
  • the metal-based oxide is selected from aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, lead oxide, tin oxide One or more combinations.
  • Example 97 provided by the present invention includes the above Example 95, wherein the metal-based oxide is alumina.
  • Example 98 provided by the present invention includes the above Example 95, wherein the oxygen-containing composite is selected from one or more combinations of titanium zirconium composite oxide or titanium barium composite oxide.
  • Example 99 provided by the present invention includes the above Example 95, wherein the oxygen-containing inorganic heteropoly acid salt is selected from one or more combinations of zirconium titanate, lead zirconate titanate, or barium titanate.
  • Example 100 provided by the present invention: including the above example 94, wherein the nitrogen-containing compound is silicon nitride.
  • Example 101 provided by the present invention includes any one of the above examples 81 to 100, wherein the material of the electret element includes an organic compound having electret properties.
  • Example 102 provided by the present invention: including the above example 101, wherein the organic compound is selected from one or more combinations of fluoropolymer, polycarbonate, PP, PE, PVC, natural wax, resin, and rosin .
  • Example 103 provided by the present invention: including the above example 102, wherein the fluoropolymer is selected from one or more of polytetrafluoroethylene, polyperfluoroethylene propylene, soluble polytetrafluoroethylene, and polyvinylidene fluoride Kinds of combinations.
  • Example 104 provided by the present invention: including the above example 102, wherein the fluoropolymer is polytetrafluoroethylene.
  • Example 105 provided by the present invention: includes any one of the above examples 2 to 104, and further includes a wind equalizing device.
  • Example 106 provided by the present invention includes the above example 105, wherein the air-equalizing device is between the inlet of the dust removal system and the ionization and dust removal electric field formed by the anode of the dust removal electric field and the cathode of the dust removal electric field.
  • the wind-equalizing device includes: an air inlet pipe provided on one side of the anode of the dust-removing electric field and an air outlet pipe provided on the other side; opposition.
  • Example 107 provided by the present invention includes the above example 105, wherein the air-equalizing device is between the inlet of the dust removal system and the ionization dust removal electric field formed by the anode of the dust removal electric field and the cathode of the dust removal electric field.
  • the air-equalizing device is composed of several rotatable air-equating blades.
  • Example 108 provided by the present invention includes the above example 105, in which the first venturi plate wind equalizing mechanism of the wind equalizing device and the second venturi plate wind equalizing mechanism provided at the outlet end of the anode of the dust removal field, so
  • the first venturi plate air distribution mechanism is provided with an air inlet hole
  • the second venturi plate air distribution mechanism is provided with an air outlet hole
  • the air inlet hole and the air outlet hole are arranged in a staggered arrangement, and the front air intake The air is emitted from the side to form a cyclone structure.
  • Example 109 provided by the present invention includes any one of the above examples 2 to 108, wherein it further includes an oxygen supplement device for adding a gas including oxygen before the ionization and dedusting electric field.
  • Example 110 provided by the present invention includes the above example 109, wherein the oxygen supplementing device adds oxygen by simply increasing oxygen, passing in outside air, passing in compressed air, and / or passing in ozone.
  • Example 111 provided by the present invention includes the above example 109 or 110, wherein the oxygen supplementation amount is determined at least according to the content of exhaust particles.
  • Example 112 provided by the present invention includes any one of the above examples 2 to 111, wherein it further includes a water removal device for removing liquid water before the inlet of the dust removal electric field device.
  • Example 113 provided by the present invention includes the above example 112, wherein, when the temperature of the exhaust gas is lower than a certain temperature, the water removal device removes the liquid water in the exhaust gas.
  • Example 114 provided by the present invention includes the above example 113, wherein the certain temperature is above 90 ° C and below 100 ° C.
  • Example 115 provided by the present invention includes the above example 113, wherein the certain temperature is above 80 ° C and below 90 ° C.
  • the example 116 provided by the present invention includes the above example 113, wherein the certain temperature is below 80 ° C.
  • Example 117 provided by the present invention includes the above examples 112 to 116, wherein the water removal device is an electrocoagulation device.
  • Example 118 provided by the present invention includes any one of the above examples 2 to 117, wherein it further includes a temperature reduction device for reducing the temperature of the exhaust gas before the entrance of the dust removal electric field device.
  • Example 119 provided by the present invention includes the above example 118, wherein the temperature lowering device includes a heat exchange unit for heat exchange with exhaust gas to heat the liquid heat exchange medium in the heat exchange unit to a gaseous exchange Thermal medium.
  • Example 120 provided by the present invention includes the above example 119, wherein the heat exchange unit includes:
  • Exhaust gas passes through the cavity and communicates with the exhaust line.
  • the exhaust gas passes through the cavity for exhaust gas to pass through;
  • a medium gasification chamber which is used to convert a liquid heat exchange medium and exhaust gas into a gaseous state after heat exchange.
  • Example 121 provided by the present invention includes the above example 119 or 120, wherein it further includes a power generation unit for converting the heat energy of the heat exchange medium and / or the heat energy of the exhaust gas into mechanical energy.
  • Example 122 provided by the present invention includes the above example 121, wherein the power generation unit includes a turbofan.
  • Example 123 provided by the present invention includes the above example 122, wherein the turbofan includes:
  • the medium cavity turbofan assembly is installed on the turbofan shaft, and the medium cavity turbofan assembly is located in the medium gasification cavity.
  • Example 124 provided by the present invention includes the above example 123, wherein the medium cavity turbofan assembly includes a medium cavity guide fan and a medium cavity power fan.
  • Example 125 provided by the present invention: including any one of the above examples 122 to 124, wherein the turbofan includes:
  • the cavity turbofan assembly is installed on the turbofan shaft, and the cavity turbofan assembly is located in the exhaust gas passing cavity.
  • Example 126 provided by the present invention includes the above example 125, wherein the cavity turbofan assembly includes an exhaust cavity guide fan and an exhaust cavity power fan.
  • Example 127 provided by the present invention includes any one of the above examples 121 to 126, wherein the temperature reduction device further includes a power generation unit for converting mechanical energy generated by the power generation unit into electrical energy.
  • Example 128 provided by the present invention includes the above example 127, wherein the power generation unit includes a generator stator and a generator rotor, and the generator rotor is connected to a turbofan shaft of the power generation unit.
  • Examples provided by the present invention include the above examples 127 or 128, wherein the power generation unit includes a battery assembly.
  • Example 130 provided by the present invention includes any one of the above examples 127 to 129, wherein the power generation unit includes a generator regulation component for regulating the electric torque of the generator.
  • Example 131 provided by the present invention includes any one of the above examples 121 to 130, wherein the temperature lowering device further includes a medium transmission unit connected between the heat exchange unit and the power generation unit.
  • Example 132 provided by the present invention: includes the above example 131, wherein the medium transmission unit includes a reverse thrust duct.
  • Example 133 provided by the present invention includes the above example 131, wherein the medium transmission unit includes a pressure-bearing pipeline.
  • Example 134 provided by the present invention includes any one of the above examples 127 to 133, wherein the cooling device further includes a coupling unit electrically connected between the power generation unit and the power generation unit.
  • Example 135 provided by the present invention includes the above example 134, wherein the coupling unit includes an electromagnetic coupler.
  • Example 136 provided by the present invention includes any one of the above examples 119 to 135, wherein the temperature lowering device further includes a heat preservation pipe, the heat preservation pipe is connected between the exhaust pipe and the heat exchange unit .
  • Example 137 provided by the present invention: including any one of the above examples 118 to 136, wherein the cooling device includes a fan, and the fan plays a role in the exhaust before passing the air into the inlet of the dust removal electric field device The role of cooling.
  • Example 138 provided by the present invention: including the above example 137, wherein the air passing in is 50% to 300% of the exhaust gas.
  • Example 139 provided by the present invention: including the above example 137, wherein the air passed in is 100% to 180% of the exhaust gas.
  • Example 140 provided by the present invention: including the above example 137, wherein the air passing in is 120% to 150% of the exhaust gas.
  • Example 141 provided by the present invention includes the above example 120, wherein the oxygen supplement device includes a fan, and the fan plays a role in cooling the exhaust gas before passing the air into the inlet of the dust removal electric field device.
  • Example 142 provided by the present invention: including the above example 141, wherein the air passing in is 50% to 300% of the exhaust gas.
  • Example 143 provided by the present invention: including the above example 141, wherein the air passed in is 100% to 180% of the exhaust gas.
  • Example 144 provided by the present invention: including the above example 141, wherein the air passing in is 120% to 150% of the exhaust gas.
  • Example 145 provided by the present invention includes any one of the above Examples 1-144, and further includes an ozone purification system including a reaction field for mixing and reacting the ozone stream with the exhaust stream.
  • Example 146 provided by the present invention: including the above example 145, wherein the reaction field includes pipes and / or reactors.
  • Example 147 provided by the present invention includes the above-mentioned example 146, in which at least one of the following technical features is also included:
  • the pipe section diameter is 100-200 mm
  • the length of the pipe is greater than 0.1 times the pipe diameter
  • the reactor is selected from at least one of the following:
  • Reactor 1 The reactor has a reaction chamber, and exhaust gas and ozone are mixed and reacted in the reaction chamber;
  • the reactor includes a number of honeycomb-shaped cavities for providing a space where exhaust gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing cold state medium to control the discharge Reaction temperature of gas and ozone;
  • Reactor 3 The reactor includes several carrier units, and the carrier unit provides a reaction site;
  • Reactor 4 The reactor includes a catalyst unit, and the catalyst unit is used to promote the oxidation reaction of exhaust gas;
  • the reaction field is provided with an ozone inlet, and the ozone inlet is selected from at least one of a nozzle, a spray grid, a nozzle, a swirl nozzle, and a nozzle provided with a venturi tube;
  • the reaction field is provided with an ozone inlet.
  • the ozone enters the reaction field through the ozone inlet and contacts the exhaust gas.
  • the setting of the ozone inlet forms at least one of the following directions: The flow direction of the air is perpendicular, tangential to the flow direction of the exhaust gas, the flow direction of the inserted exhaust gas, and multiple directions are in contact with the exhaust gas.
  • Example 148 provided by the present invention: including any one of the above examples 145 to 147, wherein the reaction field includes an exhaust pipe, a regenerator device, or a catalyst.
  • Example 149 provided by the present invention: including any one of the above examples 145 to 148, wherein the temperature of the reaction field is -50-200 ° C.
  • Example 150 provided by the present invention: including the above example 149, wherein the temperature of the reaction field is 60-70 ° C.
  • Example 151 provided by the present invention: including any one of the above examples 145 to 150, wherein the ozone purification system further includes an ozone source for providing an ozone stream.
  • Example 152 provided by the present invention includes the above example 151, wherein the ozone source includes a storage ozone unit and / or an ozone generator.
  • Example 153 provided by the present invention: including the above example 152, wherein the ozone generator includes a surface discharge ozone generator, a power frequency arc ozone generator, a high frequency induction ozone generator, a low pressure ozone generator, ultraviolet rays A combination of one or more of an ozone generator, an electrolyte ozone generator, a chemical ozone generator, and a radiation irradiation particle generator.
  • the ozone generator includes a surface discharge ozone generator, a power frequency arc ozone generator, a high frequency induction ozone generator, a low pressure ozone generator, ultraviolet rays A combination of one or more of an ozone generator, an electrolyte ozone generator, a chemical ozone generator, and a radiation irradiation particle generator.
  • Example 154 provided by the present invention includes the above example 152, wherein the ozone generator includes an electrode, and a catalyst layer is provided on the electrode, and the catalyst layer includes an oxidation catalytic bond cracking selective catalyst layer.
  • Example 155 provided by the present invention includes the above example 154, wherein the electrode includes a high-voltage electrode or a high-voltage electrode provided with a barrier dielectric layer, and when the electrode includes a high-voltage electrode, the oxidation catalytic bond cleavage selective catalyst A layer is provided on the surface of the high-voltage electrode.
  • the electrode includes the high-voltage electrode of the barrier medium layer, the selective catalytic layer for oxidative catalytic bond cleavage is provided on the surface of the barrier medium layer.
  • Example 156 provided by the present invention includes the above example 155, wherein the barrier medium layer is selected from at least one of ceramic plates, ceramic tubes, quartz glass plates, quartz plates, and quartz tubes.
  • Example 157 provided by the present invention includes the above example 155, wherein, when the electrode includes a high-voltage electrode, the thickness of the oxidation catalytic bond cleavage selective catalyst layer is 1-3 mm; when the electrode includes a barrier medium layer In the case of high-voltage electrodes, the loading of the selective catalytic layer for the oxidation catalytic bond cleavage includes 1-12 wt% of the barrier medium layer.
  • Example 158 provided by the present invention includes any one of the above examples 154 to 157, wherein the oxidation catalytic bond cleavage selective catalyst layer includes the following components in weight percentages:
  • the active component is selected from at least one of a compound of metal M and metal element M
  • the metal element M is selected from alkaline earth metal elements, transition metal elements, fourth main group metal elements, precious metal elements and lanthanide rare earth elements At least one of
  • the coating is selected from at least one of alumina, cerium oxide, zirconia, manganese oxide, metal composite oxides, porous materials, and layered materials.
  • the metal composite oxide includes aluminum, cerium, zirconium, and manganese A composite oxide of one or more metals.
  • Example 159 provided by the present invention: including the above example 158, wherein the alkaline earth metal element is selected from at least one of magnesium, strontium and calcium.
  • Example 160 provided by the present invention includes the above example 158, wherein the transition metal element is selected from at least one of titanium, manganese, zinc, copper, iron, nickel, cobalt, yttrium, and zirconium.
  • Example 161 provided by the present invention: including the above example 158, wherein the metal element of the fourth main group is tin.
  • Example 162 provided by the present invention: including the above example 158, wherein the precious metal element is selected from at least one of platinum, rhodium, palladium, gold, silver, and iridium.
  • Example 163 provided by the present invention includes the above example 158, wherein the lanthanide rare earth element is selected from at least one of lanthanum, cerium, praseodymium, and samarium.
  • Example 164 provided by the present invention: including the above example 158, wherein the compound of the metal element M is selected from at least one of oxides, sulfides, sulfates, phosphates, carbonates, and perovskites .
  • Example 165 provided by the present invention: including the above example 158, wherein the porous material is selected from at least one of molecular sieve, diatomaceous earth, zeolite, and carbon nanotubes.
  • Example 166 provided by the present invention: including the above example 158, wherein the layered material is selected from at least one of graphene and graphite.
  • Example 167 provided by the present invention: including any one of the above examples 145 to 166, wherein the ozone purification system further includes an ozone amount control device for controlling the amount of ozone so as to effectively oxidize the gas to be treated in the exhaust gas Components, the ozone amount control device includes a control unit.
  • Example 168 provided by the present invention includes the above example 167, wherein the ozone amount control device further includes an exhaust gas component detection unit before ozone treatment, for detecting the exhaust gas component content before ozone treatment.
  • Example 169 provided by the present invention includes any one of the above examples 167 to 168, wherein the control unit controls the amount of ozone required for the mixing reaction according to the content of the exhaust gas component before the ozone treatment.
  • Example 170 provided by the present invention includes the above example 168 or 169, wherein the exhaust gas component detection unit before ozone treatment is selected from at least one of the following detection units:
  • the first volatile organic compound detection unit is used to detect the content of volatile organic compounds in the exhaust gas before ozone treatment
  • the first CO detection unit is used to detect the CO content in the exhaust gas before ozone treatment
  • the first nitrogen oxide detection unit is used to detect the nitrogen oxide content in the exhaust gas before ozone treatment.
  • Example 171 provided by the present invention includes the above example 170, wherein the control unit controls the amount of ozone required for the mixed reaction according to the output value of at least one of the exhaust composition detection unit before ozone treatment.
  • Example 172 provided by the present invention includes any one of the above examples 167 to 171, wherein the control unit is used to control the amount of ozone required for the mixed reaction according to a preset mathematical model.
  • Example 173 provided by the present invention includes any one of the above examples 167 to 172, wherein the control unit is used to control the amount of ozone required for the mixed reaction according to a theoretical estimated value.
  • Example 174 provided by the present invention includes any one of the above example 173, wherein the theoretical estimated value is: the molar ratio of ozone flux to the object to be treated in the exhaust gas is 2-10.
  • Example 175 provided by the present invention includes any one of the above examples 167 to 174, wherein the ozone amount control device includes an ozone-treated exhaust gas component detection unit for detecting the exhaust gas-treated exhaust gas component content.
  • Example 176 provided by the present invention includes any one of the above examples 167 to 175, wherein the control unit controls the amount of ozone required for the mixing reaction according to the content of the exhaust gas component after the ozone treatment.
  • Example 177 provided by the present invention includes the above example 175 or 176, wherein the exhaust gas component detection unit after ozone treatment is selected from at least one of the following detection units:
  • the first ozone detection unit is used to detect the ozone content in the exhaust gas after ozone treatment
  • the second volatile organic compound detection unit is used to detect the content of volatile organic compounds in the exhaust gas after ozone treatment
  • the second CO detection unit is used to detect the CO content in the exhaust gas after ozone treatment
  • the second nitrogen oxide detection unit is used to detect the nitrogen oxide content in the exhaust gas after ozone treatment.
  • Example 178 provided by the present invention includes the above example 177, wherein the control unit controls the amount of ozone according to the output value of at least one of the ozone-treated exhaust gas composition detection unit.
  • Example 179 provided by the present invention includes any one of the above examples 145 to 178, wherein the ozone purification system further includes a denitration device for removing the mixed reaction product of the ozone stream and the exhaust stream Nitric acid.
  • Example 180 provided by the present invention includes the above example 179, wherein the denitration device includes an electrocoagulation device, and the electrocoagulation device includes:
  • a first electrode, the first electrode is located in the electrocoagulation flow channel
  • Example 181 provided by the present invention includes the above example 180, wherein the first electrode is a solid, liquid, gas molecular group, plasma, conductive mixed-state substance, biological natural mixed conductive substance, or artificially formed by an object A combination of one or more forms in a conductive substance.
  • Example 182 provided by the present invention: including the above example 180 or 181, wherein the first electrode is solid metal, graphite, or 304 steel.
  • Example 183 provided by the present invention: including any one of the above examples 180 to 182, wherein the first electrode is dot-shaped, wire-shaped, mesh-shaped, orifice-shaped, plate-shaped, needle-rod-shaped, ball cage Shaped, box-shaped, tubular, natural form material, or processed form material.
  • Example 184 provided by the present invention includes any one of the above examples 180 to 183, wherein the first electrode is provided with a front through hole.
  • Example 185 provided by the present invention includes the above example 184, wherein the shape of the front through hole is polygon, circle, ellipse, square, rectangle, trapezoid, or rhombus.
  • Example 186 provided by the present invention: including the above example 184 or 185, wherein the hole diameter of the front through hole is 0.1-3 mm.
  • Example 187 provided by the present invention: including any one of the above examples 180 to 186, wherein the second electrode has a multi-layer mesh shape, a mesh shape, a perforated plate shape, a tubular shape, a barrel shape, a ball cage shape, Box-shaped, plate-shaped, granular layered, bent plate-shaped, or panel-shaped.
  • Example 188 provided by the present invention includes any one of the above examples 180 to 187, wherein the second electrode is provided with a rear through hole.
  • Example 189 provided by the present invention: including the above example 188, wherein the rear through hole is polygonal, circular, elliptical, square, rectangular, trapezoidal, or rhombic.
  • Example 190 provided by the present invention: including the above example 188 or 189, wherein the diameter of the rear through hole is 0.1-3 mm.
  • Example 191 provided by the present invention includes any one of the above examples 180 to 190, wherein the second electrode is made of a conductive substance.
  • Example 192 provided by the present invention: including any one of the above examples 180 to 191, wherein the surface of the second electrode has a conductive substance.
  • Example 193 provided by the present invention includes any one of the above examples 180 to 192, wherein there is an electrocoagulation electric field between the first electrode and the second electrode, the electrocoagulation electric field is a point-surface electric field, a line A combination of one or more electric fields in the surface electric field, mesh surface electric field, dot barrel electric field, line barrel electric field, or mesh barrel electric field.
  • Example 194 provided by the present invention includes any one of the above examples 180 to 193, wherein the first electrode is linear and the second electrode is planar.
  • Example 195 provided by the present invention includes any one of the above examples 180 to 194, wherein the first electrode is perpendicular to the second electrode.
  • Example 196 provided by the present invention includes any one of the above examples 180 to 195, wherein the first electrode is parallel to the second electrode.
  • Example 197 provided by the present invention includes any one of the above examples 180 to 196, wherein the first electrode is curved or arc-shaped.
  • Example 198 provided by the present invention includes any one of the above examples 180 to 197, wherein both the first electrode and the second electrode are planar, and the first electrode is parallel to the second electrode.
  • Example 199 provided by the present invention includes any one of the above examples 180 to 198, wherein the first electrode uses a wire mesh.
  • Example 200 provided by the present invention: including any one of the above examples 180 to 199, wherein the first electrode is planar or spherical.
  • Example 201 provided by the present invention includes any one of the above examples 180 to 200, wherein the second electrode is curved or spherical.
  • Example 202 provided by the present invention includes any one of the above examples 180 to 201, wherein the first electrode has a dot shape, a line shape, or a mesh shape, and the second electrode has a barrel shape, the The first electrode is located inside the second electrode, and the first electrode is located on the central axis of symmetry of the second electrode.
  • Example 203 provided by the present invention includes any one of the above examples 180 to 202, wherein the first electrode is electrically connected to one electrode of the power supply, and the second electrode is electrically connected to the other electrode of the power supply connection.
  • Example 204 provided by the present invention includes any one of the above examples 180 to 203, wherein the first electrode is electrically connected to the cathode of the power supply, and the second electrode is electrically connected to the anode of the power supply
  • Example 205 provided by the present invention includes the above example 203 or 204, wherein the voltage of the power supply is 5-50KV.
  • Example 206 provided by the present invention includes any one of the above examples 203 to 205, wherein the voltage of the power supply is less than the initial halo voltage.
  • Example 207 provided by the present invention: including any one of the above examples 203 to 206, wherein the voltage of the power supply is 0.1kv-2kv / mm.
  • Example 208 provided by the present invention includes any one of the above examples 203 to 207, wherein the voltage waveform of the power supply is a DC waveform, a sine wave, or a modulation waveform.
  • Example 209 provided by the present invention includes any one of the above examples 203 to 208, wherein the power supply is an AC power supply, and the frequency conversion pulse range of the power supply is 0.1 Hz to 5 GHz.
  • Example 210 provided by the present invention includes any one of the above examples 180 to 209, wherein the first electrode and the second electrode both extend in the left-right direction, and the left end of the first electrode is located on the second electrode Left of the left end.
  • Example 211 provided by the present invention includes any one of the above examples 180 to 210, wherein there are two second electrodes, and the first electrode is located between the two second electrodes.
  • Example 212 provided by the present invention includes any one of the above examples 180 to 211, wherein the distance between the first electrode and the second electrode is 5-50 mm.
  • Example 213 provided by the present invention includes any one of the above examples 180 to 212, wherein the first electrode and the second electrode constitute an adsorption unit, and there are a plurality of adsorption units.
  • Example 214 provided by the present invention includes the above example 213, wherein all the adsorption units are distributed in one or more directions of the left-right direction, the front-rear direction, the oblique direction, or the spiral direction.
  • Example 215 provided by the present invention includes any one of the above examples 180 to 214, wherein it further includes an electrocoagulation housing including an electrocoagulation inlet, an electrocoagulation outlet, and the electrocoagulation For the flow channel, the two ends of the electrocoagulation flow channel are respectively connected to the electrocoagulation inlet and the electrocoagulation outlet.
  • Example 216 provided by the present invention includes the above example 215, wherein the electrocoagulation inlet is circular, and the diameter of the electrocoagulation inlet is 300-1000 mm, or 500 mm.
  • Example 217 provided by the present invention includes the above example 215 or 216, wherein the electrocoagulation outlet is circular, and the diameter of the electrocoagulation outlet is 300-1000 mm, or 500 mm.
  • Example 218 provided by the present invention includes any one of the above examples 215 to 217, wherein the electrocoagulation housing includes a first housing portion and a second housing that are sequentially distributed from the electrocoagulation inlet to the electrocoagulation outlet In the housing portion and the third housing portion, the electrocoagulation inlet is located at one end of the first housing portion, and the electrocoagulation outlet is located at the one end of the third housing portion.
  • the electrocoagulation housing includes a first housing portion and a second housing that are sequentially distributed from the electrocoagulation inlet to the electrocoagulation outlet In the housing portion and the third housing portion, the electrocoagulation inlet is located at one end of the first housing portion, and the electrocoagulation outlet is located at the one end of the third housing portion.
  • Example 219 provided by the present invention includes the above example 218, wherein the outline size of the first housing portion gradually increases from the direction of the electrocoagulation inlet to the electrocoagulation outlet.
  • Example 220 provided by the present invention: including the above example 218 or 219, wherein the first housing portion has a straight tubular shape.
  • Example 221 provided by the present invention: including any one of the above examples 218 to 220, wherein the second housing portion has a straight tubular shape, and the first electrode and the second electrode are mounted on the second housing Ministry.
  • Example 222 provided by the present invention: including any one of the above examples 218 to 221, wherein the size of the outline of the third housing portion gradually decreases from the electrocoagulation inlet to the electrocoagulation outlet direction.
  • Example 223 provided by the present invention includes any one of the above examples 218 to 222, wherein the first housing portion, the second housing portion, and the third housing portion are all rectangular in cross section.
  • Example 224 provided by the present invention includes any one of the above examples 215 to 223, wherein the material of the electrocoagulation shell is stainless steel, aluminum alloy, iron alloy, cloth, sponge, molecular sieve, activated carbon, foamed iron, Or foamed silicon carbide.
  • the material of the electrocoagulation shell is stainless steel, aluminum alloy, iron alloy, cloth, sponge, molecular sieve, activated carbon, foamed iron, Or foamed silicon carbide.
  • Example 225 provided by the present invention: including any one of the above examples 180 to 224, wherein the first electrode is connected to the electrocoagulation case through an electrocoagulation insulator.
  • Example 226 provided by the present invention includes the above example 225, wherein the material of the electrocoagulation insulating member is insulating mica.
  • Example 227 provided by the present invention includes the above example 225 or 226, wherein the electrocoagulation insulating member is in the shape of a column or a tower.
  • Example 228 provided by the present invention includes any one of the above examples 180 to 227, wherein a cylindrical front connection portion is provided on the first electrode, and the front connection portion and the electrocoagulation insulating member Fixed connection.
  • Example 229 provided by the present invention includes any one of the above examples 180 to 228, wherein the second electrode is provided with a cylindrical rear connection portion, and the rear connection portion and the electrocoagulation insulating member Fixed connection.
  • Example 230 provided by the present invention includes any one of the above examples 180 to 229, wherein the ratio of the cross-sectional area of the first electrode to the cross-sectional area of the electrocoagulation channel is 99% -10%, or 90- 10%, or 80-20%, or 70-30%, or 60-40%, or 50%.
  • Example 231 provided by the present invention includes any one of the above examples 179 to 230, wherein the denitration device includes a condensation unit for condensing the exhaust gas after ozone treatment to achieve gas-liquid separation.
  • Example 232 provided by the present invention includes any one of the above examples 179 to 231, wherein the denitration device includes a rinsing unit for rinsing the exhaust gas after ozone treatment.
  • Example 233 provided by the present invention includes the above example 232, wherein the denitration device further includes a rinsing liquid unit for supplying the rinsing liquid to the rinsing unit.
  • Example 234 provided by the present invention includes the above example 233, wherein the eluent in the eluent unit includes water and / or alkali.
  • Example 235 provided by the present invention: including any one of the above examples 179 to 234, wherein the denitration device further includes a denitration liquid collection unit for storing the nitric acid aqueous solution and / or nitrate removed in the exhaust gas Aqueous solution.
  • Example 236 provided by the present invention includes the above example 235, wherein, when a nitric acid aqueous solution is stored in the denitration liquid collection unit, the denitration liquid collection unit is provided with an alkaline liquid addition unit for forming nitrate with nitric acid .
  • Example 237 provided by the present invention includes any one of the above examples 145 to 236, wherein the ozone purification system further includes an ozone digester for digesting ozone in the exhaust gas treated by the reaction field.
  • Example 238 provided by the present invention includes the above example 237, wherein the ozone digester is selected from at least one of an ultraviolet ozone digester and a catalytic ozone digester.
  • Example 239 provided by the present invention: including any one of the above examples 145 to 238, wherein the ozone purification system further includes a first denitration device for removing nitrogen oxides in exhaust gas; the reaction field It is used for mixing and reacting the exhaust gas processed by the first denitration device with the ozone stream, or for mixing and reacting the exhaust gas with the ozone stream before being processed by the first denitration device.
  • a first denitration device for removing nitrogen oxides in exhaust gas
  • the reaction field It is used for mixing and reacting the exhaust gas processed by the first denitration device with the ozone stream, or for mixing and reacting the exhaust gas with the ozone stream before being processed by the first denitration device.
  • Example 240 provided by the present invention includes the above example 239, wherein the first denitration device is selected from at least one of a non-catalytic reduction device, a selective catalytic reduction device, a non-selective catalytic reduction device, and an electron beam denitration device Species.
  • Example 241 provided by the present invention: a method for removing carbon black from an exhaust electric field, including the following steps:
  • the dust-containing gas passes through the ionization and dust removal electric field generated by the anode of the dust removal electric field and the cathode of the dust removal electric field;
  • Example 242 provided by the present invention: an exhaust electric field carbon black removal method including Example 241, wherein the carbon black cleaning process is completed using an electric field back-corona discharge phenomenon.
  • Example 243 provided by the present invention: an exhaust electric field carbon black removal method including Example 241, in which the electric field reverse corona discharge phenomenon is used to increase the voltage and limit the injection current to complete the carbon black cleaning process.
  • Example 244 provided by the present invention: Exhaust electric field carbon black removal method including Example 241, wherein the electric field reverse corona discharge phenomenon is used to increase the voltage and limit the injection current to cause a sharp discharge that occurs at the position of the anode dust Plasma, the plasma deeply oxidizes the organic components of the cleaned carbon black, breaks the polymer bonds, forms small molecule carbon dioxide and water, and completes the cleaned carbon black treatment.
  • Example 245 provided by the present invention: a method for removing carbon black from exhaust gas electric field including any one of Examples 241 to 244, wherein when the electric field device detects that the electric field current increases to a given value, the electric field device performs cleaning Dust treatment.
  • Example 246 provided by the present invention: a method for removing carbon black from an exhaust gas electric field including any one of Examples 241 to 245, wherein the dust-removing electric field cathode includes at least one electrode rod.
  • Example 247 provided by the present invention: an exhaust electric field carbon black removal method including Example 246, wherein the diameter of the electrode rod is not greater than 3 mm.
  • Example 248 provided by the present invention: a method for removing carbon black from an exhaust electric field including example 246 or 247, wherein the electrode rod has a needle shape, a polygonal shape, a burr shape, a threaded rod shape, or a column shape.
  • Example 249 provided by the present invention: an exhaust electric field carbon black removal method including any one of Examples 241 to 248, wherein the dust removal electric field anode is composed of a hollow tube bundle.
  • Example 250 provided by the present invention: a method for removing carbon black from an exhaust electric field including Example 249, wherein the hollow cross section of the anode tube bundle adopts a circular or polygonal shape.
  • Example 251 provided by the present invention: an exhaust electric field carbon black removal method including Example 250, wherein the polygon is a hexagon.
  • Example 252 provided by the present invention: a method for removing carbon black from an exhaust electric field including any one of Examples 249 to 251, wherein the tube bundle of the anode of the dust removing electric field is honeycomb-shaped.
  • Example 253 provided by the present invention: a method for removing carbon black from an exhaust gas field including any one of Examples 241 to 252, wherein the dust-removing electric field cathode penetrates the dust-removing electric field anode.
  • Example 254 provided by the present invention: an exhaust electric field carbon black removal method including any one of Examples 241 to 253, wherein when the detected electric field current increases to a given value, a carbon black cleaning process is performed.
  • Example 255 provided by the present invention: a method for reducing electric field coupling of exhaust dust removal, including the following steps:
  • Example 256 provided by the present invention: a method for reducing exhaust dust electric field coupling including Example 255, which includes selecting a ratio of a dust collecting area of the dust collecting electric field anode to a discharge area of the dust removing electric field cathode.
  • Example 257 provided by the present invention: a method for reducing exhaust dust electric field coupling including Example 256, wherein the ratio of the dust accumulation area including the selection of the anode of the dust removal electric field to the discharge area of the cathode of the dust removal electric field is 1.667: 1 -1680: 1.
  • Example 258 provided by the present invention: a method for reducing exhaust dust electric field coupling including Example 256, wherein the ratio of the dust accumulation area including the selection of the anode of the dust removal electric field to the discharge area of the cathode of the dust removal electric field is 6.67: 1 -56.67: 1.
  • Example 259 provided by the present invention: a method for reducing coupling of an exhaust dust-removing electric field including any one of Examples 255 to 258, including selecting a cathode diameter of the dust-removing electric field of 1-3 mm, The pole spacing of the cathode of the dust removal electric field is 2.5-139.9 mm; the ratio of the dust accumulation area of the anode of the dust removal electric field to the discharge area of the cathode of the dust removal electric field is 1.667: 1-1680: 1.
  • Example 260 provided by the present invention: A method for reducing coupling of an exhaust gas dust-removing electric field including any one of Examples 255 to 259, wherein the electrode separation between the dust-removing electric field anode and the dust-removing electric field cathode is selected to be less than 150 mm.
  • Example 261 provided by the present invention: a method for reducing coupling of an exhaust dust-removing electric field including any one of Examples 255 to 259, which includes selecting a pole spacing of the dust-removing electric field anode and the dust-removing electric field cathode to be 2.5-139.9 mm .
  • Example 262 provided by the present invention: A method for reducing coupling of an exhaust gas dust-removing electric field including any one of Examples 255 to 259, which includes selecting a pole spacing of the dust-removing electric field anode and the dust-removing electric field cathode to be 5-100 mm.
  • Example 263 provided by the present invention: a method for reducing coupling of an electric field for exhaust dust removal including any one of Examples 255 to 262, including selecting the anode length of the dust removal electric field to be 10-180 mm.
  • Example 264 provided by the present invention: The method for reducing the electric field coupling of exhaust dust removal including any one of Examples 255 to 262, which includes selecting the anode length of the dust removal electric field to be 60-180 mm.
  • Example 265 provided by the present invention: A method for reducing coupling of an exhaust dust-removing electric field including any one of Examples 255 to 264, which includes selecting a cathode length of the dust-removing electric field of 30-180 mm.
  • Example 266 provided by the present invention: A method for reducing coupling of an electric field for exhaust dust removal including any one of Examples 255 to 264, which includes selecting the cathode length of the dust removal electric field to be 54-176 mm.
  • Example 267 provided by the present invention: The method for reducing exhaust dust electric field coupling including any one of Examples 255 to 266, which includes selecting that the dust electric field cathode includes at least one electrode rod.
  • Example 268 provided by the present invention: The method for reducing the electric field coupling of exhaust dust removal including Example 267, which includes selecting that the diameter of the electrode rod is not greater than 3 mm.
  • Example 269 provided by the present invention: The method for reducing exhaust dust electric field coupling including Example 267 or 268, which includes selecting the shape of the electrode rod to be needle, polygon, burr, threaded rod or column.
  • Example 270 provided by the present invention: A method for reducing coupling of an electric field for exhaust dust removal including any one of Examples 255 to 269, which includes selecting the anode of the dust removal electric field to be composed of a hollow tube bundle.
  • Example 271 provided by the present invention: a method for reducing exhaust dust electric field coupling including Example 270, wherein the hollow cross section including the anode tube bundle is selected to be circular or polygonal.
  • Example 272 provided by the present invention: The method for reducing exhaust dust electric field coupling including Example 271, which includes selecting the polygon to be a hexagon.
  • Example 273 provided by the present invention: A method for reducing coupling of an electric field for exhaust dust removal including any one of Examples 270 to 272, wherein the tube bundle including selecting the anode of the dust removal electric field is honeycomb-shaped.
  • Example 274 provided by the present invention: The method for reducing exhaust dust electric field coupling including any one of Examples 255 to 273, which includes selecting the cathode of the dust electric field to penetrate the anode of the dust electric field.
  • Example 275 provided by the present invention: A method for reducing electric field coupling of exhaust dust removal including any one of Examples 255 to 274, wherein the size of the anode or / and the cathode of the dust removal electric field including the selected size of the electric field coupling ⁇ 3 .
  • Example 276 provided by the present invention: an exhaust dust removal method, including the following steps: when the exhaust gas temperature is lower than 100 ° C, the liquid water in the exhaust gas is removed, and then the ionization dust is removed.
  • Example 277 provided by the present invention: an exhaust dust removing method including Example 276, wherein, when the exhaust gas temperature is ⁇ 100 ° C, the exhaust gas is ionized and dust-removed.
  • Example 278 provided by the present invention: the exhaust dust removing method including Example 276 or 277, wherein, when the exhaust gas temperature is ⁇ 90 ° C, the liquid water in the exhaust gas is removed, and then the ionized dust is removed.
  • Example 279 provided by the present invention: the exhaust dust removal method including Example 276 or 277, wherein when the exhaust gas temperature is ⁇ 80 ° C, the liquid water in the exhaust gas is removed, and then the ionization dust is removed.
  • Example 280 provided by the present invention: the exhaust dust removing method including Example 276 or 277, wherein when the exhaust gas temperature is ⁇ 70 ° C, the liquid water in the exhaust gas is removed, and then the ionized dust is removed.
  • Example 281 provided by the present invention: Exhaust dust removal method including Example 276 or 277, wherein the liquid water in the exhaust gas is removed by the electrocoagulation defogging method, and then ionized to remove dust.
  • Example 282 provided by the present invention: An exhaust dust removal method, including the following steps: adding a gas including oxygen before the ionization dust removal electric field to perform ionization dust removal.
  • Example 283 provided by the present invention: The exhaust dust removal method including Example 282, wherein oxygen is added by simply increasing oxygen, passing in outside air, passing in compressed air, and / or passing in ozone.
  • Example 284 provided by the present invention: an exhaust dust removing method including Example 282 or 283, wherein the amount of supplemental oxygen is determined at least according to the content of exhaust particles.
  • Example 285 provided by the present invention: An exhaust dust removal method, including the following steps:
  • Example 286 provided by the present invention: The exhaust dust removal method including Example 285, wherein the electret element is close to the outlet of the dust removal electric field device, or the electret element is provided at the outlet of the dust removal electric field device.
  • Example 287 provided by the present invention: an exhaust dust removal method including Example 285, wherein the dust removal electric field anode and the dust removal electric field cathode form an exhaust gas flow path, and the electret element is provided in the exhaust gas flow Daozhong.
  • Example 288 provided by the present invention: The exhaust dust removing method including Example 287, wherein the exhaust runner includes an exhaust runner outlet, and the electret element is close to the exhaust runner outlet, or, The electret element is provided at the outlet of the exhaust runner.
  • Example 289 provided by the present invention: The exhaust dust removal method including any one of Examples 282 to 288, wherein when the ionization dust removal electric field has no electrified driving voltage, the charged electret element is used to adsorb particulate matter in the exhaust gas.
  • Example 290 provided by the present invention: the exhaust dust removing method including Example 288, wherein after the charged electret element adsorbs certain particulate matter in the exhaust gas, it is replaced with a new electret element.
  • Example 291 provided by the present invention: Exhaust dust removal method including Example 290, in which the ionization dust removal electric field is restarted after replacing with a new electret element to adsorb particulate matter in the exhaust and charge the new electret element .
  • Example 292 provided by the present invention: The exhaust dust removing method including any one of Examples 285 to 291, wherein the material of the electret element includes an inorganic compound having electret properties.
  • Example 293 provided by the present invention: the exhaust dust removing method including Example 292, wherein the inorganic compound is selected from one or more combinations of oxygen-containing compounds, nitrogen-containing compounds, or glass fibers.
  • Example 294 provided by the present invention: an exhaust dust removing method including Example 293, wherein the oxygen-containing compound is selected from one of metal-based oxides, oxygen-containing composites, and oxygen-containing inorganic heteropoly acid salts or Various combinations.
  • Example 295 provided by the present invention an exhaust dust removal method including Example 294, wherein the metal-based oxide is selected from aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, oxide One or more combinations of lead and tin oxide.
  • the metal-based oxide is selected from aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, oxide One or more combinations of lead and tin oxide.
  • Example 296 provided by the present invention: an exhaust dust removing method including Example 294, wherein the metal-based oxide is alumina.
  • Example 297 provided by the present invention: The exhaust dust removing method including Example 294, wherein the oxygen-containing composite is selected from one or more combinations of titanium-zirconium composite oxide or titanium-barium composite oxide.
  • Example 298 provided by the present invention: an exhaust dust removal method including Example 294, wherein the oxygen-containing inorganic heteropoly acid salt is selected from one or more of zirconium titanate, lead zirconate titanate, or barium titanatekinds of combinations.
  • Example 299 provided by the present invention: an exhaust dust removing method including Example 293, wherein the nitrogen-containing compound is silicon nitride.
  • Example 300 provided by the present invention: the exhaust dust removing method including any one of Examples 285 to 291, wherein the material of the electret element includes an organic compound having electret properties.
  • Example 301 provided by the present invention: an exhaust dust removing method including Example 300, wherein the organic compound is selected from one of fluoropolymer, polycarbonate, PP, PE, PVC, natural wax, resin, and rosin Or multiple combinations.
  • the organic compound is selected from one of fluoropolymer, polycarbonate, PP, PE, PVC, natural wax, resin, and rosin Or multiple combinations.
  • Example 302 provided by the present invention: an exhaust dust removing method including Example 301, wherein the fluoropolymer is selected from polytetrafluoroethylene, polyperfluoroethylene propylene, soluble polytetrafluoroethylene, and polyvinylidene fluoride One or more combinations.
  • the fluoropolymer is selected from polytetrafluoroethylene, polyperfluoroethylene propylene, soluble polytetrafluoroethylene, and polyvinylidene fluoride One or more combinations.
  • Example 303 provided by the present invention: an exhaust dust removing method including Example 301, wherein the fluoropolymer is polytetrafluoroethylene.
  • FIG. 1 is a schematic diagram of the exhaust ozone purification system of the present invention.
  • FIG. 2 is a schematic diagram 1 of an electrode for an ozone generator of the present invention.
  • FIG 3 is a schematic diagram 2 of the electrode for the ozone generator of the present invention.
  • Fig. 4 is a structural schematic diagram of a discharge type ozone generator in the prior art.
  • FIG. 5 is a schematic diagram of an exhaust dust removal system according to Embodiment 1 of the present invention.
  • FIG. 6 is a schematic diagram of an exhaust dust removal system according to Embodiment 2 of the present invention.
  • FIG. 7 is a three-dimensional schematic diagram of an exhaust gas treatment device in an embodiment of the exhaust gas treatment system of the present invention.
  • FIG. 8 is a schematic structural diagram of an umbrella-shaped insulation mechanism of an exhaust gas treatment device in an exhaust gas treatment system of the present invention in an embodiment.
  • 9A is an implementation structure diagram of an air-equalizing device of an exhaust gas treatment device in an exhaust gas treatment system of the present invention.
  • FIG. 9B is another implementation structure diagram of the air equalizing device of the exhaust gas treatment device in the exhaust gas treatment system of the present invention.
  • FIG. 9C is another embodiment structure diagram of the air equalizing device of the exhaust gas treatment device in the exhaust gas treatment system of the present invention.
  • FIG. 10 is a schematic diagram of an exhaust ozone purification system according to Embodiment 4 of the present invention.
  • FIG. 11 is a plan view of a reaction field in an exhaust ozone purification system according to Embodiment 4 of the present invention.
  • FIG. 12 is a schematic diagram of the ozone quantity control device of the present invention.
  • FIG. 13 is a schematic diagram of the structure of the electric field generating unit.
  • FIG. 14 is an A-A view of the electric field generating unit of FIG.
  • Fig. 15 is an A-A view of the electric field generating unit of Fig. 13 marked with length and angle.
  • 16 is a schematic diagram of the structure of an electric field device with two electric field levels.
  • Embodiment 17 is a schematic structural diagram of an electric field device in Embodiment 24 of the present invention.
  • Embodiment 26 of the present invention is a schematic structural diagram of an electric field device in Embodiment 26 of the present invention.
  • Embodiment 27 of the present invention is a schematic structural diagram of an electric field device in Embodiment 27 of the present invention.
  • Embodiment 29 is a schematic structural diagram of an exhaust dust removal system in Embodiment 29 of the present invention.
  • FIG. 21 is a schematic structural view of an impeller duct in Embodiment 29 of the present invention.
  • FIG. 22 is a schematic structural diagram of an electrocoagulation device in Embodiment 30 of the present invention.
  • Embodiment 23 is a left side view of the electrocoagulation device in Embodiment 30 of the present invention.
  • Embodiment 24 is a perspective view of an electrocoagulation device in Embodiment 30 of the present invention.
  • FIG. 25 is a schematic structural diagram of an electrocoagulation device in Embodiment 31 of the present invention.
  • FIG. 26 is a top view of the electrocoagulation device in Embodiment 31 of the present invention.
  • FIG. 27 is a schematic structural diagram of an electrocoagulation device in Embodiment 32 of the present invention.
  • FIG. 28 is a schematic structural diagram of an electrocoagulation device in Embodiment 33 of the present invention.
  • Embodiment 34 of the present invention is a schematic structural diagram of an electrocoagulation device in Embodiment 34 of the present invention.
  • FIG. 30 is a schematic structural diagram of an electrocoagulation device in Embodiment 35 of the present invention.
  • FIG. 31 is a schematic structural diagram of an electrocoagulation device in Embodiment 36 of the present invention.
  • FIG. 32 is a schematic structural diagram of an electrocoagulation device in Embodiment 37 of the present invention.
  • Embodiment 38 is a schematic structural diagram of an electrocoagulation device in Embodiment 38 of the present invention.
  • Embodiment 40 of the present invention is a schematic structural diagram of an electrocoagulation device in Embodiment 40 of the present invention.
  • FIG. 36 is a schematic structural diagram of an electrocoagulation device in Embodiment 41 of the present invention.
  • FIG. 37 is a schematic structural diagram of an electrocoagulation device in Embodiment 42 of the present invention.
  • Embodiment 43 of the present invention is a schematic structural diagram of an electrocoagulation device in Embodiment 43 of the present invention.
  • Embodiment 44 of the present invention is a schematic structural diagram of an exhaust gas treatment system in Embodiment 44 of the present invention.
  • FIG. 40 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 45 of the present invention.
  • Embodiment 46 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 46 of the present invention.
  • Embodiment 47 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 47 of the present invention.
  • Embodiment 48 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 48 of the present invention.
  • Embodiment 44 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 49 of the present invention.
  • Embodiment 45 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 50 of the present invention.
  • Embodiment 46 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 51 of the present invention.
  • Embodiment 47 is a schematic structural diagram of an exhaust gas treatment system in Embodiment 52 of the present invention.
  • FIG. 48 is a schematic structural diagram of an exhaust temperature reducing device in Embodiment 53 of the present invention.
  • FIG. 49 is a schematic structural diagram of an exhaust gas cooling device in Embodiment 54 of the present invention.
  • FIG. 50 is a schematic structural diagram of an exhaust temperature reducing device in Embodiment 55 of the present invention.
  • Embodiment 51 is a schematic structural diagram of a heat exchange unit in Embodiment 55 of the present invention.
  • FIG. 52 is a schematic structural diagram of an exhaust gas cooling device in Embodiment 56 of the present invention.
  • an exhaust gas treatment system includes an exhaust dust removal system and an exhaust ozone purification system.
  • the exhaust gas treatment system includes an exhaust dust removal system.
  • the exhaust dust removal system is connected to the outlet of the exhaust discharge equipment. Exhaust gas discharged by exhaust emission equipment will flow through the exhaust dust removal system.
  • the exhaust dust removal system further includes a water removal device for removing liquid water before the entrance of the electric field device.
  • the exhaust gas when the temperature of the exhaust gas or the temperature of the exhaust discharge device is lower than a certain temperature, the exhaust gas may contain liquid water, and the water removal device removes the liquid water in the exhaust gas.
  • the certain temperature is above 90 ° C and below 100 ° C.
  • the certain temperature is above 80 ° C and below 90 ° C.
  • the certain temperature is below 80 ° C.
  • the water removal device is an electrocoagulation device.
  • the water removal device removes the water droplets or liquid water in the exhaust gas before the exhaust gas discharge equipment is cold-started before the exhaust gas enters the electric field device inlet, thereby reducing the ionization and dust removal electric field Uneven discharge and breakdown of the cathode of the dust-removing electric field and the anode of the dust-removing electric field, thereby improving the efficiency of ionization and dust removal, and obtaining unexpected technical effects.
  • the water removal device is not particularly limited, and the present invention can be applied to remove liquid water in exhaust gas in the prior art.
  • the exhaust dust removal system further includes an oxygen supplement device, which is used to add a gas including oxygen, such as air, before the ionization dust removal electric field.
  • an oxygen supplement device which is used to add a gas including oxygen, such as air, before the ionization dust removal electric field.
  • the oxygen supplementing device adds oxygen by simply adding oxygen, passing in outside air, passing in compressed air, and / or passing in ozone.
  • the amount of oxygen supplementation is determined based at least on the content of exhaust particles.
  • the exhaust gas will not have enough oxygen to generate enough oxygen ions, resulting in poor dust removal effect, that is, the person skilled in the art does not recognize the oxygen in the exhaust gas It may not be sufficient to support effective ionization, and the inventor of the present application discovered this problem and proposed the exhaust dust removal system of the present invention: including an oxygen supplement device, which can be simply oxygenated, vented to outside air, vented to compressed air and / or vented Oxygen is added in the way of ozone to increase the oxygen content of the exhaust gas entering the ionization and dust removal electric field, so that when the exhaust gas flows through the ionization and dust removal electric field between the cathode of the dust removal electric field and the anode of the dust removal electric field, the ionized oxygen is increased to make more of the exhaust The dust is charged, and then more charged dust is collected under the action of the anode of the dust removal electric field, which makes the dust removal efficiency of the electric field device higher, which is
  • the exhaust system may include a wind equalizing device.
  • the air-equalizing device is arranged before the exhaust electric field device, and can evenly pass the airflow entering the electric field device.
  • the dust-removing electric field anode of the electric field device may be a cube
  • the air-equalizing device may include an air inlet pipe on one side of the cathode support plate and an air outlet pipe on the other side of the cathode support plate.
  • the intake end of the anode of the dust removal electric field; wherein, the side where the intake pipe is installed is opposite to the side where the outlet pipe is installed.
  • the air leveling device can make the exhaust gas entering the electric field device evenly pass through the electrostatic field.
  • the anode of the dust-removing electric field may be a cylinder
  • the air-equalizing device is located between the entrance of the dust-removing system and the ionizing dust-removing electric field formed by the anode of the dust-removing electric field and the cathode of the dust-removing electric field. Fan blades rotating around the center of the entrance of the electric field device.
  • the air-equalizing device can make all kinds of varying intake air evenly pass through the electric field generated by the anode of the dust removal electric field. At the same time, it can keep the internal temperature of the anode of the dust removal electric field constant and the oxygen is sufficient.
  • the air leveling device can make the exhaust gas entering the electric field device evenly pass through the electrostatic field.
  • the air equalizing device includes an air inlet plate provided at the air inlet end of the anode of the dust removal electric field and an air outlet plate provided at the air outlet end of the anode of the dust removal electric field.
  • the air leveling device can make the exhaust gas entering the electric field device evenly pass through the electrostatic field.
  • the exhaust dust removal system may include a dust removal system inlet, a dust removal system outlet, and an electric field device.
  • the electric field device may include an electric field device inlet, an electric field device outlet, and a front electrode between the electric field device inlet and the electric field device outlet.
  • the electric field device includes a front electrode between the entrance of the electric field device and the ionization and dust removal electric field formed by the anode of the dust removal electric field and the cathode of the dust removal electric field.
  • the shape of the front electrode may be dot-shaped, linear, mesh-shaped, orifice-shaped, plate-shaped, needle-rod-shaped, ball-cage-shaped, box-shaped, tubular, natural form of matter, or processed form of matter .
  • the front electrode has a hole structure, one or more exhaust vent holes are provided on the front electrode.
  • the shape of the exhaust vent hole may be polygon, circle, ellipse, square, rectangle, trapezoid, or rhombus.
  • the outline size of the exhaust through hole may be 0.1 to 3 mm, 0.1 to 0.2 mm, 0.2 to 0.5 mm, 0.5 to 1 mm, 1 to 1.2 mm, 1.2 to 1.5 mm, 1.5 to 2 mm, 2 to 2.5mm, 2.5 ⁇ 2.8mm, or 2.8 ⁇ 3mm.
  • the shape of the front electrode may be one or more of solid, liquid, gas molecular group, plasma, conductive mixed state substance, biological natural mixed conductive substance, or artificially processed object to form conductive substance Combinations of various forms.
  • the front electrode is solid, solid metal, such as 304 steel, or other solid conductors, such as graphite, can be used.
  • the front electrode is a liquid, it may be an ion-conducting liquid.
  • the front electrode charges the pollutants in the gas.
  • the anode of the dedusting electric field exerts an attractive force on the charged pollutants, so that the pollutants move toward the anode of the dedusting electric field until the pollutants adhere to the anode of the dedusting electric field.
  • the front electrode introduces electrons into the pollutants.
  • the electrons are transferred between the pollutants between the front electrode and the anode of the dust removal electric field, so that more pollutants are charged.
  • Between the front electrode and the anode of the dust-removing electric field electrons are conducted through pollutants and an electric current is formed.
  • the front electrode charges the pollutant by contacting the pollutant. In an embodiment of the invention, the front electrode charges the pollutants by means of energy fluctuations. In an embodiment of the present invention, the front electrode transfers electrons to the pollutant by contacting the pollutant and charges the pollutant. In an embodiment of the present invention, the front electrode transfers electrons to the pollutants by means of energy fluctuations, and charges the pollutants.
  • the front electrode is linear, and the anode of the dust removal electric field is planar. In an embodiment of the invention, the front electrode is perpendicular to the anode of the dust removal electric field. In an embodiment of the invention, the front electrode is parallel to the anode of the dust removal electric field. In an embodiment of the invention, the front electrode is curved or arc-shaped. In an embodiment of the invention, the front electrode uses a wire mesh. In an embodiment of the invention, the voltage between the front electrode and the anode of the dust removal electric field is different from the voltage between the cathode of the dust removal electric field and the anode of the dust removal electric field.
  • the voltage between the front electrode and the anode of the dust removal electric field is less than the initial halo voltage.
  • the initial halo voltage is the minimum value of the voltage between the cathode of the dust removal electric field and the anode of the dust removal electric field.
  • the voltage between the front electrode and the anode of the dedusting electric field may be 0.1-2 kV / mm.
  • the electric field device includes an exhaust runner, and the front electrode is located in the exhaust runner.
  • the ratio of the cross-sectional area of the front electrode to the cross-sectional area of the exhaust runner is 99% to 10%, or 90 to 10%, or 80 to 20%, or 70 to 30%, or 60 to 40%, or 50%.
  • the cross-sectional area of the front electrode refers to the total area of the front electrode along the solid part of the cross-section. In an embodiment of the invention, the front electrode has a negative potential.
  • the metal powder, mist, or aerosol pollutants with strong conductivity in the exhaust gas are in contact with the front electrode, or When the distance to the front electrode reaches a certain range, it will be directly negatively charged. Then, all pollutants will enter the ionization and dust removal electric field with the airflow.
  • the anode of the dust removal electric field exerts attractive force on the negatively charged metal dust, mist, or aerosol, so that The negatively charged pollutants move toward the anode of the dedusting electric field until the part of the pollutants adheres to the anode of the dedusting electric field to collect the part of the pollutants.
  • the ionizing dedusting electric field formed between the anode of the dedusting electric field and the cathode of the dedusting electric field passes Oxygen in the ionized gas obtains oxygen ions, and the negatively charged oxygen ions combine with ordinary dust to make the ordinary dust negatively charged.
  • the anode of the dust removal electric field exerts an attractive force on this part of negatively charged dust and other pollutants to make the dust Wait for the pollutants to move to the anode of the dust removal electric field until the part of the pollutants adheres to the anode of the dust removal electric field.
  • Other pollutants are also collected, so that the more conductive and weaker conductive pollutants in the exhaust gas are collected, and the anode of the dust removal electric field can collect a wider range of pollutants in the exhaust gas, and the collection ability is stronger , The collection efficiency is higher.
  • the inlet of the electric field device is connected to the outlet of the exhaust discharge device.
  • the electric field device may include a dust removal electric field cathode and a dust removal electric field anode, and an ionization dust removal electric field is formed between the dust removal electric field cathode and the dust removal electric field anode.
  • Exhaust gas enters the ionization and dedusting electric field.
  • Oxygen ions in the exhaust gas will be ionized and form a large number of charged oxygen ions.
  • the oxygen ions are combined with dust and other particulate matter in the exhaust gas to charge the particulate matter.
  • the anode of the dedusting electric field is negatively charged
  • the particulate matter exerts an adsorption force, so that the particulate matter is adsorbed on the anode of the dust removal electric field to remove the particulate matter in the exhaust gas.
  • the dust-removing electric field cathode includes a plurality of cathode wires.
  • the diameter of the cathode wire can be 0.1mm-20mm, and the size parameter can be adjusted according to the application and dust accumulation requirements. In an embodiment of the invention, the diameter of the cathode wire is not greater than 3 mm.
  • the cathode wire uses a metal wire or an alloy wire that is easy to discharge, is temperature resistant, can support its own weight, and is electrochemically stable.
  • the material of the cathode wire is titanium. The specific shape of the cathode wire is adjusted according to the shape of the anode of the dust removal electric field.
  • the cross section of the cathode wire is circular; if the dust collection surface of the anode of the dust removal electric field is an arc surface, the cathode wire Need to be designed as a polyhedron. The length of the cathode wire is adjusted according to the anode of the dust removal electric field.
  • the dust-removing electric field cathode includes a plurality of cathode rods.
  • the diameter of the cathode rod is not greater than 3 mm.
  • a metal rod or an alloy rod that is easy to discharge is used as the cathode rod.
  • the shape of the cathode rod may be needle-shaped, polygonal, burr-shaped, threaded rod-shaped, columnar or the like. The shape of the cathode rod can be adjusted according to the shape of the anode of the dust-removing electric field.
  • the cross-section of the cathode rod needs to be designed to be circular; if the dust-collecting surface of the anode of the dust-removing electric field is an arc surface , The cathode rod needs to be designed into a polyhedron shape.
  • the cathode of the dust-removing electric field passes through the anode of the dust-removing electric field.
  • the anode of the dust removal electric field includes one or more hollow anode tubes arranged in parallel.
  • all the hollow anode tubes constitute a honeycomb-shaped dust-removing electric field anode.
  • the hollow anode tube may have a circular or polygonal cross section. If the cross section of the hollow anode tube is circular, a uniform electric field can be formed between the anode of the dedusting electric field and the cathode of the dedusting electric field, and the inner wall of the hollow anode tube is not easy to accumulate dust.
  • the cross section of the hollow anode tube is a triangular shape, three dust accumulation surfaces and three distant dust holding angles can be formed on the inner wall of the hollow anode tube.
  • This structure of the hollow anode tube has the highest dust holding rate. If the cross section of the hollow anode tube is quadrangular, 4 dust-collecting surfaces and 4 dust-holding angles can be obtained, but the grouping structure is unstable. If the cross section of the hollow anode tube is hexagonal, 6 dust accumulation surfaces and 6 dust accumulation angles can be formed, and the dust accumulation surface and the dust accumulation rate are balanced. If the cross section of the hollow anode tube is more polygonal, more dust accumulation edges can be obtained, but the dust holding rate is lost.
  • the diameter of the inscribed circle diameter of the hollow anode tube ranges from 5 mm to 400 mm.
  • the dust-removing electric field cathode is installed on a cathode support plate, and the cathode support plate and the dust-removing electric field anode are connected by an insulating mechanism.
  • the dust-removing electric field anode includes a first anode part and a second anode part, that is, the first anode part is close to the entrance of the electric field device, and the second anode part is close to the exit of the electric field device.
  • the cathode support plate and the insulation mechanism are between the first anode part and the second anode part, that is, the insulation mechanism is installed in the middle of the ionization electric field or the cathode of the dust removal electric field, which can play a good supporting role for the dust removal electric field cathode and the dust removal electric field
  • the cathode plays a fixed role with respect to the anode of the dust-removing electric field, so as to maintain a set distance between the cathode of the dust-removing electric field and the anode of the dust-removing electric field.
  • the support point of the cathode is at the end of the cathode, and it is difficult to maintain the distance between the cathode and the anode.
  • the insulation mechanism is provided outside the electric field flow path, that is, outside the second-stage flow path, to prevent or reduce dust and the like in the exhaust gas from collecting on the insulation mechanism, resulting in breakdown or conduction of the insulation mechanism.
  • the insulating mechanism uses a high-pressure-resistant ceramic insulator to insulate the dedusting electric field cathode and the dedusting electric field anode.
  • the anode of the dust-removing electric field is also called a kind of housing.
  • the first anode portion is located in front of the cathode support plate and the insulation mechanism in the gas flow direction, the first anode portion can remove water in the exhaust gas, prevent water from entering the insulation mechanism, and cause the insulation mechanism to short circuit and catch fire .
  • the first anode part can remove a considerable part of the dust in the exhaust gas. When the exhaust gas passes through the insulation mechanism, a considerable part of the dust has been eliminated, reducing the possibility of the dust causing the insulation mechanism to short circuit.
  • the insulating mechanism includes an insulating ceramic post. The design of the first anode part is mainly to protect the insulating ceramic column from being contaminated by particulate matter in the gas.
  • the design of the first anode part can effectively reduce the pollution of the insulating ceramic column and improve the use time of the product.
  • the first anode part and the dust-removing electric field cathode contact the polluting gas first, and the insulation mechanism contacts the gas, so as to achieve the purpose of first removing dust and then passing through the insulation mechanism, reducing the impact on the insulation mechanism Pollution, extend the cleaning and maintenance cycle, the corresponding electrode insulation support after use.
  • the length of the first anode portion is long enough to remove part of the dust, reduce the dust accumulated on the insulation mechanism and the cathode support plate, and reduce the electrical breakdown caused by the dust .
  • the length of the first anode portion accounts for 1/10 to 1/4, 1/4 to 1/3, 1/3 to 1/2, 1/2 to 2/3 of the total length of the anode of the dust removal electric field , 2/3 to 3/4, or 3/4 to 9/10.
  • the second anode portion is located behind the cathode support plate and the insulating mechanism in the exhaust gas flow direction.
  • the second anode part includes a dust accumulation section and a reserved dust accumulation section.
  • the dust accumulation section uses static electricity to adsorb the particulate matter in the exhaust gas.
  • the dust accumulation section is used to increase the dust accumulation area and prolong the use time of the electric field device.
  • the reserved dust accumulation section can provide failure protection for the dust accumulation section.
  • the dust accumulation section is reserved to further increase the dust accumulation area on the premise of meeting the design dust removal requirements.
  • the dust accumulation section is reserved for supplementing the dust accumulation in the previous section.
  • different power sources can be used for the reserved dust accumulation section and the first anode portion.
  • the insulation mechanism is provided between the cathode of the dust removal electric field and the anode of the dust removal electric field. Outside the secondary flow path. Therefore, the insulation mechanism is suspended outside the anode of the dust removal electric field.
  • the insulating mechanism may use non-conductor temperature-resistant materials, such as ceramics and glass.
  • completely sealed air-free material insulation requires an insulation isolation thickness> 0.3 mm / kv; air insulation requirements> 1.4 mm / kv.
  • the insulation distance can be set according to 1.4 times the pole spacing between the cathode of the dust removal electric field and the anode of the dust removal electric field.
  • the insulating mechanism uses ceramics and the surface is glazed; the connection cannot be filled with glue or organic materials, and the temperature resistance is greater than 350 degrees Celsius.
  • the insulation mechanism includes an insulation portion and a heat insulation portion.
  • the material of the insulation part is ceramic material or glass material.
  • the insulating portion may be an umbrella-shaped string ceramic column or a glass column, and the umbrella is glazed inside and outside. The distance between the outer edge of the umbrella-shaped string ceramic column or the glass column and the anode of the dust removal electric field is greater than 1.4 times the electric field distance, that is, greater than 1.4 times the pole spacing. The sum of the umbrella flange spacing of the umbrella-shaped string ceramic column or glass column is greater than 1.4 times the insulation spacing of the umbrella-shaped string ceramic column.
  • the total length of the inner depth of the umbrella-shaped string ceramic column or glass column is 1.4 times greater than the insulation distance of the umbrella-shaped string ceramic column.
  • the insulating part can also be a columnar string ceramic column or a glass column with glaze inside and outside. In an embodiment of the present invention, the insulating portion may also have a tower shape.
  • a heating rod is provided in the insulating portion.
  • the heating rod is activated and heated. Due to the temperature difference between the inside and outside of the insulating part during use, condensation is likely to occur inside and outside of the insulating part and outside.
  • the outer surface of the insulation may spontaneously or be heated by gas to generate high temperature, which requires necessary isolation and protection to prevent burns.
  • the heat insulation part includes a protective baffle located outside the second insulation part and a denitration purification reaction chamber.
  • the tail portion of the insulating portion needs to be insulated at the same location to prevent the environment and heat dissipation from heating the condensation component.
  • the lead-out line of the power source of the exhaust electric field device uses an umbrella-shaped string of ceramic columns or glass columns to connect through the wall, an elastic contact is used in the wall to connect the cathode support plate, and a sealed insulating protective wiring cap is used to insert and pull out the wall
  • the insulation distance between the lead-out conductor and the wall is greater than that of the umbrella-shaped string ceramic column or glass column.
  • the high-voltage part is eliminated from the lead, and directly installed on the end to ensure safety.
  • the overall outer insulation of the high-voltage module is protected by ip68, and the medium is used for heat dissipation.
  • an asymmetric structure is adopted between the cathode of the dust removal electric field and the anode of the dust removal electric field.
  • polar particles are subjected to a force of the same size but in opposite directions, and polar particles reciprocate in the electric field; in an asymmetric electric field, polar particles are subjected to two forces of different sizes, and polar particles act Moving in the direction of high force can avoid coupling.
  • the ionization and dust removal electric field is formed between the dust removal electric field cathode and the dust removal electric field anode of the electric field device of the present invention.
  • the method of reducing electric field coupling includes the following steps: selecting the ratio of the dust collecting area of the anode of the dust removing electric field to the discharge area of the cathode of the dust removing electric field to make the number of electric field couplings ⁇ 3.
  • the ratio of the dust collection area of the anode of the dust removal electric field to the discharge area of the cathode of the dust removal electric field may be: 1.667: 1-1680: 1; 3.334: 1-113.34: 1; 6.67: 1-56.67: 1; 13.34: 1-28.33: 1.
  • the dust collecting area of the relatively large-area dust-removing electric field anode and the relatively small dust-removing electric field cathode discharge area are selected.
  • the above-mentioned area ratio can reduce the discharge area of the dust-removing electric field cathode, reduce suction, and expand the dust-removing electric field anode.
  • the dust collecting area increases the suction, that is, the asymmetric electrode suction between the cathode of the dust-removing electric field and the anode of the dust-removing electric field, so that the charged dust falls on the dust-collecting surface of the anode of the dust-removing electric field.
  • the dust collection area refers to the area of the anode working surface of the dust removal electric field.
  • the dust collection area is the inner surface area of the hollow regular hexagonal tube.
  • the dust collection area is also called dust accumulation. area.
  • the discharge area refers to the area of the working surface of the cathode of the dust removal electric field.
  • the cathode of the dust removal electric field is rod-shaped, the discharge area is the rod-shaped outer surface area.
  • the length of the anode of the dust removal electric field may be 10 to 180 mm, 10 to 20 mm, 20 to 30 mm, 60 to 180 mm, 30 to 40 mm, 40 to 50 mm, 50 to 60 mm, 60 to 70 mm, 70 to 80 mm, 80-90mm, 90-100mm, 100-110mm, 110-120mm, 120-130mm, 130-140mm, 140-150mm, 150-160mm, 160-170mm, 170-180mm, 60mm, 180mm, 10mm or 30mm.
  • the length of the anode of the dust removal electric field refers to the minimum length from one end to the other end of the working surface of the anode of the dust removal electric field. The selection of the length of the anode of the dust removal electric field can effectively reduce the electric field coupling.
  • the length of the anode of the dust removal electric field may be 10 to 90 mm, 15 to 20 mm, 20 to 25 mm, 25 to 30 mm, 30 to 35 mm, 35 to 40 mm, 40 to 45 mm, 45 to 50 mm, 50 to 55 mm, 55 ⁇ 60mm, 60 ⁇ 65mm, 65 ⁇ 70mm, 70 ⁇ 75mm, 75 ⁇ 80mm, 80 ⁇ 85mm or 85 ⁇ 90mm, the design of this length can make the dust removal electric field anode and electric field device have high temperature resistance, and make the electric field device It has high efficiency dust collection ability under high temperature impact.
  • the length of the dust-removing electric field cathode can be 30 to 180 mm, 54 to 176 mm, 30 to 40 mm, 40 to 50 mm, 50 to 54 mm, 54 to 60 mm, 60 to 70 mm, 70 to 80 mm, 80 to 90 mm, 90 to 100 mm, 100 to 110 mm, 110 to 120 mm, 120 to 130 mm, 130 to 140 mm, 140 to 150 mm, 150 to 160 mm, 160 to 170 mm, 170 to 176 mm, 170 to 180 mm, 54 mm, 180 mm, or 30 mm.
  • the length of the cathode of the dust removal electric field refers to the minimum length from one end to the other end of the working surface of the cathode of the dust removal electric field.
  • the selection of the cathode of the dust removal electric field can effectively reduce the electric field coupling.
  • the length of the dust-removing electric field cathode can be 10 to 90 mm, 15 to 20 mm, 20 to 25 mm, 25 to 30 mm, 30 to 35 mm, 35 to 40 mm, 40 to 45 mm, 45 to 50 mm, 50 to 55 mm, 55 ⁇ 60mm, 60 ⁇ 65mm, 65 ⁇ 70mm, 70 ⁇ 75mm, 75 ⁇ 80mm, 80 ⁇ 85mm or 85 ⁇ 90mm, the design of this length can make the dust removal electric field cathode and electric field device have high temperature resistance characteristics, and make the electric field device It has high efficiency dust collection ability under high temperature impact.
  • the corresponding dust collection efficiency is 99.9%; when the electric field temperature is 400 °C, the corresponding dust collection efficiency is 90%; when the electric field temperature is 500 °C, the corresponding dust collection efficiency is 50 %.
  • the distance between the anode of the dust-removing electric field and the cathode of the dust-removing electric field may be 5-30 mm, 2.5-139.9 mm, 9.9-139.9 mm, 2.5-9.9 mm, 9.9-20 mm, 20-30 mm, 30-40 mm , 40-50mm, 50-60mm, 60-70mm, 70-80mm, 80-90mm, 90-100mm, 100-110mm, 110-120mm, 120-130mm, 130-139.9mm, 9.9mm, 139.9mm, or 2.5 mm.
  • the distance between the anode of the dust-removing electric field and the cathode of the dust-removing electric field is also called the pole spacing.
  • the pole spacing specifically refers to the minimum vertical distance between the working surface of the anode of the dust removal electric field and the cathode of the dust removal electric field. This choice of pole spacing can effectively reduce the electric field coupling and make the exhaust electric field device have high temperature resistance characteristics.
  • the diameter of the cathode of the dust-removing electric field is 1-3 mm, and the pole spacing between the anode of the dust-removing electric field and the cathode of the tail gas-removing electric field is 2.5-139.9 mm;
  • the ratio of the discharge area of the cathode of the dedusting electric field is 1.667: 1-1680: 1.
  • ionization dust removal can be applied to remove particulate matter in the gas.
  • the existing electric field dust removal device can only remove about 70% of the particulate matter, and cannot meet the emission standards of many countries.
  • the volume of the electric field dust removal device in the prior art is too large.
  • the inventor of the present invention has found that the disadvantages of the electric field dust removal device in the prior art are caused by electric field coupling.
  • the present invention can significantly reduce the size (ie, volume) of the electric field dust removal device by reducing the number of electric field couplings.
  • the size of the ionization and dust removal device provided by the present invention is about one fifth of the size of the existing ionization and dust removal device.
  • the current ionization dust removal device sets the gas flow rate to about 1 m / s, and the present invention can still obtain a higher gas flow rate when the gas flow rate is increased to 6 m / s. Particle removal rate.
  • the size of the electric field dust collector can be reduced.
  • the present invention can significantly improve the particle removal efficiency. For example, when the gas flow rate is about 1m / s, the prior art electric field dust removal device can remove about 70% of the particulate matter in the engine exhaust, but the present invention can remove about 99% of the particulate matter, even when the gas flow rate is 6m / s .
  • the present invention achieves the above unexpected results.
  • the ionization and dust removal electric field between the anode of the dust removal electric field and the cathode of the dust removal electric field is also called a third electric field.
  • a fourth electric field that is not parallel to the third electric field is formed between the anode of the dust removal electric field and the cathode of the dust removal electric field.
  • the fourth electric field is not perpendicular to the flow channel of the ionization and dust removal electric field.
  • the fourth electric field is also called an auxiliary electric field and can be formed by one or two second auxiliary electrodes.
  • the second auxiliary electrode When the fourth electric field is formed by a second auxiliary electrode, the second auxiliary electrode may be placed at the inlet or the outlet of the ionization electric field, and the second auxiliary electrode may have a negative potential or a positive potential.
  • the fourth electric field is formed by two second auxiliary electrodes, one of the second auxiliary electrodes can have a negative potential and the other second auxiliary electrode can have a positive potential; one second auxiliary electrode can be placed at the entrance of the ionization dust removal electric field, Another second auxiliary electrode is placed at the outlet of the ionization dust removal electric field.
  • the second auxiliary electrode may be a part of the dust-removing electric field cathode or the dust-removing electric field anode, that is, the second auxiliary electrode may be formed by an extension of the dust-removing electric field cathode or the dust-removing electric field anode. same.
  • the second auxiliary electrode may also be a separate electrode, that is, the second auxiliary electrode may not be a part of the cathode of the dedusting electric field or the anode of the dedusting electric field. In this case, the voltage of the fourth electric field is different from the voltage of the third electric field. Working conditions are controlled individually.
  • the fourth electric field can apply a force toward the outlet of the ionized electric field between the anode of the dust-removing electric field and the cathode of the dust-removing electric field, so that the stream of negatively-charged oxygen ions between the anode of the dust-removing electric field and the cathode of the dust-removing electric field has an outlet.
  • Moving speed When the exhaust gas flows into the ionization electric field and flows toward the exit of the ionization electric field, the negatively charged oxygen ions also move toward the anode of the dust removal electric field and toward the exit of the ionization electric field, and the negatively charged oxygen ions move toward the dust removal electric field.
  • the anode will be combined with the particulate matter in the exhaust gas when moving toward the outlet of the ionization electric field. Because oxygen ions have a moving speed toward the outlet, when the oxygen ions are combined with the particulate matter, there will be no strong collision between the two. , So as to avoid greater energy consumption due to strong collision, ensure that oxygen ions are easily combined with particulate matter, and make the particulate matter in the gas charge more efficiently, and then under the action of the anode of the dust removal electric field, more The particulate matter is collected to ensure a higher dust removal efficiency of the electric field device.
  • the collection rate of the electric field device for particles entering the electric field in the direction of ion flow is nearly double that of the particles entering the electric field in the direction of counter ion flow, thereby increasing the dust collection efficiency of the electric field and reducing the electric power consumption of the electric field.
  • the main reason for the low dust removal efficiency of the dust collection electric field in the prior art is that the direction of the dust entering the electric field is opposite to or perpendicular to the direction of the ion flow in the electric field, which causes the dust and ion flow to collide violently with each other and produce greater energy consumption. It also affects the charging efficiency, thereby reducing the electric field dust collection efficiency and increasing energy consumption in the prior art.
  • the electric field device collects the dust in the gas, the gas and dust enter the electric field along the ion flow direction, the dust is fully charged, and the electric field consumption is small; the unipolar electric field dust collection efficiency will reach 99.99%.
  • the exhaust gas and dust enter the electric field in the direction of ion flow the dust is not fully charged, the electric power consumption of the electric field will also increase, and the dust collection efficiency will be 40% -75%.
  • the ion flow formed by the electric field device is beneficial to fluid transmission, oxygenation, or heat exchange of the unpowered fan.
  • the particulate matter As the anode of the dust-removing electric field continues to collect particulate matter and the like in the exhaust gas, the particulate matter accumulates and forms carbon black on the anode of the dust-removing electric field, and the thickness of the carbon black continues to increase, which reduces the pole spacing.
  • the phenomenon of electric field back-corona discharge is used in conjunction with an increased voltage to limit the injection current, so that a large amount of plasma is generated by a sudden discharge at the carbon deposit.
  • These low-temperature plasma cause carbon black
  • the middle organic components are deeply oxidized, and the polymer bonds are broken to form small molecules of carbon dioxide and water to complete carbon black cleaning.
  • the ozone molecular cluster catches the deposited oil pollution molecular cluster at the same time, accelerates the breakage of the hydrocarbon bonds in the oil pollution molecules, and carbonizes some oil molecules to achieve the purpose of purifying exhaust volatiles.
  • carbon black cleaning uses plasma to achieve effects that conventional cleaning methods cannot.
  • Plasma is a state of matter, also called the fourth state of matter, and does not belong to the common three states of solid, liquid, and gas. Apply enough energy to the gas to ionize it into a plasma state.
  • the "active" components of plasma include: ions, electrons, atoms, active groups, excited nuclides (meta-stable state), photons, etc.
  • the electric field device detects the electric field current and adopts any of the following methods to achieve carbon black cleaning:
  • the electric field device increases the electric field voltage.
  • the electric field device uses the electric field back-corona discharge phenomenon to complete the carbon black cleaning.
  • the electric field device uses the electric field back-corona discharge phenomenon to increase the voltage, limit the injection current, and complete the carbon black cleaning.
  • the electric field device uses the electric field back-corona discharge phenomenon to increase the voltage and limit the injection current, so that the rapid discharge occurring at the position of the anode carbon deposit generates plasma, the plasma causes The organic components of carbon black are deeply oxidized, the polymer bonds are broken, and small molecules of carbon dioxide and water are formed to complete the carbon black cleaning.
  • the anode of the dust removal electric field and the cathode of the dust removal electric field are electrically connected to the two electrodes of the power source, respectively.
  • the voltage loaded on the anode of the dust-removing electric field and the cathode of the dust-removing electric field need to select an appropriate voltage level, and the specific voltage level to be selected depends on the volume, temperature resistance, and dust-holding rate of the electric field device.
  • the voltage is from 1kv to 50kv; the temperature resistance conditions are first considered in the design, the parameters of the pole spacing and temperature: 1MM ⁇ 30 degrees, the dust accumulation area is greater than 0.1 square / thousand cubic meters / hour, and the electric field length is greater than 5 Times, control the electric field air flow velocity to be less than 9 meters per second.
  • the anode of the dust-removing electric field is composed of a second hollow anode tube and has a honeycomb shape.
  • the shape of the second hollow anode tube port may be circular or polygonal.
  • the value of the inscribed circle of the second hollow anode tube ranges from 5-400mm, the corresponding voltage is between 0.1-120kv, the corresponding current of the second hollow anode tube is between 0.1-30A;
  • the tangent circle corresponds to different corona voltage, about 1KV / 1MM.
  • the electric field device includes a second electric field stage.
  • the second electric field stage includes a plurality of second electric field generating units, and there may be one or more second electric field generating units.
  • the second electric field generating unit is also called a second dust collecting unit.
  • the second dust collecting unit includes the above-mentioned anode of the dust removing electric field and the cathode of the dust removing electric field. There are one or more second dust collecting units.
  • the dust collection efficiency of the electric field device can be effectively improved.
  • the anodes of each dust removal electric field are of the same polarity
  • the cathodes of each dust removal electric field are of the same polarity.
  • the electric field device further includes a plurality of connecting housings, and the second electric field stages connected in series are connected through the connecting housings; the distance between the second electric field stages of two adjacent stages is greater than 1.4 times the pole spacing.
  • the electret material is charged with an electric field.
  • the charged electret material will be used to remove dust.
  • the electric field device includes an electret element.
  • the electret element is provided in the anode of the dust-removing electric field.
  • the anode of the dedusting electric field and the cathode of the dedusting electric field exhaust when the power is turned on, and the electret element is in the ionizing dedusting electric field.
  • the electret element is close to the outlet of the electric field device, or the electret element is provided at the outlet of the electric field device.
  • the anode of the dedusting electric field and the cathode of the dedusting electric field form an exhaust gas flow channel, and the electret element is provided in the exhaust gas flow channel.
  • the exhaust runner includes an exhaust runner outlet, the electret element is close to the exhaust runner outlet, or the electret element is provided on the exhaust Runner exit.
  • the cross section of the electret element in the flow channel occupies 5% to 100% of the cross section of the exhaust flow channel.
  • the cross-section of the electret element in the exhaust runner accounts for 10% -90%, 20% -80%, or 40% -60% of the exhaust runner cross-section.
  • the ionization and dust removal electric field charges the electret element.
  • the electret element has a porous structure.
  • the electret element is a fabric.
  • the anode of the dedusting electric field is tubular, the outside of the electret element is tubular, and the outside of the electret element is sleeved inside the anode of the dusting electric field.
  • the electret element and the anode of the dust-removing electric field are detachably connected.
  • the material of the electret element includes an inorganic compound having electret properties.
  • the electret performance refers to that the electret element is charged after being charged by an external power source, and still retains a certain charge when completely disconnected from the power source, thereby acting as an electrode as an electric field electrode.
  • the inorganic compound is selected from one or more combinations of oxygen-containing compounds, nitrogen-containing compounds, or glass fibers.
  • the oxygen-containing compound is selected from one or more combinations of metal-based oxides, oxygen-containing composites, and oxygen-containing inorganic heteropoly acid salts.
  • the metal-based oxide is selected from one or more combinations of aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, lead oxide, and tin oxide .
  • the metal-based oxide is alumina.
  • the oxygen-containing composite is selected from one or more combinations of titanium-zirconium composite oxide or titanium-barium composite oxide.
  • the oxygen-containing inorganic heteropoly acid salt is selected from one or more combinations of zirconium titanate, lead zirconate titanate, or barium titanate.
  • the nitrogen-containing compound is silicon nitride.
  • the material of the electret element includes an organic compound having electret properties.
  • the electret performance refers to that the electret element is charged after being charged by an external power source, and still retains a certain charge when completely disconnected from the power source, thereby acting as an electrode as an electric field electrode.
  • the organic compound is selected from one or more combinations of fluoropolymer, polycarbonate, PP, PE, PVC, natural wax, resin, and rosin.
  • the fluoropolymer is selected from polytetrafluoroethylene (PTFE), polyperfluoroethylene propylene (Teflon-FEP), soluble polytetrafluoroethylene (PFA), and polyvinylidene fluoride (PVDF) One or more combinations.
  • PTFE polytetrafluoroethylene
  • Teflon-FEP polyperfluoroethylene propylene
  • PFA soluble polytetrafluoroethylene
  • PVDF polyvinylidene fluoride
  • the fluoropolymer is polytetrafluoroethylene.
  • the ionization and dust removal electric field is generated under the condition of power-on driving voltage.
  • the ionization and dust removal electric field is used to ionize part of the object to be treated, adsorb the particulate matter in the exhaust gas, and charge the electret element at the same time.
  • the electric field device fails, there is no power-on driving voltage At this time, the charged electret element generates an electric field, and the electric field generated by the charged electret element absorbs the particulate matter in the exhaust gas, that is, the particulate matter can still be adsorbed in the event of a failure in the ionization and dust removal electric field.
  • a method for exhaust dust removal includes the following steps: when the temperature of the exhaust gas is lower than 100 ° C, the liquid water in the exhaust gas is removed, and then the ionization dust is removed.
  • the exhaust gas when the temperature of the exhaust gas is ⁇ 100 ° C, the exhaust gas is ionized and dedusted.
  • the liquid water in the exhaust gas is removed, and then ionized to remove dust.
  • the liquid water in the exhaust gas is removed, and then the dust is ionized and removed.
  • the liquid water in the exhaust gas is removed, and then the ionization dust is removed.
  • the liquid water in the exhaust gas is removed by the electrocoagulation and defogging method, and then the dust is ionized and removed.
  • An exhaust dust removal method includes the following steps: adding a gas including oxygen before the ionization dust removal electric field to perform ionization dust removal.
  • oxygen is added by simply increasing oxygen, passing in outside air, passing in compressed air, and / or passing in ozone.
  • the amount of oxygen supplementation is determined based at least on the content of exhaust particles.
  • the present invention provides an electric field dust removal method, including the following steps:
  • the dust-containing gas passes through the ionization and dust removal electric field generated by the anode of the dust removal electric field and the cathode of the dust removal electric field;
  • the dust removal process is performed.
  • the dust is cleaned in any of the following ways:
  • the dust is carbon black.
  • the dust-removing electric field cathode includes a plurality of cathode wires.
  • the diameter of the cathode wire can be 0.1mm-20mm, and the size parameter can be adjusted according to the application and dust accumulation requirements. In an embodiment of the invention, the diameter of the cathode wire is not greater than 3 mm.
  • the cathode wire uses a metal wire or an alloy wire that is easy to discharge, is temperature resistant, can support its own weight, and is electrochemically stable.
  • the material of the cathode wire is titanium. The specific shape of the cathode wire is adjusted according to the shape of the anode of the dust removal electric field.
  • the cross section of the cathode wire is circular; if the dust collection surface of the anode of the dust removal electric field is an arc surface, the cathode wire Need to be designed as a polyhedron. The length of the cathode wire is adjusted according to the anode of the dust removal electric field.
  • the dust-removing electric field cathode includes a plurality of cathode rods.
  • the diameter of the cathode rod is not greater than 3 mm.
  • a metal rod or an alloy rod that is easy to discharge is used as the cathode rod.
  • the shape of the cathode rod may be needle-shaped, polygonal, burr-shaped, threaded rod-shaped, columnar or the like. The shape of the cathode rod can be adjusted according to the shape of the anode of the dust-removing electric field.
  • the cross-section of the cathode rod needs to be designed to be circular; if the dust-collecting surface of the anode of the dust-removing electric field is an arc surface , The cathode rod needs to be designed into a polyhedron shape.
  • the cathode of the dust-removing electric field is disposed in the anode of the dust-removing electric field.
  • the dust-removing electric field anode includes one or more hollow anode tubes arranged in parallel. When there are multiple hollow anode tubes, all the hollow anode tubes constitute a honeycomb-shaped dust-removing electric field anode.
  • the hollow anode tube may have a circular or polygonal cross section. If the cross section of the hollow anode tube is circular, a uniform electric field can be formed between the anode of the dedusting electric field and the cathode of the dedusting electric field, and the inner wall of the hollow anode tube is not easy to accumulate dust.
  • the cross section of the hollow anode tube is a triangular shape, three dust accumulation surfaces and three distant dust holding angles can be formed on the inner wall of the hollow anode tube.
  • This structure of the hollow anode tube has the highest dust holding rate. If the cross section of the hollow anode tube is quadrangular, 4 dust-collecting surfaces and 4 dust-holding angles can be obtained, but the grouping structure is unstable. If the cross section of the hollow anode tube is hexagonal, 6 dust accumulation surfaces and 6 dust accumulation angles can be formed, and the dust accumulation surface and the dust accumulation rate are balanced. If the cross section of the hollow anode tube is more polygonal, more dust accumulation edges can be obtained, but the dust holding rate is lost.
  • the diameter of the inscribed circle diameter of the hollow anode tube ranges from 5 mm to 400 mm.
  • the present invention provides a method for reducing the electric field coupling of dust removal, including the following steps:
  • the anode of the dedusting electric field or / and the cathode of the dedusting electric field are selected.
  • the size of the anode of the dedusting electric field or / and the cathode of the dedusting electric field is selected such that the number of electric field couplings is ⁇ 3.
  • the ratio of the dust collection area of the dust removal electric field anode to the discharge area of the dust removal electric field cathode is selected.
  • the ratio of the dust accumulation area of the dust removal electric field anode to the discharge area of the dust removal electric field cathode is 1.667: 1-1680: 1.
  • the ratio of the dust accumulation area of the dust-removing electric field anode to the discharge area of the dust-removing electric field cathode is selected to be 6.67: 1-56.67: 1.
  • the diameter of the cathode of the dust-removing electric field is 1-3 mm, and the pole spacing between the anode of the dust-removing electric field and the cathode of the tail gas-removing electric field is 2.5-139.9 mm;
  • the ratio of the discharge area of the cathode of the dedusting electric field is 1.667: 1-1680: 1.
  • the pole separation between the anode of the dust removal electric field and the cathode of the dust removal electric field is selected to be less than 150 mm.
  • the pole distance between the anode of the dust-removing electric field and the cathode of the dust-removing electric field is selected to be 2.5-139.9 mm. More preferably, the pole spacing between the anode of the dust-removing electric field and the cathode of the dust-removing electric field is selected to be 5.0-100 mm.
  • the length of the anode of the dust removal electric field is selected to be 10-180 mm. More preferably, the anode length of the dust removal electric field is selected to be 60-180 mm.
  • the cathode length of the dust removal electric field is selected to be 30-180 mm. More preferably, the cathode length of the dust removal electric field is selected to be 54-176 mm.
  • the dust-removing electric field cathode includes a plurality of cathode wires.
  • the diameter of the cathode wire can be 0.1mm-20mm, and the size parameter can be adjusted according to the application and dust accumulation requirements. In an embodiment of the invention, the diameter of the cathode wire is not greater than 3 mm.
  • the cathode wire uses a metal wire or an alloy wire that is easy to discharge, is temperature resistant, can support its own weight, and is electrochemically stable.
  • the material of the cathode wire is titanium. The specific shape of the cathode wire is adjusted according to the shape of the anode of the dust removal electric field.
  • the cross section of the cathode wire is circular; if the dust collection surface of the anode of the dust removal electric field is an arc surface, the cathode wire Need to be designed as a polyhedron. The length of the cathode wire is adjusted according to the anode of the dust removal electric field.
  • the dust-removing electric field cathode includes a plurality of cathode rods.
  • the diameter of the cathode rod is not greater than 3 mm.
  • a metal rod or an alloy rod that is easy to discharge is used as the cathode rod.
  • the shape of the cathode rod may be needle-shaped, polygonal, burr-shaped, threaded rod-shaped, columnar or the like. The shape of the cathode rod can be adjusted according to the shape of the anode of the dust-removing electric field.
  • the cross-section of the cathode rod needs to be designed to be circular; if the dust-collecting surface of the anode of the dust-removing electric field is an arc surface , The cathode rod needs to be designed into a polyhedron shape.
  • the cathode of the dust-removing electric field is disposed in the anode of the dust-removing electric field.
  • the dust-removing electric field anode includes one or more hollow anode tubes arranged in parallel. When there are multiple hollow anode tubes, all the hollow anode tubes constitute a honeycomb-shaped dust-removing electric field anode.
  • the hollow anode tube may have a circular or polygonal cross section. If the cross section of the hollow anode tube is circular, a uniform electric field can be formed between the anode of the dedusting electric field and the cathode of the dedusting electric field, and the inner wall of the hollow anode tube is not easy to accumulate dust.
  • the cross section of the hollow anode tube is a triangular shape, three dust accumulation surfaces and three distant dust holding angles can be formed on the inner wall of the hollow anode tube.
  • This structure of the hollow anode tube has the highest dust holding rate. If the cross section of the hollow anode tube is quadrangular, 4 dust-collecting surfaces and 4 dust-holding angles can be obtained, but the grouping structure is unstable. If the cross section of the hollow anode tube is hexagonal, 6 dust accumulation surfaces and 6 dust accumulation angles can be formed, and the dust accumulation surface and the dust accumulation rate are balanced. If the cross section of the hollow anode tube is more polygonal, more dust accumulation edges can be obtained, but the dust holding rate is lost.
  • the diameter of the inscribed circle diameter of the hollow anode tube ranges from 5 mm to 400 mm.
  • An exhaust dust removal method includes the following steps:
  • the electret element is close to the outlet of the electric field device, or the electret element is provided at the outlet of the electric field device.
  • the anode of the dedusting electric field and the cathode of the dedusting electric field form an exhaust gas flow channel, and the electret element is provided in the exhaust gas flow channel.
  • the exhaust runner includes an exhaust runner outlet, the electret element is close to the exhaust runner outlet, or the electret element is provided on the exhaust Runner exit.
  • the charged electret element when there is no electrified driving voltage in the ionization and dust removal electric field, the charged electret element is used to adsorb the particulate matter in the exhaust gas.
  • the charged electret element adsorbs certain particulate matter in the exhaust gas, it is replaced with a new electret element.
  • the ionization and dust removal electric field is restarted to adsorb particulate matter in the exhaust gas and charge the new electret element.
  • the material of the electret element includes an inorganic compound having electret properties.
  • the electret performance refers to that the electret element is charged after being charged by an external power source, and still retains a certain charge when completely disconnected from the power source, thereby acting as an electrode as an electric field electrode.
  • the inorganic compound is selected from one or more combinations of oxygen-containing compounds, nitrogen-containing compounds, or glass fibers.
  • the oxygen-containing compound is selected from one or more combinations of metal-based oxides, oxygen-containing composites, and oxygen-containing inorganic heteropoly acid salts.
  • the metal-based oxide is selected from one or more combinations of aluminum oxide, zinc oxide, zirconium oxide, titanium oxide, barium oxide, tantalum oxide, silicon oxide, lead oxide, and tin oxide .
  • the metal-based oxide is alumina.
  • the oxygen-containing composite is selected from one or more combinations of titanium-zirconium composite oxide or titanium-barium composite oxide.
  • the oxygen-containing inorganic heteropoly acid salt is selected from one or more combinations of zirconium titanate, lead zirconate titanate, or barium titanate.
  • the nitrogen-containing compound is silicon nitride.
  • the material of the electret element includes an organic compound having electret properties.
  • the electret performance means that the electret element is charged after being charged by an external power source, and still retains a certain charge even when completely disconnected from the power source, thereby acting as an electrode as an electric field electrode.
  • the organic compound is selected from one or more combinations of fluoropolymer, polycarbonate, PP, PE, PVC, natural wax, resin, and rosin.
  • the fluoropolymer is selected from polytetrafluoroethylene (PTFE), polyperfluoroethylene propylene (Teflon-FEP), soluble polytetrafluoroethylene (PFA), and polyvinylidene fluoride (PVDF) One or more combinations.
  • PTFE polytetrafluoroethylene
  • Teflon-FEP polyperfluoroethylene propylene
  • PFA soluble polytetrafluoroethylene
  • PVDF polyvinylidene fluoride
  • the fluoropolymer is polytetrafluoroethylene.
  • the exhaust gas treatment system includes an exhaust gas ozone purification system.
  • the exhaust ozone purification system includes a reaction field for mixing and reacting the ozone stream with the exhaust stream.
  • the exhaust ozone purification system can be used to treat the exhaust of the exhaust discharge device 210, using the water in the exhaust and the exhaust pipe 220 to generate an oxidation reaction to oxidize the organic volatiles in the exhaust to carbon dioxide and Water; sulfur, nitrate and other harmless collection.
  • the exhaust ozone purification system may further include an external ozone generator 230, which supplies ozone to the exhaust pipe 220 through the ozone delivery pipe 240, as shown in FIG. 1, where the arrow direction is the exhaust gas flow direction.
  • the molar ratio of the ozone stream to the exhaust stream can be 2 to 10, such as 5 to 6, 5.5 to 6.5, 5 to 7, 4.5 to 7.5, 4 to 8, 3.5 to 8.5, 3 to 9, 2.5 to 9.5, 2 ⁇ 10.
  • ozone produced by extended surface discharge is composed of tubular, plate-type discharge parts and AC high-voltage power supply.
  • the air after electrostatic adsorption of dust, water and oxygen-rich air enters the discharge channel.
  • the air oxygen is ionized to produce ozone, high-energy ions, and high-energy particles. Pass into the reaction field such as exhaust channel through positive or negative pressure.
  • a cooling liquid is passed inside the discharge tube and outside the outer discharge tube, forming an electrode between the inner electrode of the tube and the outer tube conductor, 18kHz, 10kV high-voltage alternating current is passed between the electrodes, the inner wall of the outer tube and the inner tube High-energy ionization occurs on the outer wall surface, oxygen is ionized, and ozone is generated. Ozone is sent into the reaction field such as the exhaust channel using positive pressure.
  • the VOCs removal rate is 50%; when the molar ratio of the ozone stream to the exhaust stream is 5, the VOCs removal rate is more than 95%, and then the nitrogen oxide gas concentration decreases
  • the nitrogen oxide removal rate is 90%; when the molar ratio of the ozone stream to the exhaust stream is greater than 10, the VOCs removal rate is more than 99%, and then the nitrogen oxide gas concentration decreases, and the nitrogen oxide removal rate is 99%. Power consumption increased to 30w / g.
  • the ozone generated by the ultraviolet lamp generates 11-195 nanometer wavelength ultraviolet rays by gas discharge, directly irradiates the air around the lamp, generates ozone, high-energy ions, and high-energy particles, and passes into the reaction field such as the exhaust channel through positive pressure or negative pressure.
  • the reaction field such as the exhaust channel through positive pressure or negative pressure.
  • 172 nanometer wavelength and 185 nanometer wavelength ultraviolet discharge tubes by lighting the lamp, oxygen in the gas on the outer wall of the lamp tube is ionized, generating a large amount of oxygen ions, combined into ozone. It is fed into the reaction field such as the exhaust channel by positive pressure.
  • the VOCs removal rate is 40%; when the molar ratio of 185 nanometer ultraviolet ozone stream to exhaust stream is 5, the VOCs removal rate is more than 85%. Then the nitrogen oxide gas concentration drops, and the nitrogen oxide removal rate is 70%; when the molar ratio of the 185 nm ultraviolet ozone stream to the exhaust stream is greater than 10, the VOCs removal rate is more than 95%, and then the nitrogen oxide gas concentration decreases, nitrogen Oxygen compound removal rate is 95%. Power consumption is 25w / g.
  • the VOCs removal rate is 45%; when the molar ratio of 172 nanometer ultraviolet ozone stream to exhaust stream is 5, the VOCs removal rate is more than 89% , Then the nitrogen oxide gas concentration drops, and the nitrogen oxide removal rate is 75%; when the molar ratio of the 172 nm ultraviolet ozone stream to the exhaust stream is greater than 10, the VOCs removal rate is more than 97%, and then the nitrogen oxide gas concentration decreases The removal rate of nitrogen oxides is 95%. Power consumption 22w / g.
  • the reaction field includes pipes and / or reactors.
  • the reaction field further includes at least one of the following technical features:
  • the diameter of the pipeline is 100-200 mm;
  • the length of the pipeline is greater than 0.1 times the diameter of the pipeline
  • the reactor is selected from at least one of the following:
  • Reactor 1 The reactor has a reaction chamber, and exhaust gas and ozone are mixed and reacted in the reaction chamber;
  • the reactor includes a number of honeycomb-shaped cavities for providing a space where exhaust gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing cold state medium to control the discharge Reaction temperature of gas and ozone;
  • the reactor includes several carrier units.
  • the carrier unit provides a reaction site (such as a mesoporous ceramic body carrier with a honeycomb structure). When there is no carrier unit, the reaction is in the gas phase, and when there is a carrier unit, it is an interface reaction. Speed up the response time;
  • Reactor 4 The reactor includes a catalyst unit, and the catalyst unit is used to promote the oxidation reaction of exhaust gas;
  • the reaction field is provided with an ozone inlet, the ozone inlet is selected from at least one of a nozzle, a spray grid, a nozzle, a swirl nozzle, a nozzle provided with a venturi tube; a nozzle provided with a venturi tube:
  • the venturi tube is set in the spout, and the ozone is mixed into the venturi principle;
  • the reaction field is provided with an ozone inlet.
  • the ozone enters the reaction field through the ozone inlet and contacts the exhaust gas.
  • the setting of the ozone inlet forms at least one of the following directions:
  • the direction of gas flow is perpendicular, tangent to the direction of exhaust gas flow, insert the direction of exhaust gas flow, and multiple directions are in contact with the exhaust gas;
  • the direction opposite to the direction of exhaust gas flow is the opposite direction, increasing the reaction time and reducing
  • the volume is perpendicular to the direction of exhaust gas flow, using the Venturi effect; tangential to the direction of exhaust gas flow for easy mixing; inserting the direction of exhaust gas flow to overcome vortex flow; multiple directions to overcome gravity.
  • the reaction field includes an exhaust pipe, a regenerator device, or a catalyst, and ozone can clean and regenerate the regenerator, catalyst, and ceramic body.
  • the temperature of the reaction field is -50 to 200 ° C, may be 60 to 70 ° C, 50 to 80 ° C, 40 to 90 ° C, 30 to 100 ° C, 20 to 110 ° C, 10 to 120 °C, 0 ⁇ 130 °C, -10 ⁇ 140 °C, -20 ⁇ 150 °C, -30 ⁇ 160 °C, -40 ⁇ 170 °C, -50 ⁇ 180 °C, -180 ⁇ 190 °C or 190 ⁇ 200 °C.
  • the temperature of the reaction field is 60-70 ° C.
  • the exhaust ozone purification system further includes an ozone source, which is used to provide an ozone stream.
  • the ozone stream can be generated instantly by the ozone generator or stored ozone.
  • the reaction field can be in fluid communication with an ozone source, and the ozone stream provided by the ozone source can be introduced into the reaction field, so that it can be mixed with the exhaust stream to subject the exhaust stream to oxidation treatment.
  • the ozone source includes a storage ozone unit and / or an ozone generator.
  • the ozone source may include an ozone introduction pipe, and may also include an ozone generator.
  • the ozone generator may include, but is not limited to, an arc ozone generator, that is, a extended surface discharge ozone generator, a power frequency arc ozone generator, and a high frequency induction
  • arc ozone generator that is, a extended surface discharge ozone generator, a power frequency arc ozone generator, and a high frequency induction
  • ozone generators low-pressure ozone generators
  • ultraviolet ozone generators ultraviolet ozone generators
  • electrolyte ozone generators chemical agent ozone generators
  • radiation irradiation particle generators etc.
  • the ozone generator includes an extended surface discharge ozone generator, a power frequency arc ozone generator, a high-frequency induction ozone generator, a low-pressure ozone generator, an ultraviolet ozone generator, and an electrolyte ozone generator A combination of one or more of the device, chemical ozone generator and radiation irradiation particle generator.
  • the ozone generator includes an electrode, and a catalyst layer is provided on the electrode, and the catalyst layer includes an oxidation catalytic bond cracking selective catalyst layer.
  • the electrode includes a high-voltage electrode or a high-voltage electrode provided with a barrier medium layer.
  • the oxidation catalytic bond cleavage selective catalyst layer 250 is provided on the high-voltage electrode On the surface of 260 (as shown in FIG. 2), when the electrode includes the high-voltage electrode 260 of the blocking medium layer 270, the oxidation catalytic bond cleavage selective catalyst layer 250 is provided on the surface of the blocking medium layer 270 (as shown in FIG. 3 Shown).
  • Electrode refers to the electrode plate used to input or export current in a conductive medium (solid, gas, vacuum or electrolyte solution).
  • a conductive medium solid, gas, vacuum or electrolyte solution.
  • One pole of input current is called anode or anode, and one pole of current is called cathode or cathode.
  • the discharge ozone generation mechanism is mainly a physical (electrical) method.
  • a schematic diagram of the structure of an existing discharge-type ozone generator is shown in FIG. 4.
  • the discharge-type ozone generator includes a high-voltage AC power supply 280, a high-voltage electrode 260, a barrier dielectric layer 270, an air gap 290, and a ground electrode 291. Under the action of a high-voltage electric field, the dioxygen bond of the oxygen molecules in the air gap 290 is broken by electrical energy to produce ozone.
  • the use of electric field energy to generate ozone has its limits. Current industry standards require that the power consumption per kg of ozone does not exceed 8kWh, and the industry average level is about 7.5kWh.
  • the barrier medium layer is selected from at least one of ceramic plates, ceramic tubes, quartz glass plates, quartz plates, and quartz tubes.
  • the ceramic plates and ceramic tubes may be ceramic plates or ceramic tubes of oxides such as alumina, zirconia, silicon oxide, or their composite oxides.
  • the thickness of the oxidation catalytic bond cracking selective catalyst layer is 1 to 3 mm, and the oxidation catalytic bond cracking selective catalyst layer also serves as a blocking medium, such as 1 to 1.5mm or 1.5 ⁇ 3mm; when the electrode includes a high-voltage electrode that blocks the dielectric layer, the loading of the selective catalyst layer for the oxidation catalytic bond cleavage includes 1-12 wt% of the barrier dielectric layer, such as 1-5 wt% or 5 ⁇ 12wt%.
  • the oxidation catalytic bond cleavage selective catalyst layer includes the following weight percent components:
  • Active components 5 to 15%, such as 5 to 8%, 8 to 10%, 10 to 12%, 12 to 14% or 14 to 15%;
  • the coating is 85-95%, such as 85-86%, 86-88%, 88-90%, 90-92% or 92-95%;
  • the active component is selected from at least one of a compound of metal M and metal element M
  • the metal element M is selected from alkaline earth metal elements, transition metal elements, fourth main group metal elements, precious metal elements and lanthanide rare earth elements At least one of
  • the coating is selected from at least one of alumina, cerium oxide, zirconia, manganese oxide, metal composite oxides, porous materials, and layered materials.
  • the metal composite oxide includes aluminum, cerium, zirconium, and manganese A composite oxide of one or more metals.
  • the alkaline earth metal element is selected from at least one of magnesium, strontium and calcium.
  • the transition metal element is selected from at least one of titanium, manganese, zinc, copper, iron, nickel, cobalt, yttrium, and zirconium.
  • the fourth main group metal element is tin.
  • the precious metal element is at least one selected from platinum, rhodium, palladium, gold, silver and iridium.
  • the lanthanide rare earth element is selected from at least one of lanthanum, cerium, praseodymium, and samarium.
  • the compound of the metal element M is at least one selected from oxides, sulfides, sulfates, phosphates, carbonates, and perovskites.
  • the porous material is selected from at least one of molecular sieve, diatomaceous earth, zeolite, and carbon nanotubes.
  • the porosity of the porous material is more than 60%, such as 60-80%, the specific surface area is 300-500 square meters / gram, and the average pore size is 10-100 nanometers.
  • the layered material is selected from at least one of graphene and graphite.
  • the selective catalytic layer for oxidative catalytic bond cleavage combines chemical and physical methods to reduce, weaken or even directly break the dioxygen bond, fully exert and utilize the synergistic effect of electric field and catalysis, and achieve a significant increase in ozone generation rate and amount
  • the purpose of the invention is to compare the ozone generator of the present invention with the existing discharge type ozone generator, under the same conditions, the ozone generation amount is increased by 10-30%, and the generation rate is increased by 10-20%.
  • the exhaust ozone purification system further includes an ozone amount control device for controlling the amount of ozone so as to effectively oxidize gas components to be treated in the exhaust gas.
  • the ozone amount control device includes a control unit.
  • the ozone quantity control device further includes an exhaust component detection unit before ozone treatment, which is used to detect the exhaust component content before ozone treatment.
  • control unit controls the amount of ozone required for the mixed reaction according to the content of the exhaust gas component before the ozone treatment.
  • the exhaust gas component detection unit before ozone treatment is selected from at least one of the following detection units:
  • the first volatile organic compound detection unit is used to detect the content of volatile organic compounds in the exhaust gas before ozone treatment, such as volatile organic compound sensors;
  • the first CO detection unit is used to detect the CO content in the exhaust gas before ozone treatment, such as a CO sensor;
  • the first nitrogen oxide detection unit is used to detect the nitrogen oxide content in the exhaust gas before ozone treatment, such as a nitrogen oxide (NO x ) sensor.
  • a nitrogen oxide (NO x ) sensor such as a nitrogen oxide (NO x ) sensor.
  • control unit controls the amount of ozone required for the mixed reaction according to at least one output value of the exhaust component detection unit before ozone treatment.
  • control unit is used to control the amount of ozone required for the mixed reaction according to a preset mathematical model.
  • the preset mathematical model is related to the content of the exhaust component before ozone treatment.
  • the amount of ozone required for the mixed reaction is determined by the above content and the reaction molar ratio of the exhaust component to ozone. Increase the amount of ozone to make ozone excessive.
  • control unit is used to control the amount of ozone required for the mixed reaction according to the theoretical estimated value.
  • the theoretical estimated value is: the molar ratio of ozone flux to the object to be treated in the exhaust gas is 2-10.
  • 13L diesel exhaust equipment can control the ozone flux from 300 to 500g
  • 2L gasoline exhaust equipment can control the ozone flux from 5 to 20g.
  • the ozone quantity control device includes an exhaust component detection unit after ozone treatment, which is used to detect the exhaust component content after ozone treatment.
  • control unit controls the amount of ozone required for the mixed reaction according to the content of the exhaust gas component after the ozone treatment.
  • the exhaust gas component detection unit after ozone treatment is selected from at least one of the following detection units:
  • the first ozone detection unit is used to detect the ozone content in the exhaust gas after ozone treatment
  • the second volatile organic compound detection unit is used to detect the content of volatile organic compounds in the exhaust gas after ozone treatment
  • the second CO detection unit is used to detect the CO content in the exhaust gas after ozone treatment
  • the second nitrogen oxide detection unit is used to detect the nitrogen oxide content in the exhaust gas after ozone treatment.
  • control unit controls the amount of ozone according to at least one output value of the ozone-treated exhaust gas composition detection unit.
  • the exhaust ozone purification system further includes a denitration device for removing nitric acid from the mixed reaction product of the ozone stream and the exhaust stream.
  • the denitration device includes an electrocoagulation device.
  • the electrocoagulation device includes an electrocoagulation flow channel, a first electrode located in the electrocoagulation flow channel, and a second electrode.
  • the denitration device includes a condensing unit for condensing the exhaust gas after ozone treatment to achieve gas-liquid separation.
  • the denitration device includes a rinsing unit for rinsing the exhaust gas after ozone treatment, for example, rinsing with water and / or alkali.
  • the denitration device further includes an eluent unit for supplying the eluent to the eluent unit.
  • the eluent in the eluent unit includes water and / or alkali.
  • the denitration device further includes a denitration liquid collection unit for storing the nitric acid aqueous solution and / or the nitrate aqueous solution removed in the exhaust gas.
  • the denitration liquid collection unit when a nitric acid aqueous solution is stored in the denitration liquid collection unit, the denitration liquid collection unit is provided with an alkaline liquid addition unit for forming nitrate with nitric acid.
  • the exhaust gas ozone purification system further includes an ozone digester for digesting ozone in the exhaust gas treated by the reaction field.
  • the ozone digester can perform ozone digestion by means of ultraviolet rays, catalysis and the like.
  • the ozone digester is selected from at least one of an ultraviolet ozone digester and a catalytic ozone digester.
  • the exhaust gas ozone purification system further includes a first denitration device for removing nitrogen oxides in the exhaust gas; the reaction field is used for processing the first denitration device The exhaust gas is mixed and reacted with the ozone stream, or used for mixing and reacting the exhaust gas with the ozone stream before being processed by the first denitration device.
  • the first denitration device may be a device for realizing denitration in the prior art, for example: a non-catalytic reduction device (such as ammonia denitration), a selective catalytic reduction device (SCR: ammonia gas plus catalyst denitration), and a non-selective catalytic reduction At least one of a device (SNCR) and an electron beam denitration device.
  • a non-catalytic reduction device such as ammonia denitration
  • SCR selective catalytic reduction device
  • SNCR non-selective catalytic reduction
  • the content of nitrogen oxides (NO x ) in the exhaust gas after treatment by the first denitration device does not reach the standard, and the mixed reaction of the exhaust gas and the ozone stream after or before the first denitration device treatment can reach the latest standard.
  • NO x nitrogen oxides
  • the first denitration device is selected from at least one of a non-catalytic reduction device, a selective catalytic reduction device, a non-selective catalytic reduction device, and an electron beam denitration device.
  • the ozone When the exhaust gas treated with ozone, the ozone is reacted with the highest priority VOC volatile organic compound, is oxidized to CO 2 and water, then the nitrogen oxides NO X, is oxidized to nitrogen oxides, such as high NO 2, N 2 O 5 and NO 3, etc., and finally react with carbon monoxide CO to be oxidized to CO 2 , that is, the reaction priority is VOC > nitrogen oxide NO X > carbon monoxide CO, and there are enough volatile organic compounds in the exhaust
  • the compound VOC produces enough water to fully react with high-valent nitrogen oxides to generate nitric acid. Therefore, the treatment of exhaust gas with ozone makes ozone more effective in removing NO X , which is unexpected for those skilled in the art. Technical effect.
  • Exhaust ozone treatment can be removed to achieve the following effects: the nitrogen oxide NO X removal efficiency: 60 - 99.97%; the efficiency of removal of carbon monoxide CO: 1-50%; volatile organic compounds VOC removal efficiency: 60 to 99.97% It is an unexpected technical effect for those skilled in the art.
  • the nitric acid obtained by reacting the high-valent nitrogen oxide with the water obtained by oxidizing the volatile organic compound VOC is easier to remove and the removed nitric acid can be recycled.
  • Nitric acid is removed by methods for removing nitric acid in the prior art, such as alkali elution.
  • the electrocoagulation device of the present invention includes a first electrode and a second electrode. When the nitric acid-containing water mist flows through the first electrode, the nitric acid-containing water mist will be charged, and the second electrode applies attraction to the charged nitric acid-containing water mist, and the nitric acid-containing water mist Move to the second electrode until the nitric acid-containing water mist adheres to the second electrode, and then collect again.
  • the electrocoagulation device of the present invention has stronger collection capacity and higher collection efficiency for nitric acid-containing water mist.
  • the ozone formed by ionization can be used to oxidize pollutants in the exhaust, such as nitrogen oxides NO X , volatilization
  • pollutants in the exhaust such as nitrogen oxides NO X , volatilization
  • the organic compounds VOC and carbon monoxide CO, that is, the ozone formed by ionization can be used by ozone treatment NO X to treat pollutants.
  • the oxidation of nitrogen oxides NO X will also oxidize the volatile organic compounds VOC and carbon monoxide CO, saving ozone treatment NO X Ozone depletion, and there is no need to increase the ozone removal mechanism to digest the ozone formed by ionization, which will not cause the greenhouse effect and destroy the ultraviolet rays in the atmosphere.
  • the combination of the exhaust dust removal system and the exhaust ozone purification system Functionally support each other and achieve new technical effects: the ozone formed by ionization is used by the exhaust ozone purification system to treat pollutants, saving ozone consumption of ozone treatment pollutants, and there is no need to increase the ozone removal mechanism for ionization
  • the formed ozone will be digested without causing the greenhouse effect, destroying the ultraviolet rays in the atmosphere, and having outstanding Substantive features and notable progress.
  • An exhaust ozone purification method includes the following steps: mixing and reacting an ozone stream with an exhaust stream.
  • the exhaust stream includes nitrogen oxides and volatile organic compounds.
  • the exhaust stream may be exhaust gas, and the exhaust gas discharge device is generally a device that converts chemical energy of fuel into mechanical energy, and may specifically be an internal combustion engine or the like.
  • Nitrogen oxides (NO x ) in the exhaust stream are mixed and reacted with the ozone stream to be oxidized into high-valent nitrogen oxides such as NO 2 , N 2 O 5 and NO 3 .
  • the volatile organic compounds (VOC) in the exhaust stream are mixed with the ozone stream to be oxidized into CO 2 and water.
  • the high-valent nitrogen oxide reacts with water obtained by oxidation of volatile organic compounds (VOC) to obtain nitric acid.
  • nitrogen oxides (NO x ) in the exhaust stream are removed, and they are present in the exhaust gas in the form of nitric acid.
  • the ozone stream and the exhaust stream are mixed and reacted.
  • the mixing reaction temperature of the ozone stream and the exhaust stream is -50 to 200 ° C, may be 60 to 70 ° C, 50 to 80 ° C, 40 to 90 ° C, 30 to 100 ° C, 20 to 110 °C, 10 ⁇ 120 °C, 0 ⁇ 130 °C, -10 ⁇ 140 °C, -20 ⁇ 150 °C, -30 ⁇ 160 °C, -40 ⁇ 170 °C, -50 ⁇ 180 °C, -180 ⁇ 190 °C or 190 ⁇ 200 °C.
  • the mixing reaction temperature of the ozone stream and the exhaust stream is 60-70 ° C.
  • the mixing method of the ozone stream and the exhaust stream is selected from at least one of Venturi mixing, positive pressure mixing, plug-in mixing, dynamic mixing, and fluid mixing.
  • the pressure of the ozone inlet gas is greater than the pressure of the exhaust gas.
  • the Venturi mixing method can be used at the same time.
  • the velocity of the exhaust stream is increased, and the ozone stream is mixed using the Venturi principle.
  • the mixing method of the ozone stream and the exhaust stream is selected from the reverse flow of the exhaust outlet, the mixing in the front section of the reaction field, the front and rear insertion of the dust collector, the mixing of the denitration device, the mixing of the catalyst device, and the mixing of the water washing device.
  • At least one of passage, front and back mixing of the filtering device, front and back mixing of the muffler device, mixing in the exhaust pipe, external mixing of the adsorption device and front and back mixing of the condensation device. Can be set in the low temperature section of the exhaust to avoid ozone digestion.
  • the reaction field in which the ozone stream and the exhaust stream are mixed and reacted includes pipes and / or reactors.
  • the reaction field includes an exhaust pipe, a regenerator device, or a catalyst.
  • the diameter of the pipeline is 100-200 mm;
  • the length of the pipeline is greater than 0.1 times the diameter of the pipeline
  • the reactor is selected from at least one of the following:
  • Reactor 1 The reactor has a reaction chamber, and exhaust gas and ozone are mixed and reacted in the reaction chamber;
  • the reactor includes a number of honeycomb-shaped cavities for providing a space where exhaust gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing cold state medium to control the discharge Reaction temperature of gas and ozone;
  • the reactor includes several carrier units.
  • the carrier unit provides a reaction site (such as a mesoporous ceramic body carrier with a honeycomb structure). When there is no carrier unit, the reaction is in the gas phase, and when there is a carrier unit, it is an interface reaction. Speed up the response time;
  • Reactor 4 The reactor includes a catalyst unit, and the catalyst unit is used to promote the oxidation reaction of exhaust gas;
  • the reaction field is provided with an ozone inlet.
  • the ozone inlet is selected from at least one of a nozzle, a spray grid, a nozzle, a swirl nozzle, and a nozzle provided with a venturi tube; a nozzle provided with a venturi tube: The venturi tube is set in the spout, and the ozone is mixed into the venturi principle;
  • the reaction field is provided with an ozone inlet.
  • the ozone enters the reaction field through the ozone inlet and contacts the exhaust gas.
  • the setting of the ozone inlet forms at least one of the following directions:
  • the direction of gas flow is perpendicular, tangent to the direction of exhaust gas flow, insert the direction of exhaust gas flow, and multiple directions are in contact with the exhaust gas;
  • the direction opposite to the direction of exhaust gas flow is the opposite direction, increasing the reaction time and reducing
  • the volume is perpendicular to the direction of exhaust gas flow, using the Venturi effect; tangential to the direction of exhaust gas flow for easy mixing; inserting the direction of exhaust gas flow to overcome vortex flow; multiple directions to overcome gravity.
  • the ozone stream is provided by a storage ozone unit and / or an ozone generator.
  • the ozone generator includes an extended surface discharge ozone generator, a power frequency arc ozone generator, a high-frequency induction ozone generator, a low-pressure ozone generator, an ultraviolet ozone generator, and an electrolyte ozone generator A combination of one or more of the device, chemical ozone generator and radiation irradiation particle generator.
  • the ozone stream providing method: under the action of an electric field and an oxidation catalytic bond cracking selective catalyst layer, a gas containing oxygen generates ozone, wherein the electrode forming the electric field is loaded with an oxidation catalytic bond cracking selectivity Catalyst layer.
  • the electrode includes a high-voltage electrode or an electrode provided with a barrier medium layer.
  • the selective catalytic layer for oxidative catalytic bond cleavage is supported on the surface of the high-voltage electrode
  • the selective catalytic layer for oxidative catalytic bond cleavage is supported on the surface of the blocking dielectric layer.
  • the thickness of the oxidation catalytic bond cracking selective catalyst layer is 1 to 3 mm, and the oxidation catalytic bond cracking selective catalyst layer also serves as a blocking medium, such as 1 to 1.5mm or 1.5 ⁇ 3mm; when the electrode includes a high-voltage electrode that blocks the dielectric layer, the loading of the selective catalyst layer for the oxidation catalytic bond cleavage includes 1-12 wt% of the barrier dielectric layer, such as 1-5 wt% or 5 ⁇ 12wt%.
  • the oxidation catalytic bond cleavage selective catalyst layer includes the following weight percent components:
  • Active components 5 to 15%, such as 5 to 8%, 8 to 10%, 10 to 12%, 12 to 14% or 14 to 15%;
  • the coating is 85-95%, such as 85-86%, 86-88%, 88-90%, 90-92% or 92-95%;
  • the active component is selected from at least one of a compound of metal M and metal element M
  • the metal element M is selected from alkaline earth metal elements, transition metal elements, fourth main group metal elements, precious metal elements and lanthanide rare earth elements At least one of
  • the coating is selected from at least one of alumina, cerium oxide, zirconia, manganese oxide, metal composite oxides, porous materials, and layered materials.
  • the metal composite oxide includes aluminum, cerium, zirconium, and manganese A composite oxide of one or more metals.
  • the alkaline earth metal element is selected from at least one of magnesium, strontium and calcium.
  • the transition metal element is selected from at least one of titanium, manganese, zinc, copper, iron, nickel, cobalt, yttrium, and zirconium.
  • the fourth main group metal element is tin.
  • the precious metal element is at least one selected from platinum, rhodium, palladium, gold, silver and iridium.
  • the lanthanide rare earth element is selected from at least one of lanthanum, cerium, praseodymium, and samarium.
  • the compound of the metal element M is at least one selected from oxides, sulfides, sulfates, phosphates, carbonates, and perovskites.
  • the porous material is selected from at least one of molecular sieve, diatomaceous earth, zeolite, and carbon nanotubes.
  • the porosity of the porous material is more than 60%, such as 60-80%, the specific surface area is 300-500 square meters / gram, and the average pore size is 10-100 nanometers.
  • the layered material is selected from at least one of graphene and graphite.
  • the electrode is loaded with an oxygen double catalytic bond cracking selective catalyst by dipping and / or spraying methods.
  • the slurry of the coating material is loaded on the surface of the high-voltage electrode or the surface of the barrier medium layer, dried, and calcined to obtain the coated high-voltage electrode or the barrier medium layer;
  • the raw material solution or slurry containing the metal element M is loaded onto the step 1) to obtain the coating, dried, and calcined.
  • the barrier The medium layer is provided with a high-voltage electrode relative to the other side of the loaded coating, to obtain the electrode for the ozone generator; or, according to the catalyst composition ratio, the raw material solution or slurry containing the metal element M is loaded to step 1) to obtain a coating
  • drying, calcining and post-processing when the coating layer is loaded on the surface of the barrier medium layer, after post-processing, a high-voltage electrode is provided on the other side of the barrier medium layer relative to the load coating layer to obtain the electrode for the ozone generator;
  • the control of the morphology of the active component in the catalyst for electrodes is achieved through the calcination temperature and atmosphere, and post-treatment.
  • the raw material solution or slurry containing the metal element M is loaded on the coating raw material, dried and calcined to obtain the coating material loaded with the active component;
  • the coating material loaded with active components obtained in step 1) is made into a slurry, which is loaded on the surface of the high-voltage electrode or the surface of the barrier medium layer, dried, calcined, when the coating is loaded When it is on the surface of the barrier medium layer, after calcination, a high-voltage electrode is provided on the other side of the barrier medium layer relative to the supporting coating layer, that is, the electrode for the ozone generator; or, according to the catalyst composition ratio, obtained in step 1)
  • the coating material loaded with the active component is made into a slurry, which is loaded on the surface of the high-voltage electrode or the surface of the barrier medium layer, dried, calcined and post-treated. When the coating layer is loaded on the surface of the barrier medium layer, the post-treatment Then, a high-voltage electrode is provided on the other side of the barrier medium layer relative to the load coating layer to obtain the electrode for the ozone generator;
  • the control of the morphology of the active component in the catalyst for electrodes is achieved through the calcination temperature and atmosphere, and post-treatment.
  • the above loading method may be dipping, spraying, painting, etc., and the loading can be realized.
  • the active component includes at least one of sulfates, phosphates, and carbonates of the metal element M
  • a solution or slurry loaded coating containing at least one of the sulfates, phosphates, and carbonates of the metal element M
  • the calcination temperature cannot exceed the decomposition temperature of the active component, for example: to obtain the sulfate of the metal element M, the calcination temperature cannot exceed the decomposition temperature of the sulfate (the decomposition temperature is generally above 600 ° C).
  • the control of the morphology of the active component in the catalyst for the electrode is achieved through the calcination temperature and atmosphere, and post-treatment, for example: when the active component includes metal M, it can be obtained by reducing gas after calcination (post-treatment) When the active component includes the sulfide of the metal element M, it can be obtained by reacting (post-treatment) with hydrogen sulfide after calcination, and the calcination temperature can be 200-550 ° C.
  • it includes: controlling the amount of ozone in the ozone stream so as to effectively oxidize the gas components to be treated in the exhaust gas.
  • controlling the amount of ozone in the ozone stream achieves the following removal efficiency:
  • Nitrogen oxide removal efficiency 60-99.97%
  • it includes: detecting the content of exhaust components before ozone treatment.
  • the amount of ozone required for the mixing reaction is controlled according to the content of the exhaust gas component before ozone treatment.
  • the content of the exhaust component before ozone treatment is selected from at least one of the following:
  • the amount of ozone required for the mixed reaction is controlled according to at least one output value that detects the content of exhaust components before ozone treatment.
  • the amount of ozone required for the mixed reaction is controlled according to a preset mathematical model.
  • the preset mathematical model is related to the content of the exhaust component before ozone treatment.
  • the amount of ozone required for the mixed reaction is determined by the above content and the reaction molar ratio of the exhaust component to ozone. Increase the amount of ozone to make ozone excessive.
  • the amount of ozone required for the mixed reaction is controlled according to the theoretical estimate.
  • the theoretical estimated value is: the molar ratio of ozone flux to the object to be treated in the exhaust gas is 2-10, such as 5-6, 5.5-6.5, 5-7, 4.5-7.5 , 4-8, 3.5-8.5, 3-9, 2.5-9.5, 2-10.
  • 13L diesel exhaust equipment can control the ozone flux from 300 to 500g
  • 2L gasoline exhaust equipment can control the ozone flux from 5 to 20g.
  • it includes: detecting the content of exhaust components after ozone treatment.
  • the amount of ozone required for the mixing reaction is controlled according to the content of exhaust components after the ozone treatment.
  • the content of exhaust components after ozone treatment is selected from at least one of the following:
  • the amount of ozone is controlled according to at least one output value that detects the content of exhaust components after ozone treatment.
  • the exhaust gas ozone purification method further includes the following steps: removing nitric acid from the mixed reaction product of the ozone stream and the exhaust gas stream.
  • the gas with nitric acid mist flows through the first electrode; when the gas with nitric acid mist flows through the first electrode, the first electrode charges the nitric acid mist in the gas, and the second electrode charges The nitric acid mist exerts an attractive force to move the nitric acid mist toward the second electrode until the nitric acid mist adheres to the second electrode.
  • a method for removing nitric acid in a mixed reaction product of an ozone stream and an exhaust stream condensing the mixed reaction product of the ozone stream and the exhaust stream.
  • a method for removing nitric acid in a mixed reaction product of an ozone stream and an exhaust stream washing the mixed reaction product of the ozone stream and the exhaust stream.
  • the method for removing nitric acid from the mixed reaction product of the ozone stream and the exhaust stream further includes: providing an eluent to the mixed reaction product of the ozone stream and the exhaust stream.
  • the eluent is water and / or alkali.
  • the method for removing nitric acid in the mixed reaction product of the ozone stream and the exhaust stream further includes: storing the removed nitric acid aqueous solution and / or nitrate aqueous solution in the exhaust gas.
  • an alkaline solution is added to form nitrate with nitric acid.
  • the exhaust gas ozone purification method further includes the following steps: performing ozone digestion on the exhaust gas from which nitric acid is removed, for example, it can be digested by ultraviolet rays, catalysis, or the like.
  • the ozone digestion is selected from at least one of ultraviolet digestion and catalytic digestion.
  • the exhaust ozone purification method further includes the following steps: the first removal of nitrogen oxides in the exhaust; the exhaust stream and the ozone stream after the first removal of nitrogen oxides Mixed reaction, or mixed with ozone stream before removing nitrogen oxides from the exhaust gas for the first time.
  • the first removal of nitrogen oxides in the exhaust gas can be a method for denitrification in the prior art, for example: non-catalytic reduction methods (such as ammonia denitration), selective catalytic reduction methods (SCR: ammonia plus catalyst denitration), At least one of a non-selective catalytic reduction method (SNCR) and an electron beam denitration method.
  • non-catalytic reduction methods such as ammonia denitration
  • SCR selective catalytic reduction methods
  • SNCR non-selective catalytic reduction method
  • the content of nitrogen oxides (NO x ) in the exhaust gas after the first removal of nitrogen oxides in the exhaust gas does not reach the standard, and can be achieved after the first removal of nitrogen oxides in the exhaust gas or after a mixed reaction with ozone The latest standards.
  • the first removal of nitrogen oxides in the exhaust gas is at least one selected from a non-catalytic reduction method, a selective catalytic reduction method, a non-selective catalytic reduction method, an electron beam denitration method, etc. Species.
  • An embodiment of the present invention provides an electrocoagulation device, including: an electrocoagulation flow channel, a first electrode located in the electrocoagulation flow channel, and a second electrode.
  • an electrocoagulation device including: an electrocoagulation flow channel, a first electrode located in the electrocoagulation flow channel, and a second electrode.
  • the first electrode of the electrocoagulation device may be one of a solid, a liquid, a gas molecular group, a plasma, a conductive mixed state substance, a biological natural mixed conductive substance, or an object artificially processed to form a conductive substance Or a combination of multiple forms.
  • the first electrode may use solid metal, such as 304 steel, or other solid conductor, such as graphite, etc .; when the first electrode is liquid, the first electrode may be an ion-containing conductive liquid.
  • the shape of the first electrode may be dot-shaped, wire-shaped, mesh-shaped, orifice-shaped, plate-shaped, needle-rod-shaped, ball-cage-shaped, box-shaped, tubular, natural form substance, or processed form substance Wait.
  • the first electrode may have a plate shape, a ball cage shape, a box shape or a tube shape
  • the first electrode may have a non-porous structure or a porous structure.
  • one or more front through holes may be provided on the first electrode.
  • the shape of the front through hole may be a polygon, a circle, an ellipse, a square, a rectangle, a trapezoid, or a diamond.
  • the aperture size of the front through hole may be 10-100 mm, 10-20 mm, 20-30 mm, 30-40 mm, 40-50 mm, 50-60 mm, 60-70 mm, 70-80 mm, 80-90 mm , Or 90 ⁇ 100mm.
  • the first electrode may have other shapes.
  • the shape of the second electrode of the electrocoagulation device may be a multi-layer mesh, mesh, orifice plate, tube, barrel, ball cage, box, plate, particle accumulation layer, Bend a plate or panel.
  • the second electrode may also have a non-porous structure or a porous structure.
  • the second electrode has a hole structure, one or more rear through holes may be provided on the second electrode.
  • the shape of the rear through hole may be polygon, circle, ellipse, square, rectangle, trapezoid, or rhombus.
  • the diameter of the rear through hole may be 10-100 mm, 10-20 mm, 20-30 mm, 30-40 mm, 40-50 mm, 50-60 mm, 60-70 mm, 70-80 mm, 80-90 mm, or 90-100 mm.
  • the second electrode of the electrocoagulation device is made of a conductive substance.
  • the surface of the second electrode has a conductive substance.
  • the electrocoagulation electric field may be a point-surface electric field, a line-surface electric field, a mesh surface electric field, a point barrel electric field, a line barrel electric field , Or a combination of one or more electric fields in the electric field of the net bucket.
  • the first electrode is needle-shaped or linear, the second electrode is planar, and the first electrode is perpendicular or parallel to the second electrode, thereby forming a linear electric field; or the first electrode is mesh-shaped, and the second electrode is planar
  • the first electrode is parallel to the second electrode to form a mesh electric field; or the first electrode is dot-shaped and fixed by a wire or a metal needle, the second electrode is barrel-shaped, and the first electrode is located on the second electrode At the center of geometric symmetry, thereby forming a point barrel electric field; or the first electrode is linear and fixed by a wire or a metal needle, the second electrode is barrel-shaped, and the first electrode is located on the geometric symmetry axis of the second electrode, thereby A wire barrel electric field is formed; or the first electrode is mesh-shaped and fixed by a wire or a metal needle, the second electrode is barrel-shaped, and the first electrode is located at the geometrically symmetric center of the second electrode, thereby forming a mesh-barrel electric field.
  • the second electrode When the second electrode is planar, it may be flat, curved, or spherical.
  • the first electrode When the first electrode is linear, it may be linear, curvilinear, or circular.
  • the first electrode may be arc-shaped.
  • the first electrode When the first electrode is mesh-shaped, it may be flat, spherical or other geometric plane, rectangular, or irregular shape.
  • the first electrode may also be in a dot shape, and may be a real point with a small diameter, a small ball, or a mesh ball.
  • the second electrode When the second electrode has a barrel shape, the second electrode can further evolve into various box shapes.
  • the first electrode can also be changed accordingly to form an electrode and electrocoagulation electric field layer.
  • the first electrode of the electrocoagulation device is linear, and the second electrode is planar. In an embodiment of the invention, the first electrode is perpendicular to the second electrode. In an embodiment of the invention, the first electrode and the second electrode are parallel. In an embodiment of the present invention, both the first electrode and the second electrode are planar, and the first electrode and the second electrode are parallel. In an embodiment of the invention, the first electrode uses a wire mesh. In an embodiment of the invention, the first electrode is planar or spherical. In an embodiment of the invention, the second electrode is curved or spherical. In an embodiment of the present invention, the first electrode is dot-shaped, linear, or mesh-shaped, the second electrode is barrel-shaped, the first electrode is located inside the second electrode, and the first electrode is located on the central axis of symmetry of the second electrode on.
  • the first electrode of the electrocoagulation device is electrically connected to one electrode of the power supply; the second electrode is electrically connected to the other electrode of the power supply.
  • the first electrode is electrically connected to the cathode of the power supply, and the second electrode is electrically connected to the anode of the power supply.
  • the first electrode of the electrocoagulation device may have a positive potential or a negative potential; when the first electrode has a positive potential, the second electrode has a negative potential; when the first electrode has a negative potential, the first The two electrodes have a positive potential, and both the first electrode and the second electrode are electrically connected to the power supply, specifically, the first electrode and the second electrode may be electrically connected to the positive and negative electrodes of the power supply, respectively.
  • the voltage of this power supply is called the power-on driving voltage, and the choice of the power-on driving voltage depends on the ambient temperature, the medium temperature, and so on.
  • the power-on driving voltage range of the power supply can be 5-50KV, 10-50KV, 5-10KV, 10-20KV, 20-30KV, 30-40KV, or 40-50KV, from bioelectricity to space haze treatment power .
  • the power supply may be a DC power supply or an AC power supply, and the waveform of the power-up driving voltage may be a DC waveform, a sine wave, or a modulated waveform.
  • DC power supply is used as the basic application of adsorption; sine wave is used as mobile.
  • sine wave's electrified driving voltage acts between the first electrode and the second electrode. The generated coagulation electric field will drive the charged particles in the coagulation electric field.
  • the droplets move toward the second electrode; the ramp wave is used as a pull, and the waveform needs to be modulated according to the pulling force.
  • the edges of both ends of the asymmetric electrocoagulation electric field have obvious directionality to the pulling force generated by the medium in it.
  • the medium in the driving electrocoagulation electric field moves in this direction.
  • the frequency conversion pulse range can be 0.1Hz ⁇ 5GHz, 0.1Hz ⁇ 1Hz, 0.5Hz ⁇ 10Hz, 5Hz ⁇ 100Hz, 50Hz ⁇ 1KHz, 1KHz ⁇ 100KHz, 50KHz ⁇ 1MHz, 1MHz ⁇ 100MHz, 50MHz ⁇ 1GHz, 500MHz ⁇ 2GHz, or 1GHz ⁇ 5GHz, suitable for the adsorption of organisms to pollutant particles.
  • the first electrode can be used as a wire, and when in contact with the nitric acid-containing water mist, positive and negative electrons are directly introduced into the nitric acid-containing water mist. At this time, the nitric acid-containing water mist itself can be used as an electrode.
  • the first electrode can transfer electrons to the water mist or electrode containing nitric acid by means of energy fluctuation, so that the first electrode can not be contacted with the water mist containing nitric acid.
  • the transmission between the mists causes more mist droplets to be charged, and finally reaches the second electrode, thereby forming a current, which is also called a power-on driving current.
  • the magnitude of the power-on drive current is related to the ambient temperature, medium temperature, electron quantity, adsorbed substance mass, and escape quantity. For example, as the amount of electrons increases, movable particles, such as fog droplets, increase the current formed by the moving charged particles. The more charged substances, such as mist droplets, are adsorbed per unit time, the greater the current. The escaped droplets are only charged, but do not reach the second electrode, which means that no effective electrical neutralization is formed, so that under the same conditions, the more the droplets escape, the smaller the current.
  • the two electrodes are attracted, resulting in escape, but because its escape occurs after electrical neutralization, and possibly after repeated electrical neutralization multiple times, the electron conduction speed is increased accordingly, and the current is increased accordingly.
  • the power-on driving voltage needs to be increased.
  • the limit of the power-on driving voltage is to achieve the effect of air breakdown.
  • the influence of medium temperature is basically equivalent to the influence of ambient temperature. The lower the temperature of the medium, the smaller the energy required to excite the medium, such as mist droplets, and the smaller the kinetic energy it has.
  • the electrocoagulation device Under the action of the same electrocoagulation electric field force, it is easier to be adsorbed on the second electrode, thereby forming Has a higher current.
  • the electrocoagulation device has better adsorption effect on cold nitric acid-containing water mist. As the concentration of the medium, such as mist droplets, increases, the more likely the charged medium has electron transfer with other medium before colliding with the second electrode, the greater the chance of effective electrical neutralization, and the resulting current Correspondingly, it will be larger; so the higher the concentration of the medium, the greater the current formed.
  • the relationship between power-on driving voltage and medium temperature is basically the same as the relationship between power-on driving voltage and ambient temperature.
  • the power-up driving voltage of the power source connected to the first electrode and the second electrode may be less than the initial halo voltage.
  • the initial halo voltage is the minimum voltage value that can cause a discharge between the first electrode and the second electrode and ionize the gas.
  • the initial halo voltage may be different.
  • the power-on driving voltage of the power supply may specifically be 0.1-2 kV / mm. The power-on driving voltage of the power supply is lower than the air corona starting voltage.
  • both the first electrode and the second electrode extend in the left-right direction, and the left end of the first electrode is located to the left of the left end of the second electrode.
  • the first electrode is located between the two second electrodes.
  • the distance between the first electrode and the second electrode of the electrocoagulation device can be set according to the magnitude of the power-on driving voltage between them, the flow velocity of the water mist, and the charging ability of the water mist containing nitric acid.
  • the distance between the first electrode and the second electrode may be 5-50 mm, 5-10 mm, 10-20 mm, 20-30 mm, 30-40 mm, or 40-50 mm.
  • the larger the distance between the first electrode and the second electrode the higher the power-up driving voltage required to form a sufficiently strong electrocoagulation electric field, which is used to drive the charged medium to quickly move to the second electrode to prevent the medium from escaping.
  • the power-on driving voltage is constant, as the distance increases, the strength of the electrocoagulation electric field continues to decrease, and the ability of the medium to charge in the electrocoagulation electric field becomes weaker.
  • the first electrode and the second electrode of the electrocoagulation device constitute an adsorption unit.
  • the distribution form of all adsorption units can be flexibly adjusted as needed; all adsorption units can be the same or different.
  • all adsorption units can be distributed in one or more directions of the left-right direction, the front-rear direction, the oblique direction or the spiral direction to meet the requirements of different air volumes. All adsorption units can be distributed in a rectangular array or a pyramid.
  • the above-mentioned first and second electrodes of various shapes can be freely combined to form an adsorption unit.
  • the linear first electrode is inserted into the tubular second electrode to form an adsorption unit, and then combined with the linear first electrode to form a new adsorption unit.
  • the two linear first electrodes can be electrically connected; the new The adsorption units are distributed in one or more directions of the left-right direction, the up-down direction, the oblique direction or the spiral direction.
  • the linear first electrode is inserted into the tubular second electrode to form an adsorption unit, and the adsorption unit is distributed in one or more directions of the left-right direction, the up-down direction, the oblique direction, or the spiral direction to form a new adsorption unit
  • the new adsorption unit is then combined with the first electrodes of various shapes described above to form a new adsorption unit.
  • the distance between the first electrode and the second electrode in the adsorption unit can be arbitrarily adjusted to suit the requirements of different operating voltages and adsorption objects.
  • Different adsorption units can be combined. Different adsorption units can use the same power supply or different power supplies. When different power supplies are used, the power-on driving voltage of each power supply may be the same or different.
  • there may be a plurality of electrocoagulation devices and all electrocoagulation devices may be distributed in one or more directions of the left-right direction, the up-down direction, the spiral direction, or the oblique direction.
  • the electrocoagulation device further includes an electrocoagulation housing.
  • the electrocoagulation housing includes an electrocoagulation inlet, an electrocoagulation outlet, and an electrocoagulation flow channel.
  • the condensate outlet is connected.
  • the electrocoagulation inlet is circular, and the diameter of the electrocoagulation inlet is 300-1000 mm, or 500 mm.
  • the electrocoagulation outlet is circular, and the diameter of the electrocoagulation outlet is 300-1000 mm, or 500 mm.
  • the electrocoagulation housing includes a first housing portion, a second housing portion, and a third housing portion that are sequentially distributed from the electrocoagulation inlet to the electrocoagulation outlet.
  • the electrocoagulation inlet is located in the first housing At one end of the body portion, the electrocoagulation outlet is located at one end of the third housing portion.
  • the outline size of the first housing portion gradually increases from the electrocoagulation inlet to the electrocoagulation outlet.
  • the first housing portion has a straight tubular shape.
  • the second housing portion has a straight tube shape, and the first electrode and the second electrode are installed in the second housing portion.
  • the outline size of the third housing portion gradually decreases from the electrocoagulation inlet to the electrocoagulation outlet.
  • the cross sections of the first housing portion, the second housing portion, and the third housing portion are all rectangular.
  • the material of the electrocoagulation shell is stainless steel, aluminum alloy, iron alloy, cloth, sponge, molecular sieve, activated carbon, foamed iron, or foamed silicon carbide.
  • the first electrode is connected to the electrocoagulation housing through an electrocoagulation insulator.
  • the material of the electrocoagulation insulating member is insulating mica.
  • the electrocoagulation insulating member has a column shape or a tower shape.
  • a cylindrical front connection portion is provided on the first electrode, and the front connection portion is fixedly connected to the electrocoagulation insulating member.
  • the second electrode is provided with a cylindrical rear connection portion, and the rear connection portion is fixedly connected to the electrocoagulation insulating member.
  • the first electrode is located in the electrocoagulation channel.
  • the ratio of the cross-sectional area of the first electrode to the cross-sectional area of the electrocoagulation channel is 99% to 10%, or 90 to 10%, or 80 to 20%, or 70 to 30%, or 60 to 40%, or 50%.
  • the cross-sectional area of the first electrode refers to the sum of the areas of the first electrode along the solid part of the cross-section.
  • the nitric acid-containing water mist During the collection of nitric acid-containing water mist, the nitric acid-containing water mist enters the electrocoagulation shell from the electrocoagulation inlet and moves toward the electrocoagulation outlet; during the movement of the nitric acid-containing water mist toward the electrocoagulation outlet, the nitric acid-containing water mist The water mist will pass through the first electrode and be charged; the second electrode will attract the charged nitric acid-containing water mist to collect the nitric acid-containing water mist on the second electrode.
  • the invention uses the electrocoagulation shell to guide the exhaust gas and the water mist containing nitric acid to flow through the first electrode, so as to charge the water mist of nitric acid with the first electrode, and collect the water mist of nitric acid with the second electrode, thereby effectively reducing the electricity A mist of nitric acid flowing out of the condensation outlet.
  • the material of the electrocoagulation shell may be metal, non-metal, conductor, non-conductor, water, various conductive liquids, various porous materials, or various foam materials.
  • the material of the electrocoagulation shell is metal, the material may be stainless steel, aluminum alloy, or the like.
  • the material of the electrocoagulation shell When the material of the electrocoagulation shell is non-metal, the material may specifically be cloth, sponge, or the like. When the material of the electrocoagulation casing is a conductor, the material may specifically be an iron alloy or the like. When the material of the electrocoagulation shell is a non-conductor, a water layer is formed on the surface and the water becomes an electrode, such as a sand layer after absorbing water. When the material of the electrocoagulation shell is water and various conductive liquids, the electrocoagulation shell is still or flowing. When the material of the electrocoagulation shell is various porous materials, the material may specifically be molecular sieve or activated carbon.
  • the material of the electrocoagulation shell is various types of foam materials, the material may specifically be foam iron, foam silicon carbide, or the like.
  • the first electrode is fixedly connected to the coagulation housing through an coagulation insulation member.
  • the material of the coagulation insulation member may be insulating mica.
  • the second electrode is directly electrically connected to the electrocoagulation housing. This connection mode allows the electrocoagulation housing to have the same potential as the second electrode, so that the electrocoagulation housing can also absorb charged
  • the water mist of nitric acid and the electrocoagulation casing also constitute a second electrode.
  • the electrocoagulation flow channel is provided in the electrocoagulation case, and the first electrode is installed in the electrocoagulation flow channel.
  • the second electrode may extend in the up and down direction, so that when the condensation accumulated on the second electrode reaches a certain weight, it will flow downward along the second electrode under the influence of gravity and finally gather in the device In a fixed position or device, the nitric acid solution attached to the second electrode can be recovered.
  • the electrocoagulation device can be used for refrigeration and defogging.
  • the substance adhering to the second electrode may be collected by applying an electrocoagulation electric field.
  • the material collection direction on the second electrode may be the same as the air flow, or may be different from the air flow direction.
  • the current existing electrostatic field charging theory is to use corona discharge to ionize oxygen to generate a large amount of negative oxygen ions.
  • the negative oxygen ions are in contact with the dust.
  • the dust is charged, and the charged dust is adsorbed by the heteropolar.
  • the existing electric field adsorption has little effect.
  • the low specific resistance substance is easy to lose electricity after being charged, when the moving negative oxygen ions charge the low specific resistance substance, the low specific resistance substance will quickly lose power, and the negative oxygen ion only moves once, resulting in It is difficult to recharge low-resistance substances such as nitric acid-containing water mist after being de-energized, or this charging method greatly reduces the probability of low-specific resistance substances being charged, making the entire low-specific resistance substance in an uncharged state, so that it is difficult for different poles to The low specific resistance substance continues to apply the adsorption force, which ultimately results in the extremely low adsorption efficiency of the existing electric field on the low specific resistance substance such as nitric acid-containing water mist.
  • the above-mentioned electrocoagulation device and electrocoagulation method do not use the charging method to charge the water mist, but directly transfer the electrons to the water mist containing nitric acid to make them charged. After a certain droplet is charged and loses power, the new electron will It is quickly transferred from the first electrode and through other droplets to the de-energized droplets, so that the droplets can be quickly recharged after being de-energized, greatly increasing the probability of the droplets being charged, such as repeated, so that the droplets are in the whole
  • the second electrode can continue to apply attraction force to the mist droplets until the mist droplets are adsorbed, thereby ensuring that the electrocoagulation device has a higher collection efficiency for nitric acid-containing water mist.
  • the above method for charging mist droplets adopted by the present invention does not require the use of corona wires, corona poles, or corona plates, etc., which simplifies the overall structure of the electrocoagulation device and reduces the manufacturing cost of the electrocoagulation device.
  • the present invention adopts the above-mentioned power-on method, so that a large amount of electrons on the first electrode will be transferred to the second electrode through the mist droplets, and a current is formed.
  • the electrocoagulation device When the concentration of the water mist flowing through the electrocoagulation device is greater, the electrons on the first electrode are more easily transferred to the second electrode through the water mist containing nitric acid, and more electrons will be transferred between the droplets, making the first The current formed between the electrode and the second electrode is greater, and makes the mist droplets more likely to be charged, and makes the electrocoagulation device more efficient in collecting water mist.
  • An embodiment of the present invention provides an electrocoagulation defogging method, which includes the following steps:
  • the first electrode charges the water mist in the gas
  • the second electrode applies an attractive force to the charged water mist, so that the water mist moves toward the second electrode until the water mist adheres to On the second electrode.
  • the first electrode introduces electrons into the water mist, and the electrons are transferred between the mist droplets between the first electrode and the second electrode, so that more mist droplets are charged.
  • electrons are conducted between the first electrode and the second electrode through water mist, and an electric current is formed.
  • the first electrode charges the water mist by contact with the water mist.
  • the first electrode charges the water mist by means of energy fluctuation.
  • the water mist attached to the second electrode forms water droplets, and the water droplets on the second electrode flow into the collection tank.
  • the water droplets on the second electrode flow into the collection tank under the action of gravity.
  • the blowing water droplets flow into the collection tank.
  • the gas with nitric acid mist flows through the first electrode; when the gas with nitric acid mist flows through the first electrode, the first electrode charges the nitric acid mist in the gas, and the second electrode gives the charged nitric acid The mist exerts an attractive force to move the nitric acid mist toward the second electrode until the nitric acid mist adheres to the second electrode.
  • the first electrode introduces electrons into the nitric acid mist, and the electrons are transferred between the mist droplets between the first electrode and the second electrode, so that more mist droplets are charged.
  • a nitric acid mist conducts electrons between the first electrode and the second electrode and forms a current.
  • the first electrode charges the nitric acid mist by contact with the nitric acid mist.
  • the first electrode charges the nitric acid mist by means of energy fluctuation.
  • the nitric acid mist attached to the second electrode forms water droplets, and the water droplets on the second electrode flow into the collection tank.
  • the water droplets on the second electrode flow into the collection tank under the action of gravity.
  • the blowing water droplets flow into the collection tank.
  • the exhaust gas treatment system can be applied in the fields of environmental protection, chemical industry, and air pollution control, especially in the field of combustion flue gas treatment.
  • the present exhaust gas treatment system can be applied to the treatment of exhaust gas from power stations.
  • the exhaust dust removal system includes a water removal device 207 and an electric field device.
  • the electric field device includes a dust removal electric field anode 10211 and a dust removal electric field cathode 10212.
  • the dust removal electric field anode 10211 and the dust removal electric field cathode 10212 are used to generate an ionization dust removal electric field.
  • the water removal device 207 is used to remove liquid water before the entrance of the electric field device. When the temperature of the exhaust gas is lower than 100 ° C, the water removal device removes the liquid water in the exhaust gas.
  • the water removal device 207 is electrocoagulation For the device, the direction of the arrow in the figure is the direction of exhaust gas flow.
  • a method for exhaust dust removal includes the following steps: when the temperature of the exhaust gas is lower than 100 ° C, the liquid water in the exhaust gas is removed, and then the ionized dust is removed, in which the liquid water in the exhaust gas is removed by the electrocoagulation defogging method.
  • the exhaust gas is the exhaust gas during the cold start of the gasoline exhaust equipment, which reduces the water droplets in the exhaust gas, that is, the liquid water, reduces the uneven discharge of the ionization and dust removal electric field and the breakdown of the cathode of the dust removal electric field and the anode of the dust removal electric field, and improves the efficiency of ionization and dust removal.
  • the ionization dust removal efficiency is 99.9% or more, and the ionization dust removal efficiency of the dust removal method that does not remove the liquid water in the exhaust gas is 70% or less. Therefore, when the temperature of the exhaust gas is lower than 100 °C, remove the liquid water in the exhaust gas, and then ionize the dust, reduce the water droplets in the exhaust gas, that is, liquid water, reduce the uneven discharge of the ionization and dust removal electric field, and the cathode and anode of the dust removal electric field Breakdown, improve ionization dust removal efficiency.
  • the exhaust dust removal system includes an oxygen supplement device 208 and an electric field device.
  • the electric field device includes a dust removal electric field anode 10211 and a dust removal electric field cathode 10212.
  • the dust removal electric field anode 10211 and the dust removal electric field cathode 10212 are used to generate an ionization dust removal electric field.
  • the oxygen supplementing device 208 is used to add gas including oxygen before the ionization and dedusting electric field.
  • the oxygen supplementing device 208 adds oxygen by passing in external air, and determines the oxygen supplementing amount according to the content of exhaust particles.
  • the direction of the arrow in the figure is the flow direction of the oxygen supplementing device including oxygen.
  • An exhaust dust removal method includes the following steps: adding a gas including oxygen before the ionization dust removal electric field, performing ionization dust removal, adding oxygen by passing in outside air, and determining the amount of oxygen supplement according to the content of exhaust particles.
  • the exhaust dust removal system of the present invention includes an oxygen supplement device, which can add oxygen by simply adding oxygen, passing in outside air, passing in compressed air, and / or passing in ozone to increase the oxygen content of the exhaust gas entering the ionization and dust removal electric field.
  • the ionized oxygen is increased, so that more dust in the exhaust gas is charged, which in turn will charge more under the action of the anode of the dust-removing electric field
  • the collection of electric dust makes the dust removal efficiency of the electric field device higher, which is conducive to the collection of exhaust particulates in the ionization and dust removal electric field, and can also play a role in cooling, increasing the efficiency of the power system, and supplementing oxygen will also increase the ozone of the ionization and dust removal electric field.
  • the content is conducive to improving the efficiency of purification, self-cleaning, denitration and other treatment of organic matter in the exhaust gas by the ionization dust removal electric field.
  • the exhaust gas treatment system in this embodiment further includes an exhaust gas treatment device, which is used to treat exhaust gas to be discharged into the atmosphere.
  • FIG. 7 is a schematic structural diagram of an exhaust gas treatment device in an embodiment.
  • the exhaust gas treatment device 102 includes an electric field device 1021, an insulation mechanism 1022, an air distribution device, a water filtering mechanism, and an exhaust ozone mechanism.
  • the water filtering mechanism in the present invention is optional, that is, the exhaust gas dedusting system provided by the present invention may or may not include a water filtering mechanism.
  • the electric field device 1021 includes a dedusting electric field anode 10211 and a dedusting electric field cathode 10212 provided in the dedusting electric field anode 10211.
  • An asymmetric electrostatic field is formed between the dedusting electric field anode 10211 and the dedusting electric field cathode 10212.
  • the cathode 10212 of the dust removal electric field discharges, ionizes the gas, so that the particulate matter obtains a negative charge, moves toward the anode 10211 of the dust removal electric field, and deposits on the dust removal
  • the electric field is on the cathode 10212.
  • the interior of the dedusting electric field cathode 10212 is composed of a honeycomb-shaped and hollow anode tube bundle group, and the shape of the anode tube bundle port is a hexagon.
  • the dust-removing electric field cathode 10212 includes a plurality of electrode rods, one for each anode tube bundle in the anode tube bundle group corresponding to each other, wherein the electrode rods are shaped like needles, polygons, burrs, and threads Rod-shaped or columnar.
  • the inlet end of the dust removal electric field cathode 10212 is lower than the inlet end of the dust removal electric field anode 10211, and the outlet end of the dust removal electric field cathode 10212 is the same as the outlet end of the dust removal electric field anode 10211 Level, so that an acceleration electric field is formed inside the electric field device 1021.
  • the insulation mechanism 1022 overhanging the airway includes an insulation portion and a heat insulation portion.
  • the material of the insulating part is a ceramic material or a glass material.
  • the insulation part is an umbrella-shaped string ceramic column, and the umbrella is glazed inside and outside. Please refer to FIG. 8, which shows a schematic structural diagram of an umbrella-shaped insulating mechanism in one embodiment.
  • the dust-removing electric field cathode is mounted on an exhaust cathode support plate 10213, and the exhaust-cathode supporting plate 10213 and the dust-removing electric field anode 10211 are connected by an insulating mechanism 1022.
  • the dust-removing electric field anode 10211 includes a first anode portion 102112 and a second anode portion 102111, that is, the first anode portion 102112 is near the entrance of the electric field device, and the second anode portion 102111 is near the exit of the electric field device.
  • the exhaust cathode support plate 10213 and the insulation mechanism 1022 are between the first anode portion 102112 and the second anode portion 102111, that is, the insulation mechanism 1022 is installed in the middle of the exhaust ionization electric field or the dust removal electric field cathode 10212, and the dust removal electric field cathode 10212 It plays a good supporting role and fixes the dedusting electric field cathode 10212 relative to the dedusting electric field anode 10211, so that the dedusting electric field cathode 10212 and the dedusting electric field anode 10211 maintain a set distance.
  • the wind equalizing device 1023 is disposed at the intake end of the electric field device 1021. Please refer to FIG. 9A, FIG. 9B and FIG. 9C, which are structural diagrams of three implementations of the air equalizing device.
  • the air-equalizing device 1023 when the anode of the dust removal field 10211 is cylindrical, the air-equalizing device 1023 is located at the air inlet and is composed of a number of air-equating blades 10231 rotating around the center of the air inlet .
  • the air-equalizing device 1023 can make the intake air amount of the exhaust discharge device changing at various rotation speeds evenly pass through the electric field generated by the anode of the dust removal electric field.
  • the internal temperature of the anode of the dust removal electric field can be kept constant, and the oxygen is sufficient.
  • the wind equalizing device includes:
  • An air inlet pipe 10232 located on one side of the anode of the dedusting electric field.
  • An air outlet pipe 10233 provided on the other side of the anode of the dust removal electric field; wherein the side where the air inlet pipe 10232 is installed is opposite to the other side where the air outlet pipe 10233 is installed.
  • the air-equalizing device may further include a second venturi plate air-equalizing mechanism 10234 provided at the intake end of the anode of the dust removal electric field and a third venturi plate provided at the air outlet end of the anode of the dust removal electric field
  • a wind-sharing mechanism 10235 (the third venturi plate wind-shaping mechanism is folded in a plan view), the third venturi plate wind-shaping mechanism is provided with an air inlet, and the third venturi plate wind-shaping mechanism is provided with Air outlet holes, the air inlet holes and the air outlet holes are arranged in a staggered arrangement, and the front air inlet and side air outlets form a cyclone structure.
  • the exhaust water filtering mechanism provided in the electric field device 1021 includes a conductive mesh plate as a first electrode, and the conductive mesh plate is used to conduct electrons to water (low specific resistance substance) after power-on.
  • the second electrode for adsorbing charged water is the dust removal electric field anode 10211 of the electric field device.
  • the first electrode of the water filtering mechanism is arranged at the air inlet, and the first electrode is a conductive mesh plate with a negative potential.
  • the second electrode of this embodiment is provided in the air intake device in a net shape, and the second electrode has a positive electric potential.
  • the second electrode is also called a collector.
  • the second electrode is specifically planar and the first electrode is parallel to the second electrode.
  • a mesh electric field is formed between the first electrode and the second electrode.
  • the first electrode is a mesh structure made of wire, and the first electrode is composed of a wire mesh. In this embodiment, the area of the second electrode is larger than the area of the first electrode.
  • An exhaust ozone purification system as shown in Figure 10, includes:
  • the ozone source 201 is used to provide an ozone stream, which is generated instantly by an ozone generator.
  • the reaction field 202 is used for mixing and reacting the ozone stream and the exhaust stream.
  • a denitration device 203 is used to remove nitric acid from the mixed reaction product of the ozone stream and the exhaust stream; the denitration device 203 includes an electrocoagulation device 2031 for electrocoagulation of the ozone-treated exhaust gas, containing nitric acid Water mist accumulates on the second electrode in the electrocoagulation device.
  • the denitration device 203 further includes a denitration liquid collection unit 2032 for storing the nitric acid aqueous solution and / or nitrate aqueous solution removed in the exhaust gas; when the denitration liquid collection unit stores a nitric acid aqueous solution, the denitration liquid collection unit There is a lye addition unit for forming nitrate with nitric acid.
  • the ozone digester 204 is used to digest ozone in the exhaust gas treated by the reaction field.
  • the ozone digester can perform ozone digestion by means of ultraviolet rays and catalysis.
  • the reaction field 202 is the second reactor. As shown in FIG. 11, a plurality of honeycomb-shaped cavities 2021 are provided for providing a space where exhaust gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities 2022, used to introduce cold medium to control the reaction temperature of exhaust gas and ozone.
  • the right arrow in the figure is the refrigerant inlet, and the left arrow is the refrigerant outlet.
  • the electrocoagulation device includes:
  • the first electrode 301 can conduct electrons to nitric acid-containing water mist (low specific resistance substance); when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged mist containing nitric acid.
  • the electrocoagulation device in this embodiment further includes a housing 303 having an inlet 3031 and an outlet 3032, and both the first electrode 301 and the second electrode 302 are installed in the housing 303.
  • the first electrode 301 is fixed to the inner wall of the housing 303 through the insulating member 304, and the second electrode 302 is directly fixed to the housing 303.
  • the insulating member 304 has a column shape, which is also called an insulating column.
  • the first electrode 301 has a negative potential
  • the second electrode 302 has a positive potential.
  • the casing 303 and the second electrode 302 have the same electric potential, and the casing 303 also has an adsorption effect on the charged substance.
  • the electrocoagulation device in this embodiment is used to treat industrial exhaust gas containing acid mist.
  • the inlet 3031 communicates with the port that discharges industrial exhaust.
  • the working principle of the electrocoagulation device in this embodiment is as follows: the industrial exhaust gas flows into the housing 303 from the inlet 3031 and flows out through the outlet 3032; in this process, the industrial exhaust gas will first flow through one of the first electrodes 301, when the industrial exhaust When the acid mist in the gas contacts the first electrode 301, or when the distance from the first electrode 301 reaches a certain value, the first electrode 301 transfers electrons to the acid mist, part of the acid mist is charged, and the second electrode 302 is charged The acid mist exerts an attractive force, and the acid mist moves toward the second electrode 302 and attaches to the second electrode 302; another part of the acid mist is not adsorbed on the second electrode 302, and the acid mist continues to flow toward the outlet 3032 , When the part of the acid mist is in contact with another first electrode 301,
  • the exhaust ozone purification system in Embodiment 4 further includes an ozone amount control device 209 for controlling the ozone amount so as to effectively oxidize the gas component to be treated in the exhaust gas
  • the ozone amount control device 209 includes a control Unit 2091.
  • the ozone quantity control device 209 further includes an exhaust component detection unit 2092 before ozone treatment, configured to detect the exhaust component content before ozone treatment.
  • the control unit controls the amount of ozone required for the mixed reaction according to the content of exhaust components before the ozone treatment.
  • the exhaust gas component detection unit before ozone treatment is selected from at least one of the following detection units:
  • the first volatile organic compound detection unit 20921 is used to detect the content of volatile organic compounds in the exhaust gas before ozone treatment, such as volatile organic compound sensors;
  • the first CO detection unit 20922 is used to detect the CO content in the exhaust gas before ozone treatment, such as a CO sensor;
  • the first nitrogen oxide detection unit 20923 is used to detect the nitrogen oxide content in the exhaust gas before ozone treatment, such as a nitrogen oxide (NO x ) sensor.
  • a nitrogen oxide (NO x ) sensor such as a nitrogen oxide (NO x ) sensor.
  • the control unit controls the amount of ozone required for the mixed reaction according to the output value of at least one of the exhaust component detection units before ozone treatment.
  • the control unit is used to control the amount of ozone required for the mixed reaction according to the theoretical estimated value.
  • the theoretical estimated value is: the molar ratio of ozone flux to the object to be treated in the exhaust gas is 2-10.
  • the ozone quantity control device includes an exhaust component detection unit 2093 after ozone treatment, which is used to detect the exhaust component content after ozone treatment.
  • the control unit controls the amount of ozone required for the mixed reaction according to the content of exhaust components after the ozone treatment.
  • the exhaust gas component detection unit after ozone treatment is selected from at least one of the following detection units:
  • the first ozone detection unit 20931 is used to detect the ozone content in the exhaust gas after ozone treatment
  • the second volatile organic compound detection unit 20932 is used to detect the content of volatile organic compounds in the exhaust gas after ozone treatment
  • the second CO detection unit 20933 is used to detect the CO content in the exhaust gas after ozone treatment
  • the second nitrogen oxide detection unit 20934 is used to detect the nitrogen oxide content in the exhaust gas after ozone treatment.
  • the control unit controls the amount of ozone according to at least one output value of the ozone-treated exhaust component detection unit.
  • the catalyst (including the coating layer and the active component) is coated on one side of the barrier medium layer. After the catalyst is coated, the catalyst is 12% of the mass of the barrier medium layer.
  • the catalyst includes the following components in weight percentages: The active component is 12wt%, and the coating is 88wt%, wherein the active component is cerium oxide and zirconia (the amount of substances in sequence is 1: 1.3), and the coating is gama alumina;
  • a copper foil is attached to the other side of the catalyst-coated barrier medium layer to form an electrode.
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 160g / hour. Under the experimental conditions, the power loss is 830W.
  • the catalyst (including the coating layer and the active component) is coated on one side of the barrier medium layer. After the catalyst is coated, the catalyst is 5% of the mass of the barrier medium layer.
  • the catalyst includes the following components in weight percentages: The active component accounts for 15wt% of the total weight of the catalyst, and the coating is 85%, wherein the active components are MnO and CuO, and the coating is gama alumina;
  • a copper foil is attached to the other side of the catalyst-coated barrier medium layer to form an electrode.
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 168g / hour. Under the experimental conditions, the power loss is 830W.
  • a quartz glass plate with a length of 300mm, a width of 30mm, and a thickness of 1.5mm is used as the barrier medium layer;
  • the catalyst (including the coating layer and the active component) is coated on one side of the barrier medium layer. After the catalyst is coated, the catalyst is 1% of the mass of the barrier medium layer.
  • the catalyst includes the following components in weight percentages: The active component is 5 wt%, and the coating is 95 wt%, wherein the active components are silver, rhodium, platinum, cobalt and lanthanum (the amount of substances in turn is 1: 1: 1: 1: 1.5), the The coating is zirconia;
  • a copper foil is attached to the other side of the catalyst-coated barrier medium layer to form an electrode.
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 140g / hour. Under the experimental conditions, the power loss is 830W.
  • the catalyst (including the coating and the active component) is coated on one side of the copper foil (electrode). After the catalyst is coated, the thickness of the catalyst is 1.5 mm, and the catalyst includes the following components in weight percent: active component 8wt%, the coating is 92wt%, wherein the active components are zinc sulfate, calcium sulfate, titanium sulfate and magnesium sulfate (the amount of substances in order is 1: 2: 1: 1), the coating is Graphene.
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 165g / hour. Under the experimental conditions, the power loss is 830W.
  • the catalyst (including the coating layer and the active component) is coated on one side of the copper foil (electrode). After the catalyst is coated, the thickness of the catalyst is 3 mm.
  • the catalyst includes the following components in weight percentage: the active component is 10wt%, the coating is 90wt%, wherein the active components are praseodymium oxide, samarium oxide, and yttrium oxide (the amount of substances in sequence is 1: 1: 1), and the coating is cerium oxide and manganese oxide ( The quantity ratio of the substances in turn is 1: 1).
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 155g / hour. Under the experimental conditions, the power loss is 830W.
  • the catalyst (including the coating layer and the active component) is coated on one side of the copper foil (electrode). After the catalyst is coated, the thickness of the catalyst is 1 mm.
  • the catalyst includes the following components in weight percentage: the active component is 14wt%, the coating is 86wt%, wherein the active components are strontium sulfide, nickel sulfide, tin sulfide and iron sulfide (the amount of substances in sequence is 2: 1: 1: 1: 1), the coating is silicon Algae soil, the porosity is 80%, the specific surface area is 350 square meters / gram, and the average pore diameter is 30 nanometers.
  • the catalyst coating method is as follows:
  • XF-B-3-100 type original ozone generation amount is 120g / hour; after electrode replacement, under the same test conditions, ozone generation amount is 155g / hour. Under the experimental conditions, the power loss is 830W.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field in this embodiment is a hollow regular hexagonal tube
  • the cathode 4052 of the dust removal electric field is rod-shaped
  • the cathode 4052 of the dust removal electric field passes through the anode 4051 of the dust removal electric field.
  • the method of reducing electric field coupling includes the following steps: the ratio of the dust collecting area of the dust collecting anode 4051 to the discharge area of the dust removing electric field cathode 4052 is 6.67: 1, and the pole spacing between the dust removing electric field anode 4051 and the dust removing electric field cathode 4052 is 9.9mm, The length of the dust-removing electric field anode 4051 is 60 mm, and the length of the dust-removing electric field cathode 4052 is 54 mm.
  • the dust-removing electric field anode 4051 includes a fluid channel.
  • the fluid channel includes an inlet end and an outlet end.
  • the dust-removing electric field cathode 4052 is placed in the fluid channel
  • the dedusting electric field cathode 4052 extends in the direction of the dust collector fluid channel, the inlet end of the dedusting electric field anode 4051 is flush with the near inlet end of the dedusting electric field cathode 4052, and the outlet end of the dedusting electric field anode 4051 is close to the dedusting electric field cathode 4052
  • There is an angle ⁇ between the outlet ends, and ⁇ 118 °, and under the action of the dust-removing electric field anode 4051 and the dust-removing electric field cathode 4052, more substances to be treated can be collected, and the number of electric field couplings ⁇ 3 can be reduced Electric field coupling consumption of aerosol, water mist, oil mist, loose smooth particles can save electric energy of electric field by 30-50%.
  • the electric field device includes an electric field stage composed of a plurality of the above electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each dust removal electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the electric field stages of the multiple electric field stages are connected in series, and the series electric field stages are connected by a connecting shell.
  • the distance between the adjacent two electric field stages is greater than 1.4 times the pole spacing.
  • the electric field levels are two levels, that is, a first level electric field and a second level electric field.
  • the first level electric field and the second level electric field are connected in series through a connection housing.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field has a hollow regular hexagonal tube shape
  • the cathode 4052 of the dust removal electric field has a rod shape
  • the cathode 4052 of the dust removal electric field passes through the anode 4051 of the dust removal electric field.
  • the method for reducing electric field coupling includes the following steps: the ratio of the dust collecting area of the dust collecting field anode 4051 to the discharge area of the dust removing electric field cathode 4052 is 1680: 1, and the pole spacing between the dust removing electric field anode 4051 and the dust removing electric field cathode 4052 is 139.9mm, The length of the dust-removing electric field anode 4051 is 180 mm, and the length of the dust-removing electric field cathode 4052 is 180 mm.
  • the dust-removing electric field anode 4051 includes a fluid channel.
  • the fluid channel includes an inlet end and an outlet end.
  • the dust-removing electric field cathode 4052 is placed in the fluid channel
  • the dedusting electric field cathode 4052 extends in the direction of the dust collector fluid channel, the inlet end of the dedusting electric field anode 4051 is flush with the near inlet end of the dedusting electric field cathode 4052, and the outlet end of the dedusting electric field anode 4051 is close to the dedusting electric field cathode 4052
  • the outlet end is flush, and under the action of the dedusting electric field anode 4051 and the dedusting electric field cathode 4052, more materials to be treated can be collected, and the number of electric field couplings is ⁇ 3, which can reduce the electric field to aerosol, water mist, oil mist 3. Coupling consumption of loose and smooth particles saves 20-40% of electric energy in the electric field.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field has a hollow regular hexagonal tube shape
  • the cathode 4052 of the dust removal electric field has a rod shape
  • the cathode 4052 of the dust removal electric field passes through the anode 4051 of the dust removal electric field.
  • the method of reducing electric field coupling includes the following steps: the ratio of the dust collecting area of the dust collecting field anode 4051 to the discharge area of the dust removing electric field cathode 4052 is 1.667: 1, the pole spacing between the dust removing electric field anode 4051 and the dust removing electric field cathode 4052 is 2.5mm,
  • the dust removal field anode 4051 has a length of 30 mm and the dust removal field cathode 4052 has a length of 30 mm.
  • the dust removal field anode 4051 includes a fluid channel including an inlet end and an outlet end.
  • the dust removal field cathode 4052 is placed in the fluid channel
  • the dedusting electric field cathode 4052 extends in the direction of the dust collector fluid channel, the inlet end of the dedusting electric field anode 4051 is flush with the near inlet end of the dedusting electric field cathode 4052, and the outlet end of the dedusting electric field anode 4051 is close to the dedusting electric field cathode 4052
  • the outlet end is flush, and under the action of the dedusting electric field anode 4051 and the dedusting electric field cathode 4052, more materials to be treated can be collected, and the number of electric field couplings is ⁇ 3, which can reduce the electric field to aerosol, water mist, oil mist 1. Coupling consumption of loose and smooth particles, saving electric field electric energy by 10-30%.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field in this embodiment is a hollow regular hexagonal tube
  • the cathode 4052 of the dust removal electric field is rod-shaped
  • the cathode 4052 of the dust removal electric field is installed in the anode 4051 of the dust removal electric field.
  • the ratio of the dust collecting area of the anode 4051 to the discharge area of the cathode 4052 of the dedusting electric field is 6.67: 1, the pole spacing between the anode 4051 of the dedusting electric field and the cathode 4052 of the dedusting electric field is 9.9 mm, the length of the anode 4051 of the dedusting electric field is 60 mm, and the cathode of the dedusting electric field The length of 4052 is 54mm.
  • the anode 4051 of the dedusting electric field includes a fluid channel.
  • the fluid channel includes an inlet end and an outlet end.
  • the cathode 4052 of the dedusting electric field is placed in the fluid channel.
  • the cathode 4052 of the dedusting electric field is along the dust collector.
  • the direction of the fluid channel extends.
  • the inlet end of the anode 4051 of the dust removal electric field is flush with the near inlet end of the cathode 4052 of the dust removal electric field.
  • There is an angle ⁇ between the outlet end of the anode 4051 of the dust removal electric field and the near outlet end of the cathode 4052 of the dust removal electric field. 118 °, and under the action of the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field, more substances to be treated can be collected to ensure the development of the electric field
  • the dust collection efficiency of the raw unit is higher, and the typical exhaust particle pm0.23 dust collection efficiency is 99.99%.
  • the electric field device includes an electric field stage composed of a plurality of the above electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each dust removal electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the electric field stages of the multiple electric field stages are connected in series, and the series electric field stages are connected by a connecting shell.
  • the distance between the adjacent two electric field stages is greater than 1.4 times the pole spacing.
  • the electric field levels are two levels, that is, a first-level electric field 4053 and a second-level electric field 4054.
  • the first-level electric field 4053 and the second-level electric field 4054 are connected in series through a connection housing 4055.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the dust-removing electric field anode 4051 is a hollow regular hexagonal tube, and the dust-removing electric field cathode 4052 is rod-shaped.
  • the dust-removing electric field cathode 4052 is interposed in the dust-removing electric field anode 4051.
  • the discharge area ratio is 1680: 1, the pole spacing between the dedusting electric field anode 4051 and the dedusting electric field cathode 4052 is 139.9mm, the length of the dedusting electric field anode 4051 is 180mm, the length of the dedusting electric field cathode 4052 is 180mm, and the dedusting electric field anode 4051 includes A fluid channel including an inlet end and an outlet end, the dust-removing electric field cathode 4052 is placed in the fluid channel, the dust-removing electric field cathode 4052 extends in the direction of the dust collector fluid channel, and the inlet of the dust-removing electric field anode 4051 The end is flush with the near inlet end of the dedusting electric field cathode 4052, the exit end of the dedusting electric field anode 4051 is flush with the near exit end of the dedusting electric field cathode 4052, and then under the action of the dedusting electric field anode 4051 and the dedusting electric field cathode
  • the electric field device includes an electric field stage composed of a plurality of the above electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each dust removal electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply
  • the two electrodes are electrically connected, the power supply is a DC power supply, and the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the dust-removing electric field anode 4051 is a hollow regular hexagonal tube, and the dust-removing electric field cathode 4052 is rod-shaped.
  • the dust-removing electric field cathode 4052 is interposed in the dust-removing electric field anode 4051.
  • the dust-collecting area of the dust-removing electric field anode 4051 and the dust-removing electric field cathode 4052 The ratio of the discharge area is 1.667: 1, and the pole spacing between the dust-removing electric field anode 4051 and the dust-removing electric field cathode 4052 is 2.5 mm.
  • the dust removal field anode 4051 has a length of 30 mm and the dust removal field cathode 4052 has a length of 30 mm.
  • the dust removal field anode 4051 includes a fluid channel including an inlet end and an outlet end.
  • the dust removal field cathode 4052 is placed in the fluid channel
  • the dedusting electric field cathode 4052 extends in the direction of the dust collector fluid channel, the inlet end of the dedusting electric field anode 4051 is flush with the near inlet end of the dedusting electric field cathode 4052, and the outlet end of the dedusting electric field anode 4051 is close to the dedusting electric field cathode 4052
  • the outlet end is flush, and under the action of the dust removal electric field anode 4051 and the dust removal electric field cathode 4052, more materials to be treated can be collected to ensure a higher dust collection efficiency of the electric field device.
  • Typical exhaust particles pm0.23 are collected The dust efficiency is 99.99%.
  • the dust-removing electric field anode 4051 and the dust-removing electric field cathode 4052 constitute a dust collecting unit, and there are a plurality of dust collecting units, so as to effectively improve the dust collecting efficiency of the electric field device by using a plurality of dust collecting units.
  • the substance to be treated may be particulate dust or other impurities to be treated, such as aerosol, water mist, oil mist, etc.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the exhaust system in this embodiment includes the electric field device in Embodiment 15, Embodiment 16, or Embodiment 17 described above.
  • the gas discharged by the exhaust discharge equipment must first flow through the electric field device to effectively remove the dust and other pollutants in the gas; then, the processed gas is discharged to the atmosphere to reduce the exhaust The impact on the atmosphere.
  • This exhaust system is also called an exhaust gas treatment device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field has a hollow regular hexagonal tube shape
  • the cathode 4052 of the dust removal electric field has a rod shape.
  • the cathode 4052 of the dust removal electric field is installed in the anode 4051 of the dust removal electric field.
  • the anode 4051 of the dust removal electric field has a length of 5 cm, and the cathode 4052 of the dust removal electric field has 5cm, the dedusting electric field anode 4051 includes a fluid channel, the fluid channel includes an inlet end and an outlet end, the dedusting electric field cathode 4052 is placed in the fluid channel, the dedusting electric field cathode 4052 is along the dust collector fluid channel The direction extends, the inlet end of the dust removal electric field anode 4051 is flush with the near inlet end of the dust removal electric field cathode 4052, the outlet end of the dust removal electric field anode 4051 is flush with the near outlet end of the dust removal electric field cathode 4052, the dust removal electric field anode 4051 and the dust removal electric field
  • the pole spacing of the cathode 4052 is 9.9mm, and under the action of the dedusting electric field anode 4051 and the dedusting electric field cathode 4052, it makes it resistant to high temperature shock
  • the electric field device includes an electric field stage composed of a plurality of the above electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each dust removal electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the substance to be treated may be particulate dust.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the dust-removing electric field anode 4051 is a hollow regular hexagonal tube
  • the dust-removing electric field cathode 4052 is rod-shaped
  • the dust-removing electric field cathode 4052 is inserted in the dust-removing electric field anode 4051
  • the dust-removing electric field anode 4051 is 9 cm in length
  • the dust-removing electric field cathode 4052 is 9cm
  • the dust-removing electric field anode 4051 includes a fluid channel
  • the fluid channel includes an inlet end and an outlet end
  • the dust-removing electric field cathode 4052 is placed in the fluid channel
  • the dust-removing electric field cathode 4052 is located along the dust collector fluid channel The direction extends, the inlet end of the dust removal electric field anode 4051 is flush with the near inlet end of the dust removal electric field cathode 4052, the outlet end of the dust removal electric field anode 4051 is flush with the near outlet end of the dust removal electric field cathode 4052, the dust removal
  • the electric field device includes an electric field stage composed of a plurality of the above electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each storage electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the substance to be treated may be particulate dust.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.
  • the electric field generating unit in this embodiment can be applied to an electric field device. As shown in FIG. 13, it includes a dust removal electric field anode 4051 and a dust removal electric field cathode 4052 for generating an electric field.
  • the dust removal electric field anode 4051 and the dust removal electric field cathode 4052 are respectively connected to the power supply The two electrodes are electrically connected.
  • the power supply is a DC power supply.
  • the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field are electrically connected to the anode and the cathode of the DC power supply, respectively.
  • the anode 4051 of the dust removal electric field has a positive potential
  • the cathode 4052 of the dust removal electric field has a negative potential.
  • the DC power supply may specifically be a DC high-voltage power supply.
  • a discharge electric field is formed between the above-mentioned dedusting electric field anode 4051 and the dedusting electric field cathode 4052, and the discharge electric field is an electrostatic field.
  • the anode 4051 of the dust removal electric field has a hollow regular hexagonal tube shape
  • the cathode 4052 of the dust removal electric field has a rod shape.
  • the cathode 4052 of the dust removal electric field is installed in the anode 4051 of the dust removal electric field.
  • the dedusting electric field anode 4051 includes a fluid channel, the fluid channel includes an inlet end and an outlet end, the dedusting electric field cathode 4052 is placed in the fluid channel, the dedusting electric field cathode 4052 is along the dust collector fluid channel The direction extends, the inlet end of the dust removal electric field anode 4051 is flush with the near inlet end of the dust removal electric field cathode 4052, the outlet end of the dust removal electric field anode 4051 is flush with the near outlet end of the dust removal electric field cathode 4052, the dust removal electric field anode 4051 and the dust removal electric field
  • the pole spacing of the cathode 4052 is 2.5mm, and under the action of the anode 4051 of the dust removal electric field and the cathode 4052 of the dust removal electric field, it makes it resistant to high temperature shocks, and can collect more to-be-processed materials to ensure the dust collection of the electric field generating unit higher efficiency.
  • the electric field device includes an electric field stage composed of a plurality of the above-mentioned electric field generating units, and there are a plurality of the electric field stages, so as to effectively improve the dust collection efficiency of the electric field device by using a plurality of dust collection units.
  • the anode of each dust removal electric field is the same polarity
  • the cathode of each dust removal electric field is the same polarity.
  • the electric field stages of the multiple electric field stages are connected in series, and the series electric field stages are connected by a connecting shell.
  • the distance between the adjacent two electric field stages is greater than 1.4 times the pole spacing.
  • the electric field levels are two levels, namely, the first level electric field and the second level electric field, and the first level electric field and the second level electric field are connected in series through a connection housing.
  • the substance to be treated may be particulate dust.
  • the above-mentioned gas may be a gas to be entered into the exhaust discharge device, or a gas discharged from the exhaust discharge device.

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Abstract

一种排气处理系统，包括臭氧净化系统；所述臭氧净化系统包括臭氧量控制装置（209），用于控制臭氧量以致有效氧化排气中待处理的气体组分，所述臭氧量控制装置（209）包括控制单元（2091）。该排气处理系统能够有效去除排气中的颗粒物，对排气的净化处理效果更好。

Description

排气处理系统及方法 技术领域
本发明属于环保领域，涉及一种排气处理系统及方法。
背景技术
燃烧形成的排气中通常含有大量污染物，排气直接排放到大气中将会对环境造成严重污染。因此，在排气排放前需对排气进行净化处理。目前对于排气净化，常规的技术路线是采用氧化催化剂DOC除去碳氢化合物THC和CO，同时把低价态NO氧化成高价态的NO 2；在DOC之后采用柴油机微粒捕集器DPF对颗粒物PM进行过滤；在柴油机微粒捕集器DPF之后喷射尿素，尿素在排气中分解成氨气NH 3，NH 3在其后的选择性催化剂SCR上和NO 2发生选择性催化还原反应，生成氮气N 2和水。在最后在氨气氧化催化剂ASC上将过量的NH 3氧化成N 2和水，现有技术对排气的净化需添加大量尿素，且净化效果一般。
现有技术中，通常通过颗粒物过滤器来进行颗粒物过滤。其中，DPF以燃烧方式工作，即利用积碳在多孔结构中充分堵塞后升温达到燃点后通过自然或者助燃的方式燃烧。具体地，DPF的工作原理如下：带有颗粒物的进气进入DPF的蜂窝状载体，颗粒物在蜂窝装载体中被拦截，当排气流出DPF时大部分的颗粒物已经被过滤掉。DPF的载体材料主要为堇青石、碳化硅、钛酸铝等，具体可根据实际情况进行选择使用。然而，上述方式存储以下缺陷：
(1)当DPF捕集到一定程度的颗粒物后就需要再生，否则排气背压上升，工作状态恶化，严重影响性能。因此，DPF需要定期维护和添加催化剂。即使有定期维护，颗粒物的积聚限制了排气流，因此增加了背压，这会影响性能和燃油消耗。
(2)DPF的除尘效果不稳定，无法满足排气处理的最新过滤要求。
静电除尘是一种气体除尘方法，通常在冶金、化学等工业领域中用以净化气体或回收有用尘粒。现有技术中，由于占用空间较大、系统结构复杂、除尘效果差等问题。
发明内容
鉴于以上所述现有技术的缺点，本发明的目的在于提供一种对排气净化处理效果更好的排气处理系统。同时，本发明通过研究发现了现有电离除尘技术中存在的新问题，并通过一系列技术手段来解决，例如，当排气温度低于一定温度时，排气中可能含有液体水，本发明在电场装置前安装除水装置，脱除排气中的液体水，提高电离除尘效果；在高温条件下，通过控制电场装置阳极的集尘面积与阴极的放电面积比、阴极/阳极的长度、极间距以及设置辅 助电场等，有效减少电场耦合，并使得电场装置在高温冲击下仍具有高效率的集尘能力。因此，本发明适合在苛刻条件下作业，并保证除尘效率。
1.为实现上述目的及其他目的，本发明提供以下示例：本发明提供的示例1：一种排放处理系统。
2.本发明提供的示例2：包括上述示例1，包括除尘系统，所述除尘系统包括除尘系统入口、除尘系统出口、除尘电场装置。
3.本发明提供的示例3：包括上述示例2，其中，所述除尘电场装置包括除尘电场装置入口、除尘电场装置出口、除尘电场阴极和除尘电场阳极，所述除尘电场阴极和所述除尘电场阳极用于产生电离除尘电场。
4.本发明提供的示例4：包括上述示例3，其中，所述除尘电场阳极包括第一阳极部和第二阳极部，所述第一阳极部靠近除尘电场装置入口，第二阳极部靠近除尘电场装置出口，所述第一阳极部和所述第二阳极部之间设置有至少一个阴极支撑板。
5.本发明提供的示例5：包括上述示例4，其中，所述除尘电场装置还包括绝缘机构，用于实现所述阴极支撑板和所述除尘电场阳极之间的绝缘。
6.本发明提供的示例6：包括上述示例5，其中，所述除尘电场阳极和所述除尘电场阴极之间形成电场流道，所述绝缘机构设置在所述电场流道外。
7.本发明提供的示例7：包括上述示例5或6，其中，所述绝缘机构包括绝缘部和隔热部；所述绝缘部的材料采用陶瓷材料或玻璃材料。
8.本发明提供的示例8：包括上述示例7，其中，所述绝缘部为伞状串陶瓷柱、伞状串玻璃柱、柱状串陶瓷柱或柱状玻璃柱，伞内外或柱内外挂釉。
9.本发明提供的示例9：包括上述示例8，其中，伞状串陶瓷柱或伞状串玻璃柱的外缘与所述除尘电场阳极的距离大于电场距离1.4倍，伞状串陶瓷柱或伞状串玻璃柱的伞突边间距总和大于伞状串陶瓷柱或伞状串玻璃柱的绝缘间距1.4倍，伞状串陶瓷柱或伞状串玻璃柱的伞边内深总长大于伞状串陶瓷柱或伞状串玻璃柱的绝缘距离1.4倍。
10.本发明提供的示例10：包括上述示例4至9中的任一项，其中，所述第一阳极部的长度是所述除尘电场阳极长度的1/10至1/4、1/4至1/3、1/3至1/2、1/2至2/3、2/3至3/4，或3/4至9/10。
11.本发明提供的示例11：包括上述示例4至10中的任一项，其中，所述第一阳极部的长度是足够的长，以清除部分灰尘，减少积累在所述绝缘机构和所述阴极支撑板上的灰尘，减少灰尘造成的电击穿。
12.本发明提供的示例12：包括上述示例4至11中的任一项，其中，所述第二阳极部包括积尘段和预留积尘段。
13.本发明提供的示例13：包括上述示例3至12中的任一项，其中，所述除尘电场阴极包括至少一根电极棒。
14.本发明提供的示例14：包括上述示例13，其中，所述电极棒的直径不大于3mm。
15.本发明提供的示例15：包括上述示例13或14，其中，所述电极棒的形状呈针状、多角状、毛刺状、螺纹杆状或柱状。
16.本发明提供的示例16：包括上述示例3至15中的任一项，其中，所述除尘电场阳极由中空的管束组成。
17.本发明提供的示例17：包括上述示例16，其中，所述除尘电场阳极管束的中空的截面采用圆形或多边形。
18.本发明提供的示例18：包括上述示例17，其中，所述多边形为六边形。
19.本发明提供的示例19：包括上述示例16至18中的任一项，其中，所述除尘电场阳极的管束呈蜂窝状。
20.本发明提供的示例20：包括上述示例3至19中的任一项，其中，所述除尘电场阴极穿射于所述除尘电场阳极内。
21.本发明提供的示例21：包括上述示例3至20中的任一项，其中，当电场积尘到一定程度时，所述除尘电场装置进行除碳黑处理。
22.本发明提供的示例22：包括上述示例21，其中，所述除尘电场装置检测电场电流来确定是否积尘到一定程度，需要进行除碳黑处理。
23.本发明提供的示例23：包括上述示例21或22，其中，所述除尘电场装置增高电场电压来进行除碳黑处理。
24.本发明提供的示例24：包括上述示例21或22，其中，所述除尘电场装置利用电场反电晕放电现象来进行除碳黑处理。
25.本发明提供的示例25：包括上述示例21或22，其中，所述除尘电场装置利用电场反电晕放电现象，增高电压，限制入注电流，使发生在阳极积碳位置的急剧放电产生等离子，所述等离子使碳黑有机成分深度氧化，高分子键断裂，形成小分子二氧化碳和水，来进行除碳黑处理。
26.本发明提供的示例26：包括上述示例3至25中的任一项，其中，所述除尘电场阳极长度为10-90mm，所述除尘电场阴极长度为10-90mm。
27.本发明提供的示例27：包括上述示例26，其中，当电场温度为200℃时，对应的集尘效率为99.9％。
28.本发明提供的示例28：包括上述示例26或27，其中，当电场温度为400℃时，对应的集尘效率为90％。
29.本发明提供的示例29：包括上述示例26至28中的任一项，其中，当电场温度为500℃时，对应的集尘效率为50％。
30.本发明提供的示例30：包括上述示例3至29中的任一项，其中，所述除尘电场装置还包括辅助电场单元，用于产生与所述电离除尘电场不平行的辅助电场。
31.本发明提供的示例31：包括上述示例3至29中的任一项，其中，所述除尘电场装置还包括辅助电场单元，所述电离除尘电场包括流道，所述辅助电场单元用于产生与所述流道不垂直的辅助电场。
32.本发明提供的示例32：包括上述示例30或31，其中，所述辅助电场单元包括第一电极，所述辅助电场单元的第一电极设置在或靠近所述电离除尘电场的进口。
33.本发明提供的示例33：包括上述示例32，其中，所述第一电极为阴极。
34.本发明提供的示例34：包括上述示例32或33，其中，所述辅助电场单元的第一电极是所述除尘电场阴极的延伸。
35.本发明提供的示例35：包括上述示例34，其中，所述辅助电场单元的第一电极与所述除尘电场阳极具有夹角α，且0°＜α≤125°、或45°≤α≤125°、或60°≤α≤100°、或α＝90°。
36.本发明提供的示例36：包括上述示例30至35中的任一项，其中，所述辅助电场单元包括第二电极，所述辅助电场单元的第二电极设置在或靠近所述电离除尘电场的出口。
37.本发明提供的示例37：包括上述示例36，其中，所述第二电极为阳极。
38.本发明提供的示例38：包括上述示例36或37，其中，所述辅助电场单元的第二电极是所述除尘电场阳极的延伸。
39.本发明提供的示例39：包括上述示例38，其中，所述辅助电场单元的第二电极与所述除尘电场阴极具有夹角α，且0°＜α≤125°、或45°≤α≤125°、或60°≤α≤100°、或α＝90°。
40.本发明提供的示例40：包括上述示例30至33、36和37中的任一项，其中，所述辅助电场的电极与所述电离除尘电场的电极独立设置。
41.本发明提供的示例41：包括上述示例3至40中的任一项，其中，所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
42.本发明提供的示例42：包括上述示例3至40中的任一项，其中，所述除尘电场阳极 的积尘面积与所述除尘电场阴极的放电面积的比为6.67：1-56.67：1。
43.本发明提供的示例43：包括上述示例3至42中的任一项，其中，所述除尘电场阴极直径为1-3毫米，所述除尘电场阳极与所述除尘电场阴极的极间距为2.5-139.9毫米；所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
44.本发明提供的示例44：包括上述示例3至42中的任一项，其中，所述除尘电场阳极和所述除尘电场阴极的极间距小于150mm。
45.本发明提供的示例45：包括上述示例3至42中的任一项，其中，所述除尘电场阳极与所述除尘电场阴极的极间距为2.5-139.9mm。
46.本发明提供的示例46：包括上述示例3至42中的任一项，其中，所述除尘电场阳极与所述除尘电场阴极的极间距为5-100mm。
47.本发明提供的示例47：包括上述示例3至46中的任一项，其中，所述除尘电场阳极长度为10-180mm。
48.本发明提供的示例48：包括上述示例3至46中的任一项，其中，所述除尘电场阳极长度为60-180mm。
49.本发明提供的示例49：包括上述示例3至48中的任一项，其中，所述除尘电场阴极长度为30-180mm。
50.本发明提供的示例50：包括上述示例3至48中的任一项，其中，所述除尘电场阴极长度为54-176mm。
51.本发明提供的示例51：包括上述示例41至50中的任一项，其中，当运行时，所述电离除尘电场的耦合次数≤3。
52.本发明提供的示例52：包括上述示例30至50中的任一项，其中，当运行时，所述电离除尘电场的耦合次数≤3。
53.本发明提供的示例53：包括上述示例3至52中的任一项，其中，所述电离除尘电场电压的取值范围为1kv-50kv。
54.本发明提供的示例54：包括上述示例3至53中的任一项，其中，所述除尘电场装置还包括若干连接壳体，串联电场级通过所述连接壳体连接。
55.本发明提供的示例55：包括上述示例54，其中，相邻的电场级的距离大于所述极间距的1.4倍。
56.本发明提供的示例56：包括上述示例3至55中的任一项，其中，所述除尘电场装置还包括前置电极，所述前置电极在所述除尘电场装置入口与所述除尘电场阳极和所述除尘电 场阴极形成的电离除尘电场之间。
57.本发明提供的示例57：包括上述示例56，其中，所述前置电极呈点状、线状、网状、孔板状、板状、针棒状、球笼状、盒状、管状、物质自然形态、或物质加工形态。
58.本发明提供的示例58：包括上述示例56或57，其中，所述前置电极上设有通孔。
59.本发明提供的示例59：包括上述示例58，其中，所述通孔呈多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形。
60.本发明提供的示例60：包括上述示例58或59，其中，所述通孔的大小为0.1-3毫米。
61.本发明提供的示例61：包括上述示例56至60中的任一项，其中，所述前置电极为固体、液体、气体分子团、或等离子体中的一种或多种形态的组合。
62.本发明提供的示例62：包括上述示例56至61中的任一项，其中，所述前置电极为导电混合态物质、生物体自然混合导电物质、或物体人工加工形成导电物质。
63.本发明提供的示例63：包括上述示例56至62中的任一项，其中，所述前置电极为304钢或石墨。
64.本发明提供的示例64：包括上述示例56至62中的任一项，其中，所述前置电极为含离子导电液体。
65.本发明提供的示例65：包括上述示例56至64中的任一项，其中，在工作时，在带污染物的气体进入所述除尘电场阴极、除尘电场阳极形成的电离除尘电场之前，且带污染物的气体通过所述前置电极时，所述前置电极使气体中的污染物带电。
66.本发明提供的示例66：包括上述示例65，其中，当带污染物的气体进入所述电离除尘电场时，所述除尘电场阳极给带电的污染物施加吸引力，使污染物向所述除尘电场阳极移动，直至污染物附着在所述除尘电场阳极上。
67.本发明提供的示例67：包括上述示例65或66，其中，所述前置电极将电子导入污染物，电子在位于所述前置电极和所述除尘电场阳极之间的污染物之间进行传递，使更多污染物带电。
68.本发明提供的示例68：包括上述示例64至66中的任一项，其中，所述前置电极和所述除尘电场阳极之间通过污染物传导电子、并形成电流。
69.本发明提供的示例69：包括上述示例65至68中的任一项，其中，所述前置电极通过与污染物接触的方式使污染物带电。
70.本发明提供的示例70：包括上述示例65至69中的任一项，其中，所述前置电极通过能量波动的方式使污染物带电。
71.本发明提供的示例71：包括上述示例65至70中的任一项，其中，所述前置电极上设有通孔。
72.本发明提供的示例72：包括上述示例56至71中的任一项，其中，所述前置电极呈线状，所述除尘电场阳极呈面状。
73.本发明提供的示例73：包括上述示例56至72中的任一项，其中，所述前置电极垂直于所述除尘电场阳极。
74.本发明提供的示例74：包括上述示例56至73中的任一项，其中，所述前置电极与所述除尘电场阳极相平行。
75.本发明提供的示例75：包括上述示例56至74中的任一项，其中，所述前置电极呈曲线状或圆弧状。
76.本发明提供的示例76：包括上述示例56至75中的任一项，其中，所述前置电极采用金属丝网。
77.本发明提供的示例77：包括上述示例56至76中的任一项，其中，所述前置电极与所述除尘电场阳极之间的电压不同于所述除尘电场阴极与所述除尘电场阳极之间的电压。
78.本发明提供的示例78：包括上述示例56至77中的任一项，其中，所述前置电极与所述除尘电场阳极之间的电压小于起始起晕电压。
79.本发明提供的示例79：包括上述示例56至78中的任一项，其中，所述前置电极与所述除尘电场阳极之间的电压为0.1kv-2kv/mm。
80.本发明提供的示例80：包括上述示例56至79中的任一项，其中，所述除尘电场装置包括排气流道，所述前置电极位于所述排气流道中；所述前置电极的截面面积与排气流道的截面面积比为99％-10％、或90-10％、或80-20％、或70-30％、或60-40％、或50％。
81.本发明提供的示例81：包括上述示例3至80中的任一项，其中，所述除尘电场装置包括驻极体元件。
82.本发明提供的示例82：包括上述示例81，其中，所述除尘电场阳极和所述除尘电场阴极接通电源时，所述驻极体元件在所述电离除尘电场中。
83.本发明提供的示例83：包括上述示例81或82，其中，所述驻极体元件靠近所述除尘电场装置出口，或者，所述驻极体元件设于所述除尘电场装置出口。
84.本发明提供的示例84：包括上述示例81至83中的任一项，其中，所述除尘电场阳极和所述除尘电场阴极形成排气流道，所述驻极体元件设于所述排气流道中。
85.本发明提供的示例85：包括上述示例84，其中，所述排气流道包括排气流道出口，所 述驻极体元件靠近所述排气流道出口，或者，所述驻极体元件设于所述排气流道出口。
86.本发明提供的示例86：包括上述示例84或85，其中，所述驻极体元件于所述排气流道中的横截面占排气流道横截面5％-100％。
87.本发明提供的示例87：包括上述示例86，其中，所述驻极体元件于所述排气流道中的横截面占排气流道横截面10％-90％、20％-80％、或40％-60％。
88.本发明提供的示例88：包括上述示例81至87中的任一项，其中，所述电离除尘电场给所述驻极体元件充电。
89.本发明提供的示例89：包括上述示例81至88中的任一项，其中，所述驻极体元件具有多孔结构。
90.本发明提供的示例90：包括上述示例81至89中的任一项，其中，所述驻极体元件为织品。
91.本发明提供的示例91：包括上述示例81至90中的任一项，其中，所述除尘电场阳极内部为管状，所述驻极体元件外部为管状，所述驻极体元件外部套设于所述除尘电场阳极内部。
92.本发明提供的示例92：包括上述示例81至91中的任一项，其中，所述驻极体元件与所述除尘电场阳极为可拆卸式连接。
93.本发明提供的示例93：包括上述示例81至92中的任一项，其中，所述驻极体元件的材料包括具有驻极性能的无机化合物。
94.本发明提供的示例94：包括上述示例93，其中，所述无机化合物选自含氧化合物、含氮化合物或玻璃纤维中的一种或多种组合。
95.本发明提供的示例95：包括上述示例94，其中，所述含氧化合物选自金属基氧化物、含氧复合物、含氧的无机杂多酸盐中的一种或多种组合。
96.本发明提供的示例96：包括上述示例95，其中，所述金属基氧化物选自氧化铝、氧化锌、氧化锆、氧化钛、氧化钡、氧化钽、氧化硅、氧化铅、氧化锡中的一种或多种组合。
97.本发明提供的示例97：包括上述示例95，其中，所述金属基氧化物为氧化铝。
98.本发明提供的示例98：包括上述示例95，其中，所述含氧复合物选自钛锆复合氧化物或钛钡复合氧化物中的一种或多种组合。
99.本发明提供的示例99：包括上述示例95，其中，所述含氧的无机杂多酸盐选自钛酸锆、锆钛酸铅或钛酸钡中的一种或多种组合。
100.本发明提供的示例100：包括上述示例94，其中，所述含氮化合物为氮化硅。
101.本发明提供的示例101：包括上述示例81至100中的任一项，其中，所述驻极体元件的材料包括具有驻极性能的有机化合物。
102.本发明提供的示例102：包括上述示例101，其中，所述有机化合物选自氟聚合物、聚碳酸酯、PP、PE、PVC、天然蜡、树脂、松香中的一种或多种组合。
103.本发明提供的示例103：包括上述示例102，其中，所述氟聚合物选自聚四氟乙烯、聚全氟乙丙烯、可溶性聚四氟乙烯、聚偏氟乙烯中的一种或多种组合。
104.本发明提供的示例104：包括上述示例102，其中，所述氟聚合物为聚四氟乙烯。
105.本发明提供的示例105：包括上述示例2至104中的任一项，其中，还包括均风装置。
106.本发明提供的示例106：包括上述示例105，其中，所述均风装置在所述除尘系统入口与所述除尘电场阳极和所述除尘电场阴极形成的电离除尘电场之间，当所述除尘电场阳极为四方体时，述均风装置包括：设置于所述除尘电场阳极一侧边的进气管和设置于另一侧边的出气管；其中，所述进气管与所述出气管相对立。
107.本发明提供的示例107：包括上述示例105，其中，所述均风装置在所述除尘系统入口与所述除尘电场阳极和所述除尘电场阴极形成的电离除尘电场之间，当所述除尘电场阳极为圆柱体时，所述均风装置由若干可旋转的均风叶片组成。
108.本发明提供的示例108：包括上述示例105，其中，所述均风装置第一文氏板均风机构和设置于所述除尘电场阳极的出气端的第二文氏板均风机构，所述第一文氏板均风机构上开设有进气孔，所述第二文氏板均风机构上开设有出气孔，所述进气孔与所述出气孔错位排布，且正面进气侧面出气，形成旋风结构。
109.本发明提供的示例109：包括上述示例2至108中的任一项，其中，还包括补氧装置，用于在所述电离除尘电场之前添加包括氧气的气体。
110.本发明提供的示例110：包括上述示例109，其中，所述补氧装置通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气。
111.本发明提供的示例111：包括上述示例109或110，其中，至少根据排气颗粒含量决定补氧量。
112.本发明提供的示例112：包括上述示例2至111中的任一项，其中，还包括除水装置，用于在所述除尘电场装置入口之前去除液体水。
113.本发明提供的示例113：包括上述示例112，其中，当排气温度低于一定温度时，所述除水装置脱除排气中的液体水。
114.本发明提供的示例114：包括上述示例113，其中，所述一定温度在90℃以上、100℃以下。
115.本发明提供的示例115：包括上述示例113，其中，所述一定温度在80℃以上、90℃以下。
116.本发明提供的示例116：包括上述示例113，其中，所述一定温度为80℃以下。
117.本发明提供的示例117：包括上述示例112至116，其中，所述除水装置为电凝装置。
118.本发明提供的示例118：包括上述示例2至117中的任一项，其中，还包括降温装置，用于在所述除尘电场装置入口之前降低排气温度。
119.本发明提供的示例119：包括上述示例118，其中，所述降温装置包括换热单元，用于与排气进行热交换，以将换热单元中液态的换热介质加热成气态的换热介质。
120.本发明提供的示例120：包括上述示例119，其中，所述换热单元包括：
排气通过腔，与排气管路相连通，所述排气通过腔用于供排气通过；
介质气化腔，所述介质气化腔用于将液态换热介质与排气发生热交换后转化成气态。
121.本发明提供的示例121：包括上述示例119或120，其中，还包括动力产生单元，所述动力产生单元用于将换热介质的热能和/或排气的热能转换为机械能。
122.本发明提供的示例122：包括上述示例121，其中，所述动力产生单元包括涡扇。
123.本发明提供的示例123：包括上述示例122，其中，所述涡扇包括：
涡扇轴；
介质腔涡扇组件，安装在涡扇轴上，且所述介质腔涡扇组件位于介质气化腔中。
124.本发明提供的示例124：包括上述示例123，其中，所述介质腔涡扇组件包括介质腔导流扇和介质腔动力扇。
125.本发明提供的示例125：包括上述示例122至124中的任一项，其中，所述涡扇包括：
腔涡扇组件，安装在涡扇轴上，且所述腔涡扇组件位于排气通过腔中。
126.本发明提供的示例126：包括上述示例125，其中，所述腔涡扇组件包括排气腔导流扇和排气腔动力扇。
127.本发明提供的示例127：包括上述示例121至126中的任一项，其中，所述降温装置还包括发电单元，所述发电单元用于将动力产生单元产生的机械能转换为电能。
128.本发明提供的示例128：包括上述示例127，其中，所述发电单元包括发电机定子和发电机转子，所述发电机转子与动力产生单元的涡扇轴相连接。
129.本发明提供的示例：包括上述示例127或128，其中，所述发电单元包括电池组件。
130.本发明提供的示例130：包括上述示例127至129中的任一项，其中，所述发电单元包括发电机调控组件，所述发电机调控组件用于调节发电机的电动转矩。
131.本发明提供的示例131：包括上述示例121至130中的任一项，其中，所述降温装置还包括介质传输单元，所述介质传输单元连接于换热单元和动力产生单元之间。
132.本发明提供的示例132：包括上述示例131，其中，所述介质传输单元包括反推涵道。
133.本发明提供的示例133：包括上述示例131，其中，所述介质传输单元包括承压管路。
134.本发明提供的示例134：包括上述示例127至133中的任一项，其中，所述降温装置还包括耦合单元，所述耦合单元电性连接于动力产生单元和发电单元之间。
135.本发明提供的示例135：包括上述示例134，其中，所述耦合单元包括电磁耦合器。
136.本发明提供的示例136：包括上述示例119至135中的任一项，其中，所述降温装置还包括保温管路，所述保温管路连接于排气管路和换热单元之间。
137.本发明提供的示例137：包括上述示例118至136中的任一项，其中，所述降温装置包括风机，所述风机将空气通入所述除尘电场装置入口之前，对排气起到降温的作用。
138.本发明提供的示例138：包括上述示例137，其中，通入的空气是排气的50％至300％。
139.本发明提供的示例139：包括上述示例137，其中，通入的空气是排气的100％至180％。
140.本发明提供的示例140：包括上述示例137，其中，通入的空气是排气的120％至150％。
141.本发明提供的示例141：包括上述示例120，其中，所述补氧装置包括风机，所述风机将空气通入所述除尘电场装置入口之前，对排气起到降温的作用。
142.本发明提供的示例142：包括上述示例141，其中，通入的空气是排气的50％至300％。
143.本发明提供的示例143：包括上述示例141，其中，通入的空气是排气的100％至180％。
144.本发明提供的示例144：包括上述示例141，其中，通入的空气是排气的120％至150％。
145.本发明提供的示例145：包括上述示例1-144中的任一项，还包括臭氧净化系统，所述臭氧净化系统包括反应场，用于将臭氧流股与排气流股混合反应。
146.本发明提供的示例146：包括上述示例145，其中，所述反应场包括管道和/或反应器。
147.本发明提供的示例147：包括上述示例146，其中，还包括如下技术特征中的至少一项：
1)管道的管段通径为100-200毫米；
2)管道的长度大于管径0.1倍；
3)所述反应器选自如下至少一种：
反应器一：所述反应器具有反应腔室，排气与臭氧在所述反应腔室混合并反应；
反应器二：所述反应器包括若干蜂窝状腔体，用于提供排气与臭氧混合并反应的空间；所述蜂窝状腔体内之间设有间隙，用于通入冷态介质，控制排气与臭氧的反应温度；
反应器三：所述反应器包括若干载体单元，所述载体单元提供反应场地；
反应器四：所述反应器包括催化剂单元，所述催化剂单元用于促进排气的氧化反应；
4)所述反应场设有臭氧进口，所述臭氧进口选自喷口、喷格栅、喷嘴、旋流喷嘴、设有文丘里管的喷口中的至少一种；
5)所述反应场设有臭氧进口，所述臭氧通过所述臭氧进口进入反应场与排气进行接触，臭氧进口的设置形成如下方向中至少一种：与排气流动的方向相反、与排气流动的方向垂直、与排气流动的方向相切、插入排气流动方向、多个方向与排气进行接触。
148.本发明提供的示例148：包括上述示例145至147中的中的任一项，其中，所述反应场包括排气管、蓄热体装置或催化器。
149.本发明提供的示例149：包括上述示例145至148中的中的任一项，其中，所述反应场的温度为-50-200℃。
150.本发明提供的示例150：包括上述示例149，其中，所述反应场的温度为60-70℃。
151.本发明提供的示例151：包括上述示例145至150中的中的任一项，其中，所述臭氧净化系统还包括臭氧源，用于提供臭氧流股。
152.本发明提供的示例152：包括上述示例151，其中，所述臭氧源包括存储臭氧单元和/或臭氧发生器。
153.本发明提供的示例153：包括上述示例152，其中，所述臭氧发生器包括延面放电臭氧发生器、工频电弧臭氧发生器、高频感应臭氧发生器、低气压臭氧发生器、紫外线臭氧发生器、电解液臭氧发生器、化学药剂臭氧发生器和射线辐照粒子发生器中的一种或多种的组合。
154.本发明提供的示例154：包括上述示例152，其中，所述臭氧发生器包括电极，所述电极上设有催化剂层，所述催化剂层包括氧化催化键裂解选择性催化剂层。
155.本发明提供的示例155：包括上述示例154，其中，所述电极包括高压电极或设有阻挡介质层的高压电极，当所述电极包括高压电极时，所述氧化催化键裂解选择性催化剂层设于所述高压电极表面上，当所述电极包括阻挡介质层的高压电极时，所述氧化催化键裂解选择性催化剂层设于阻挡介质层的表面上。
156.本发明提供的示例156：包括上述示例155，其中，所述阻挡介质层选自陶瓷板、陶 瓷管、石英玻璃板、石英板和石英管中的至少一种。
157.本发明提供的示例157：包括上述示例155，其中，当所述电极包括高压电极时，所述氧化催化键裂解选择性催化剂层的厚度为1-3mm；当所述电极包括阻挡介质层的高压电极时，所述氧化催化键裂解选择性催化剂层的负载量包括阻挡介质层的1-12wt％。
158.本发明提供的示例158：包括上述示例154至157中的中的任一项，其中，所述氧化催化键裂解选择性催化剂层包括如下重量百分比的各组分：
活性组分 5-15％；
涂层 85-95％；
其中，所述活性组分选自金属M和金属元素M的化合物中的至少一种，金属元素M选自碱土金属元素、过渡金属元素、第四主族金属元素、贵金属元素和镧系稀土元素中的至少一种；
所述涂层选自氧化铝、氧化铈、氧化锆、氧化锰、金属复合氧化物、多孔材料和层状材料中的至少一种，所述金属复合氧化物包括铝、铈、锆和锰中一种或多种金属的复合氧化物。
159.本发明提供的示例159：包括上述示例158，其中，所述碱土金属元素选自镁、锶和钙中的至少一种。
160.本发明提供的示例160：包括上述示例158，其中，所述过渡金属元素选自钛、锰、锌、铜、铁、镍、钴、钇和锆中的至少一种。
161.本发明提供的示例161：包括上述示例158，其中，所述第四主族金属元素为锡。
162.本发明提供的示例162：包括上述示例158，其中，所述贵金属元素选自铂、铑、钯、金、银和铱中的至少一种。
163.本发明提供的示例163：包括上述示例158，其中，所述镧系稀土元素选自镧、铈、镨和钐中的至少一种。
164.本发明提供的示例164：包括上述示例158，其中，所述金属元素M的化合物选自氧化物、硫化物、硫酸盐、磷酸盐、碳酸盐，以及钙钛矿中的至少一种。
165.本发明提供的示例165：包括上述示例158，其中，所述多孔材料选自分子筛、硅藻土、沸石和纳米碳管中的至少一种。
166.本发明提供的示例166：包括上述示例158，其中，所述层状材料选自石墨烯和石墨中的至少一种。
167.本发明提供的示例167：包括上述示例145至166中的任一项，其中，所述臭氧净化系统还包括臭氧量控制装置，用于控制臭氧量以致有效氧化排气中待处理的气体组分，所述 臭氧量控制装置包括控制单元。
168.本发明提供的示例168：包括上述示例167，其中，所述臭氧量控制装置还包括臭氧处理前排气组分检测单元，用于检测臭氧处理前排气组分含量。
169.本发明提供的示例169：包括上述示例167至168中的任一项，其中，所述控制单元根据所述臭氧处理前排气组分含量控制混合反应所需臭氧量。
170.本发明提供的示例170：包括上述示例168或169，其中，所述臭氧处理前排气组分检测单元选自以下检测单元中至少一个：
第一挥发性有机化合物检测单元，用于检测臭氧处理前排气中挥发性有机化合物含量；
第一CO检测单元，用于检测臭氧处理前排气中CO含量；
第一氮氧化物检测单元，用于检测臭氧处理前排气中氮氧化物含量。
171.本发明提供的示例171：包括上述示例170，其中，所述控制单元根据至少一个所述臭氧处理前排气组分检测单元的输出值控制混合反应所需臭氧量。
172.本发明提供的示例172：包括上述示例167至171中的任一项，其中，所述控制单元用于按照预设的数学模型控制混合反应所需臭氧量。
173.本发明提供的示例173：包括上述示例167至172中的任一项，其中，所述控制单元用于按照理论估计值控制混合反应所需臭氧量。
174.本发明提供的示例174：包括上述示例173中的任一项，其中，所述理论估计值为：臭氧通入量与排气中待处理物的摩尔比为2-10。
175.本发明提供的示例175：包括上述示例167至174中的任一项，其中，所述臭氧量控制装置包括臭氧处理后排气组分检测单元，用于检测臭氧处理后排气组分含量。
176.本发明提供的示例176：包括上述示例167至175中的任一项，其中，所述控制单元根据所述臭氧处理后排气组分含量控制混合反应所需臭氧量。
177.本发明提供的示例177：包括上述示例175或176，其中，所述臭氧处理后排气组分检测单元选自以下检测单元中至少一个：
第一臭氧检测单元，用于检测臭氧处理后排气中臭氧含量；
第二挥发性有机化合物检测单元，用于检测臭氧处理后排气中挥发性有机化合物含量；
第二CO检测单元，用于检测臭氧处理后排气中CO含量；
第二氮氧化物检测单元，用于检测臭氧处理后排气中氮氧化物含量。
178.本发明提供的示例178：包括上述示例177，其中，所述控制单元根据至少一个所述臭氧处理后排气组分检测单元的输出值控制臭氧量。
179.本发明提供的示例179：包括上述示例145至178中的任一项，其中，所述臭氧净化系统还包括脱硝装置，用于脱除臭氧流股与排气流股混合反应产物中的硝酸。
180.本发明提供的示例180：包括上述示例179，其中，所述脱硝装置包括电凝装置，所述电凝装置包括：
电凝流道；
第一电极，所述第一电极位于电凝流道中；
第二电极。
181.本发明提供的示例181：包括上述示例180，其中，所述第一电极为固体、液体、气体分子团、等离子体、导电混合态物质、生物体自然混合导电物质、或物体人工加工形成导电物质中的一种或多种形态的组合。
182.本发明提供的示例182：包括上述示例180或181，其中，所述第一电极为固态金属、石墨、或304钢。
183.本发明提供的示例183：包括上述示例180至182中的任一项，其中，所述第一电极呈点状、线状、网状、孔板状、板状、针棒状、球笼状、盒状、管状、自然形态物质、或加工形态物质。
184.本发明提供的示例184：包括上述示例180至183中的任一项，其中，所述第一电极上设有前通孔。
185.本发明提供的示例185：包括上述示例184，其中，所述前通孔的形状为多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形。
186.本发明提供的示例186：包括上述示例184或185，其中，所述前通孔的孔径为0.1-3毫米。
187.本发明提供的示例187：包括上述示例180至186中的任一项，其中，所述第二电极呈多层网状、网状、孔板状、管状、桶状、球笼状、盒状、板状、颗粒堆积层状、折弯板状、或面板状。
188.本发明提供的示例188：包括上述示例180至187中的任一项，其中，所述第二电极上设有后通孔。
189.本发明提供的示例189：包括上述示例188，其中，所述后通孔呈多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形。
190.本发明提供的示例190：包括上述示例188或189，其中，所述后通孔的孔径为0.1-3毫米。
191.本发明提供的示例191：包括上述示例180至190中的任一项，其中，所述第二电极由导电物质制成。
192.本发明提供的示例192：包括上述示例180至191中的任一项，其中，所述第二电极的表面具有导电物质。
193.本发明提供的示例193：包括上述示例180至192中的任一项，其中，所述第一电极和第二电极之间具有电凝电场，所述电凝电场为点面电场、线面电场、网面电场、点桶电场、线桶电场、或网桶电场中的一种或多种电场的组合。
194.本发明提供的示例194：包括上述示例180至193中的任一项，其中，所述第一电极呈线状，所述第二电极呈面状。
195.本发明提供的示例195：包括上述示例180至194中的任一项，其中，所述第一电极垂直于第二电极。
196.本发明提供的示例196：包括上述示例180至195中的任一项，其中，所述第一电极与第二电极相平行。
197.本发明提供的示例197：包括上述示例180至196中的任一项，其中，所述第一电极呈曲线状或圆弧状。
198.本发明提供的示例198：包括上述示例180至197中的任一项，其中，所述第一电极和第二电极均呈面状，且所述第一电极与第二电极相平行。
199.本发明提供的示例199：包括上述示例180至198中的任一项，其中，所述第一电极采用金属丝网。
200.本发明提供的示例200：包括上述示例180至199中的任一项，其中，所述第一电极呈平面状或球面状。
201.本发明提供的示例201：包括上述示例180至200中的任一项，其中，所述第二电极呈曲面状或球面状。
202.本发明提供的示例202：包括上述示例180至201中的任一项，其中，所述第一电极呈点状、线状、或网状，所述第二电极呈桶状，所述第一电极位于第二电极的内部，且所述第一电极位于第二电极的中心对称轴上。
203.本发明提供的示例203：包括上述示例180至202中的任一项，其中，所述第一电极与电源的一个电极电性连接，所述第二电极与电源的另一个电极电性连接。
204.本发明提供的示例204：包括上述示例180至203中的任一项，其中，所述第一电极与电源的阴极电性连接，所述第二电极与电源的阳极电性连接
205.本发明提供的示例205：包括上述示例203或204，其中，所述电源的电压为5-50KV。
206.本发明提供的示例206：包括上述示例203至205中的任一项，其中，所述电源的电压小于起始起晕电压。
207.本发明提供的示例207：包括上述示例203至206中的任一项，其中，所述电源的电压为0.1kv-2kv/mm。
208.本发明提供的示例208：包括上述示例203至207中的任一项，其中，所述电源的电压波形为直流波形、正弦波、或调制波形。
209.本发明提供的示例209：包括上述示例203至208中的任一项，其中，所述电源为交流电源，所述电源的变频脉冲范围为0.1Hz-5GHz。
210.本发明提供的示例210：包括上述示例180至209中的任一项，其中，所述第一电极和第二电极均沿左右方向延伸，所述第一电极的左端位于第二电极的左端的左方。
211.本发明提供的示例211：包括上述示例180至210中的任一项，其中，所述第二电极有两个，所述第一电极位于两个第二电极之间。
212.本发明提供的示例212：包括上述示例180至211中的任一项，其中，所述第一电极和第二电极之间的距离为5-50毫米。
213.本发明提供的示例213：包括上述示例180至212中的任一项，其中，所述第一电极和第二电极构成吸附单元，且所述吸附单元有多个。
214.本发明提供的示例214：包括上述示例213，其中，全部吸附单元沿左右方向、前后方向、斜向、或螺旋方向中的一个方向或多个方向上进行分布。
215.本发明提供的示例215：包括上述示例180至214中的任一项，其中，还包括电凝壳体，所述电凝壳体包括电凝进口、电凝出口、及所述电凝流道，所述电凝流道的两端分别与电凝进口和电凝出口相连通。
216.本发明提供的示例216：包括上述示例215，其中，所述电凝进口呈圆形，且所述电凝进口的直径为300-1000mm、或500mm。
217.本发明提供的示例217：包括上述示例215或216，其中，所述电凝出口呈圆形，且所述电凝出口的直径为300-1000mm、或500mm。
218.本发明提供的示例218：包括上述示例215至217中的任一项，其中，所述电凝壳体包括由电凝进口至电凝出口方向依次分布的第一壳体部、第二壳体部、及第三壳体部，所述电凝进口位于第一壳体部的一端，所述电凝出口位于第三壳体部的一端。
219.本发明提供的示例219：包括上述示例218，其中，所述第一壳体部的轮廓大小由电 凝进口至电凝出口方向逐渐增大。
220.本发明提供的示例220：包括上述示例218或219，其中，所述第一壳体部呈直管状。
221.本发明提供的示例221：包括上述示例218至220中的任一项，其中，所述第二壳体部呈直管状，且所述第一电极和第二电极安装在第二壳体部中。
222.本发明提供的示例222：包括上述示例218至221中的任一项，其中，所述第三壳体部的轮廓大小由电凝进口至电凝出口方向逐渐减小。
223.本发明提供的示例223：包括上述示例218至222中的任一项，其中，所述第一壳体部、第二壳体部、及第三壳体部的截面均呈矩形。
224.本发明提供的示例224：包括上述示例215至223中的任一项，其中，所述电凝壳体的材质为不锈钢、铝合金、铁合金、布、海绵、分子筛、活性炭、泡沫铁、或泡沫碳化硅。
225.本发明提供的示例225：包括上述示例180至224中的任一项，其中，所述第一电极通过电凝绝缘件与电凝壳体相连接。
226.本发明提供的示例226：包括上述示例225，其中，所述电凝绝缘件的材质为绝缘云母。
227.本发明提供的示例227：包括上述示例225或226，其中，所述电凝绝缘件呈柱状、或塔状。
228.本发明提供的示例228：包括上述示例180至227中的任一项，其中，所述第一电极上设有呈圆柱形的前连接部，且所述前连接部与电凝绝缘件固接。
229.本发明提供的示例229：包括上述示例180至228中的任一项，其中，所述第二电极上设有呈圆柱形的后连接部，且所述后连接部与电凝绝缘件固接。
230.本发明提供的示例230：包括上述示例180至229中的任一项，其中，所述第一电极的截面面积与电凝流道的截面面积比为99％-10％、或90-10％、或80-20％、或70-30％、或60-40％、或50％。
231.本发明提供的示例231：包括上述示例179至230中的任一项，其中，所述脱硝装置包括冷凝单元，用于将臭氧处理后的排气进行冷凝，实现气液分离。
232.本发明提供的示例232：包括上述示例179至231中的任一项，其中，所述脱硝装置包括淋洗单元，用于将臭氧处理后的排气进行淋洗。
233.本发明提供的示例233：包括上述示例232，其中，所述脱硝装置还包括淋洗液单元，用于向所述淋洗单元提供淋洗液。
234.本发明提供的示例234：包括上述示例233，其中，所述淋洗液单元中淋洗液包括水 和/或碱。
235.本发明提供的示例235：包括上述示例179至234中的任一项，其中，所述脱硝装置还包括脱硝液收集单元，用于存储排气中脱除的硝酸水溶液和/或硝酸盐水溶液。
236.本发明提供的示例236：包括上述示例235，其中，当所述脱硝液收集单元中存储有硝酸水溶液时，所述脱硝液收集单元设有碱液加入单元，用于与硝酸形成硝酸盐。
237.本发明提供的示例237：包括上述示例145至236中的任一项，其中，所述臭氧净化系统还包括臭氧消解器，用于消解经反应场处理后的排气中的臭氧。
238.本发明提供的示例238：包括上述示例237，其中，所述臭氧消解器选自紫外线臭氧消解器和催化臭氧消解器中的至少一种。
239.本发明提供的示例239：包括上述示例145至238中的任一项，其中，所述臭氧净化系统还包括第一脱硝装置，用于脱除排气中氮氧化物；所述反应场用于将经所述第一脱硝装置处理后的排气与臭氧流股混合反应，或者，用于将排气在经所述第一脱硝装置处理前先与臭氧流股混合反应。
240.本发明提供的示例240：包括上述示例239，其中，所述第一脱硝装置选自非催化还原装置、选择性催化还原装置、非选择性催化还原装置和电子束脱硝装置中的至少一种。
241.本发明提供的示例241：一种排气电场除炭黑方法，包括以下步骤：
使含尘气体通过除尘电场阳极和除尘电场阴极产生的电离除尘电场；
电场积尘时，进行清理炭黑处理。
242.本发明提供的示例242：包括示例241的排气电场除炭黑方法，其中，利用电场反电晕放电现象完成清理炭黑处理。
243.本发明提供的示例243：包括示例241的排气电场除炭黑方法，其中，利用电场反电晕放电现象，增高电压，限制入注电流，完成清理炭黑处理。
244.本发明提供的示例244：包括示例241的排气电场除炭黑方法，其中，利用电场反电晕放电现象，增高电压，限制入注电流，使发生在阳极积尘位置的急剧放电产生等离子，所述等离子使清理炭黑有机成分深度氧化，高分子键断裂，形成小分子二氧化碳和水，完成清理炭黑处理。
245.本发明提供的示例245：包括示例241至244任一项的排气电场除炭黑方法，其中，当所述电场装置检测到电场电流增加到一个给定值，所述电场装置进行清尘处理。
246.本发明提供的示例246：包括示例241至245任一项的排气电场除炭黑方法，其中，所述除尘电场阴极包括至少一根电极棒。
247.本发明提供的示例247：包括示例246的排气电场除炭黑方法，其中，所述电极棒的直径不大于3mm。
248.本发明提供的示例248：包括示例246或247的排气电场除炭黑方法，其中，所述电极棒的形状呈针状、多角状、毛刺状、螺纹杆状或柱状。
249.本发明提供的示例249：包括示例241至248任一项的排气电场除炭黑方法，其中，所述除尘电场阳极由中空的管束组成。
250.本发明提供的示例250：包括示例249的排气电场除炭黑方法，其中，所述阳极管束的中空的截面采用圆形或多边形。
251.本发明提供的示例251：包括示例250的排气电场除炭黑方法，其中，所述多边形为六边形。
252.本发明提供的示例252：包括示例249至251任一项的排气电场除炭黑方法，其中，所述除尘电场阳极的管束呈蜂窝状。
253.本发明提供的示例253：包括示例241至252任一项的排气电场除炭黑方法，其中，所述除尘电场阴极穿射于所述除尘电场阳极内。
254.本发明提供的示例254：包括示例241至253任一项的排气电场除炭黑方法，其中，当检测到的电场电流增加到一个给定值时，进行清理炭黑处理。
255.本发明提供的示例255：一种减少排气除尘电场耦合的方法，包括以下步骤：
选择除尘电场阳极参数或/和除尘电场阴极参数以减少电场耦合次数。
256.本发明提供的示例256：包括示例255的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极的集尘面积与除尘电场阴极的放电面积的比。
257.本发明提供的示例257：包括示例256的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
258.本发明提供的示例258：包括示例256的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为6.67：1-56.67：1。
259.本发明提供的示例259：包括示例255至258任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阴极直径为1-3毫米，所述除尘电场阳极与所述除尘电场阴极的极间距为2.5-139.9毫米；所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
260.本发明提供的示例260：包括示例255至259任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极和所述除尘电场阴极的极间距小于150mm。
261.本发明提供的示例261：包括示例255至259任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极与所述除尘电场阴极的极间距为2.5-139.9mm。
262.本发明提供的示例262：包括示例255至259任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极与所述除尘电场阴极的极间距为5-100mm。
263.本发明提供的示例263：包括示例255至262任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极长度为10-180mm。
264.本发明提供的示例264：包括示例255至262任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极长度为60-180mm。
265.本发明提供的示例265：包括示例255至264任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阴极长度为30-180mm。
266.本发明提供的示例266：包括示例255至264任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阴极长度为54-176mm。
267.本发明提供的示例267：包括示例255至266任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阴极包括至少一根电极棒。
268.本发明提供的示例268：包括示例267的减少排气除尘电场耦合的方法，其中，包括选择所述电极棒的直径不大于3mm。
269.本发明提供的示例269：包括示例267或268的减少排气除尘电场耦合的方法，其中，包括选择所述电极棒的形状呈针状、多角状、毛刺状、螺纹杆状或柱状。
270.本发明提供的示例270：包括示例255至269任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极由中空的管束组成。
271.本发明提供的示例271：包括示例270的减少排气除尘电场耦合的方法，其中，包括选择所述阳极管束的中空的截面采用圆形或多边形。
272.本发明提供的示例272：包括示例271的减少排气除尘电场耦合的方法，其中，包括选择所述多边形为六边形。
273.本发明提供的示例273：包括示例270至272任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阳极的管束呈蜂窝状。
274.本发明提供的示例274：包括示例255至273任一项的减少排气除尘电场耦合的方法，其中，包括选择所述除尘电场阴极穿射于所述除尘电场阳极内。
275.本发明提供的示例275：包括示例255至274任一项的减少排气除尘电场耦合的方法，其中，包括选择的所述除尘电场阳极或/和除尘电场阴极尺寸使电场耦合次数≤3。
276.本发明提供的示例276：一种排气除尘方法，包括以下步骤：排气温度低于100℃时，脱除排气中的液体水，然后电离除尘。
277.本发明提供的示例277：包括示例276的排气除尘方法，其中，排气温度≥100℃时，对排气进行电离除尘。
278.本发明提供的示例278：包括示例276或277的排气除尘方法，其中，排气温度≤90℃时，脱除排气中的液体水，然后电离除尘。
279.本发明提供的示例279：包括示例276或277的排气除尘方法，其中，排气温度≤80℃时，脱除排气中的液体水，然后电离除尘。
280.本发明提供的示例280：包括示例276或277的排气除尘方法，其中，排气温度≤70℃时，脱除排气中的液体水，然后电离除尘。
281.本发明提供的示例281：包括示例276或277的排气除尘方法，其中，采用电凝除雾方法脱除排气中的液体水，然后电离除尘。
282.本发明提供的示例282：一种排气除尘方法，包括以下步骤：在电离除尘电场之前添加包括氧气的气体，进行电离除尘。
283.本发明提供的示例283：包括示例282的排气除尘方法，其中，通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气。
284.本发明提供的示例284：包括示例282或283的排气除尘方法，其中，至少根据排气颗粒含量决定补氧量。
285.本发明提供的示例285：一种排气除尘方法，包括如下步骤：
1)利用电离除尘电场吸附排气中的颗粒物；
2)利用电离除尘电场给驻极体元件充电。
286.本发明提供的示例286：包括示例285的排气除尘方法，其中，所述驻极体元件靠近除尘电场装置出口，或者，所述驻极体元件设于除尘电场装置出口。
287.本发明提供的示例287：包括示例285的排气除尘方法，其中，所述除尘电场阳极和所述除尘电场阴极形成排气流道，所述驻极体元件设于所述排气流道中。
288.本发明提供的示例288：包括示例287的排气除尘方法，其中，所述排气流道包括排气流道出口，所述驻极体元件靠近所述排气流道出口，或者，所述驻极体元件设于所述排气流道出口。
289.本发明提供的示例289：包括示例282至288任一项的排气除尘方法，其中，当电离除尘电场无上电驱动电压时，利用充电的驻极体元件吸附排气中的颗粒物。
290.本发明提供的示例290：包括示例288的排气除尘方法，其中，在充电的驻极体元件吸附一定的排气中的颗粒物后，将其替换为新的驻极体元件。
291.本发明提供的示例291：包括示例290的排气除尘方法，其中，替换为新的驻极体元件后重新启动电离除尘电场吸附排气中的颗粒物，并给新的驻极体元件充电。
292.本发明提供的示例292：包括示例285至291任一项的排气除尘方法，其中，所述驻极体元件的材料包括具有驻极性能的无机化合物。
293.本发明提供的示例293：包括示例292的排气除尘方法，其中，所述无机化合物选自含氧化合物、含氮化合物或玻璃纤维中的一种或多种组合。
294.本发明提供的示例294：包括示例293的排气除尘方法，其中，所述含氧化合物选自金属基氧化物、含氧复合物、含氧的无机杂多酸盐中的一种或多种组合。
295.本发明提供的示例295：包括示例294的排气除尘方法，其中，所述金属基氧化物选自氧化铝、氧化锌、氧化锆、氧化钛、氧化钡、氧化钽、氧化硅、氧化铅、氧化锡中的一种或多种组合。
296.本发明提供的示例296：包括示例294的排气除尘方法，其中，所述金属基氧化物为氧化铝。
297.本发明提供的示例297：包括示例294的排气除尘方法，其中，所述含氧复合物选自钛锆复合氧化物或钛钡复合氧化物中的一种或多种组合。
298.本发明提供的示例298：包括示例294的排气除尘方法，其中，所述含氧的无机杂多酸盐选自钛酸锆、锆钛酸铅或钛酸钡中的一种或多种组合。
299.本发明提供的示例299：包括示例293的排气除尘方法，其中，所述含氮化合物为氮化硅。
300.本发明提供的示例300：包括示例285至291任一项的排气除尘方法，其中，所述驻极体元件的材料包括具有驻极性能的有机化合物。
301.本发明提供的示例301：包括示例300的排气除尘方法，其中，所述有机化合物选自氟聚合物、聚碳酸酯、PP、PE、PVC、天然蜡、树脂、松香中的一种或多种组合。
302.本发明提供的示例302：包括示例301的排气除尘方法，其中，所述氟聚合物选自聚四氟乙烯、聚全氟乙丙烯、可溶性聚四氟乙烯、聚偏氟乙烯中的一种或多种组合。
303.本发明提供的示例303：包括示例301的排气除尘方法，其中，所述氟聚合物为聚四氟乙烯。
附图说明
图1为本发明排气臭氧净化系统的示意图。
图2为本发明臭氧发生器用电极的示意图一。
图3为本发明臭氧发生器用电极的示意图二。
图4为现有技术中放电式臭氧发生器结构原理图。
图5为本发明实施例1排气除尘系统的示意图。
图6为本发明实施例2排气除尘系统的示意图。
图7为本发明排气处理系统中排气处理装置于一实施例中的立体结构示意图。
图8为本发明排气处理系统中排气处理装置呈伞状的绝缘机构于一实施例中的结构示意图。
图9A为本发明排气处理系统中排气处理装置的均风装置的一种实施结构图。
图9B为本发明排气处理系统中排气处理装置的均风装置的另一种实施结构图。
图9C为本发明排气处理系统中排气处理装置的均风装置的又一种实施结构图。
图10为本发明实施例4排气臭氧净化系统的示意图。
图11为本发明实施例4排气臭氧净化系统中反应场的俯视图。
图12为本发明臭氧量控制装置的示意图。
图13为电场发生单元结构示意图。
图14为图13电场发生单元的A-A视图。
图15为标注长度和角度的图13电场发生单元的A-A视图。
图16为两个电场级的电场装置结构示意图。
图17为本发明实施例24中电场装置的结构示意图。
图18为本发明实施例26中电场装置的结构示意图。
图19为本发明实施例27中电场装置的结构示意图。
图20为本发明中实施例29中排气除尘系统的结构示意图。
图21为本发明实施例29中叶轮涵道的结构示意图。
图22为本发明实施例30中电凝装置的结构示意图。
图23为本发明实施例30中电凝装置的左视图。
图24为本发明实施例30中电凝装置的立体图。
图25为本发明实施例31中电凝装置的结构示意图。
图26为本发明实施例31中电凝装置的俯视图。
图27为本发明实施例32中电凝装置的结构示意图。
图28为本发明实施例33中电凝装置的结构示意图。
图29为本发明实施例34中电凝装置的结构示意图。
图30为本发明实施例35中电凝装置的结构示意图。
图31为本发明实施例36中电凝装置的结构示意图。
图32为本发明实施例37中电凝装置的结构示意图。
图33为本发明实施例38中电凝装置的结构示意图。
图34为本发明实施例39中电凝装置的结构示意图。
图35为本发明实施例40中电凝装置的结构示意图。
图36为本发明实施例41中电凝装置的结构示意图。
图37为本发明实施例42中电凝装置的结构示意图。
图38为本发明实施例43中电凝装置的结构示意图。
图39为本发明实施例44中排气处理系统的结构示意图。
图40为本发明实施例45中排气处理系统的结构示意图。
图41为本发明实施例46中排气处理系统的结构示意图。
图42为本发明实施例47中排气处理系统的结构示意图。
图43为本发明实施例48中排气处理系统的结构示意图。
图44为本发明实施例49中排气处理系统的结构示意图。
图45为本发明实施例50中排气处理系统的结构示意图。
图46为本发明实施例51中排气处理系统的结构示意图。
图47为本发明实施例52中排气处理系统的结构示意图。
图48为本发明实施例53中排气降温装置的结构示意图。
图49为本发明实施例54中排气降温装置的结构示意图。
图50为本发明实施例55中排气降温装置的结构示意图。
图51为本发明实施例55中换热单元的结构示意图。
图52为本发明实施例56中排气降温装置的结构示意图。
具体实施方式
以下由特定的具体实施例说明本发明的实施方式，熟悉此技术的人士可由本说明书所揭露的内容轻易地了解本发明的其他优点及功效。
须知，本说明书所附图式所绘示的结构、比例、大小等，均仅用以配合说明书所揭示的 内容，以供熟悉此技术的人士了解与阅读，并非用以限定本发明可实施的限定条件，故不具技术上的实质意义，任何结构的修饰、比例关系的改变或大小的调整，在不影响本发明所能产生的功效及所能达成的目的下，均应仍落在本发明所揭示的技术内容得能涵盖的范围内。同时，本说明书中所引用的如“上”、“下”、“左”、“右”、“中间”及“一”等的用语，亦仅为便于叙述的明了，而非用以限定本发明可实施的范围，其相对关系的改变或调整，在无实质变更技术内容下，当亦视为本发明可实施的范畴。
根据本发明的一个方面，排气处理系统，包括排气除尘系统和排气臭氧净化系统。
于本发明一实施例中排气处理系统包括排气除尘系统。排气除尘系统与排气排放设备的出口相连通。排气排放设备排放的排气将流经排气除尘系统。
于本发明一实施例中，所述排气除尘系统还包括除水装置，用于在电场装置入口之前去除液体水。
于本发明一实施例中，当排气温度或排气排放设备温度低于一定温度时，排气中可能含有液体水，所述除水装置脱除排气中的液体水。
于本发明一实施例中，所述一定温度在90℃以上、100℃以下。
于本发明一实施例中，所述一定温度在80℃以上、90℃以下。
于本发明一实施例中，所述一定温度为80℃以下。
于本发明一实施例中，所述除水装置为电凝装置。
本领域技术人员没有认识到如下技术问题：在排气温度低时，排气中会有液体水，吸附在除尘电场阴极和除尘电场阳极上，造成电离除尘电场放电不均匀、打火，而本申请的发明人发现此问题，并提出排气除尘系统设置除水装置，用于在电场装置入口之前去除液体水，液体水具有导电性，会缩短电离距离，导致电离除尘电场放电不均匀，易导致电极击穿。所述除水装置在排气排放设备冷启动时，在排气进入电场装置入口之前脱除排气中的水珠即液体水，从而减少排气中的水珠即液体水，减少电离除尘电场放电不均匀及除尘电场阴极和除尘电场阳极击穿，从而提高电离除尘效率，取得预料不到的技术效果。所述除水装置没有特别的限制，现有技术中能实现去除排气中的液体水都适用本发明。
于本发明一实施例中，所述排气除尘系统还包括补氧装置，用于在电离除尘电场之前添加包括氧气的气体，比如空气。
于本发明一实施例中，所述补氧装置通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气。
于本发明一实施例中，至少根据排气颗粒含量决定补氧量。
本领域技术人员没有认识到如下技术问题：在某些情况下，排气会没有足够的氧气产生足够的氧离子，造成除尘效果不好，即，本领域技术人员没有认识到排气中的氧气可能不足以支持有效电离，而本申请的发明人发现此问题，并提出本发明排气除尘系统：包括补氧装置，可以通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气，提高进入电离除尘电场排气含氧量，从而当排气流经除尘电场阴极和除尘电场阳极之间的电离除尘电场时，增加电离的氧气，使得排气中更多的粉尘荷电，进而在除尘电场阳极的作用下将更多的荷电的粉尘收集起来，使得电场装置的除尘效率更高，有利于电离除尘电场收集排气颗粒物，取得预料不到的技术效果，同时还取得新的技术效果：能起到降温的作用，增加电力系统效率，而且，补氧也会提高电离除尘电场臭氧含量，有利于提高电离除尘电场对排气中有机物进行净化、自洁、脱硝等处理的效率。
于本发明一实施例中排气系统可包括均风装置。该均风装置设置在排气电场装置之前，能使进入电场装置的气流均匀通过。
于本发明一实施例中电场装置的除尘电场阳极可为立方体，均风装置可包括位于阴极支撑板一侧边的进气管、及位于阴极支撑板另一侧边的出气管，阴极支撑板位于除尘电场阳极的进气端；其中，安装进气管的侧边与安装出气管的侧边相对立。均风装置能使进入电场装置的排气均匀通过静电场。
于本发明一实施例中除尘电场阳极可为圆柱体，均风装置在所述除尘系统入口与所述除尘电场阳极和所述除尘电场阴极形成的电离除尘电场之间，且均风装置包括若干围绕电场装置入口中心旋转的均风叶片。均风装置能够使各种变化的进气量均匀通过除尘电场阳极产生的电场，同时，能够保持除尘电场阳极内部温度恒定，氧气充足。均风装置能使进入电场装置的排气均匀通过静电场。
于本发明一实施例中均风装置包括设置于除尘电场阳极的进气端的进风板和设置于除尘电场阳极出气端的出风板，进风板上开设有进气孔，出风板上开设有出气孔，进气孔与出气孔错位排布，且正面进气、侧面出气，形成旋风结构。均风装置能使进入电场装置的排气均匀通过静电场。
于本发明一实施例中排气除尘系统可包括除尘系统入口、除尘系统出口和电场装置。且于本发明一实施例中电场装置可包括电场装置入口、电场装置出口、及位于电场装置入口和电场装置出口之间的前置电极，当排气排放设备排放的排气由电场装置入口流经前置电极时，排气中的颗粒物等将带电。
于本发明一实施例中电场装置包括前置电极，该前置电极在电场装置入口与除尘电场阳 极和除尘电场阴极形成的电离除尘电场之间。当气体由电场装置入口流经前置电极时，气体中的颗粒物等将带电。
于本发明一实施例中前置电极的形状可以为点状、线状、网状、孔板状、板状、针棒状、球笼状、盒状、管状、物质自然形态、或物质加工形态。当前置电极为有孔结构时，前置电极上设有一个或多个排气通孔。于本发明一实施例中排气通孔的形状可以为多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形。于本发明一实施例中排气通孔的轮廓大小可以为0.1～3mm、0.1～0.2mm、0.2～0.5mm、0.5～1mm、1～1.2mm、1.2～1.5mm、1.5～2mm、2～2.5mm、2.5～2.8mm、或2.8～3mm。
于本发明一实施例中前置电极的形态可以为固体、液体、气体分子团、等离子体、导电混合态物质、生物体自然混合导电物质、或物体人工加工形成导电物质中的一种或多种形态的组合。当前置电极为固体时，可采用固态金属，比如304钢，或其它固态的导体、比如石墨等。当前置电极为液体时，可以是含离子导电液体。
在工作时，在带污染物的气体进入除尘电场阳极和除尘电场阴极形成的电离除尘电场之前，且带污染物的气体通过前置电极时，前置电极使气体中的污染物带电。当带污染物的气体进入电离除尘电场时，除尘电场阳极给带电的污染物施加吸引力，使污染物向除尘电场阳极移动，直至污染物附着在除尘电场阳极上。
于本发明一实施例中前置电极将电子导入污染物，电子在位于前置电极和除尘电场阳极之间的污染物之间进行传递，使更多污染物带电。前置电极和除尘电场阳极之间通过污染物传导电子、并形成电流。
于本发明一实施例中前置电极通过与污染物接触的方式使污染物带电。于本发明一实施例中前置电极通过能量波动的方式使污染物带电。于本发明一实施例中前置电极通过与污染物接触的方式将电子转移到污染物上，并使污染物带电。于本发明一实施例中前置电极通过能量波动的方式将电子转移到污染物上，并使污染物带电。
于本发明一实施例中前置电极呈线状，除尘电场阳极呈面状。于本发明一实施例中前置电极垂直于除尘电场阳极。于本发明一实施例中前置电极与除尘电场阳极相平行。于本发明一实施例中前置电极呈曲线状或圆弧状。于本发明一实施例中前置电极采用金属丝网。于本发明一实施例中前置电极与除尘电场阳极之间的电压不同于除尘电场阴极和除尘电场阳极之间的电压。于本发明一实施例中前置电极与除尘电场阳极之间的电压小于起始起晕电压。起始起晕电压为除尘电场阴极和除尘电场阳极之间的电压的最小值。于本发明一实施例中前置电极与除尘电场阳极之间的电压可以为0.1-2kv/mm。
于本发明一实施例中电场装置包括排气流道，前置电极位于排气流道中。于本发明一实施例中前置电极的截面面积与排气流道的截面面积比为99％～10％、或90～10％、或80～20％、或70～30％、或60～40％、或50％。前置电极的截面面积是指前置电极沿截面上实体部分的面积之和。于本发明一实施例中前置电极带负电势。
于本发明一实施例中当排气通过电场装置入口流入排气流道中，排气中导电性较强的金属粉尘、雾滴、或气溶胶等污染物在与前置电极相接触时，或与前置电极的距离达到一定范围时会直接带负电，随后，全部污染物随气流进入电离除尘电场，除尘电场阳极给已带负电的金属粉尘、雾滴、或气溶胶等施加吸引力，使已带负电的污染物向除尘电场阳极移动，直至该部分污染物附着在除尘电场阳极上，实现将该部分污染物收集起来，同时，除尘电场阳极与除尘电场阴极之间形成的电离除尘电场通过电离气体中的氧获得氧离子，且带负电荷的氧离子在与普通粉尘结合后，使普通粉尘带负电荷，除尘电场阳极给该部分带负电荷的粉尘等污染物施加吸引力，使粉尘等污染物向除尘电场阳极移动，直至该部分污染物附着在除尘电场阳极上，实现将该部分普通粉尘等污染物也收集起来，从而将排气中导电性较强和导电性较弱的污染物均收集起来，并使得除尘电场阳极能收集排气中污染物的种类更广泛，且收集能力更强，收集效率更高。
于本发明一实施例中电场装置入口与排气排放设备的出口相连通。
于本发明一实施例中电场装置可包括除尘电场阴极和除尘电场阳极，除尘电场阴极与除尘电场阳极之间形成电离除尘电场。排气进入电离除尘电场，排气中的氧离子将被电离，并形成大量带有电荷的氧离子，氧离子与排气中粉尘等颗粒物结合，使得颗粒物荷电，除尘电场阳极给带负电荷的颗粒物施加吸附力，使得颗粒物被吸附在除尘电场阳极上，以清除掉排气中的颗粒物。
于本发明一实施例中除尘电场阴极包括若干根阴极丝。阴极丝的直径可为0.1mm-20mm，该尺寸参数根据应用场合及积尘要求做调整。于本发明一实施例中阴极丝的直径不大于3mm。于本发明一实施例中阴极丝使用容易放电的金属丝或合金丝，耐温且能支撑自身重量，电化学稳定。于本发明一实施例中阴极丝的材质选用钛。阴极丝的具体形状根据除尘电场阳极的形状调整，例如，若除尘电场阳极的积尘面是平面，则阴极丝的截面呈圆形；若除尘电场阳极的积尘面是圆弧面，阴极丝需要设计成多面形。阴极丝的长度根据除尘电场阳极进行调整。
于本发明一实施例中除尘电场阴极包括若干阴极棒。于本发明一实施例中阴极棒的直径不大于3mm。于本发明一实施例中阴极棒使用容易放电的金属棒或合金棒。阴极棒的形状可以为针状、多角状、毛刺状、螺纹杆状或柱状等。阴极棒的形状可以根据除尘电场阳极的形 状进行调整，例如，若除尘电场阳极的积尘面是平面，则阴极棒的截面需要设计成圆形；若除尘电场阳极的积尘面是圆弧面，则阴极棒需要设计成多面形。
于本发明一实施例中除尘电场阴极穿设于除尘电场阳极内。
于本发明一实施例中除尘电场阳极包括一个或多个并行设置的中空阳极管。当中空阳极管有多个时，全部中空阳极管构成蜂窝状的除尘电场阳极。于本发明一实施例中中空阳极管的截面可呈圆形或多边形。若中空阳极管的截面呈圆形，除尘电场阳极和除尘电场阴极之间能形成均匀电场，中空阳极管的内壁不容易积尘。若中空阳极管的截面为三边形时，中空阳极管的内壁上可以形成3个积尘面，3个远角容尘角，此种结构的中空阳极管的容尘率最高。若中空阳极管的截面为四边形，可以获得4个积尘面，4个容尘角，但拼组结构不稳定。若中空阳极管的截面为六边形，可以形成6个积尘面，6个容尘角，积尘面和容尘率达到平衡。若中空阳极管的截面呈更多边形时，可以获得更多的积尘边，但损失容尘率。于本发明一实施例中中空阳极管的管内切圆直径取值范围为5mm-400mm。
于本发明一实施例中除尘电场阴极安装在阴极支撑板上，阴极支撑板与除尘电场阳极通过绝缘机构相连接。于本发明一实施例中除尘电场阳极包括第一阳极部和第二阳极部，即所述第一阳极部靠近电场装置入口，第二阳极部靠近电场装置出口。阴极支撑板和绝缘机构在第一阳极部和第二阳极部之间，即绝缘机构安装在电离电场中间、或除尘电场阴极中间，可以对除尘电场阴极起到良好的支撑作用，并对除尘电场阴极起到相对于除尘电场阳极的固定作用，使除尘电场阴极和除尘电场阳极之间保持设定的距离。而现有技术中，阴极的支撑点在阴极的端点，难以保持阴极和阳极之间的距离。于本发明一实施例中绝缘机构设置在电场流道外、即第二级流道外，以防止或减少排气中的灰尘等聚集在绝缘机构上，导致绝缘机构击穿或导电。
于本发明一实施例中绝缘机构采用耐高压陶瓷绝缘子，对除尘电场阴极和除尘电场阳极之间进行绝缘。除尘电场阳极也称作一种外壳。
于本发明一实施例中第一阳极部在气体流动方向上位于阴极支撑板和绝缘机构之前，第一阳极部能够除去排气中的水，防止水进入绝缘机构，造成绝缘机构短路、打火。另外，第一阳极部能够除去排气中相当一部分的灰尘，当排气通过绝缘机构时，相当一部分的灰尘已被消除，减少灰尘造成绝缘机构短路的可能性。于本发明一实施例中绝缘机构包括绝缘瓷柱。第一阳极部的设计，主要是为了保护绝缘瓷柱不被气体中颗粒物等污染，一旦气体污染绝缘瓷柱将会造成除尘电场阳极和除尘电场阴极导通，从而使除尘电场阳极的积尘功能失效，故第一阳极部的设计，能有效减少绝缘瓷柱被污染，提高产品的使用时间。在排气流经第二级 流道过程中，第一阳极部和除尘电场阴极先接触具有污染性的气体，绝缘机构后接触气体，达到先除尘后经过绝缘机构的目的，减少对绝缘机构造成的污染，延长清洁维护周期，对应电极使用后绝缘支撑。于本发明一实施例中，所述第一阳极部的长度是足够的长，以清除部分灰尘，减少积累在所述绝缘机构和所述阴极支撑板上的灰尘，减少灰尘造成的电击穿。于本发明一实施例中第一阳极部长度占除尘电场阳极总长度的1/10至1/4、1/4至1/3、1/3至1/2、1/2至2/3、2/3至3/4，或3/4至9/10。
于本发明一实施例中第二阳极部在排气流动方向上位于阴极支撑板和绝缘机构之后。第二阳极部包括积尘段和预留积尘段。其中，积尘段利用静电吸附排气中的颗粒物，该积尘段是为了增加积尘面积，延长电场装置的使用时间。预留积尘段能为积尘段提供失效保护。预留积尘段是为了在满足设计除尘要求的前提下，进一步提高积尘面积。预留积尘段作为补充前段积尘使用。于本发明一实施例中预留积尘段和第一阳极部可使用不同的电源。
于本发明一实施例中由于除尘电场阴极和除尘电场阳极之间存在极高电位差，为了防止除尘电场阴极和除尘电场阳极导通，绝缘机构设置在除尘电场阴极和除尘电场阳极之间的第二级流道之外。因此，绝缘机构外悬于除尘电场阳极的外侧。于本发明一实施例中绝缘机构可采用非导体耐温材料，比如陶瓷、玻璃等。于本发明一实施例中，完全密闭无空气的材料绝缘要求绝缘隔离厚度>0.3mm/kv；空气绝缘要求>1.4mm/kv。可根据除尘电场阴极和除尘电场阳极之间的极间距的1.4倍设置绝缘距离。于本发明一实施例中绝缘机构使用陶瓷，表面上釉；不能使用胶粘或有机材料填充连接，耐温大于350摄氏度。
于本发明一实施例中绝缘机构包括绝缘部和隔热部。为了使绝缘机构具有抗污功能，绝缘部的材料采用陶瓷材料或玻璃材料。于本发明一实施例中绝缘部可为伞状串陶瓷柱或玻璃柱，伞内外挂釉。伞状串陶瓷柱或玻璃柱的外缘与除尘电场阳极的距离大于电场距离的1.4倍、即大于极间距的1.4倍。伞状串陶瓷柱或玻璃柱的伞突边间距总和大于伞状串陶瓷柱的绝缘间距的1.4倍。伞状串陶瓷柱或玻璃柱的伞边内深总长大于伞状串陶瓷柱的绝缘距离1.4倍。绝缘部还可为柱状串陶瓷柱或玻璃柱，柱内外挂釉。于本发明一实施例中绝缘部还可呈塔状。
于本发明一实施例中，绝缘部内设置加热棒，当绝缘部周围温度接近露点时，加热棒启动并进行加热。由于使用中绝缘部的内外存在温差，绝缘部的内外、外部容易产生凝露。绝缘部的外表面可能自发或被气体加热产生高温，需要必要的隔离防护，防烫伤。隔热部包括位于第二绝缘部外部的防护围挡板、脱硝净化反应腔。于本发明一实施例中绝缘部的尾部需要凝露位置同样需要隔热，防止环境以及散热高温加热凝露组件。
于本发明一实施例中排气电场装置的电源的引出线使用伞状串陶瓷柱或玻璃柱过墙式连 接，墙内使用弹性碰头连接阴极支撑板，墙外使用密闭绝缘防护接线帽插拔连接，引出线过墙导体与墙绝缘距离大于伞状串陶瓷柱或玻璃柱的陶瓷绝缘距离。于本发明一实施例中高压部分取消引线，直接安装在端头上，确保安全，高压模块整体外绝缘使用ip68防护，使用介质换热散热。
于本发明一实施例中除尘电场阴极和除尘电场阳极之间采用非对称结构。在对称电场中极性粒子受到一个相同大小而方向相反的作用力，极性粒子在电场中往复运动；在非对称电场中，极性粒子受到两个大小不同的作用力，极性粒子向作用力大的方向移动，可以避免产生耦合。
本发明的电场装置的除尘电场阴极和除尘电场阳极之间形成电离除尘电场。为了减少所述电离除尘电场的电场耦合，于本发明一实施例中，减少电场耦合的方法包括如下步骤：选择除尘电场阳极的集尘面积与除尘电场阴极的放电面积的比，使电场耦合次数≤3。于本发明一实施例中除尘电场阳极的集尘面积与除尘电场阴极的放电面积的比可以为：1.667：1-1680：1；3.334：1-113.34：1；6.67：1-56.67：1；13.34：1-28.33：1。该实施例选择相对大面积的除尘电场阳极的集尘面积和相对极小的除尘电场阴极的放电面积，具体选择上述面积比，可以减少除尘电场阴极的放电面积，减小吸力，扩大除尘电场阳极的集尘面积，扩大吸力，即除尘电场阴极和除尘电场阳极间产生不对称的电极吸力，使荷电后粉尘落入除尘电场阳极的集尘表面，虽极性改变但无法再被除尘电场阴极吸走，减少电场耦合，实现电场耦合次数≤3。即在电场极间距小于150mm时电场耦合次数≤3，电场能耗低，能够减少电场对气溶胶、水雾、油雾、松散光滑颗粒物的耦合消耗，节省电场电能30～50％。集尘面积是指除尘电场阳极工作面的面积，比如，若除尘电场阳极呈中空的正六边形管状，集尘面积即为中空的正六边形管状的内表面积，集尘面积也称作积尘面积。放电面积指除尘电场阴极工作面的面积，比如，若除尘电场阴极呈棒状，放电面积即为棒状的外表面积。
于本发明一实施例中除尘电场阳极的长度可以为10～180mm、10～20mm、20～30mm、60～180mm、30～40mm、40～50mm、50～60mm、60～70mm、70～80mm、80～90mm、90～100mm、100～110mm、110～120mm、120～130mm、130～140mm、140～150mm、150～160mm、160～170mm、170～180mm、60mm、180mm、10mm或30mm。除尘电场阳极的长度是指除尘电场阳极工作面的一端至另一端的最小长度。除尘电场阳极选择此种长度，可以有效减少电场耦合。
于本发明一实施例中除尘电场阳极的长度可以为10～90mm、15～20mm、20～25mm、25～30mm、30～35mm、35～40mm、40～45mm、45～50mm、50～55mm、55～60mm、60～65mm、65～70mm、70～75mm、75～80mm、80～85mm或85～90mm，此种长度的设计可以使除尘电场 阳极及电场装置具有耐高温特性，并使得电场装置在高温冲击下具有高效率的集尘能力。
于本发明一实施例中除尘电场阴极的长度可以为30～180mm、54～176mm、30～40mm、40～50mm、50～54mm、54～60mm、60～70mm、70～80mm、80～90mm、90～100mm、100～110mm、110～120mm、120～130mm、130～140mm、140～150mm、150～160mm、160～170mm、170～176mm、170～180mm、54mm、180mm、或30mm。除尘电场阴极的长度是指除尘电场阴极工作面的一端至另一端的最小长度。除尘电场阴极选择此种长度，可以有效减少电场耦合。
于本发明一实施例中除尘电场阴极的长度可以为10～90mm、15～20mm、20～25mm、25～30mm、30～35mm、35～40mm、40～45mm、45～50mm、50～55mm、55～60mm、60～65mm、65～70mm、70～75mm、75～80mm、80～85mm或85～90mm，此种长度的设计可以使除尘电场阴极及电场装置具有耐高温特性，并使得电场装置在高温冲击下具有高效率的集尘能力。其中，当电场温度为200℃时，对应的集尘效率为99.9％；电场温度为400℃时，对应的集尘效率为90％；当电场温度为500℃时，对应的集尘效率为50％。
于本发明一实施例中除尘电场阳极和除尘电场阴极之间的距离可以为5～30mm、2.5～139.9mm、9.9～139.9mm、2.5～9.9mm、9.9～20mm、20～30mm、30～40mm、40～50mm、50～60mm、60～70mm、70～80mm、80～90mm、90～100mm、100～110mm、110～120mm、120～130mm、130～139.9mm、9.9mm、139.9mm、或2.5mm。除尘电场阳极和除尘电场阴极之间的距离也称作极间距。极间距具体是指除尘电场阳极、除尘电场阴极工作面之间的最小垂直距离。此种极间距的选择可以有效减少电场耦合，并使排气电场装置具有耐高温特性。
于本发明一实施例中，所述除尘电场阴极直径为1-3毫米，所述除尘电场阳极与所述尾气除尘电场阴极的极间距为2.5-139.9毫米；所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
鉴于电离除尘的特有性能，电离除尘可适用去除气体中的颗粒物。但是，经过许多大学、研究机构、企业的多年的研究，现有电场除尘装置只能去除约70％的颗粒物，不能满足许多国家的排放标准。另外，现有技术中的电场除尘装置体积过于庞大。
本发明的发明人研究发现，现有技术中电场除尘装置的缺点是由电场耦合引起的。本发明通过减小电场耦合次数，可以显著减小电场除尘装置的尺寸(即体积)。比如，本发明提供的电离除尘装置的尺寸约为现有电离除尘装置尺寸的五分之一。原因是，为了获得可接受的颗粒去除率，现有电离除尘装置中将气体流速设为1m/s左右，而本发明在将气体流速提高到6m/s的情况下，仍能获得较高的颗粒去除率。当处理一给定流量的气体时，随着气体速度的提高，电场除尘装置的尺寸可以减小。
另外，本发明可以显著提高颗粒去除效率。例如，在气体流速为1m/s左右时，现有技术电场除尘装置可以去除发动机排气中大约70％的颗粒物，但是本发明可以去除大约99％的颗粒物，即使在气体流速为6m/s时。
由于发明人发现了电场耦合的作用，并且找到了减少电场耦合次数的方法，本发明获得了上述预料不到的结果。
除尘电场阳极和除尘电场阴极之间的电离除尘电场也称作第三电场。于本发明一实施例中除尘电场阳极和除尘电场阴极之间还形成有与第三电场不平行的第四电场。于本发明另一实施例中，所述第四电场与所述电离除尘电场的流道不垂直。第四电场也称作辅助电场，可以通过一个或两个第二辅助电极形成。当第四电场由一个第二辅助电极形成时，该第二辅助电极可以放在电离电场的进口或出口，该第二辅助电极可以带负电势、或正电势。其中，当所述第二辅助电极为阴极时，设置在或靠近所述电离除尘电场的进口；所述第二辅助电极与所述除尘电场阳极具有夹角α，且0°＜α≤125°、或45°≤α≤125°、或60°≤α≤100°、或α＝90°。当所述第二辅助电极为阳极时，设置在或靠近所述电离除尘电场的出口；所述第二辅助电极与所述除尘电场阴极具有夹角α，且0°＜α≤125°、或45°≤α≤125°、或60°≤α≤100°、或α＝90°。当第四电场由两个第二辅助电极形成时，其中一个第二辅助电极可以带负电势，另一个第二辅助电极可以带正电势；一个第二辅助电极可以放在电离除尘电场的进口，另一个第二辅助电极放在电离除尘电场的出口。另外，第二辅助电极可以是除尘电场阴极或除尘电场阳极的一部分，即第二辅助电极可以是由除尘电场阴极或除尘电场阳极的延伸段构成，此时除尘电场阴极和除尘电场阳极的长度不一样。第二辅助电极也可以是一个单独的电极，也就是说第二辅助电极可以不是除尘电场阴极或除尘电场阳极的一部分，此时，第四电场的电压和第三电场的电压不一样，可以根据工作状况单独地控制。
第四电场能给除尘电场阳极和除尘电场阴极之间带负电荷的氧离子流施加朝向电离电场的出口的力，使得除尘电场阳极和除尘电场阴极之间带负电荷的氧离子流具有向出口的移动速度。在排气流入电离电场，并向电离电场的出口方向流动过程中，带负电荷的氧离子也在向除尘电场阳极且向电离电场的出口方向移动，且带负电荷的氧离子在向除尘电场阳极且向电离电场的出口移动过程中将与排气中的颗粒物等相结合，由于氧离子具有向出口的移动速度，氧离子在与颗粒物相结合时，两者间不会产生较强的碰撞，从而避免因较强碰撞而造成较大的能量消耗，保证氧离子易于与颗粒物相结合，并使得气体中的颗粒物的荷电效率更高，进而在除尘电场阳极的作用下，能将更多的颗粒物收集起来，保证电场装置的除尘效率更高。电场装置对顺离子流方向进入电场的颗粒物的收集率比对逆离子流方向进入电场的颗粒物的 收集率提高近一倍，从而提高电场的积尘效率，减少电场电耗。另外，现有技术中集尘电场的除尘效率较低的主要原因也是粉尘进入电场方向与电场内离子流方向相反或垂直交叉，从而导致粉尘与离子流相互冲撞剧烈并产生较大能量消耗，同时也影响荷电效率，进而使现有技术中电场集尘效率下降，且能耗增加。电场装置在收集气体中的粉尘时，气体及粉尘顺离子流方向进入电场，粉尘荷电充分，电场消耗小；单极电场集尘效率会达到99.99％。当排气及粉尘逆离子流方向进入电场，粉尘荷电不充分，电场电耗也会增加，集尘效率会在40％-75％。于本发明一实施例中电场装置形成的离子流有利于无动力风扇流体输送、增氧、或热量交换等。
随着，除尘电场阳极持续收集排气中的颗粒物等，颗粒物等在除尘电场阳极上堆积并形成碳黑，且碳黑厚度不断增加，使极间距减小。于本发明一实施例中，待检测到电场电流增加，利用电场反电晕放电现象，配合增高电压，限制入注电流，使发生在积碳位置急剧放电产生大量等离子，这些低温等离子使碳黑中有机成分深度氧化，高分子键断裂，形成小分子二氧化碳和水，完成碳黑清洁。由于空气中的氧气同时参与电离，形成臭氧，臭氧分子团同时扑捉沉积的油污分子团，加速油污分子中碳氢键断裂，使部分油分子碳化，以达到排气挥发份净化目的。另外，碳黑清洁是利用等离子体来达到常规清洗方法无法达到的效果。等离子体是物质的一种状态，也叫做物质的第四态，并不属于常见的固、液、气三态。对气体施加足够的能量使之离化便成为等离子状态。等离子体的“活性”组分包括：离子、电子、原子、活性基团、激发态的核素(亚稳态)、光子等。于本发明一实施例中，当电场积尘时，所述电场装置检测电场电流，采用以下任一方式实现碳黑清洁：
(1)当电场电流增加到一个给定值，所述电场装置增高电场电压。
(2)当电场电流增加到一个给定值，所述电场装置利用电场反电晕放电现象完成碳黑清洁。
(3)当电场电流增加到一个给定值，所述电场装置利用电场反电晕放电现象，增高电压，限制入注电流，完成碳黑清洁。
(4)当电场电流增加到一个给定值，所述电场装置利用电场反电晕放电现象，增高电压，限制入注电流，使发生在阳极积碳位置的急剧放电产生等离子，所述等离子使碳黑有机成分深度氧化，高分子键断裂，形成小分子二氧化碳和水，完成碳黑清洁。
于本发明一实施例中除尘电场阳极和除尘电场阴极分别与电源的两个电极电性连接。加载在除尘电场阳极和除尘电场阴极上的电压需选择适当的电压等级，具体选择何种电压等级取决于电场装置的体积、耐温、容尘率等。例如，电压从1kv至50kv；设计时首先考虑耐温 条件，极间距与温度的参数：1MM<30度，积尘面积大于0.1平方/千立方米/小时，电场长度大于单管内切圆的5倍，控制电场气流流速小于9米/秒。于本发明一实施例中除尘电场阳极由第二中空阳极管构成、并呈蜂窝状。第二中空阳极管端口的形状可以为圆形或多边形。于本发明一实施例中第二中空阳极管的管内切圆取值范围在5-400mm，对应电压在0.1-120kv之间，第二中空阳极管对应电流在0.1-30A之间；不同的内切圆对应不同的电晕电压，约为1KV/1MM。
于本发明一实施例中电场装置包括第二电场级，该第二电场级包括若干个第二电场发生单元，第二电场发生单元可以有一个或多个。第二电场发生单元也称作第二集尘单元，第二集尘单元包括上述除尘电场阳极和除尘电场阴极，第二集尘单元有一个或多个。第二电场级有多个时，能有效提高电场装置的集尘效率。同一第二电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。且第二电场级有多个时，各第二电场级之间串联。于本发明一实施例中电场装置还包括若干个连接壳体，串联第二电场级通过连接壳体连接；相邻两级的第二电场级的距离大于极间距的1.4倍。
于本发明一实施例中用电场充电驻极体材料。电场装置有故障时，充电驻极体材料会用来除尘。
于本发明一实施例中，所述电场装置包括驻极体元件。
于本发明一实施例中，所述驻极体元件设于所述除尘电场阳极内。
于本发明一实施例中，所述除尘电场阳极和所述除尘电场阴极接通电源时排气，所述驻极体元件在所述电离除尘电场中。
于本发明一实施例中，所述驻极体元件靠近电场装置出口，或者，所述驻极体元件设于电场装置出口。
于本发明一实施例中，所述除尘电场阳极和所述除尘电场阴极形成排气流道，所述驻极体元件设于所述排气流道中。
于本发明一实施例中，所述排气流道包括排气流道出口，所述驻极体元件靠近所述排气流道出口，或者，所述驻极体元件设于所述排气流道出口。
于本发明一实施例中，所述驻极体元件于所述流道中的横截面占排气流道横截面5％～100％。
于本发明一实施例中，所述驻极体元件于所述排气流道中的横截面占排气流道横截面10％-90％、20％-80％、或40％-60％。
于本发明一实施例中，所述电离除尘电场给所述驻极体元件充电。
于本发明一实施例中，所述驻极体元件具有多孔结构。
于本发明一实施例中，所述驻极体元件为织品。
于本发明一实施例中，所述除尘电场阳极内部为管状，所述驻极体元件外部为管状，所述驻极体元件外部套设于所述除尘电场阳极内部。
于本发明一实施例中，所述驻极体元件与所述除尘电场阳极为可拆卸式连接。
于本发明一实施例中，所述驻极体元件的材料包括具有驻极性能的无机化合物。所述驻极性能是指驻极体元件在外接电源充电后带有电荷，并在完全脱离电源的条件下，依然保持有一定的电荷，从而作为电极起到电场电极作用的能力。
于本发明一实施例中，所述无机化合物选自含氧化合物、含氮化合物或玻璃纤维中的一种或多种组合。
于本发明一实施例中，所述含氧化合物选自金属基氧化物、含氧复合物、含氧的无机杂多酸盐中的一种或多种组合。
于本发明一实施例中，所述金属基氧化物选自氧化铝、氧化锌、氧化锆、氧化钛、氧化钡、氧化钽、氧化硅、氧化铅、氧化锡中的一种或多种组合。
于本发明一实施例中，所述金属基氧化物为氧化铝。
于本发明一实施例中，所述含氧复合物选自钛锆复合氧化物或钛钡复合氧化物中的一种或多种组合。
于本发明一实施例中，所述含氧的无机杂多酸盐选自钛酸锆、锆钛酸铅或钛酸钡中的一种或多种组合。
于本发明一实施例中，所述含氮化合物为氮化硅。
于本发明一实施例中，所述驻极体元件的材料包括具有驻极性能的有机化合物。所述驻极性能是指驻极体元件在外接电源充电后带有电荷，并在完全脱离电源的条件下，依然保持有一定的电荷，从而作为电极起到电场电极作用的能力。
于本发明一实施例中，所述有机化合物选自氟聚合物、聚碳酸酯、PP、PE、PVC、天然蜡、树脂、松香中的一种或多种组合。
于本发明一实施例中，所述氟聚合物选自聚四氟乙烯(PTFE)、聚全氟乙丙烯(Teflon-FEP)、可溶性聚四氟乙烯(PFA)、聚偏氟乙烯(PVDF)中的一种或多种组合。
于本发明一实施例中，所述氟聚合物为聚四氟乙烯。
在上电驱动电压条件下产生电离除尘电场，利用电离除尘电场电离部分待处理物，吸附排气中的颗粒物，同时向驻极体元件进行充电，当电场装置出现故障时即无上电驱动电压时， 充电的驻极体元件产生电场，利用充电的驻极体元件产生的电场吸附排气中的颗粒物，即在电离除尘电场出现故障情况下仍然可以进行颗粒物的吸附。
一种排气除尘方法，包括以下步骤：排气温度低于100℃时，脱除排气中的液体水，然后电离除尘。
于本发明一实施例中，排气温度≥100℃时，对排气进行电离除尘。
于本发明一实施例中，排气温度≤90℃时，脱除排气中的液体水，然后电离除尘。
于本发明一实施例中，排气温度≤80℃时，脱除排气中的液体水，然后电离除尘。
于本发明一实施例中，排气温度≤70℃时，脱除排气中的液体水，然后电离除尘。
于本发明一实施例中，采用电凝除雾方法脱除排气中的液体水，然后电离除尘。
一种排气除尘方法，包括以下步骤：在电离除尘电场之前添加包括氧气的气体，进行电离除尘。
于本发明一实施例中，通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气。
于本发明一实施例中，至少根据排气颗粒含量决定补氧量。
对于排气系统，于本发明一实施例中，本发明提供一种电场除尘方法，包括以下步骤：
使含尘气体通过除尘电场阳极和除尘电场阴极产生的电离除尘电场；
电场积尘时，进行清尘处理。
于本发明一实施例中，当检测到的电场电流增加到一个给定值时，进行清尘处理。
于本发明一实施例中，当电场积尘时，通过以下任一方式进行灰尘清洁：
(1)利用电场反电晕放电现象完成清尘处理。
(2)利用电场反电晕放电现象，增高电压，限制入注电流，完成清尘处理。
(3)利用电场反电晕放电现象，增高电压，限制入注电流，使发生在阳极积尘位置的急剧放电产生等离子，所述等离子使灰尘有机成分深度氧化，高分子键断裂，形成小分子二氧化碳和水，完成清尘处理。
优选地，所述灰尘为炭黑。
于本发明一实施例中，所述除尘电场阴极包括若干根阴极丝。阴极丝的直径可为0.1mm-20mm，该尺寸参数根据应用场合及积尘要求做调整。于本发明一实施例中阴极丝的直径不大于3mm。于本发明一实施例中阴极丝使用容易放电的金属丝或合金丝，耐温且能支撑自身重量，电化学稳定。于本发明一实施例中阴极丝的材质选用钛。阴极丝的具体形状根据除尘电场阳极的形状调整，例如，若除尘电场阳极的积尘面是平面，则阴极丝的截面呈圆形；若除 尘电场阳极的积尘面是圆弧面，阴极丝需要设计成多面形。阴极丝的长度根据除尘电场阳极进行调整。
于本发明一实施例中，所述除尘电场阴极包括若干阴极棒。于本发明一实施例中，所述阴极棒的直径不大于3mm。于本发明一实施例中阴极棒使用容易放电的金属棒或合金棒。阴极棒的形状可以为针状、多角状、毛刺状、螺纹杆状或柱状等。阴极棒的形状可以根据除尘电场阳极的形状进行调整，例如，若除尘电场阳极的积尘面是平面，则阴极棒的截面需要设计成圆形；若除尘电场阳极的积尘面是圆弧面，则阴极棒需要设计成多面形。
于本发明一实施例中，除尘电场阴极穿设于除尘电场阳极内。
于本发明一实施例中，除尘电场阳极包括一个或多个并行设置的中空阳极管。当中空阳极管有多个时，全部中空阳极管构成蜂窝状的除尘电场阳极。于本发明一实施例中，中空阳极管的截面可呈圆形或多边形。若中空阳极管的截面呈圆形，除尘电场阳极和除尘电场阴极之间能形成均匀电场，中空阳极管的内壁不容易积尘。若中空阳极管的截面为三边形时，中空阳极管的内壁上可以形成3个积尘面，3个远角容尘角，此种结构的中空阳极管的容尘率最高。若中空阳极管的截面为四边形，可以获得4个积尘面，4个容尘角，但拼组结构不稳定。若中空阳极管的截面为六边形，可以形成6个积尘面，6个容尘角，积尘面和容尘率达到平衡。若中空阳极管的截面呈更多边形时，可以获得更多的积尘边，但损失容尘率。于本发明一实施例中，中空阳极管的管内切圆直径取值范围为5mm-400mm。
对于排气系统，于一实施例中，本发明提供一种减少除尘电场耦合的方法，包括以下步骤：
使排气通过除尘电场阳极和除尘电场阴极产生的电离除尘电场；
选择所述除尘电场阳极或/和除尘电场阴极。
于本发明一实施例中，选择的所述除尘电场阳极或/和除尘电场阴极尺寸使电场耦合次数≤3。
具体地，选择所述除尘电场阳极的集尘面积与除尘电场阴极的放电面积的比。优选地，选择所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
更为优选地，选择所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为6.67：1-56.67：1。
于本发明一实施例中，所述除尘电场阴极直径为1-3毫米，所述除尘电场阳极与所述尾气除尘电场阴极的极间距为2.5-139.9毫米；所述除尘电场阳极的积尘面积与所述除尘电场阴极的放电面积的比为1.667：1-1680：1。
优选地，选择所述除尘电场阳极和所述除尘电场阴极的极间距小于150mm。
优选地，选择所述除尘电场阳极与所述除尘电场阴极的极间距为2.5～139.9mm。更为优选地，选择所述除尘电场阳极与所述除尘电场阴极的极间距为5.0～100mm。
优选地，选择所述除尘电场阳极长度为10～180mm。更为优选地，选择所述除尘电场阳极长度为60～180mm。
优选地，选择所述除尘电场阴极长度为30～180mm。更为优选地，选择所述除尘电场阴极长度为54～176mm。
于本发明一实施例中，所述除尘电场阴极包括若干根阴极丝。阴极丝的直径可为0.1mm-20mm，该尺寸参数根据应用场合及积尘要求做调整。于本发明一实施例中阴极丝的直径不大于3mm。于本发明一实施例中阴极丝使用容易放电的金属丝或合金丝，耐温且能支撑自身重量，电化学稳定。于本发明一实施例中阴极丝的材质选用钛。阴极丝的具体形状根据除尘电场阳极的形状调整，例如，若除尘电场阳极的积尘面是平面，则阴极丝的截面呈圆形；若除尘电场阳极的积尘面是圆弧面，阴极丝需要设计成多面形。阴极丝的长度根据除尘电场阳极进行调整。
于本发明一实施例中，所述除尘电场阴极包括若干阴极棒。于本发明一实施例中，所述阴极棒的直径不大于3mm。于本发明一实施例中阴极棒使用容易放电的金属棒或合金棒。阴极棒的形状可以为针状、多角状、毛刺状、螺纹杆状或柱状等。阴极棒的形状可以根据除尘电场阳极的形状进行调整，例如，若除尘电场阳极的积尘面是平面，则阴极棒的截面需要设计成圆形；若除尘电场阳极的积尘面是圆弧面，则阴极棒需要设计成多面形。
于本发明一实施例中，除尘电场阴极穿设于除尘电场阳极内。
于本发明一实施例中，除尘电场阳极包括一个或多个并行设置的中空阳极管。当中空阳极管有多个时，全部中空阳极管构成蜂窝状的除尘电场阳极。于本发明一实施例中，中空阳极管的截面可呈圆形或多边形。若中空阳极管的截面呈圆形，除尘电场阳极和除尘电场阴极之间能形成均匀电场，中空阳极管的内壁不容易积尘。若中空阳极管的截面为三边形时，中空阳极管的内壁上可以形成3个积尘面，3个远角容尘角，此种结构的中空阳极管的容尘率最高。若中空阳极管的截面为四边形，可以获得4个积尘面，4个容尘角，但拼组结构不稳定。若中空阳极管的截面为六边形，可以形成6个积尘面，6个容尘角，积尘面和容尘率达到平衡。若中空阳极管的截面呈更多边形时，可以获得更多的积尘边，但损失容尘率。于本发明一实施例中，中空阳极管的管内切圆直径取值范围为5mm-400mm。
一种排气除尘方法，包括如下步骤：
1)利用电离除尘电场吸附排气中的颗粒物；
2)利用电离除尘电场给驻极体元件充电。
于本发明一实施例中，所述驻极体元件靠近电场装置出口，或者，所述驻极体元件设于电场装置出口。
于本发明一实施例中，所述除尘电场阳极和所述除尘电场阴极形成排气流道，所述驻极体元件设于所述排气流道中。
于本发明一实施例中，所述排气流道包括排气流道出口，所述驻极体元件靠近所述排气流道出口，或者，所述驻极体元件设于所述排气流道出口。
于本发明一实施例中，当电离除尘电场无上电驱动电压时，利用充电的驻极体元件吸附排气中的颗粒物。
于本发明一实施例中，在充电的驻极体元件吸附一定的排气中的颗粒物后，将其替换为新的驻极体元件。
于本发明一实施例中，替换为新的驻极体元件后重新启动电离除尘电场吸附排气中的颗粒物，并给新的驻极体元件充电。
于本发明一实施例中，所述驻极体元件的材料包括具有驻极性能的无机化合物。所述驻极性能是指驻极体元件在外接电源充电后带有电荷，并在完全脱离电源的条件下，依然保持有一定的电荷，从而作为电极起到电场电极作用的能力。
于本发明一实施例中，所述无机化合物选自含氧化合物、含氮化合物或玻璃纤维中的一种或多种组合。
于本发明一实施例中，所述含氧化合物选自金属基氧化物、含氧复合物、含氧的无机杂多酸盐中的一种或多种组合。
于本发明一实施例中，所述金属基氧化物选自氧化铝、氧化锌、氧化锆、氧化钛、氧化钡、氧化钽、氧化硅、氧化铅、氧化锡中的一种或多种组合。
于本发明一实施例中，所述金属基氧化物为氧化铝。
于本发明一实施例中，所述含氧复合物选自钛锆复合氧化物或钛钡复合氧化物中的一种或多种组合。
于本发明一实施例中，所述含氧的无机杂多酸盐选自钛酸锆、锆钛酸铅或钛酸钡中的一种或多种组合。
于本发明一实施例中，所述含氮化合物为氮化硅。
于本发明一实施例中，所述驻极体元件的材料包括具有驻极性能的有机化合物。所述驻 极性能是指驻极体元件在外接电源充电后带有电荷，并在完全脱离电源的条件下，依然保持有一定的电荷，从而作为电极起到电场电极作用的能力。
于本发明一实施例中，所述有机化合物选自氟聚合物、聚碳酸酯、PP、PE、PVC、天然蜡、树脂、松香中的一种或多种组合。
于本发明一实施例中，所述氟聚合物选自聚四氟乙烯(PTFE)、聚全氟乙丙烯(Teflon-FEP)、可溶性聚四氟乙烯(PFA)、聚偏氟乙烯(PVDF)中的一种或多种组合。
于本发明一实施例中，所述氟聚合物为聚四氟乙烯。
于本发明一实施例中，所述排气处理系统包括排气臭氧净化系统。
于本发明一实施例中，所述排气臭氧净化系统包括反应场，用于将臭氧流股与排气流股混合反应。例如：所述排气臭氧净化系统可以用于处理排气排放设备210的排气，利用排气中的水以及排气管道220，产生氧化反应，将排气中的有机挥发份氧化为二氧化碳和水；硫、硝等无害化收集。所述排气臭氧净化系统还可以包括外置的臭氧发生器230，通过臭氧输送管240给排气管道220提供臭氧，如图1所示，图中箭头方向为排气流动方向。
臭氧流股与排气流股的摩尔比可为2～10，如5～6、5.5～6.5、5～7、4.5～7.5、4～8、3.5～8.5、3～9、2.5～9.5、2～10。
本发明一实施例可以采用不同方式获得臭氧。比如，延面放电产生臭氧为管式、板式放电部件和交流高压电源组成，利用静电吸附粉尘、除水、富氧后的空气进入放电通道，空气氧被电离产生臭氧、高能离子、高能粒子，通过正压或负压通入反应场如排气通道中。使用管式延面放电结构，放电管内和外层放电管外都通入一冷却液，在管内电极和外管导体间形成电极，电极间通入18kHz、10kV高压交流电，外管内壁和内管外壁面产生高能电离，氧气被电离，产生臭氧。臭氧使用正压送入反应场如排气通道。臭氧流股与排气流股的摩尔比为2时，VOCs去除率50％；臭氧流股与排气流股的摩尔比为5时，VOCs去除率95％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率90％；臭氧流股与排气流股的摩尔比大于10时，VOCs去除率99％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率99％。电耗增加到30w/克。
紫外线灯管产生臭氧为气体放电产生11-195纳米波长紫外线，直接辐照灯管周围空气，产生生臭氧、高能离子、高能粒子，通过正压或负压通入反应场如排气通道中。使用172纳米波长和185纳米波长紫外放电管，通过点亮灯管，在灯管外壁的气体中氧气被电离，产生大量氧离子，结合为臭氧。通过正压送入反应场如排气通道。使用185纳米紫外线臭氧流股与排气流股的摩尔比为2时，VOCs去除率40％；185纳米紫外线臭氧流股与排气流股的摩尔比为5 时，VOCs去除率85％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率70％；185纳米紫外线臭氧流股与排气流股的摩尔比大于10时，VOCs去除率95％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率95％。电耗25w/克。
使用172纳米紫外线臭氧流股与排气流股的摩尔比为2时，VOCs去除率45％；172纳米紫外线臭氧流股与排气流股的的摩尔比为5时，VOCs去除率89％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率75％；172纳米紫外线臭氧流股与排气流股的的摩尔比大于10时，VOCs去除率97％以上，然后氮氧化合物气体浓度下降，氮氧化合物去除率95％。电耗22w/克。
于本发明一实施例中，所述反应场包括管道和/或反应器。
于本发明一实施例中，所述反应场还包括如下技术特征中的至少一项：
6)管道直径为100-200毫米；
7)管道长度大于管道直径0.1倍；
8)所述反应器选自如下至少一种：
反应器一：所述反应器具有反应腔室，排气与臭氧在所述反应腔室混合并反应；
反应器二：所述反应器包括若干蜂窝状腔体，用于提供排气与臭氧混合并反应的空间；所述蜂窝状腔体内之间设有间隙，用于通入冷态介质，控制排气与臭氧的反应温度；
反应器三：所述反应器包括若干载体单元，所述载体单元提供反应场地(例如蜂窝结构的介孔陶瓷体载体)，没有载体单元时为气相中反应，有载体单元时则为界面反应，加快反应时间；
反应器四：所述反应器包括催化剂单元，所述催化剂单元用于促进排气的氧化反应；
9)所述反应场设有臭氧进口，所述臭氧进口选自喷口、喷格栅、喷嘴、旋流喷嘴、设有文丘里管的喷口中的至少一种；设有文丘里管的喷口：所述文丘里管设于喷口中，采用文丘里原理混入臭氧；
10)所述反应场设有臭氧进口，所述臭氧通过所述臭氧进口进入反应场与排气进行接触，臭氧进口的设置形成如下方向中至少一种：与排气流动的方向相反、与排气流动的方向垂直、与排气流动的方向相切、插入排气流动方向、多个方向与排气进行接触；所述与排气流动的方向相反即为反方向进入，增加反应时间，减少体积；所述与排气流动的方向垂直，使用文氏效应；与排气流动的方向相切，便于混合；插入排气流动方向，克服漩涡流；多个方向，克服重力。
于本发明一实施例中，所述反应场包括排气管、蓄热体装置或催化器，臭氧可对蓄热体、 催化剂、陶瓷体清洁再生。
于本发明一实施例中，所述反应场的温度为-50～200℃，可以为60～70℃，50～80℃、40～90℃、30～100℃、20～110℃、10～120℃、0～130℃、-10～140℃、-20～150℃、-30～160℃、-40～170℃、-50～180℃、-180～190℃或190～200℃。
于本发明一实施例中，所述反应场的温度为60～70℃。
于本发明一实施例中，所述排气臭氧净化系统还包括臭氧源，用于提供臭氧流股。所述臭氧流股可以为臭氧发生器即时生成也可以为存储的臭氧。所述反应场可以与臭氧源流体连通，臭氧源所提供的臭氧流股可以被引入反应场中，从而可以与排气流股混合，使排气流股经受氧化处理。
于本发明一实施例中，所述臭氧源包括存储臭氧单元和/或臭氧发生器。所述臭氧源可以包括臭氧引入管道，还可以包括臭氧发生器，所述臭氧发生器可以是包括但不限于电弧臭氧发生器即延面放电臭氧发生器、工频电弧臭氧发生器、高频感应臭氧发生器、低气压臭氧发生器、紫外线臭氧发生器、电解液臭氧发生器、化学药剂臭氧发生器、射线辐照粒子发生器等中的一种或多种的组合。
于本发明一实施例中，所述臭氧发生器包括延面放电臭氧发生器、工频电弧臭氧发生器、高频感应臭氧发生器、低气压臭氧发生器、紫外线臭氧发生器、电解液臭氧发生器、化学药剂臭氧发生器和射线辐照粒子发生器中的一种或多种的组合。
于本发明一实施例中，所述臭氧发生器包括电极，所述电极上设有催化剂层，所述催化剂层包括氧化催化键裂解选择性催化剂层。
于本发明一实施例中，所述电极包括高压电极或设有阻挡介质层的高压电极，当所述电极包括高压电极时，所述氧化催化键裂解选择性催化剂层250设于所述高压电极260表面上(如图2所示)，当所述电极包括阻挡介质层270的高压电极260时，所述氧化催化键裂解选择性催化剂层250设于阻挡介质层270的表面上(如图3所示)。
高压电极是指电压高于500V的直流或交流电极。电极是指用做导电介质(固体、气体、真空或电解质溶液)中输入或导出电流的极板。输入电流的一极叫阳极或正极，放出电流的一极叫阴极或负极。
放电式臭氧产生机理主要为物理(电学)方法。放电式臭氧发器也有很多类型，但其基本原理就是利用高电压产生电场，再利用电场的电能削弱乃至打断氧气的双键，生成臭氧。现有的放电式臭氧发生器结构原理图如图4所示，该放电式臭氧发生器包括高压交流电源280、高压电极260、阻挡介质层270、气隙290、地极291。在高压电场作用下，气隙290中 的氧气分子的双氧键被电能打断，产生臭氧。但利用电场能量产生臭氧是有极限的，目前行业标准要求每kg臭氧的电耗不超过8kWh，行业平均水平7.5kWh左右。
于本发明一实施例中，所述阻挡介质层选自陶瓷板、陶瓷管、石英玻璃板、石英板和石英管中的至少一种。所述陶瓷板、陶瓷管可以为氧化铝、氧化锆、氧化硅等氧化物或其复合氧化物的陶瓷板、陶瓷管。
于本发明一实施例中，当所述电极包括高压电极时，所述氧化催化键裂解选择性催化剂层的厚度为1～3mm，该氧化催化键裂解选择性催化剂层兼作阻挡介质，如1～1.5mm或1.5～3mm；当所述电极包括阻挡介质层的高压电极时，所述氧化催化键裂解选择性催化剂层的负载量包括阻挡介质层的1～12wt％，如1～5wt％或5～12wt％。
于本发明一实施例中，所述氧化催化键裂解选择性催化剂层包括如下重量百分比的各组分：
活性组分 5～15％，如5～8％、8～10％、10～12％、12～14％或14～15％；
涂层 85～95％，如85～86％、86～88％、88～90％、90～92％或92～95％；
其中，所述活性组分选自金属M和金属元素M的化合物中的至少一种，金属元素M选自碱土金属元素、过渡金属元素、第四主族金属元素、贵金属元素和镧系稀土元素中的至少一种；
所述涂层选自氧化铝、氧化铈、氧化锆、氧化锰、金属复合氧化物、多孔材料和层状材料中的至少一种，所述金属复合氧化物包括铝、铈、锆和锰中一种或多种金属的复合氧化物。
于本发明一实施例中，所述碱土金属元素选自镁、锶和钙中的至少一种。
于本发明一实施例中，所述过渡金属元素选自钛、锰、锌、铜、铁、镍、钴、钇和锆中的至少一种。
于本发明一实施例中，所述第四主族金属元素为锡。
于本发明一实施例中，所述贵金属元素选自铂、铑、钯、金、银和铱中的至少一种。
于本发明一实施例中，所述镧系稀土元素选自镧、铈、镨和钐中的至少一种。
于本发明一实施例中，所述金属元素M的化合物选自氧化物、硫化物、硫酸盐、磷酸盐、碳酸盐，以及钙钛矿中的至少一种。
于本发明一实施例中，所述多孔材料选自分子筛、硅藻土、沸石和纳米碳管中的至少一种。多孔材料孔隙率为60％以上，如60～80％，比表面积为300-500平方米/克，平均孔径为10-100纳米。
于本发明一实施例中，所述层状材料选自石墨烯和石墨中的至少一种。
所述氧化催化键裂解选择性催化剂层将化学和物理方法相结合，降低、削弱甚至直接打断双氧键，充分发挥和利用电场和催化的协同作用，达到大幅度提高臭氧产生速率和产生量的目的，以本发明的臭氧发生器与现有的放电式臭氧发生器相比，同样条件臭氧产生量提高10～30％、产生速率提高10～20％。
于本发明一实施例中，所述排气臭氧净化系统还包括臭氧量控制装置，用于控制臭氧量以致有效氧化排气中待处理的气体组分，所述臭氧量控制装置包括控制单元。
于本发明一实施例中，所述臭氧量控制装置还包括臭氧处理前排气组分检测单元，用于检测臭氧处理前排气组分含量。
于本发明一实施例中，所述控制单元根据所述臭氧处理前排气组分含量控制混合反应所需臭氧量。
于本发明一实施例中，所述臭氧处理前排气组分检测单元选自以下检测单元中至少一个：
第一挥发性有机化合物检测单元，用于检测臭氧处理前排气中挥发性有机化合物含量，如挥发性有机化合物传感器等；
第一CO检测单元，用于检测臭氧处理前排气中CO含量，如CO传感器等；
第一氮氧化物检测单元，用于检测臭氧处理前排气中氮氧化物含量，如氮氧化物(NO x)传感器等。
于本发明一实施例中，所述控制单元根据至少一个所述臭氧处理前排气组分检测单元的输出值控制混合反应所需臭氧量。
于本发明一实施例中，所述控制单元用于按照预设的数学模型控制混合反应所需臭氧量。所述预设的数学模型与臭氧处理前排气组分含量相关，通过上述含量及排气组分与臭氧的反应摩尔比来确定混合反应所需臭氧量，确定混合反应所需臭氧量时可增加臭氧量，使臭氧过量。
于本发明一实施例中，所述控制单元用于按照理论估计值控制混合反应所需臭氧量。
于本发明一实施例中，所述理论估计值为：臭氧通入量与排气中待处理物的摩尔比为2～10。例如：13L柴油排气排放设备可控制臭氧通入量为300～500g；2L汽油排气排放设备可控制臭氧通入量为5～20g。
于本发明一实施例中，所述臭氧量控制装置包括臭氧处理后排气组分检测单元，用于检测臭氧处理后排气组分含量。
于本发明一实施例中，所述控制单元根据所述臭氧处理后排气组分含量控制混合反应所需臭氧量。
于本发明一实施例中，所述臭氧处理后排气组分检测单元选自以下检测单元中至少一个：
第一臭氧检测单元，用于检测臭氧处理后排气中臭氧含量；
第二挥发性有机化合物检测单元，用于检测臭氧处理后排气中挥发性有机化合物含量；
第二CO检测单元，用于检测臭氧处理后排气中CO含量；
第二氮氧化物检测单元，用于检测臭氧处理后排气中氮氧化物含量。
于本发明一实施例中，所述控制单元根据至少一个所述臭氧处理后排气组分检测单元的输出值控制臭氧量。
于本发明一实施例中，所述排气臭氧净化系统还包括脱硝装置，用于脱除臭氧流股与排气流股混合反应产物中的硝酸。
于本发明一实施例中，所述脱硝装置包括电凝装置，所述电凝装置包括：电凝流道、位于电凝流道中的第一电极、及第二电极。
于本发明一实施例中，所述脱硝装置包括冷凝单元，用于将臭氧处理后的排气进行冷凝，实现气液分离。
于本发明一实施例中，所述脱硝装置包括淋洗单元，用于将臭氧处理后的排气进行淋洗，例如：水和/或碱进行淋洗。
于本发明一实施例中，所述脱硝装置还包括淋洗液单元，用于向所述淋洗单元提供淋洗液。
于本发明一实施例中，所述淋洗液单元中淋洗液包括水和/或碱。
于本发明一实施例中，所述脱硝装置还包括脱硝液收集单元，用于存储排气中脱除的硝酸水溶液和/或硝酸盐水溶液。
于本发明一实施例中，当所述脱硝液收集单元中存储有硝酸水溶液时，所述脱硝液收集单元设有碱液加入单元，用于与硝酸形成硝酸盐。
于本发明一实施例中，所述排气臭氧净化系统还包括臭氧消解器，用于消解经反应场处理后的排气中的臭氧。所述臭氧消解器可以通过紫外线，催化等方式进行臭氧消解。
于本发明一实施例中，所述臭氧消解器选自紫外线臭氧消解器和催化臭氧消解器中的至少一种。
于本发明一实施例中，所述排气臭氧净化系统还包括第一脱硝装置，用于脱除排气中氮氧化物；所述反应场用于将经所述第一脱硝装置处理后的排气与臭氧流股混合反应，或者，用于将排气在经所述第一脱硝装置处理前先与臭氧流股混合反应。
所述第一脱硝装置可以为现有技术中实现脱硝的装置，例如：非催化还原装置(如氨气 脱硝)、选择性催化还原装置(SCR：氨气加催化剂脱硝)、非选择性催化还原装置(SNCR)和电子束脱硝装置等中的至少一种。所述第一脱硝装置处理后排气中氮氧化物(NO x)含量不达标，在所述第一脱硝装置处理后或者处理前的排气与臭氧流股混合反应可达到最新标准。
于本发明一实施例中，所述第一脱硝装置选自非催化还原装置、选择性催化还原装置、非选择性催化还原装置和电子束脱硝装置中的至少一种。
本领域技术人员基于现有技术认为：臭氧处理排气中氮氧化物NO X时，氮氧化物NO X被臭氧氧化成高价态氮氧化物如NO 2、N 2O 5和NO 3等，所述高价态氮氧化物还是气体，仍然不能从排气中脱除，即臭氧处理排气中氮氧化物NO X无效，但是，本申请人却发现臭氧和排气中氮氧化物反应产生的高价态氮氧化物并不是最后的产物，高价态氮氧化物会和水反应产生硝酸，硝酸则更容易从排气中脱除，比如使用电凝和冷凝，该效果对所属技术领域的技术人员来说是预料不到的。该预料不到的技术效果是因为本领域技术人员没有认识到臭氧还会和排气中的VOC反应产生足够水和高价氮氧化物反应产生硝酸。
用臭氧来处理排气时，臭氧最优先与挥发性有机化合物VOC反应，被氧化成CO 2和水，然后再与氮氧化合物NO X，被氧化成高价态氮氧化物如NO 2、N 2O 5和NO 3等，最后再与一氧化碳CO反应，被氧化成CO 2，即反应优先顺序为挥发性有机化合物VOC＞氮氧化合物NO X＞一氧化碳CO，而且排气中有足够的挥发性有机化合物VOC产生足够的水可以充分与高价态氮氧化物反应生成硝酸，因此，用臭氧来处理排气使得臭氧除NO X效果更好，该效果对所属技术领域的技术人员来说是预料不到的技术效果。
臭氧处理排气可达到如下脱除效果：氮氧化物NO X脱除效率：60～99.97％；一氧化碳CO脱除效率：1～50％；挥发性有机化合物VOC脱除效率：60～99.97％，对所属技术领域的技术人员来说是预料不到的技术效果。
所述高价态氮氧化物与挥发性有机化合物VOC被氧化得到的水反应得到的硝酸更易脱除且脱除得到的硝酸可回收利用，例如可以通过本发明的电凝装置脱除硝酸、也可以通过现有技术中脱除硝酸的方法例如碱洗脱除硝酸。本发明电凝装置包括第一电极和第二电极，含硝酸水雾流经第一电极时，含硝酸水雾将带电，第二电极给带电的含硝酸水雾施加吸引力，含硝酸水雾向第二电极移动，直至含硝酸水雾附着在第二电极上，然后再进行收集，本发明电凝装置对含硝酸水雾的收集能力更强、收集效率更高。
排气电离除尘时空气中的氧气参与电离，形成臭氧，排气除尘系统与排气臭氧净化系统结合后，电离形成的臭氧可用于氧化排气中的污染物，如氮氧化合物NO X、挥发性有机化合物VOC、一氧化碳CO，即电离形成的臭氧可被臭氧处理NO X用来处理污染物，氧化氮氧化 合物NO X的同时还会氧化挥发性有机化合物VOC、一氧化碳CO，节省臭氧处理NO X的臭氧消耗量，而且也不需要再增加除臭氧机构对电离形成的臭氧进行消解，不会造成温室效应，破坏大气中的紫外线，可见，排气除尘系统与排气臭氧净化系统结合后，在功能上彼此支持，并取得了新的技术效果：电离形成的臭氧被排气臭氧净化系统用来处理污染物，节省臭氧处理污染物的臭氧消耗量，而且也不需要再增加除臭氧机构对电离形成的臭氧进行消解，不会造成温室效应，破坏大气中的紫外线，具有突出的实质性特点和显著的进步。
一种排气臭氧净化方法，包括如下步骤：将臭氧流股与排气流股混合反应。
于本发明一实施例中，所述排气流股包括氮氧化物和挥发性有机化合物。所述排气流股可以是排气，所述排气排放设备通常是将燃料的化学能转化为机械能的装置，具体可以是内燃机等。所述排气流股中氮氧化物(NO x)与臭氧流股混合反应，被氧化成高价态的氮氧化物如NO 2、N 2O 5和NO 3等。所述排气流股中挥发性有机化合物(VOC)与臭氧流股混合反应，被氧化成CO 2和水。所述高价态的氮氧化物与挥发性有机化合物(VOC)被氧化得到的水反应得到硝酸。经过上述反应，排气流股中的氮氧化物(NO x)得以脱除，以硝酸的形态存在于废气中。
于本发明一实施例中，于排气的低温段，臭氧流股与排气流股的混合反应。
于本发明一实施例中，臭氧流股与排气流股混合反应温度为-50～200℃，可以为60～70℃，50～80℃、40～90℃、30～100℃、20～110℃、10～120℃、0～130℃、-10～140℃、-20～150℃、-30～160℃、-40～170℃、-50～180℃、-180～190℃或190～200℃。
于本发明一实施例中，臭氧流股与排气流股混合反应温度为60～70℃。
于本发明一实施例中，臭氧流股与排气流股的混合方式选自文丘里混合、正压混合、插入混合、动力混合和流体混合中至少一种。
于本发明一实施例中，当臭氧流股与排气流股的混合方式为正压混合时，臭氧进气的压力大于排气的压力。当臭氧流股进气的压力小于排气流股的排压时，可同时使用文丘里混合方式。
于本发明一实施例中，在臭氧流股与排气流股混合反应前，提高排气流股流速，采用文丘里原理混入臭氧流股。
于本发明一实施例中，臭氧流股与排气流股混合方式选自排气出口逆流通入、反应场前段混入、除尘器前后插入、脱硝装置前后混入、催化装置前后混入、水洗装置前后通入、过滤装置前后混入、消音装置前后混入、排气管道内发生混入、吸附装置外置混入和凝露装置前后混入中至少一种。可设于排气的低温段，避免臭氧的消解。
于本发明一实施例中，臭氧流股与排气流股混合反应的反应场包括管道和/或反应器。
于本发明一实施例中，所述反应场包括排气管、蓄热体装置或催化器。
于本发明一实施例中，还包括如下技术特征中的至少一项：
1)管道直径为100～200毫米；
2)管道长度大于管道直径0.1倍；
3)所述反应器选自如下至少一种：
反应器一：所述反应器具有反应腔室，排气与臭氧在所述反应腔室混合并反应；
反应器二：所述反应器包括若干蜂窝状腔体，用于提供排气与臭氧混合并反应的空间；所述蜂窝状腔体内之间设有间隙，用于通入冷态介质，控制排气与臭氧的反应温度；
反应器三：所述反应器包括若干载体单元，所述载体单元提供反应场地(例如蜂窝结构的介孔陶瓷体载体)，没有载体单元时为气相中反应，有载体单元时则为界面反应，加快反应时间；
反应器四：所述反应器包括催化剂单元，所述催化剂单元用于促进排气的氧化反应；
4)所述反应场设有臭氧进口，所述臭氧进口选自喷口、喷格栅、喷嘴、旋流喷嘴、设有文丘里管的喷口中的至少一种；设有文丘里管的喷口：所述文丘里管设于喷口中，采用文丘里原理混入臭氧；
5)所述反应场设有臭氧进口，所述臭氧通过所述臭氧进口进入反应场与排气进行接触，臭氧进口的设置形成如下方向中至少一种：与排气流动的方向相反、与排气流动的方向垂直、与排气流动的方向相切、插入排气流动方向、多个方向与排气进行接触；所述与排气流动的方向相反即为反方向进入，增加反应时间，减少体积；所述与排气流动的方向垂直，使用文氏效应；与排气流动的方向相切，便于混合；插入排气流动方向，克服漩涡流；多个方向，克服重力。
于本发明一实施例中，所述臭氧流股由存储臭氧单元和/或臭氧发生器提供。
于本发明一实施例中，所述臭氧发生器包括延面放电臭氧发生器、工频电弧臭氧发生器、高频感应臭氧发生器、低气压臭氧发生器、紫外线臭氧发生器、电解液臭氧发生器、化学药剂臭氧发生器和射线辐照粒子发生器中的一种或多种的组合。
于本发明一实施例中，所述臭氧流股提供方法：在电场和氧化催化键裂解选择性催化剂层作用下，含有氧气的气体产生臭氧，其中形成电场的电极上负载氧化催化键裂解选择性催化剂层。
于本发明一实施例中，所述电极包括高压电极或设有阻挡介质层的电极，当所述电极包 括高压电极时，所述氧化催化键裂解选择性催化剂层负载于所述高压电极表面上，当所述电极包括阻挡介质层的高压电极时，所述氧化催化键裂解选择性催化剂层负载于阻挡介质层的表面上。
于本发明一实施例中，当所述电极包括高压电极时，所述氧化催化键裂解选择性催化剂层的厚度为1～3mm，该氧化催化键裂解选择性催化剂层兼作阻挡介质，如1～1.5mm或1.5～3mm；当所述电极包括阻挡介质层的高压电极时，所述氧化催化键裂解选择性催化剂层的负载量包括阻挡介质层的1～12wt％，如1～5wt％或5～12wt％。
于本发明一实施例中，所述氧化催化键裂解选择性催化剂层包括如下重量百分比的各组分：
活性组分 5～15％，如5～8％、8～10％、10～12％、12～14％或14～15％；
涂层 85～95％，如85～86％、86～88％、88～90％、90～92％或92～95％；
其中，所述活性组分选自金属M和金属元素M的化合物中的至少一种，金属元素M选自碱土金属元素、过渡金属元素、第四主族金属元素、贵金属元素和镧系稀土元素中的至少一种；
所述涂层选自氧化铝、氧化铈、氧化锆、氧化锰、金属复合氧化物、多孔材料和层状材料中的至少一种，所述金属复合氧化物包括铝、铈、锆和锰中一种或多种金属的复合氧化物。
于本发明一实施例中，所述碱土金属元素选自镁、锶和钙中的至少一种。
于本发明一实施例中，所述过渡金属元素选自钛、锰、锌、铜、铁、镍、钴、钇和锆中的至少一种。
于本发明一实施例中，所述第四主族金属元素为锡。
于本发明一实施例中，所述贵金属元素选自铂、铑、钯、金、银和铱中的至少一种。
于本发明一实施例中，所述镧系稀土元素选自镧、铈、镨和钐中的至少一种。
于本发明一实施例中，所述金属元素M的化合物选自氧化物、硫化物、硫酸盐、磷酸盐、碳酸盐，以及钙钛矿中的至少一种。
于本发明一实施例中，所述多孔材料选自分子筛、硅藻土、沸石和纳米碳管中的至少一种。多孔材料孔隙率为60％以上，如60～80％，比表面积为300-500平方米/克，平均孔径为10-100纳米。
于本发明一实施例中，所述层状材料选自石墨烯和石墨中的至少一种。
于本发明一实施例中，所述电极通过浸渍和/或喷涂的方法负载氧双催化键裂解选择性催化剂。
于本发明一实施例中，包括如下步骤：
1)按照催化剂组成配比，将涂层原料的浆料负载于高压电极表面上或阻挡介质层的表面上，干燥，煅烧，得到负载涂层的高压电极或阻挡介质层；
2)按照催化剂组成配比，将含金属元素M的原料溶液或浆料负载到步骤1)得到涂层上，干燥，煅烧，当涂层负载于阻挡介质层的表面上时，煅烧后在阻挡介质层相对于负载涂层的另一面设置高压电极，即得所述臭氧发生器用电极；或者，按照催化剂组成配比，将含金属元素M的原料溶液或浆料负载到步骤1)得到涂层上，干燥，煅烧和后处理，当涂层负载于阻挡介质层的表面上时，后处理后在阻挡介质层相对于负载涂层的另一面设置高压电极，即得所述臭氧发生器用电极；
其中，通过对煅烧温度和气氛，以及后处理实现对电极用催化剂中活性组分形态的控制。
于本发明一实施例中，包括如下步骤：
1)按照催化剂组成配比，将含金属元素M的原料溶液或浆料负载涂层原料上，干燥，煅烧，得到负载有活性组份的涂层材料；
2)按照催化剂组成配比，将步骤1)得到的负载有活性组份的涂层材料制成浆料，负载在高压电极表面上或阻挡介质层的表面上，干燥，煅烧，当涂层负载在阻挡介质层的表面上时，煅烧后在阻挡介质层相对于负载涂层的另一面设置高压电极，即得所述臭氧发生器用电极；或者，按照催化剂组成配比，将步骤1)得到的负载有活性组份的涂层材料制成浆料，负载在高压电极表面上或阻挡介质层的表面上，干燥，煅烧和后处理，当涂层负载在阻挡介质层的表面上时，后处理后在阻挡介质层相对于负载涂层的另一面设置高压电极，即得所述臭氧发生器用电极；
其中，通过对煅烧温度和气氛，以及后处理实现对电极用催化剂中活性组分形态的控制。
上述负载方式可以为浸渍、喷涂、涂刷等等，能实现负载即可。
活性组分包括金属元素M的硫酸盐、磷酸盐、碳酸盐中的至少一种时，含金属元素M的硫酸盐、磷酸盐、碳酸盐中的至少一种的溶液或浆料负载涂层原料上，干燥，煅烧，煅烧温度不能超过活性组分的分解温度，例如：要获得金属元素M的硫酸盐则煅烧温度不能超过硫酸盐的分解温度(分解温度一般在600℃以上)。
通过对煅烧温度和气氛，以及后处理实现对电极用催化剂中活性组分形态的控制，例如：活性组分包括金属M时，煅烧后可再进行还原气还原(后处理)获得，煅烧温度可为200～550℃；活性组分包括金属元素M的硫化物时，煅烧后可再与硫化氢反应(后处理)获得，煅烧温度可为200～550℃。
于本发明一实施例中，包括：控制臭氧流股的臭氧量以致有效氧化排气中待处理的气体组分。
于本发明一实施例中，控制臭氧流股的臭氧量达到如下脱除效率：
氮氧化物脱除效率：60～99.97％；
CO脱除效率：1～50％；
挥发性有机化合物脱除效率：60～99.97％。
于本发明一实施例中，包括：检测臭氧处理前排气组分含量。
于本发明一实施例中，根据所述臭氧处理前排气组分含量控制混合反应所需臭氧量。
于本发明一实施例中，检测臭氧处理前排气组分含量选自以下至少一个：
检测臭氧处理前排气中挥发性有机化合物含量；
检测臭氧处理前排气中CO含量；
检测臭氧处理前排气中氮氧化物含量。
于本发明一实施例中，根据至少一个检测臭氧处理前排气组分含量的输出值控制混合反应所需臭氧量。
于本发明一实施例中，按照预设的数学模型控制混合反应所需臭氧量。所述预设的数学模型与臭氧处理前排气组分含量相关，通过上述含量及排气组分与臭氧的反应摩尔比来确定混合反应所需臭氧量，确定混合反应所需臭氧量时可增加臭氧量，使臭氧过量。
于本发明一实施例中，按照理论估计值控制混合反应所需臭氧量。
于本发明一实施例中，所述理论估计值为：臭氧通入量与排气中待处理物的摩尔比为2～10，如5～6、5.5～6.5、5～7、4.5～7.5、4～8、3.5～8.5、3～9、2.5～9.5、2～10。例如：13L柴油排气排放设备可控制臭氧通入量为300～500g；2L汽油排气排放设备可控制臭氧通入量为5～20g。
于本发明一实施例中，包括：检测臭氧处理后排气组分含量。
于本发明一实施例中，根据所述臭氧处理后排气组分含量控制混合反应所需臭氧量。
于本发明一实施例中，检测臭氧处理后排气组分含量选自以下至少一个：
检测臭氧处理后排气中臭氧含量；
检测臭氧处理后排气中挥发性有机化合物含量；
检测臭氧处理后排气中CO含量；
检测臭氧处理后排气中氮氧化物含量。
于本发明一实施例中，根据至少一个检测臭氧处理后排气组分含量的输出值控制臭氧量。
于本发明一实施例中，所述排气臭氧净化方法还包括如下步骤：脱除臭氧流股与排气流股混合反应产物中的硝酸。
于本发明一实施例中，使带硝酸雾的气体流经第一电极；当带硝酸雾的气体流经第一电极时，第一电极使气体中的硝酸雾带电，第二电极给带电的硝酸雾施加吸引力，使硝酸雾向第二电极移动，直至硝酸雾附着在第二电极上。
于本发明一实施例中，脱除臭氧流股与排气流股混合反应产物中的硝酸的方法：将臭氧流股与排气流股混合反应产物进行冷凝。
于本发明一实施例中，脱除臭氧流股与排气流股混合反应产物中的硝酸的方法：将臭氧流股与排气流股混合反应产物进行淋洗。
于本发明一实施例中，脱除臭氧流股与排气流股混合反应产物中的硝酸的方法还包括：向臭氧流股与排气流股混合反应产物提供淋洗液。
于本发明一实施例中，所述淋洗液为水和/或碱。
于本发明一实施例中，脱除臭氧流股与排气流股混合反应产物中的硝酸的方法还包括：存储排气中脱除的硝酸水溶液和/或硝酸盐水溶液。
于本发明一实施例中，当存储有硝酸水溶液时，加入碱液，与硝酸形成硝酸盐。
于本发明一实施例中，所述排气臭氧净化方法还包括如下步骤：对脱除硝酸的排气进行臭氧消解，例如：可以通过紫外线，催化等方式进行消解。
于本发明一实施例中，所述臭氧消解选自紫外线消解和催化消解中的至少一种。
于本发明一实施例中，所述排气臭氧净化方法还包括如下步骤：第一次脱除排气中氮氧化物；第一次脱除氮氧化物后的排气流股与臭氧流股混合反应，或者，在第一次脱除排气中氮氧化物前先与臭氧流股混合反应。
第一次脱除排气中氮氧化物可以为现有技术中实现脱硝的方法，例如：非催化还原方法(如氨气脱硝)、选择性催化还原方法(SCR：氨气加催化剂脱硝)、非选择性催化还原方法(SNCR)和电子束脱硝方法等中的至少一种。第一次脱除排气中氮氧化物后的排气中氮氧化物(NO x)含量不达标，在第一次脱除排气中氮氧化物后或前经与臭氧混合反应后可达到最新标准。于本发明一实施例中，所述第一次脱除排气中氮氧化物选自非催化还原方法、选择性催化还原方法、非选择性催化还原方法和电子束脱硝方法等中的至少一种。
于本发明一实施例中提供一种电凝装置，包括：电凝流道、位于电凝流道中的第一电极、及第二电极。当排气流经电凝流道中的第一电极时，排气中含硝酸的水雾、即硝酸液将带电，第二电极给带电的硝酸液施加吸引力，含硝酸的水雾向第二电极移动，直至含硝酸的水雾附 着在第二电极上，从而实现对排气中硝酸液的去除。该电凝装置也称作电凝除雾装置。
于本发明一实施例中电凝装置的第一电极可为固体、液体、气体分子团、等离子体、导电混合态物质、生物体自然混合导电物质、或物体人工加工形成导电物质中的一种或多种形态的组合。当第一电极为固体时，第一电极可采用固态金属、比如304钢，或其它固态的导体、比如石墨等；当第一电极为液体时，第一电极可以是含离子导电液体。
于本发明一实施例中第一电极的形状可以呈点状、线状、网状、孔板状、板状、针棒状、球笼状、盒状、管状、自然形态物质、或加工形态物质等。当第一电极呈板状、球笼状、盒状或管状时，第一电极可以是无孔结构，也可以是有孔结构。当第一电极为有孔结构时，第一电极上可以设有一个或多个前通孔。于本发明一实施例中前通孔的形状可以是多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形等。于本发明一实施例中前通孔的孔径大小可以为10～100mm、10～20mm、20～30mm、30～40mm、40～50mm、50～60mm、60～70mm、70～80mm、80～90mm、或90～100mm。另外，在其它实施例中第一电极还可以是其它形状。
于本发明一实施例中电凝装置的第二电极的形状可以呈多层网状、网状、孔板状、管状、桶状、球笼状、盒状、板状、颗粒堆积层状、折弯板状、或面板状。当第二电极呈板状、球笼状、盒状或管状时，第二电极也可以是无孔结构，或有孔结构。当第二电极为有孔结构时，第二电极上可以设有一个或多个后通孔。于本发明一实施例中后通孔的形状可以是多角形、圆形、椭圆形、正方形、长方形、梯形、或菱形等。后通孔的孔径大小可以为10～100mm、10～20mm、20～30mm、30～40mm、40～50mm、50～60mm、60～70mm、70～80mm、80～90mm、或90～100mm。
于本发明一实施例中电凝装置的第二电极由导电物质制成。于本发明一实施例中第二电极的表面具有导电物质。
于本发明一实施例中电凝装置的第一电极与第二电极之间具有电凝电场，该电凝电场可以是点面电场、线面电场、网面电场、点桶电场、线桶电场、或网桶电场中的一种或多种电场的组合。比如：第一电极呈针状或线状，第二电极呈面状，且第一电极垂直或平行于第二电极，从而形成线面电场；或第一电极呈网状，第二电极呈面状，第一电极平行于第二电极，从而形成网面电场；或第一电极呈点状，并通过金属丝或金属针进行固定，第二电极呈桶状，第一电极位于第二电极的几何对称中心处，从而形成点桶电场；或第一电极呈线状，并通过金属丝或金属针进行固定，第二电极呈桶状，第一电极位于第二电极的几何对称轴上，从而形成线桶电场；或第一电极呈网状，并通过金属丝或金属针进行固定，第二电极呈桶状，第一电极位于第二电极的几何对称中心处，从而形成网桶电场。当第二电极呈面状时，具体可 以是平面状、曲面状、或球面状。当第一电极呈线状时，具体可以是直线状、曲线状、或圆圈状。第一电极还可以是圆弧状。当第一电极呈网状时，具体可以是平面的、球面的或其它几何面状，也可以是矩形，或不规则形状。第一电极也可以呈点状，且可以是直径很小的真实点，也可以是一个小球，还可以是一个网状球。当第二电极呈桶状时，第二电极还可以进一步演化成各种盒状。第一电极也可作相应变化，形成电极和电凝电场层套。
于本发明一实施例中电凝装置的第一电极呈线状，第二电极呈面状。于本发明一实施例中第一电极垂直于第二电极。于本发明一实施例中第一电极和第二电极相平行。于本发明一实施例中第一电极和第二电极均呈面状，且第一电极和第二电极相平行。于本发明一实施例中第一电极采用金属丝网。于本发明一实施例中第一电极呈平面状或球面状。于本发明一实施例中第二电极呈曲面状或球面状。于本发明一实施例中第一电极呈点状、线状、或网状，第二电极呈桶状，第一电极位于第二电极的内部，且第一电极位于第二电极的中心对称轴上。
于本发明一实施例中电凝装置的第一电极与电源的一个电极电性连接；第二电极与电源的另一个电极电性连接。于本发明一实施例中第一电极具体与电源的阴极电性连接，第二电极具体与电源的阳极电性连接。
同时，于本发明一些实施例中电凝装置的第一电极可以具有正电势或负电势；当第一电极具有正电势时，第二电极具有负电势；当第一电极具有负电势时，第二电极具有正电势，第一电极和第二电极均与电源电性连接，具体地第一电极和第二电极可分别与电源的正负极电性连接。该电源的电压称作上电驱动电压，上电驱动电压大小的选择与环境温度、介质温度等有关。例如，电源的上电驱动电压范围可以为5～50KV、10～50KV、5～10KV、10～20KV、20～30KV、30～40KV、或40～50KV，从生物电至空间雾霾治理用电。电源可以是直流电源或交流电源，其上电驱动电压的波形可以是直流波形、正弦波、或调制波形。直流电源作为吸附的基本应用；正弦波作为移动使用，如正弦波的上电驱动电压作用于第一电极和第二电极之间，所产生的电凝电场将驱动电凝电场中带电的粒子、如雾滴等向第二电极移动；斜波作为拉动使用，根据拉动力度需要调制波形，如非对称电凝电场的两端边缘处，对其中的介质所产生的拉力具有明显的方向性，以驱动电凝电场中的介质沿该方向移动。当电源采用交流电源时，其变频脉冲的范围可以为0.1Hz～5GHz、0.1Hz～1Hz、0.5Hz～10Hz、5Hz～100Hz、50Hz～1KHz、1KHz～100KHz、50KHz～1MHz、1MHz～100MHz、50MHz～1GHz、500MHz～2GHz、或1GHz～5GHz，适用生物体至污染物颗粒的吸附。第一电极可作为导线，在与含硝酸的水雾接触时，直接将正负电子导入含硝酸的水雾，此时含硝酸的水雾本身可作为电极。第一电极可通过能量波动的方法使电子转移到含硝酸的水雾或电极上，这样第一电极就可以不接触含 硝酸的水雾。含硝酸的水雾在由第一电极向第二电极移动过程中，将重复得到电子和失去电子；与此同时，大量电子在位于第一电极和第二电极之间的多个含硝酸的水雾之间进行传递，使更多雾滴带电，并最终到达第二电极，从而形成电流，该电流也称作上电驱动电流。上电驱动电流的大小与环境温度、介质温度、电子量、被吸附物质量、逃逸量有关。比如，随电子量增加，可移动的粒子、如雾滴增加，由移动的带电粒子形成的电流会随之增加。单位时间内被吸附的带电物质、如雾滴越多，电流越大。逃逸的雾滴只是带了电，但并未到达第二电极，也就是说未形成有效的电中和，从而在相同的条件下，逃逸的雾滴越多，电流越小。相同的条件下，环境温度越高，气体粒子和雾滴速度越快，其自身的动能也就越高，其自身与第一电极和第二电极碰撞机率就会越大，也越不易被第二电极吸附住，从而产生逃逸，但由于其逃逸是发生在电中和之后，且可能是发生了反复多次的电中和之后，从而相应的增加了电子传导速度，电流也就相应增加。同时，由于环境温度越高，气体分子、雾滴等的动量越高，且越不易被第二电极吸附，即使第二电极吸附后，再次从第二电极逃逸、即电中和之后逃逸的机率也越大，因此在第一电极与第二电极的间距不变的情况下，需要增加上述上电驱动电压，该上电驱动电压的极限为达到空气击穿的效果。另外，介质温度的影响基本与环境温度的影响相当。介质温度越低，需激发介质、如雾滴带电的能量小，且其自身所具有的动能也越小，在同样的电凝电场力作用下，越容易被吸附到第二电极上，从而形成的电流较大。电凝装置对冷态的含硝酸的水雾吸附效果更好。而随介质、如雾滴的浓度增加，带电的介质在与第二电极碰撞之前已与其它介质产生电子传递的机率越大，从而形成有效电中和的机会也会越大，形成的电流也相应地会越大；所以当介质浓度越高时，形成的电流越大。上电驱动电压与介质温度的关系与上电驱动电压与环境温度的关系基本相同。
于本发明一实施例中与第一电极和第二电极相连接的电源的上电驱动电压可小于起始起晕电压。该起始起晕电压为能使第一电极和第二电极之间产生放电并电离气体的最小电压值。对于不同的气体、及不同的工作环境等，起始起晕电压的大小可能会不相同。但对于本领域技术人员来说，针对确定的气体、及工作环境，所对应的起始起晕电压是确定的。于本发明一实施例中电源的上电驱动电压具体可为0.1-2kv/mm。电源的上电驱动电压小于空气电晕起晕电压。
于本发明一实施例中第一电极和第二电极均沿左右方向延伸，第一电极的左端位于第二电极的左端的左方。
于本发明一实施例中第二电极有两个，第一电极位于两个第二电极之间。
电凝装置的第一电极与第二电极之间的距离可根据两者间的上电驱动电压大小、水雾的 流速、以及含硝酸的水雾的带电能力等进行设置。比如，第一电极和第二电极的间距可以为5～50mm、5～10mm、10～20mm、20～30mm、30～40mm、或40～50mm。第一电极和第二电极的间距越大，需要的上电驱动电压越高，以形成足够强大的电凝电场，用于驱动带电的介质快速移向第二电极，以免介质逃逸。同样的条件下，第一电极和第二电极的间距越大，顺着气流方向，越靠近中心位置，物质流速越快；越靠近第二电极的物质的流速越慢；而垂直于气流方向，带电介质粒子、如雾粒，随第一电极和第二电极的间距增加，在没有发生碰撞的情况下，被电凝电场加速的时间越长，因此，物质在接近第二电极之前沿垂直方向的移动速度越大。在同样的条件下，如果上电驱动电压不变，随距离增加，电凝电场强度不断减小，电凝电场中介质带电的能力也就越弱。
电凝装置的第一电极和第二电极构成吸附单元。吸附单元可以有一个或多个，具体数量依据实际需要来确定。在一种实施例中，吸附单元有一个。在另一种实施例中吸附单元有多个，以利用多个吸附单元吸附更多的硝酸液，从而提高收集硝酸液的效率。当吸附单元有多个时，全部吸附单元的分布形式可以根据需要灵活进行调整；全部吸附单元可以是相同的，也可以是不同的。比如，全部吸附单元可沿左右方向、前后方向、斜向或螺旋方向中的一个方向或多个方向进行分布，以满足不同风量的要求。全部吸附单元可以呈矩形阵列分布，也可以呈金字塔状分布。上述各种形状的第一电极和第二电极可以自由组合形成吸附单元。例如，线状的第一电极插入管状的第二电极形成吸附单元，再与线状的第一电极组合，形成新的吸附单元，此时两个线状的第一电极可电连接；新的吸附单元再在左右方向、上下方向、斜向或螺旋方向中的一个方向或多个方向进行分布。再例如，线状的第一电极插入管状的第二电极形成吸附单元，此吸附单元在左右方向、上下方向、斜向或螺旋方向中的一个方向或多个方向进行分布，形成新的吸附单元，该新的吸附单元再与上述各种形状的第一电极进行组合，以形成新的吸附单元。吸附单元中的第一电极和第二电极之间的距离可以任意调整，以适应不同的工作电压和吸附对象的要求。不同的吸附单元之间可以进行组合。不同的吸附单元可以使用同一电源，也可以使用不同的电源。当使用不同的电源时，各电源的上电驱动电压可以是相同的，也可以是不同的。另外，本电凝装置也可以有多个，且全部电凝装置可以沿左右方向、上下方向、螺旋方向或斜向中的一个方向或多个方向进行分布。
于本发明一实施例中电凝装置还包括电凝壳体，该电凝壳体包括电凝进口、电凝出口及电凝流道，电凝流道的两端分别与电凝进口和电凝出口相连通。于本发明一实施例中电凝进口呈圆形，且电凝进口的直径为300～1000mm、或500mm。于本发明一实施例中电凝出口呈圆形，且电凝出口的直径为300～1000mm、或500mm。于本发明一实施例中电凝壳体包括由 电凝进口至电凝出口方向依次分布的第一壳体部、第二壳体部、及第三壳体部，电凝进口位于第一壳体部的一端，电凝出口位于第三壳体部的一端。于本发明一实施例中第一壳体部的轮廓大小由电凝进口至电凝出口方向逐渐增大。于本发明一实施例中第一壳体部呈直管状。于本发明一实施例中第二壳体部呈直管状，且第一电极和第二电极安装在第二壳体部中。于本发明一实施例中第三壳体部的轮廓大小由电凝进口至电凝出口方向逐渐减小。于本发明一实施例中第一壳体部、第二壳体部、及第三壳体部的截面均呈矩形。于本发明一实施例中电凝壳体的材质为不锈钢、铝合金、铁合金、布、海绵、分子筛、活性炭、泡沫铁、或泡沫碳化硅。于本发明一实施例中第一电极通过电凝绝缘件与电凝壳体相连接。于本发明一实施例中电凝绝缘件的材质为绝缘云母。于本发明一实施例中电凝绝缘件呈柱状、或塔状。于本发明一实施例中第一电极上设有呈圆柱形的前连接部，且前连接部与电凝绝缘件固接。于本发明一实施例中第二电极上设有呈圆柱形的后连接部，且后连接部与电凝绝缘件固接。
于本发明一实施例中第一电极位于电凝流道中。于本发明一实施例中第一电极的截面面积与电凝流道的截面面积比为99％～10％、或90～10％、或80～20％、或70～30％、或60～40％、或50％。第一电极的截面面积是指第一电极沿截面上实体部分的面积之和。
在收集含硝酸的水雾过程中，含硝酸的水雾由电凝进口进入电凝壳体，并朝向电凝出口处移动；在含硝酸的水雾朝向电凝出口移动过程中，含硝酸的水雾将经过第一电极，并带电；第二电极将带电的含硝酸的水雾吸附住，以将含硝酸的水雾收集在第二电极上。本发明利用电凝壳体引导排气及含硝酸的水雾流经第一电极，以利用第一电极使硝酸的水雾带电，并利用第二电极收集硝酸的水雾，从而有效降低由电凝出口处流出的硝酸的水雾。于本发明一些实施例中电凝壳体的材质可以是金属、非金属、导体、非导体、水、各类导电液体、各类多孔材料、或各类泡沫材料等。当电凝壳体的材质为金属时，其材质具体可以是不锈钢、或铝合金等。当电凝壳体的材质是非金属时，其材质具体可以是布、或海绵等。当电凝壳体的材质是导体时，其材质具体可以是铁合金等。当电凝壳体的材质是非导体时，其表面形成水层水即成为电极，如吸水后的沙层。当电凝壳体的材质为水和各类导电液体时，电凝壳体是静止或流动的。当电凝壳体的材质为各类多孔材料时，其材质具体可以是分子筛或活性炭。当电凝壳体的材质为各类泡沫材料时，其材质具体可以是泡沫铁、泡沫碳化硅等。在一种实施例中第一电极通过电凝绝缘件与电凝壳体固接，电凝绝缘件的材质可以为绝缘云母。同时，在一种实施例中第二电极直接与电凝壳体电连接，此种连接方式使得电凝壳体可以与第二电极具有相同的电势，这样电凝壳体也能吸附带电的含硝酸的水雾，电凝壳体也构成一种第二电极。电凝壳体中设有上述电凝流道，第一电极安装在电凝流道中。
当含硝酸的水雾附着在第二电极后，将形成凝露。于本发明一些实施例中第二电极可沿上下方向延伸，这样堆积在第二电极上的凝露达到一定重量时，将在重力的作用下沿第二电极向下流动，并最终汇集在设定位置或装置中，从而实现对附着在第二电极上的硝酸液的回收。本电凝装置可用于制冷除雾。另外，也可以采用外加电凝电场的方式对附着在第二电极上的物质进行收集。对第二电极上的物质收集方向既可以同气流相同，也可以与气流方向不同。在具体实施时，因为是要充分利用重力作用，使第二电极上的水滴或水层尽快流入收集槽中的；同时会尽量利用气流方向及其作用力，来加速第二电极上水流的速度。因此会根据不同的安装条件，以及绝缘的方便性、经济性和可行性等，尽量达到上述目的，不拘束于特定的方向。
另外，当前已有的静电场荷电理论是利用电晕放电，电离氧气，产生大量的负氧离子，负氧离子和粉尘接触，粉尘荷电，荷电后的粉尘被异极吸附。但当遇到含硝酸的水雾等低比电阻物质时，现有的电场吸附作用几乎没有。因低比电阻物质在得电后容易失电，当移动中的负氧离子使低比电阻物质荷电后，低比电阻物质又将很快失电，而负氧离子只移动一次，导致如含硝酸的水雾等低比电阻物质失电后难以再带电，或此种带电方式大大降低了低比电阻物质带电的几率，使得低比电阻物质整体处于不带电状态，这样异极就难以对低比电阻物质持续施加吸附力，最终导致现有的电场对含硝酸的水雾等低比电阻物质的吸附效率极低。上述电凝装置及电凝方法，不是采用荷电方式让水雾带电，而是直接将电子传递给含硝酸的水雾使其带电，在某个雾滴带电又失电后，新的电子将快速由第一电极、并通过其它雾滴传递到该失电的雾滴上，使得雾滴失电后又能快速得电，大大增加了雾滴带电几率，如次重复，使得雾滴整体处于得电状态，并使得第二电极能持续给雾滴施加吸引力，直至吸附住雾滴，从而保证本电凝装置对含硝酸的水雾的收集效率更高。本发明采用的上述使雾滴带电的方法，不需要使用电晕线、电晕极、或电晕板等，简化了本电凝装置的整体结构，降低了本电凝装置的制造成本。同时，本发明采用上述上电方式，也使得第一电极上的大量电子，将通过雾滴传递给第二电极，并形成电流。当流经本电凝装置的水雾的浓度越大时，第一电极上的电子更容易通过含硝酸的水雾传递给第二电极，更多的电子将在雾滴间传递，使得第一电极和第二电极之间形成的电流更大，并使得雾滴的带电几率更高，且使本电凝装置对水雾的收集效率更高。
于本发明一实施例中提供一种电凝除雾方法，包括如下步骤：
使带水雾的气体流经第一电极；
当带水雾的气体流经第一电极时，第一电极使气体中的水雾带电，第二电极给带电的水 雾施加吸引力，使水雾向第二电极移动，直至水雾附着在第二电极上。
于本发明一实施例中第一电极将电子导入水雾，电子在位于第一电极和第二电极之间的雾滴之间进行传递，使更多雾滴带电。
于本发明一实施例中第一电极和第二电极之间通过水雾传导电子、并形成电流。
于本发明一实施例中第一电极通过与水雾接触的方式使水雾带电。
于本发明一实施例中第一电极通过能量波动的方式使水雾带电。
于本发明一实施例中附着在第二电极上的水雾形成水滴，第二电极上的水滴流入收集槽中。
于本发明一实施例中第二电极上的水滴在重力作用下流入收集槽。
于本发明一实施例中气体流动时，将吹动水滴流入收集槽中。
于本发明一实施例中使带硝酸雾的气体流经第一电极；当带硝酸雾的气体流经第一电极时，第一电极使气体中的硝酸雾带电，第二电极给带电的硝酸雾施加吸引力，使硝酸雾向第二电极移动，直至硝酸雾附着在第二电极上。
于本发明一实施例中第一电极将电子导入硝酸雾，电子在位于第一电极和第二电极之间的雾滴之间进行传递，使更多雾滴带电。
于本发明一实施例中第一电极和第二电极之间通过硝酸雾传导电子、并形成电流。
于本发明一实施例中第一电极通过与硝酸雾接触的方式使硝酸雾带电。
于本发明一实施例中第一电极通过能量波动的方式使硝酸雾带电。
于本发明一实施例中附着在第二电极上的硝酸雾形成水滴，第二电极上的水滴流入收集槽中。
于本发明一实施例中第二电极上的水滴在重力作用下流入收集槽。
于本发明一实施例中气体流动时，将吹动水滴流入收集槽中。
于本发明一实施例中本排气处理系统可应用于环保以及化工、大气污染治理等领域，特别是燃烧烟气的处理领域。比如，本排气处理系统可应用于对发电站排放排气的处理。
实施例1
如图5所示，所述排气除尘系统包括除水装置207和电场装置。所述电场装置包括除尘电场阳极10211和除尘电场阴极10212，所述除尘电场阳极10211和所述除尘电场阴极10212用于产生电离除尘电场。所述除水装置207用于在电场装置入口之前去除液体水，当排气温度低于100℃时，所述除水装置脱除排气中的液体水，所述除水装置207为电凝装置，图中 箭头方向为排气流动方向。
一种排气除尘方法，包括以下步骤：排气温度低于100℃时，脱除排气中的液体水，然后电离除尘，其中采用电凝除雾方法脱除排气中的液体水，所述排气为汽油排气排放设备冷启动时的排气，减少排气中的水珠即液体水，减少电离除尘电场放电不均匀及除尘电场阴极和除尘电场阳极击穿，提高电离除尘效率，电离除尘效率为99.9％以上，未脱除排气中的液体水的除尘方法的电离除尘效率为70％以下。因此，排气温度低于100℃时，脱除排气中的液体水，然后电离除尘，减少排气中的水珠即液体水，减少电离除尘电场放电不均匀及除尘电场阴极和除尘电场阳极击穿，提高电离除尘效率。
实施例2
如图6所示，所述排气除尘系统包括补氧装置208和电场装置。所述电场装置包括除尘电场阳极10211和除尘电场阴极10212，所述除尘电场阳极10211和所述除尘电场阴极10212用于产生电离除尘电场。所述补氧装置208用于在电离除尘电场之前添加包括氧气的气体，所述补氧装置208通过通入外界空气的方式添加氧气，根据排气颗粒含量决定补氧量。图中箭头方向为补氧装置添加包括氧气的气体流动方向。
一种排气除尘方法，包括以下步骤：在电离除尘电场之前添加包括氧气的气体，进行电离除尘，通过通入外界空气方式添加氧气，根据排气颗粒含量决定补氧量。
本发明排气除尘系统：包括补氧装置，可以通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气，提高进入电离除尘电场的排气含氧量，从而当排气流经除尘电场阴极和除尘电场阳极之间的电离除尘电场时，增加电离的氧气，使得排气中更多的粉尘荷电，进而在除尘电场阳极的作用下将更多的荷电的粉尘收集起来，使得电场装置的除尘效率更高，有利于电离除尘电场收集排气颗粒物，同时还能起到降温的作用，增加电力系统效率，而且，补氧也会提高电离除尘电场臭氧含量，有利于提高电离除尘电场对排气中有机物进行净化、自洁、脱硝等处理的效率。
实施例3
本实施例所述排气处理系统还包括排气处理装置，所述排气处理装置用于处理欲排入大气中的废气。
请参阅图7，显示为排气处理装置于一实施例中的结构示意图。如图7所示，所述排气处理装置102包括电场装置1021、绝缘机构1022、均风装置、滤水机构及排气臭氧机构。
本发明中滤水机构是可选的，即本发明提供的尾气除尘系统中可包括滤水机构，也可不 包括滤水机构。
所述电场装置1021包括除尘电场阳极10211和设置于除尘电场阳极10211内的除尘电场阴极10212，除尘电场阳极10211与除尘电场阴极10212之间形成非对称静电场，其中，待含有颗粒物的气体通过所述排气口进入所述电场装置1021后，由于所述除尘电场阴极10212放电，电离所述气体，以使所述颗粒物获得负电荷，向所述除尘电场阳极10211移动，并沉积在所述除尘电场阴极10212上。
具体地，所述除尘电场阴极10212的内部由呈蜂窝状、且中空的阳极管束组组成，阳极管束的端口的形状为六边形。
所述除尘电场阴极10212包括若干根电极棒，其一一对应地穿设所述阳极管束组中的每一阳极管束，其中，所述电极棒的形状呈针状、多角状、毛刺状、螺纹杆状或柱状。
在本实施例中，所述除尘电场阴极10212的进气端低于所述除尘电场阳极10211的进气端，且所述除尘电场阴极10212的出气端与所述除尘电场阳极10211的出气端齐平，以使所述电场装置1021内部形成加速电场。
气道外悬的所述绝缘机构1022包括绝缘部和隔热部。所述绝缘部的材料采用陶瓷材料或玻璃材料。所述绝缘部为伞状串陶瓷柱，伞内外挂釉。请参阅图8，显示为呈伞状的绝缘机构于一实施例中的结构示意图。
如图7所示，于本发明一实施例中除尘电场阴极安装在排气阴极支撑板10213上，排气阴极支撑板10213与除尘电场阳极10211通过绝缘机构1022相连接。于本发明一实施例中除尘电场阳极10211包括第一阳极部102112和第二阳极部102111，即所述第一阳极部102112靠近电场装置入口，第二阳极部102111靠近电场装置出口。排气阴极支撑板10213和绝缘机构1022在第一阳极部102112和第二阳极部102111之间，即绝缘机构1022安装在排气电离电场中间、或除尘电场阴极10212中间，可以对除尘电场阴极10212起到良好的支撑作用，并对除尘电场阴极10212起到相对于除尘电场阳极10211的固定作用，使除尘电场阴极10212和除尘电场阳极10211之间保持设定的距离。
所述均风装置1023设置于所述电场装置1021的进气端处的。请参阅图9A、图9B及图9C，显示为均风装置的三种实施结构图。
如图9A所示，当所述除尘电场阳极10211的外型呈圆柱体时，所述均风装置1023为位于进气口处、且由若干围绕所述进风口中心旋转的均风叶片10231组成。所述均风装置1023能够使排气排放设备在各种转速下变化的进气量均匀通过所述除尘电场阳极产生的电场。同时能够保持所述除尘电场阳极内部温度恒定，氧气充足。
如图9B所示，当所述除尘电场阳极10211的外型呈立方体时，所述均风装置包括：
设置于位于所述除尘电场阳极一侧边的进气管10232；及
设置于所述除尘电场阳极另一侧边的出气管10233；其中，安装进气管10232的侧边与安装出气管10233的另一侧边相对立。
如图9C所示，所述均风装置还可以包括设置于所述除尘电场阳极的进气端的第二文氏板均风机构10234和设置于所述除尘电场阳极的出气端的第三文氏板均风机构10235(第三文氏板均风机构俯视时呈折型)，所述第三文氏板均风机构上开设与进气孔，所述第三文氏板均风机构上开设有出气孔，所述进气孔与所述出气孔错位排布，且正面进气侧面出气，形成旋风结构。
设置于所述电场装置1021内的排气滤水机构包括作为第一电极的导电网板，所述导电网板用于在上电后，将电子传导给水(低比电阻物质)。用于吸附带电的水的第二电极于本实施例中为所述电场装置的除尘电场阳极10211。
所述滤水机构的第一电极设置于所述进气口，所述第一电极为一带有负电势导电网板。同时，本实施例的第二电极设置于所述进气装置内呈面网状，且第二电极带有正电势，该第二电极也称作收集极。本实施例中第二电极具体呈平面网状，且第一电极平行于第二电极。本实施例中第一电极和第二电极之间形成网面电场。另外，第一电极由金属丝制成的网状结构，该第一电极由金属丝网构成。本实施例中第二电极的面积大于第一电极的面积。
实施例4
一种排气臭氧净化系统，如图10所示，包括：
臭氧源201，用于提供臭氧流股，所述臭氧流股为臭氧发生器即时生成。
反应场202，用于将臭氧流股与排气流股混合反应。
脱硝装置203，用于脱除臭氧流股与排气流股混合反应产物中的硝酸；所述脱硝装置203包括电凝装置2031，用于将臭氧处理后的排气进行电凝，含硝酸的水雾堆积在电凝装置中的第二电极上。所述脱硝装置203还包括脱硝液收集单元2032，用于存储废气中脱除的硝酸水溶液和/或硝酸盐水溶液；当所述脱硝液收集单元中存储有硝酸水溶液时，所述脱硝液收集单元设有碱液加入单元，用于与硝酸形成硝酸盐。
臭氧消解器204，用于消解经反应场处理后的排气中的臭氧。臭氧消解器可以通过紫外线，催化等方式进行臭氧消解。
所述反应场202为反应器二，如图11所示，内设有若干蜂窝状腔体2021，用于提供排气与臭氧混合并反应的空间；所述蜂窝状腔体内之间设有间隙2022，用于通入冷态介质，控 制排气与臭氧的反应温度，图中右侧箭头为冷媒进口，左侧箭头为冷媒出口。
所述电凝装置包括：
第一电极301，能将电子传导给含硝酸的水雾(低比电阻物质)；当电子被传导给含硝酸的水雾时，含硝酸的水雾带电；
第二电极302，能给带电的含硝酸的水雾施加吸引力。
本实施例中第一电极301有两个，两个第一电极301均呈网状且呈球笼状。本实施例中第二电极302有一个，该第二电极302呈网状且呈球笼状。第二电极302位于两个第一电极301之间。同时，如图25所示，本实施例中电凝装置还包括具有进口3031和出口3032的外壳303，第一电极301和第二电极302均安装在外壳303中。且第一电极301通过绝缘件304与外壳303的内壁固接，第二电极302直接与外壳303固接。本实施例中绝缘件304呈柱状，又称作绝缘柱。本实施例中第一电极301具有负电势，第二电极302具有正电势。同时，本实施例中外壳303与第二电极302具有相同的电势，该外壳303同样对带电的物质具有吸附作用。
本实施例中电凝装置用于处理含有酸雾的工业排气。本实施例中进口3031与排放工业排气的口相连通。本实施例中电凝装置的工作原理如下：工业排气由进口3031流入外壳303，并经出口3032流出；在此过程中，工业排气将先流经其中一个第一电极301，当工业排气中的酸雾与该第一电极301接触时，或与该第一电极301的距离达到一定值时，第一电极301将电子传递给酸雾，部分酸雾带电，第二电极302给带电的酸雾施加吸引力，酸雾向第二电极302移动，并附着在第二电极302上；另有一部分酸雾未被吸附在第二电极302上，该部分酸雾继续向出口3032方向流动，当该部分酸雾与另一个第一电极301接触时，或与另一个第一电极301的距离达到一定值时，该部分酸雾将带电，外壳303给该部分带电的酸雾施加吸附力，使得该部分带电的酸雾附着在外壳303的内壁上，从而大大减少了工业排气中酸雾的排放量，且本实施例中处理装置能去除工业排气中90％的酸雾，去除酸雾的效果非常显著。另外，本实施例中进口3031和出口3032均呈圆形，进口3031也可称作进气口，出口3032也可称作出气口。
实施例5
如图12所示，实施例4中排气臭氧净化系统还包括臭氧量控制装置209，用于控制臭氧量以致有效氧化排气中待处理的气体组分，所述臭氧量控制装置209包括控制单元2091。所述臭氧量控制装置209还包括臭氧处理前排气组分检测单元2092，用于检测臭氧处理前排气组分含量。所述控制单元根据所述臭氧处理前排气组分含量控制混合反应所需臭氧量。
所述臭氧处理前排气组分检测单元选自以下检测单元中至少一个：
第一挥发性有机化合物检测单元20921，用于检测臭氧处理前排气中挥发性有机化合物含量，如挥发性有机化合物传感器等；
第一CO检测单元20922，用于检测臭氧处理前排气中CO含量，如CO传感器等；
第一氮氧化物检测单元20923，用于检测臭氧处理前排气中氮氧化物含量，如氮氧化物(NO x)传感器等。
所述控制单元根据至少一个所述臭氧处理前排气组分检测单元的输出值控制混合反应所需臭氧量。
所述控制单元用于按照理论估计值控制混合反应所需臭氧量。所述理论估计值为：臭氧通入量与排气中待处理物的摩尔比为2～10。
所述臭氧量控制装置包括臭氧处理后排气组分检测单元2093，用于检测臭氧处理后排气组分含量。所述控制单元根据所述臭氧处理后排气组分含量控制混合反应所需臭氧量。
所述臭氧处理后排气组分检测单元选自以下检测单元中至少一个：
第一臭氧检测单元20931，用于检测臭氧处理后排气中臭氧含量；
第二挥发性有机化合物检测单元20932，用于检测臭氧处理后排气中挥发性有机化合物含量；
第二CO检测单元20933，用于检测臭氧处理后排气中CO含量；
第二氮氧化物检测单元20934，用于检测臭氧处理后排气中氮氧化物含量。
所述控制单元根据至少一个所述臭氧处理后排气组分检测单元的输出值控制臭氧量。
实施例6
制备臭氧发生器用电极：
取长300mm，宽30mm，厚1.5mm的α-氧化铝板材作为阻挡介质层；
催化剂(含涂层和活性组份)涂覆在阻挡介质层的一面，涂覆催化剂之后，所述催化剂为所述阻挡介质层质量的12％，所述催化剂包括如下重量百分比的各组分：活性组分为12wt％，涂层为88wt％，其中，所述活性组分为氧化铈和氧化锆(依次物质的量比为1：1.3)，所述涂层为gama氧化铝；
在涂覆好催化剂的阻挡介质层另一面贴铜箔，制成电极。
其中，催化剂涂覆方法如下：
(1)取200g 800目的gama氧化铝粉、5g硝酸铈、4g硝酸锆、4g草酸、5g拟薄水铝石、1g硝酸铝、0.5g EDTA(分解用)，倒入玛瑙磨中。再加入1300g去离子水。200rpm/min 下研磨10个小时。制成浆料；
(2)把上述阻挡介质层放入烘箱中于150℃下烘干2小时，烘干时打开烘箱风扇。然后保持烘箱门关闭的条件下冷却到室温；
(3)把上述催化剂浆料装入通过高压喷枪，均匀喷涂到烘干后的阻挡介质层表面。放入真空干燥器中阴干2小时；
(4)阴干后放入马弗中加热至550℃，加热升温速度为每分钟5℃。恒温两小时，保持炉门关闭条件下，自然冷却到室温。涂覆过程完成。
以同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V、2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为160g/小时。实验条件下，功率损耗均为830W。
实施例7
制备臭氧发生器用电极：
取长300mm，宽30mm，厚1.5mm的α-氧化铝板材作为阻挡介质层；
催化剂(含涂层和活性组份)涂覆在阻挡介质层的一面，涂覆催化剂之后，所述催化剂为所述阻挡介质层质量的5％，所述催化剂包括如下重量百分比的各组分：活性组分占催化剂总重15wt％，涂层85％，其中，所述活性组分为MnO和CuO，所述涂层为gama氧化铝；
在涂覆好催化剂的阻挡介质层另一面贴铜箔，制成电极。
其中，催化剂涂覆方法如下：
(1)取200g 800目的gama氧化铝粉、4g草酸、5g拟薄水铝石、1g硝酸铝、0.5g表面活性剂(分解用)，倒入玛瑙磨中。再加入1300g去离子水。200rpm/min下研磨10个小时。制成浆料；
(2)把上述阻挡介质层放入烘箱中于150℃下烘干2小时，烘干时打开烘箱风扇。然后保持烘箱门关闭的条件下冷却到室温。通过测量烘干前后的质量变化，测出阻挡介质层的吸水量(A)；
(3)把上述浆料装入通过高压喷枪，均匀喷涂到烘干后的阻挡介质层表面。放入真空干 燥器中阴干2小时；
(4)阴干后放入马弗中加热至550℃，加热升温速度为每分钟5℃。恒温两小时，保持炉门关闭条件下，自然冷却到室温。称重。
(5)将上述负载有涂层的阻挡介质层浸入水中1分钟后取出，吹净表面浮水，称重。计算得到其吸水量(B)；
(6)计算得到涂层的净吸水量C(C＝B–A)。根据活性组份目标负载量，涂层净吸水量C，计算得活性组份水溶液的浓度。以此配制活性组份溶液；(活性组份目标负载量CuO 0.1g；MnO 0.2g)
(7)将负载有涂层的阻挡介质层150℃烘干2小时，保持烘箱门关闭条件下冷却至室温。不需负载活组份的面进行防水保护。
(8)取(6)配制好的活性组份溶液(硝酸铜和硝酸锰)，以浸渍法负载到涂层中去，吹去表面浮液。150℃烘干2小时。转入马弗炉中焙烧。以每分钟15℃加热到550℃，恒温3小时。微开炉门，冷却到室温。涂覆过程完成。
同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V,2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为168g/小时。实验条件下，功率损耗均为830W。
实施例8
制备臭氧发生器用电极：
取长300mm，宽30mm，厚1.5mm的石英玻璃板作为阻挡介质层；
催化剂(含涂层和活性组份)涂覆在阻挡介质层的一面，涂覆催化剂之后，所述催化剂为所述阻挡介质层质量的1％，所述催化剂包括如下重量百分比的各组分：活性组分为5wt％，涂层为95wt％，其中，所述活性组分为银、铑、铂、钴和镧(依次物质的量比为1：1：1：2：1.5)，所述涂层为氧化锆；
在涂覆好催化剂的阻挡介质层另一面贴铜箔，制成电极。
其中，催化剂涂覆方法如下：
(1)取400g氧化锆、1.7g硝酸银、2.89g硝酸铑、3.19g硝酸铂、4.37g硝酸钴、8.66g硝酸镧、15g草酸、25g EDTA(分解用)，倒入玛瑙磨中。再加入1500g去离子水。200rpm/min下研磨10个小时。制成浆料；
(2)把上述阻挡介质层放入烘箱中于150℃下烘干2小时，烘干时打开烘箱风扇。然后保持烘箱门关闭的条件下冷却到室温；
(3)把上述催化剂浆料装入通过高压喷枪，均匀喷涂到烘干后的阻挡介质层表面。放入真空干燥器中阴干2小时；
(4)阴干后放入马弗中加热至550℃，加热升温速度为每分钟5℃。恒温两小时，保持炉门关闭条件下，自然冷却到室温；然后于220℃在氢气还原气氛下进行还原1.5小时。涂覆过程完成。
以同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V,2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为140g/小时。实验条件下，功率损耗均为830W。
实施例9
制备臭氧发生器用电极：
催化剂(含涂层和活性组份)涂覆在铜箔(电极)的一面，涂覆催化剂之后，所述催化剂的厚度为1.5mm，所述催化剂包括如下重量百分比的各组分：活性组分为8wt％，涂层为92wt％，其中，所述活性组分为硫酸锌、硫酸钙、硫酸钛和硫酸镁(依次物质的量比为1：2：1：1)，所述涂层为石墨烯。
其中，催化剂涂覆方法如下：
(1)取100g石墨烯、1.61g硫酸锌、3.44g硫酸钙、2.39g硫酸钛、1.20g硫酸镁、25g草酸、15g EDTA(分解用)，倒入玛瑙磨中。再加入800g去离子水。200rpm/min下研磨10个小时。制成浆料；
(2)把上述催化剂浆料装入通过高压喷枪，均匀喷涂到铜箔(电极)的表面上。放入真空干燥器中阴干2小时；
(3)阴干后放入马弗中加热至350℃，加热升温速度为每分钟5℃。恒温两小时，保持 炉门关闭条件下，自然冷却到室温。
以同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V,2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为165g/小时。实验条件下，功率损耗均为830W。
实施例10
制备臭氧发生器用电极：
催化剂(含涂层和活性组份)涂覆在铜箔(电极)的一面，涂覆催化剂之后，所述催化剂的厚度为3mm，所述催化剂包括如下重量百分比的各组分：活性组分为10wt％，涂层为90wt％，其中，所述活性组分为氧化镨、氧化钐和氧化钇(依次物质的量比为1：1：1)，所述涂层为氧化铈和氧化锰(依次物质的量比为1：1)。
其中，催化剂涂覆方法如下：
(1)取62.54g氧化铈、31.59g氧化锰、3.27g硝酸镨、3.36g硝酸钐、3.83g硝酸钇、12g草酸、20g EDTA(分解用)，倒入玛瑙磨中。再加入800g去离子水。200rpm/min下研磨10个小时。制成浆料；
(2)把上述催化剂浆料装入通过高压喷枪，均匀喷涂到铜箔(电极)的表面上。放入真空干燥器中阴干2小时；
(3)阴干后放入马弗中加热至500℃，加热升温速度为每分钟5℃。恒温两小时，保持炉门关闭条件下，自然冷却到室温。
以同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V,2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为155g/小时。实验条件下，功率损耗均为830W。
实施例11
制备臭氧发生器用电极：
催化剂(含涂层和活性组份)涂覆在铜箔(电极)的一面，涂覆催化剂之后，所述催化剂的厚度为1mm，所述催化剂包括如下重量百分比的各组分：活性组分为14wt％，涂层为86wt％，其中，所述活性组分为硫化锶、硫化镍、硫化锡和硫化铁(依次物质的量比为2：1：1：1)，所述涂层为硅藻土，孔隙率为80％，比表面积为350平方米/克，平均孔径为30纳米。
其中，催化剂涂覆方法如下：
(1)取58g硅藻土、3.66g硫酸锶、2.63g硫酸镍、2.18g硫酸亚锡、2.78g硫酸亚铁、3g草酸、5g EDTA(分解用)，倒入玛瑙磨中。再加入400g去离子水。200rpm/min下研磨10个小时。制成浆料；
(2)把上述催化剂浆料装入通过高压喷枪，均匀喷涂到铜箔(电极)的表面上。放入真空干燥器中阴干2小时；
(3)阴干后放入马弗中加热至500℃，加热升温速度为每分钟5℃。恒温两小时，保持炉门关闭条件下，自然冷却到室温；然后再通入CO进行硫化反应，涂敷过程完成。
以同样的方法，制备4块电极。取河南迪诺环保科技股份有限公司XF-B-3-100型臭氧发生器，把其中的4块电极全换成上述制成的电极。进行比对试验，试验条件为：纯氧气气源，进气压力为0.6MPa，进气风量为每小时1.5立方米，交流电压，5000V,2万赫兹的正弦波。通过出气风量和质量浓度检测结果计算得每小时臭氧产生量。
实验结果如下：
XF-B-3-100型原臭氧产生量为120g/小时；更换电极后，同样的试验条件下，臭氧产生量为155g/小时。实验条件下，功率损耗均为830W。
实施例12
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
如图13、图14和图15所示，本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中。
减少电场耦合的方法，包括如下步骤：选择除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为6.67：1，除尘电场阳极4051和除尘电场阴极4052的极间距为9.9mm，除尘电场阳极4051长度为60mm，除尘电场阴极4052长度为54mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端之间具有夹角α，且α＝118°，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，实现电场耦合次数≤3，能够减少电场对气溶胶、水雾、油雾、松散光滑颗粒物的耦合消耗，节省电场电能30～50％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。
多个电场级中各电场级之间串联，串联电场级通过连接壳体连接，相邻两级的电场级的距离大于极间距的1.4倍。如图16所示，所述电场级为两级即第一级电场和第二级电场，第一级电场和第二级电场通过连接壳体串联连接。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例13
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中。
减少电场耦合的方法，包括如下步骤：选择除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为1680：1，除尘电场阳极4051和除尘电场阴极4052的极间距为139.9mm，除尘电场阳极4051长度为180mm，除尘电场阴极4052长度为180mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，实现电场耦合次数≤3，能够减少电场对气溶胶、水雾、油雾、松散光滑颗粒物的耦合消耗，节省电场电能20～40％。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例14
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中。
减少电场耦合的方法，包括如下步骤：选择除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为1.667：1，除尘电场阳极4051和除尘电场阴极4052的极间距为2.5mm，除尘电场阳极4051长度为30mm，除尘电场阴极4052长度为30mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，实现电场耦合次数≤3，能够减少电场对气溶胶、水雾、油雾、松 散光滑颗粒物的耦合消耗，节省电场电能10～30％。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例15
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
如图13、图14和图15所示，本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为6.67：1，所述除尘电场阳极4051和除尘电场阴极4052的极间距为9.9mm，除尘电场阳极4051长度为60mm，除尘电场阴极4052长度为54mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端之间具有夹角α，且α＝118°，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，保证本电场发生单元的集尘效率更高，典型排气颗粒pm0.23集尘效率为99.99％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。
多个电场级中各电场级之间串联，串联电场级通过连接壳体连接，相邻两级的电场级的距离大于极间距的1.4倍。如图16所示，所述电场级为两级即第一级电场4053和第二级电场4054，第一级电场4053和第二级电场4054通过连接壳体4055串联连接。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例16
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为1680：1，所述除尘电场阳极4051和除尘电场阴极4052的极间距为139.9mm，除尘电场阳极4051长度为180mm，除尘电场阴极4052长度为180mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，保证本电场装置的集尘效率更高，典型排气颗粒pm0.23集尘效率为99.99％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例17
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052 分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051的集尘面积与除尘电场阴极4052的放电面积的比为1.667：1，所述除尘电场阳极4051和除尘电场阴极4052的极间距为2.5mm。除尘电场阳极4051长度为30mm，除尘电场阴极4052长度为30mm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，能将更多的待处理物质收集起来，保证本电场装置的集尘效率更高，典型排气颗粒pm0.23集尘效率为99.99％。
本实施例中除尘电场阳极4051及除尘电场阴极4052构成集尘单元，且该集尘单元有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质，如气溶胶、水雾、油雾等。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例18
本实施例中排气系统，包括上述实施例15、实施例16或实施例17中的电场装置。由排气排放设备排出的气体需先流经该电场装置，以利用该电场装置有效地将气体中的粉尘等污染物清除掉；随后，经处理后的气体再排放至大气，以降低排气对大气造成的影响。该排气系统也称作排气处理装置。
实施例19
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电 场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051长度为5cm，除尘电场阴极4052长度为5cm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，所述除尘电场阳极4051和除尘电场阴极4052的极间距为9.9mm，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，使得其耐高温冲击，而且能将更多的待处理物质收集起来，保证本电场发生单元的集尘效率更高。电场温度为200℃对应的集尘效率为99.9％；电场温度为400℃对应的集尘效率为90％；电场温度为500℃对应的集尘效率为50％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。
本实施例中上述待处理物质可以是呈颗粒状的粉尘。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例20
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051长度为9cm，除尘电场阴极4052长度为9cm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体 通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，所述除尘电场阳极4051和除尘电场阴极4052的极间距为139.9mm，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，使得其耐高温冲击，而且能将更多的待处理物质收集起来，保证本电场发生单元的集尘效率更高。电场温度为200℃对应的集尘效率为99.9％；电场温度为400℃对应的集尘效率为90％；电场温度为500℃对应的集尘效率为50％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各存储电场阳极为相同极性，各除尘电场阴极为相同极性。
本实施例中上述待处理物质可以是呈颗粒状的粉尘。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例21
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051长度为1cm，除尘电场阴极4052长度为1cm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端齐平，所述除尘电场阳极4051和除尘电场阴极4052的极间距为2.5mm，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，使得其耐高温冲击，而且能将更多的待处理物质收集起来，保证本电场发生单元的集尘效率更高。电场温度为200℃对应的集尘效率为99.9％；电场温度为400℃对应的集尘效率为90％；电场温度为500℃对应的集尘效率为50％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个， 以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各除尘电场阳极为相同极性，各除尘电场阴极为相同极性。
多个电场级中各电场级之间串联，串联电场级通过连接壳体连接，相邻两级的电场级的距离大于极间距的1.4倍。所述电场级为两级即第一级电场和第二级电场，第一级电场和第二级电场通过连接壳体串联连接。
本实施例中上述待处理物质可以是呈颗粒状的粉尘。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例22
本实施例中电场发生单元可应用于电场装置，如图13所示，包括用于发生电场的除尘电场阳极4051和除尘电场阴极4052，所述除尘电场阳极4051和除尘电场阴极4052分别与电源的两个电极电性连接，所述电源为直流电源，所述除尘电场阳极4051和除尘电场阴极4052分别与直流电源的阳极和阴极电性连接。本实施例中除尘电场阳极4051具有正电势，除尘电场阴极4052具有负电势。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阳极4051和除尘电场阴极4052之间形成放电电场，该放电电场是一种静电场。
如图13和图14所示，本实施例中除尘电场阳极4051呈中空的正六边形管状，除尘电场阴极4052呈棒状，除尘电场阴极4052穿设在除尘电场阳极4051中，除尘电场阳极4051长度为3cm，除尘电场阴极4052长度为2cm，所述除尘电场阳极4051包括流体通道，所述流体通道包括进口端与出口端，所述除尘电场阴极4052置于所述流体通道中，所述除尘电场阴极4052沿集尘极流体通道的方向延伸，除尘电场阳极4051的进口端与除尘电场阴极4052的近进口端齐平，除尘电场阳极4051的出口端与除尘电场阴极4052的近出口端之间具有夹角α，且α＝90°，所述除尘电场阳极4051和除尘电场阴极4052的极间距为20mm，进而在除尘电场阳极4051和除尘电场阴极4052的作用下，使得其耐高温冲击，而且能将更多的待处理物质收集起来，保证本电场发生单元的集尘效率更高。电场温度为200℃对应的集尘效率为99.9％；电场温度为400℃对应的集尘效率为90％；电场温度为500℃对应的集尘效率为50％。
本实施例中电场装置包括由多个上述电场发生单元构成的电场级，所述电场级有多个，以利用多个集尘单元有效提高本电场装置的集尘效率。同一电场级中，各集尘极为相同极性，各放电极为相同极性。
多个电场级中各电场级之间串联，串联电场级通过连接壳体连接，相邻两级的电场级的距离大于极间距的1.4倍。如图16所示，所述电场级为两级即第一级电场和第二级电场，第 一级电场和第二级电场通过连接壳体串联连接。
本实施例中上述待处理物质可以是呈颗粒状的粉尘。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
实施例23
本实施例中排气系统，包括上述实施例19、实施例20、实施例21或实施例22中的电场装置。由排气排放设备排出的气体需先流经该电场装置，以利用该电场装置有效地将气体中的粉尘等污染物清除掉；随后，经处理后的气体再排放至大气，以降低排气对大气造成的影响。该排气系统也称作排气处理装置。
实施例24
本实施例中电场装置包括除尘电场阴极5081和除尘电场阳极5082分别与直流电源的阴极和阳极电性连接，辅助电极5083与直流电源的阳极电性连接。本实施例中除尘电场阴极5081具有负电势，除尘电场阳极5082和辅助电极5083均具有正电势。
同时，如图17所示，本实施例中辅助电极5083与除尘电场阳极5082固接。在除尘电场阳极5082与直流电源的阳极电性连接后，也实现了辅助电极5083与直流电源的阳极电性连接，且辅助电极5083与除尘电场阳极5082具有相同的正电势。
如图17所示，本实施例中辅助电极5083可沿前后方向延伸，即辅助电极5083的长度方向可与除尘电场阳极5082的长度方向相同。
如图17所示，本实施例中除尘电场阳极5082呈管状，除尘电场阴极5081呈棒状，除尘电场阴极5081穿设在除尘电场阳极5082中。同时本实施例中上述辅助电极5083也呈管状，辅助电极5083与除尘电场阳极5082构成阳极管5084。阳极管5084的前端与除尘电场阴极5081齐平，阳极管5084的后端向后超出了除尘电场阴极5081的后端，该阳极管5084相比于除尘电场阴极5081向后超出的部分为上述辅助电极5083。即本实施例中除尘电场阳极5082和除尘电场阴极5081的长度相同，除尘电场阳极5082和除尘电场阴极5081在前后方向上位置相对；辅助电极5083位于除尘电场阳极5082和除尘电场阴极5081的后方。这样，辅助电极5083与除尘电场阴极5081之间形成辅助电场，该辅助电场给除尘电场阳极5082和除尘电场阴极5081之间带负电荷的氧离子流施加向后的力，使得除尘电场阳极5082和除尘电场阴极5081间带负电荷的氧离子流具有向后的移动速度。当含有待处理物质的气体由前向后流入阳极管5084，带负电荷的氧离子在向除尘电场阳极5082且向后移动过程中将与待处理物质 相结合，由于氧离子具有向后的移动速度，氧离子在与待处理物质相结合时，两者间不会产生较强的碰撞，从而避免因较强碰撞而造成较大的能量消耗，使得氧离子易于与待处理物质相结合，并使得气体中待处理物质的荷电效率更高，进而在除尘电场阳极5082及阳极管5084的作用下，能将更多的待处理物质收集起来，保证本电场装置的除尘效率更高。
另外，如图9所示，本实施例中阳极管5084的后端与除尘电场阴极5081的后端之间具有夹角α，且0°＜α≤125°、或45°≤α≤125°、或60°≤α≤100°、或α＝90°。
本实施例中除尘电场阳极5082、辅助电极5083、及除尘电场阴极5081构成除尘单元，且该除尘单元有多个，以利用多个除尘单元有效提高本电场装置的除尘效率。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质。
本实施例中上述气体可以是欲进入排气排放设备的气体，或排气排放设备排出的气体。
本实施例中直流电源具体可为直流高压电源。上述除尘电场阴极5081和除尘电场阳极5082之间形成放电电场，该放电电场是一种静电场。在无上述辅助电极5083的情况下，除尘电场阴极5081和除尘电场阳极5082之间电场中离子流沿垂直于电极方向，且在两电极间折返流动，并导致离子在电极间来回折返消耗。为此，本实施例利用辅助电极5083使电极相对位置错开，形成除尘电场阳极5082和除尘电场阴极5081间相对不平衡，这个不平衡会使电场中离子流发生偏转。本电场装置利用辅助电极5083形成能使离子流具有方向性的电场。本实施例中上述电场装置也称作一种有加速方向电场装置。本电场装置对顺离子流方向进入电场的颗粒物的收集率比对逆离子流方向进入电场的颗粒物的收集率提高近一倍，从而提高电场积尘效率，减少电场电耗。另外，现有技术中集尘电场的除尘效率较低的主要原因也是粉尘进入电场方向与电场内离子流方向相反或垂直交叉，从而导致粉尘与离子流相互冲撞剧烈并产生较大能量消耗，同时也影响荷电效率，进而使现有技术中电场集尘效率下降，且能耗增加。
本实施例中电场装置在用于收集气体中的粉尘时，气体及粉尘顺离子流方向进入电场，粉尘荷电充分，电场消耗小；单极电场集尘效率会达到99.99％。当气体及粉尘逆离子流方向进入电场，粉尘荷电不充分，电场电耗也会增加，集尘效率会在40％-75％。另外，本实施例中电场装置形成的离子流有利于无动力风扇流体输送、增氧、热量交换等。
实施例25
本实施例中电场装置包括除尘电场阴极5081和除尘电场阳极5082分别与直流电源的阴极和阳极电性连接，辅助电极5083与直流电源的阴极电性连接。本实施例中辅助电极5083和除尘电场阴极5081均具有负电势，除尘电场阳极5082具有正电势。
本实施例中辅助电极5083可与除尘电场阴极5081固接。这样，在实现除尘电场阴极5081与直流电源的阴极电性连接后，也实现了辅助电极5083与直流电源的阴极电性连接。同时，本实施例中辅助电极5083沿前后方向延伸。
本实施例中除尘电场阳极5082呈管状，除尘电场阴极5081呈棒状，除尘电场阴极5081穿设在除尘电场阳极5082中。同时本实施例中上述辅助电极5083也棒状，且辅助电极5083和除尘电场阴极5081构成阴极棒。该阴极棒的前端向前超出除尘电场阳极5082的前端，该阴极棒与除尘电场阳极5082相比向前超出的部分为上述辅助电极5083。即本实施例中除尘电场阳极5082和除尘电场阴极5081的长度相同，除尘电场阳极5082和除尘电场阴极5081在前后方向上位置相对；辅助电极5083位于除尘电场阳极5082和除尘电场阴极5081的前方。这样，辅助电极5083与除尘电场阳极5082之间形成辅助电场，该辅助电场给除尘电场阳极5082和除尘电场阴极5081之间带负电荷的氧离子流施加向后的力，使得除尘电场阳极5082和除尘电场阴极5081间带负电荷的氧离子流具有向后的移动速度。当含有待处理物质的气体由前向后流入管状的除尘电场阳极5082，带负电荷的氧离子在向除尘电场阳极5082且向后移动过程中将与待处理物质相结合，由于氧离子具有向后的移动速度，氧离子在与待处理物质相结合时，两者间不会产生较强的碰撞，从而避免因较强碰撞而造成较大的能量消耗，使得氧离子易于与待处理物质相结合，并使得气体中待处理物质的荷电效率更高，进而在除尘电场阳极5082作用下，能将更多的待处理物质收集起来，保证本电场装置的除尘效率更高。
本实施例中除尘电场阳极5082、辅助电极5083、及除尘电场阴极5081构成除尘单元，且该除尘单元有多个，以利用多个除尘单元有效提高本电场装置的除尘效率。
本实施例中上述待处理物质可以是呈颗粒状的粉尘，也可以是其它需处理的杂质。
实施例26
如图18所示，本实施例中电场装置中，辅助电极5083沿左右方向延伸。本实施例中辅助电极5083的长度方向与除尘电场阳极5082和除尘电场阴极5081的长度方向不同。且辅助电极5083具体可与除尘电场阳极5082相垂直。
本实施例中除尘电场阴极5081和除尘电场阳极5082分别与直流电源的阴极和阳极电性连接，辅助电极5083与直流电源的阳极电性连接。本实施例中除尘电场阴极5081具有负电势，除尘电场阳极5082和辅助电极5083均具有正电势。
如图18所示，本实施例中除尘电场阴极5081和除尘电场阳极5082在前后方向上位置相对，辅助电极5083位于除尘电场阳极5082和除尘电场阴极5081的后方。这样，辅助电极 5083与除尘电场阴极5081之间形成辅助电场，该辅助电场给除尘电场阳极5082和除尘电场阴极5081之间带负电荷的氧离子流施加向后的力，使得除尘电场阳极5082和除尘电场阴极5081间带负电荷的氧离子流具有向后的移动速度。当含有待处理物质的气体由前向后流入除尘电场阳极5082和除尘电场阴极5081之间的电场，带负电荷的氧离子在向除尘电场阳极5082且向后移动过程中将与待处理物质相结合，由于氧离子具有向后的移动速度，氧离子在与待处理物质相结合时，两者间不会产生较强的碰撞，从而避免因较强碰撞而造成较大的能量消耗，使得氧离子易于与待处理物质相结合，并使得气体中待处理物质的荷电效率更高，进而在除尘电场阳极5082的作用下，能将更多的待处理物质收集起来，保证本电场装置的除尘效率更高。
实施例27
如图19所示，本实施例中电场装置中，辅助电极5083沿左右方向延伸。本实施例中辅助电极5083的长度方向与除尘电场阳极5082和除尘电场阴极5081的长度方向不同。且辅助电极5083具体可与除尘电场阴极5081相垂直。
本实施例中除尘电场阴极5081和除尘电场阳极5082分别与直流电源的阴极和阳极电性连接，辅助电极5083与直流电源的阴极电性连接。本实施例中除尘电场阴极5081和辅助电极5083均具有负电势，除尘电场阳极5082具有正电势。
如图19所示，本实施例中除尘电场阴极5081和除尘电场阳极5082在前后方向上位置相对，辅助电极5083位于除尘电场阳极5082和除尘电场阴极5081的前方。这样，辅助电极5083与除尘电场阳极5082之间形成辅助电场，该辅助电场给除尘电场阳极5082和除尘电场阴极5081之间带负电荷的氧离子流施加向后的力，使得除尘电场阳极5082和除尘电场阴极5081间带负电荷的氧离子流具有向后的移动速度。当含有待处理物质的气体由前向后流入除尘电场阳极5082和除尘电场阴极5081之间的电场，带负电荷的氧离子在向除尘电场阳极5082且向后移动过程中将与待处理物质相结合，由于氧离子具有向后的移动速度，氧离子在与待处理物质相结合时，两者间不会产生较强的碰撞，从而避免因较强碰撞而造成较大的能量消耗，使得氧离子易于与待处理物质相结合，并使得气体中待处理物质的荷电效率更高，进而在除尘电场阳极5082的作用下，能将更多的待处理物质收集起来，保证本电场装置的除尘效率更高。
实施例28
本实施例中排气装置，包括上述实施例24、25、26、或27中的电场装置。由排气排放设备排出的气体需先流经该电场装置，以利用该电场装置有效地将气体中的粉尘等污染物清除 掉；随后，经处理后的气体再排放至大气，以降低排气对大气造成的影响。本实施例中排气装置也称作电场装置。
实施例29
本实施例提供一种电场装置，包括除尘电场阴极和除尘电场阳极。除尘电场阴极和除尘电场阳极分别与直流电源的两个电极电性连接，除尘电场阴极和除尘电场阳极之间具有电离除尘电场，电场装置还包括补氧装置。补氧装置用于在所述电离除尘电场之前向排气中添加包括氧气的气体。补氧装置可通过单纯增氧、通入外界空气、通入压缩空气和/或通入臭氧的方式添加氧气。本实施例中电场装置，利用补氧装置向排气中补充氧气，以提高气体含氧量，从而当排气流经电离除尘电场时，使得气体中更多的粉尘荷电，进而在除尘电场阳极的作用下将更多的荷电的粉尘收集起来，使得本电场装置的除尘效率更高。
本实施例中至少根据排气颗粒含量决定补氧量。
本实施例中除尘电场阴极和除尘电场阳极分别与直流电源的阴极和阳极电性连接，使得除尘电场阳极具有正电势、除尘电场阴极具有负电势。同时，本实施例中直流电源具体可为高压直流电源。本实施例中除尘电场阴极和除尘电场阳极之间形成的电场具体可称作一种静电场。
本实施例中电场装置适用于低氧环境中，该电场装置也称作一种适用于低氧环境的电场装置。本实施例中补氧装置包括风机，以利用风机将外界的空气及氧气补入排气中，让进入电场的排气中氧的浓度得以提高，从而提高排气中粉尘等颗粒物的荷电几率，进而提高电场及本电场装置对氧浓度较低的排气中粉尘等物质的收集效率。另外，风机向排气中补入的空气也能作为冷却风，对排气起到降温的作用。本实施例中风机将空气通入排气中，并在电场装置入口之前，对排气起到降温的作用。通入的空气可以是排气的50％至300％、或100％至180％、或120％至150％。
本实施例中电离除尘电场及电场装置具体可用于收集燃油排气或燃烧炉排气中的粉尘等颗粒物，即上述气体具体可为燃油排气或燃烧炉排气。本实施例利用补氧装置向排气中补入新风或单纯增氧，以提高排气的含氧量，就能提升电离除尘电场收集排气中颗粒物以及气溶胶态物质的效率。同时，还能对排气起到降温的作用，从而更有利于电场收集排气中的颗粒物。
本实施例也可通过补氧装置向排气中通入压缩空气、或臭氧等方式实现排气增氧；同时调整前级排气排放设备或锅炉等设备的燃烧情况，使产生的排气含氧量稳定，从而满足电场荷电及集尘需要。
本实施例中补氧装置具体可包括正压风机和管道。除尘电场阴极和除尘电场阳极构成电场组件，且上述除尘电场阴极也称作一种电晕极。高压直流电源和电源线构成电源组件。本实施例利用补氧装置将空气中的氧气补充到排气中，使粉尘充荷电，避免排气因氧含量波动引发电场效率波动。同时，补氧也会提高电场臭氧含量，有利于提高电场对排气中有机物进行净化、自洁、脱硝等处理的效率。
本实施例中电场装置也称作一种除尘器。上述除尘电场阴极和除尘电场阳极之间具有除尘通道，该除尘通道中形成上述电离除尘电场。如图20和图21所示，本电场装置还包括与除尘通道相通的叶轮涵道3091、与叶轮涵道3091相通的排气通道3092、及与叶轮涵道3091相通的增氧涵道3093。叶轮涵道3091中安装有叶轮3094，该叶轮3094构成上述风机，即上述补氧装置包括叶轮3094。增氧涵道3093位于排气通道3092的外围，增氧涵道3093也称作外涵道。增氧涵道3093的一端设有空气进口30931，排气通道3092的一端设有排气进口30921，且该排气进口30921与排气排放设备或燃烧炉的排气口相通。这样，排气排放设备或燃烧炉等排放的排气将通过排气进口30921及排气通道3092进入叶轮涵道3091，并推动叶轮涵道3091中的叶轮3094旋转，同时起到对排气降温的作用，且叶轮3094旋转时将外界的空气由空气进口30931吸入增氧涵道3093及叶轮涵道3091，从而使空气混入排气中，达到对排气增氧降温的目的；补入氧气的排气再经叶轮涵道3091流经除尘通道，进而利用电场对增氧后的排气进行除尘，且使得除尘效率更高。本实施例中上述叶轮涵道3091及叶轮3094构成涡扇。
实施例30
如图22至图24所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给含硝酸的水雾；当电子被传导给硝酸的水雾时，硝酸的水雾带电；
第二电极302，能给带电的水雾施加吸引力。
同时，如图22所示，本实施例中电凝装置还包括具有电凝进口3031和电凝出口3032的电凝壳体303，第一电极301和第二电极302均安装在电凝壳体303中。且第一电极301通过电凝绝缘件304与电凝壳体303的内壁固接，第二电极302直接与电凝壳体303固接。本实施例中电凝绝缘件304呈柱状，又称作绝缘柱。在另一种实施例中电凝绝缘件304还可以呈塔状等。本电凝绝缘件304主要是防污染防漏电。本实施例中第一电极301和第二电极302均呈网状，且两者均于电凝进口3031和电凝出口3032之间。第一电极301具有负电势，第二电极302具有正电势。同时，本实施例中电凝壳体303与第二电极302具有相同的电势， 该电凝壳体303同样对带电的物质具有吸附作用。本实施例中电凝壳体中设有电凝流道3036，第一电极301和第二电极302均安装在电凝流道3036中，且第一电极301的截面面积与电凝流道3036的截面面积比为99％～10％、或90～10％、或80～20％、或70～30％、或60～40％、或50％。
本实施例中电凝装置还可以用于处理含有酸雾的工业排气。当电凝装置用于处理含有酸雾的工业排气时，本实施例中电凝进口3031与排放工业排气的口相连通。如图22所示，本实施例中电凝装置的工作原理如下：工业排气由电凝进口3031流入电凝壳体303，并经电凝出口3032流出；在此过程中，工业排气将流经第一电极301，当工业排气中的酸雾与第一电极301接触时，或与第一电极301的距离达到一定值时，第一电极301将电子传递给酸雾，酸雾带电，第二电极302给带电的酸雾施加吸引力，酸雾向第二电极302移动，并附着在第二电极302上；由于酸雾具有易带且易失电特性，某个带电的雾滴在向第二电极302移动过程中又将失电，此时其它带电的雾滴又将快速将电子传递给该失电的雾滴，如此重复，雾滴处于持续带电状态，第二电极302就能持续给雾滴施加吸附力，并使得雾滴附着在第二电极302，从而实现对工业排气中酸雾的去除，避免酸雾直接排放至大气中，并对大气造成污染。本实施例中上述第一电极301和第二电极302构成吸附单元。且在吸附单元仅有一个的情况下，本实施例中电凝装置能除去工业排气中80％的酸雾，大大降低了酸雾的排放量，具有显著的环保效果。
如图24所示，本实施例中第一电极301上设有3个前连接部3011，3个前连接部3011分别通过3个电凝绝缘件304与电凝壳体303的内壁上的3个连接部固接，此种连接形式能有效增强第一电极301与电凝壳体303间的连接强度。本实施例中前连接部3011呈圆柱形，在其它实施例中前连接部3011还可以呈塔状等。本实施例中电凝绝缘件304呈圆柱状，在其它实施例中电凝绝缘件304还可以呈塔状等。本实施例中后连接部呈圆柱状，在其它实施例中电凝绝缘件304还可以呈塔状等。如图22所示，本实施例中电凝壳体303包括由电凝进口3031至电凝出口3032方向依次分布的第一壳体部3033、第二壳体部3034、及第三壳体部3035。电凝进口3031位于第一壳体部3033的一端，电凝出口3032位于第三壳体部3035的一端。第一壳体部3033的轮廓大小由电凝进口3031至电凝出口3032方向逐渐增大，第三壳体部3035的轮廓大小由电凝进口3031至电凝出口3032方向逐渐减小。本实施例中第二壳体部3034的截面呈矩形。本实施例中电凝壳体303采用上述结构设计，使排气在电凝进口3031处达到一定的入口流速，更主要能使气流分布更加均匀，进而使排气中的介质、如雾滴更容易在第一电极301的激发作用下带电。同时本电凝壳体303封装更加方便，减少材料用量， 并节省空间，可以用管道连接，且还有利用于绝缘的考虑。任何可达到上述效果的电凝壳体303均可以接受。
本实施例中电凝进口3031和电凝出口3032均呈圆形，电凝进口3031也可称作进气口，电凝出口3032也可称作出气口。本实施例中电凝进口3031的直径为300mm～1000mm，具体为500mm。同时，本实施例中电凝进口3031的直径为300mm～1000mm，具体为500mm。
实施例31
如图25和图26所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给含硝酸的水雾；当电子被传导给含硝酸的水雾时，含硝酸的水雾带电；
第二电极302，能给带电的水雾施加吸引力。
如图25和图26所示，本实施例中第一电极301有两个，两个第一电极301均呈网状且呈球笼状。本实施例中第二电极302有一个，该第二电极302呈网状且呈球笼状。第二电极302位于两个第一电极301之间。同时，如图25所示，本实施例中电凝装置还包括具有电凝进口3031和电凝出口3032的电凝壳体303，第一电极301和第二电极302均安装在电凝壳体303中。且第一电极301通过电凝绝缘件304与电凝壳体303的内壁固接，第二电极302直接与电凝壳体303固接。本实施例中电凝绝缘件304呈柱状，又称作绝缘柱。本实施例中第一电极301具有负电势，第二电极302具有正电势。同时，本实施例中电凝壳体303与第二电极302具有相同的电势，该电凝壳体303同样对带电的物质具有吸附作用。
本实施例中电凝装置还可用于处理含有酸雾的工业排气。本实施例中电凝进口3031可与排放工业排气的口相连通。如图25所示，本实施例中电凝装置的工作原理如下：工业排气由电凝进口3031流入电凝壳体303，并经电凝出口3032流出；在此过程中，工业排气将先流经其中一个第一电极301，当工业排气中的酸雾与该第一电极301接触时，或与该第一电极301的距离达到一定值时，第一电极301将电子传递给酸雾，部分酸雾带电，第二电极302给带电的酸雾施加吸引力，酸雾向第二电极302移动，并附着在第二电极302上；另有一部分酸雾未被吸附在第二电极302上，该部分酸雾继续向电凝出口3032方向流动，当该部分酸雾与另一个第一电极301接触时，或与另一个第一电极301的距离达到一定值时，该部分酸雾将带电，电凝壳体303给该部分带电的酸雾施加吸附力，使得该部分带电的酸雾附着在电凝壳体303的内壁上，从而大大减少了工业排气中酸雾的排放量，且本实施例中处理装置能去除工业排气中90％的酸雾，去除酸雾的效果非常显著。另外，本实施例中电凝进口3031和电凝出口3032均呈圆形，电凝进口3031也可称作进气口，电凝出口3032也可称作出气口。
实施例32
如图27所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈针状，且第一电极301带有负电势。同时，本实施例中第二电极302呈面状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第二电极302具体呈平面状，且第一电极301垂直于第二电极302。本实施例中第一电极301和第二电极302之间形成线面电场。
实施例33
如图28所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈线状，且第一电极301带有负电势。同时，本实施例中第二电极302呈面状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第二电极302具体呈平面状，且第一电极301平行于第二电极302。本实施例中第一电极301和第二电极302之间形成线面电场。
实施例34
如图29所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈网状，且第一电极301带有负电势。同时，本实施例中第二电极302呈面状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第二电极302具体呈平面状，且第一电极301平行于第二电极302。本实施例中第一电极301和第二电极302之间形成网面电场。另外，本实施例中第一电极301由金属丝制成的网状结构，该第一电极301由金属丝网构成。本实施例中第二电极302的面积大于第一电极301的面积。
实施例35
如图30所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈点状，且第一电极301带有负电势。同时，本实施例中第二电极302呈桶状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第一电极301通过金属线或金属针进行固定。且本实施例中第一电极301位于桶状的第二电极302的几何对称中心处。本实施例中第一电极301和第二电极302之间形成点桶电场。
实施例36
如图31所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈线状，且第一电极301带有负电势。同时，本实施例中第二电极302呈桶状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第一电极301通过金属线或金属针进行固定。且本实施例中第一电极301位于桶状的第二电极302的几何对称轴上。本实施例中第一电极301和第二电极302之间形成线桶电场。
实施例37
如图32所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第一电极301呈网状，且第一电极301带有负电势。同时，本实施例中第二电极302呈桶状，且第二电极302带有正电势，该第二电极302也称作收集极。本实施例中第一电极301通过金属线或金属针进行固定。且本实施例中第一电极301位于桶状的第二电极302的几何对称中心处。本实施例中第一电极301和第二电极302之间形成网桶电凝电场。
实施例38
如图33所示，本实施例提供一种电凝装置，包括：
第一电极301，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极302，能给带电的水雾施加吸引力。
本实施例中第二电极302有两个，且第一电极301位于两个第二电极302之间，第一电极301沿左右方向方向上的长度大于第二电极302沿左右方向上的长度，有第一电极301的左端位于第二电极302的左方。第一电极301的左端与第二电极302的左端形成沿斜向延伸的电力线。本实施例中第一电极301与第二电极302之间形成非对称电凝电场。在使用时，水雾(低比电阻物质)、如雾滴由左进入两个第二电极302之间。部分雾滴带电后，由第一电极301的左端沿斜向向第二电极302的左端移动，从而对雾滴形成拉动作用。
实施例39
如图34所示，本实施例提供一种电凝装置，包括：
第一电极，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极，能给带电的水雾施加吸引力。
本实施例中第一电极和第二电极构成吸附单元3010。本实施例中吸附单元3010有多个，且全部吸附单元3010沿水平方向分布。本实施例中全部吸附单元3010具体沿左右方向分布。
实施例40
如图35所示，本实施例提供一种电凝装置，包括：
第一电极，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极，能给带电的水雾施加吸引力。
本实施例中第一电极和第二电极构成吸附单元3010。本实施例中吸附单元3010有多个，且全部吸附单元3010沿上下方向分布。
实施例41
如图36所示，本实施例提供一种电凝装置，包括：
第一电极，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极，能给带电的水雾施加吸引力。
本实施例中第一电极和第二电极构成吸附单元3010。本实施例中吸附单元3010有多个，且全部吸附单元3010沿斜向分布。
实施例42
如图37所示，本实施例提供一种电凝装置，包括：
第一电极，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极，能给带电的水雾施加吸引力。
本实施例中第一电极和第二电极构成吸附单元3010。本实施例中吸附单元3010有多个，且全部吸附单元3010沿螺旋方向分布。
实施例43
如图38所示，本实施例提供一种电凝装置，包括：
第一电极，能将电子传导给水雾；当电子被传导给水雾时，水雾带电；
第二电极，能给带电的水雾施加吸引力。
本实施例中第一电极和第二电极构成吸附单元3010。本实施例中吸附单元3010有多个，且全部吸附单元3010沿左右方向、上下方向和斜向分布。
实施例44
如图39所示，本实施例提供一种排气处理系统，包括上述电凝装置30100和文氏板3051。本实施例中电凝装置30100与文氏板3051组合使用。
实施例45
如图40所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、文氏板3051、NO x氧化催化装置3052、及臭氧消解装置3053。本实施例中电凝装置30100和文氏板3051位于NO x氧化催化装置3052和臭氧消解装置3053之间。且NO x氧化催化装置3052中具有NO x氧化催化剂，臭氧消解装置3053中具有臭氧消解催化剂。
实施例46
如图41所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、电晕装置3054和文氏板3051，其中电凝装置30100位于电晕装置3054和文氏板3051之间。
实施例47
如图42所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、加热装置3055和臭氧消解装置3053，其中加热装置3055位于电凝装置30100和臭氧消解装置3053之间。
实施例48
如图43所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、离心装置3056和文氏板3051，其中电凝装置30100位于离心装置3056和文氏板3051之间。
实施例49
如图44所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、电晕装置3054、文氏板3051、及分子筛3057，其中文氏板3051和电凝装置30100位于电晕装置3054和分子筛3057之间。
实施例50
如图45所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、电晕装置3054和电磁装置3058，其中电凝装置30100位于电晕装置3054和电磁装置3058之间。
实施例51
如图46所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、电晕装置3054和辐照装置3059，其中辐照装置3059位于电晕装置3054和电凝装置30100之间。
实施例52
如图47所示，本实施例提供一种排气处理系统，包括上述电凝装置30100、电晕装置3054和湿电除尘装置3061，其中湿电除尘装置3061位于电晕装置3054和电凝装置30100之间。
实施例53
本实施例中排气除尘系统包括排气降温装置，用于在电场装置入口之前降低排气温度。本实施例中排气降温装置可与电场装置入口相连通。
如图48所示，本实施例提供一种排气降温装置，包括：
换热单元3071，用于与排气排放设备的排气进行热交换，以将换热单元3071中液态的换热介质加热成气态的换热介质。
本实施例中换热单元3071可以包括：
排气通过腔，与排气排放设备的排气管路相连通，该排气通过腔用于供排气排放设备的排气通过；
介质气化腔，介质气化腔用于将液态换热介质与排气发生热交换后转化成气态的换热介质。
本实施例中介质气化腔中具有液态的换热介质，液态的换热介质与排气通过腔中的排气发生热交换后会转化成气态的换热介质。排气通过腔实现对排气的收集。本实施例中介质气化腔和排气通过腔的长度方向可以相同，即介质气化腔的轴线与排气通过腔的轴线相重合。本实施例中介质气化腔可以位于排气通过腔内，或位于排气通过腔外部。这样，当排气流过排气通过腔时，排气携带的热量将传递给对介质气化腔内的液体，将液体加热到沸点以上，液体汽化为高温高压的蒸气等气态介质，该蒸气将在介质气化腔中流动。本实施例中介质气化腔具体可全包覆或除其前端外的部分包覆在排气通过腔的内外侧。
本实施例中排气降温装置还包括动力产生单元3072，该动力产生单元3072用于将换热介质的热能和/或排气的热能转换为机械能。
本实施例中排气降温装置还包括发电单元3073，该发电单元3073用于将动力产生单元3072产生的机械能转换为电能。
本实施例中排气降温装置的工作原理为：换热单元3071与排气排放设备的排气进行热交换，以将换热单元3071中的液态的换热介质加热成气态的换热介质；动力产生单元3072将换热介质的热能或排气的热能转换机械能；发电单元3073将动力产生单元3072产生的机械能转换为电能，从而实现利用排气排放设备的排气进行发电，避免排气携带的热量及压力被浪费掉；且换热单元3071在与排气进行热交换时，还能起到对排气散热、降温的作用，以便于能采用其它排气净化装置等对排气进行处理，并提高后续对排气处理的效率。
本实施例中换热介质可以为水、甲醇、乙醇、油、或烷等。上述换热介质为能因温度而相变的物质，同时在相变过程其体积及压力也产生相应的变化。
本实施例中换热单元3071也称作换热器。本实施例中换热单元3071可采用管式换热设备。换热单元3071的设计考虑因素包括承压、减少体积、及增加换热面积等。
如图48所示，本实施例中排气降温装置还可以包括连接于换热单元3071与动力产生单元3072之间的介质传输单元3074。介质气化腔中形成的蒸气等气态介质通过介质传输单元3074作用于动力产生单元3072。介质传输单元3074包括承压管路。
本实施例中动力产生单元3072包括涡扇。该涡扇能将蒸气或排气等气态介质产生的压力转换成动能。且涡扇包括涡扇轴、及至少一组固定在涡扇轴上的涡扇组件。涡扇组件包括导流扇和动力扇。当蒸气的压力作用于涡扇组件时，涡扇轴将随涡扇组件一起转动，从而将蒸气的压力转换成动能。当动力产生单元3072包括涡扇时，排气的压力也可作用于涡扇上，以带动涡扇转动。这样，蒸气的压力和排气产生的压力可交替地、无缝切换作用于涡扇上。当涡扇以第一方向转动时，发电单元3073将动能转换为电能，实现余热发电；当产生的电能反过来带动涡扇转动，且涡扇以第二方向转动时，发电单元3073将电能转换为排气阻力，为排气排放设备提供排气阻力，当安装于排气排放设备上的排气制动装置起作用，产生制动高温高压排气时，涡扇将这种制动能转换为电能，实现排气排放设备排气制动和制动发电。本实施例可通过高速涡扇抽气产生恒定排气负压，减少了排气排放设备的排气阻力，实现排气排放设备助动。且当动力产生单元3072包括涡扇时，动力产生单元3072还包括涡扇调节模块，该涡扇调节模块利用排气排放设备排气压力峰值推动涡扇产生转动惯量，进一步延时产生排气负压，推动排气排放设备吸气、降低使排气排放设备排气阻力，提升排气排放设备的功率。
本实施例中排气通过腔与排气排放设备的排气口相连通。
发电单元3073包括发电机定子和发电机转子，发电机转子与动力产生单元3072的涡扇轴相连接。这样，发电机转子将随涡扇轴的转动而转动，从而与发电机定子共同作用实现发电。本实施例中发电单元3073可采用可变负荷发电机，或使用直流发电机将转矩变换为电能。同时，本发电单元3073可通过调整励磁绕组电流，调整发电量匹配排气热量的变化；以适应排气排放设备在上坡、下坡、重载、轻载等排气温度变化。本实施例中发电单元3073还可以包括电池组件，以利用该电池组件储存电能，即实现对发出的电暂时缓存。本实施例中电池组件中储存的电可供换热器动力扇、水泵、制冷压缩机以及排气排放设备中其它电器使用。
如图48所示，本实施例中排气降温装置还可以包括耦合单元3075，该耦合单元3075电性连接于动力产生单元3072和发电单元3073之间，发电单元3073通过该耦合单元3075与动力产生单元3072同轴耦合。本实施例中耦合单元3075包括电磁耦合器。
本实施例中发电单元3073还可以包括发电机调控组件，该发电机调控组件用于调节发电 机的电动转矩，产生排气负压以改变排气排放设备强制制动力大小，产生排气背压以提高余热转换效率。具体地，发电机调控组件通过调节发电励磁或发电电流，能够改变发电功输出，从而调节排气排放阻力，实现做功、排气背压、排气负压平衡，提高发电机效率。
本实施例中排气降温装置还可以包括保温管路，该保温管路连接于排气排放设备的排气管路和换热单元3071之间。具体地，保温管路的两端分别与排气排放设备的排气口和排气通过腔相连通，以利用该保温管路来维持排气的高温，并将排气引入排气通过腔中。
本实施例中排气降温装置还可以包括风机，该风机将空气通入排气中，并在电场装置入口之前，对排气起到降温的作用。通入的空气可以是排气的50％至300％、或100％至180％、或120％至150％。
本实施例中排气降温装置可以协助排气排放设备实现排气余热的回收再利用，有助于减少温室气体的排放，也助于减少有害气体的排放，并减少了污染物的排放，从而使尾的排放更环保。
排气降温装置的进气可以用来净化空气，排气除尘系统处理过的排气的颗粒含量比空气的颗粒含量还要少。
实施例54
如图49所示，本实施例在上述实施例53的基础上，其换热单元3071还可以包括介质循环回路3076；该介质循环回路3076的两端分别与介质气化腔的前后两端相连通，并形成封闭式的气液循环回路；介质循环回路3076上安装有冷凝器30761，冷凝器30761用于将气态的换热介质冷凝为液态的换热介质。介质循环回路3076通过动力产生单元3072与介质气化腔相连通。本实施例中介质循环回路3076的一端用于收集蒸气等气态换热介质，并将蒸气冷凝为液态的换热介质、即液体，另一端用于将液态的换热介质注入到介质气化腔中，以重新生成蒸气，从而实现了换热介质的循环回收利用。本实施例中介质循环回路3076包括蒸气回路30762，该蒸气回路30762与介质气化腔的后端相连通。另外，本实施例中上述冷凝器30761还通过介质传输单元3074与动力产生单元3072相连通。本实施例中气液循环回路与排气通过腔不相通。
本实施例中冷凝器30761可采用风冷散热器等散热设备，具体可采用承压翘片风冷散热器。当有自然风时，冷凝器30761通过自然风强行散热，无自然风时，可使用电扇对冷凝器30761进行散热。具体地，介质气化腔中形成的蒸气等气态介质在作用于动力产生单元3072后将进行泄压，并流入介质循环回路3076及风冷散热器，蒸气的温度随着散热器的散热而降低，并继续冷凝为液体。
如图49所示，本实施例中介质循环回路3076的一端可以设有增压模块30763，该增压模块30763用于将冷凝后的换热介质进行加压，以推动冷凝后的换热介质流入介质气化腔。本实施例中增压模块30763包括循环水泵或高压泵，液态的换热介质在循环水泵的叶轮推动下实现增压，并通过补水管道被挤压、进入介质气化腔中，以在介质气化腔中继续进行加热、并汽化。另外，涡扇转动时可替代循环水泵或高压泵，此时液体在涡扇余压的推动下，通过补水管道被挤压进介质气化腔中，继续被加热汽化。
如图49所示，本实施例中介质循环回路3076还可以包括设置在冷凝器30761和增压模块30763之间的储液模块30764，该储液模块30764用于存储经过冷凝器30761冷凝后液态的换热介质。上述增压模块30763位于储液模块30764和介质气化腔之间的一输送管路上，储液模块30764中的液体经增压模块30763增压后注入介质气化腔。本实施例中介质循环回路3076还包括液体调节模块30765，该液体调节模块30765设置于储液模块30764与介质气化腔之间，具体设置在位于储液模块30764与介质气化腔之间的另一输送管路上。上述液体调节模块30765用于调节向介质气化腔回流液体的量。当排气的温度持续高于液态换热介质的沸点温度时，液体调节模块30765将储液模块30764中的液体注入介质气化腔。本实施例中介质循环回路3076还包括设置于储液模块30764与介质气化腔之间的加注模块30766，该加注模块30766具体与上述增压模块30763和液体调节模块30765相通。本实施例中加注模块30766可包括喷嘴307661。喷嘴307661位于介质循环回路3076的一端，且喷嘴307661设置在介质气化腔的前端内，以通过该喷嘴307661向介质气化腔内注入液体。上述增压模块30763将储液模块30764中的液体加压后，经加注模块30766的喷嘴307661注入介质气化腔中。上述储液模块30764中的液体也可经液体调节模块30765注入加注模块30766，并经加注模块30766的喷嘴307661注入介质气化腔中。上述输送管路也称作热介质管道。
本实施例中排气降温装置具体应于一台13升柴油型排气排放设备上，上述排气通过腔具体与排气排放设备的排气口相连通，排气排放设备排放的排气温度为650摄氏度，流量约4000立方米/小时，排气热量约80千瓦左右。本实施例具体采用水作为介质气化腔中的换热介质，并采用涡扇为动力产生单元3072。本排气降温装置可以回收15千瓦电能，可以用于驱动电器；同时，加上循环水泵的直接效能回收利用，可回收40千瓦排气热能。本实施例中排气降温装置既可以提高燃油经济性，还可以把排气温度降低到露点以下，以有利于需要低温环境的湿电除尘和臭氧脱硝排气净化工艺的进行。
综上所述，本排气降温装置可应用于柴油、汽油、燃气型的排气排放设备的节能减排领域，是效率提升、节省燃料技术、提高经济性的创新技术。本排气降温装置能够帮助排气排 放设备省油、提高燃油经济性；也能使废热得到回收利用，实现能源高效利用。
实施例55
如图50和图51所示，本实施例中上述实施例54的基础上，其动力产生单元3072具体采用涡扇。同时，本实施例中涡扇包括涡扇轴30721和介质腔涡扇组件30722，介质腔涡扇组件30722安装在涡扇轴30721上，且介质腔涡扇组件30722位于介质气化腔30711中，具体可位于介质气化腔30711中的后端处。
本实施例中介质腔涡扇组件30722包括介质腔导流扇307221和介质腔动力扇307222。
本实施例中涡扇包括排气腔涡扇组件30723，安装在涡扇轴30721上，且排气腔涡扇组件30723位于排气通过腔30712中。
本实施例中排气腔涡扇组件30723包括排气腔导流扇307231和排气腔动力扇307232。
本实施例中排气通过腔30712位于介质气化腔30711中，即介质气化腔30711套设在排气通过腔30712的外侧。本实施例中介质气化腔30711具体可全包覆或除其前端外的部分包覆在排气通过腔30712的外侧。介质气化腔30711中形成的蒸气等气态介质流过介质腔涡扇组件30722，在蒸气压力的作用下推动介质腔涡扇组件30722及涡扇轴30721运转。介质腔导流扇307221具体设置在介质气化腔30711的后端处，蒸气等气态介质流经介质腔导流扇307221时，推动介质腔导流扇307221运转，并在该介质腔导流扇307221的作用下，蒸气按设定的路径流动至介质腔动力扇307222；介质腔动力扇307222设置在介质气化腔30711的后端处，具体位于介质腔导流扇307221的后方，流过介质腔导流扇307221的蒸气流动至介质腔动力扇307222，并推动介质腔动力扇307222及涡扇轴30721运转。本实施例中介质腔动力扇307222又称作第一级动力扇。排气腔涡扇组件30723设置在介质腔涡扇组件30722的后方或前方，与介质腔涡扇组件30722同轴运转。排气腔导流扇307231设置在排气通过腔30712中，排气流经排气通过腔30712时，推动排气腔导流扇307231运转，并在该排气腔导流扇307231的作用下，排气按设定的路径流动至排气腔动力扇307232。排气腔动力扇307232设置在排气通过腔30712中，具体位于排气腔导流扇307231的后方，流过排气腔导流扇307231的排气流动至排气腔动力扇307232，且在排气压力作用下推动排气腔动力扇307232及涡扇轴30721运转，最后排气经排气腔动力扇307232及排气通过腔30712排出。本实施例中排气腔动力扇307232又称作第二级动力扇。
如图50所示，本实施例中发电单元3073包括发电机定子30731和发电机转子30732。另外，本实施例中上述发电单元3073也设置在排气通过腔30712外部，并与涡扇同轴连接，即发电机转子30732与涡扇轴30721相连接，这样发电机转子30732将随涡扇轴30721的转 动而转动。
本实施例中动力产生单元3072正是采用涡扇，使得蒸气和排气能够快速移动，节省了体积和重量，满足排气能量转换的需求。当本实施例中涡扇以第一方向转动时，发电单元3073将涡扇轴30721的动能转换为电能，从而实现余热发电；当涡扇以第二方向转动时，发电单元3073将电能转换为排气阻力，为排气排放设备提供排气阻力，当安装于排气排放设备上的排气制动装置起作用，产生制动高温高压排气时，涡扇将这种制动能转换为电能，实现排气制动和制动发电。具体地，涡扇产生的动能可以用于发电，从而实现排气余热发电；所产生的电能反过来带动涡扇转动，为排气排放设备提供排气负压，从而就实现排气制动和制动发电，极大地提升了排气排放设备的效率。
如图50和图51所示，本实施例中排气通过腔30712全部设置在介质气化腔30711内，从而实现排气收集。本实施例中介质气化腔30711与排气通过腔30712的横向轴向相重合。
本实施例中动力产生单元3072还包括涡扇转动负压调节模块，该涡扇转动负压调节模块利用排气排放设备排气压力峰值推动涡扇产生转动惯量，进一步延时产生排气负压，推动排气排放设备吸气、降低排气阻力，提升功率。
如图50所示，本实施例中发电单元3073包括电池组件30733，以利用该电池组件30733储存电能，即实现对发出的电暂时缓存。本实施例中电池组件30733中储存的电可供换热器动力扇、水泵、制冷压缩机以及排气排放设备中其它电器使用。
本实施例中排气降温装置能够利用排气的余热进行发电，同时兼顾了体积和重量的要求，且热能转换效率高，换热介质可循环利用，极大地提升了能源利用率，绿色环保，实用性强。
在初始状态下，排气排放设备排放的排气推动排气腔动力扇307232旋转，实现排气压力直接换能；由排气腔动力扇307232和涡扇轴30721的转动惯量，实现排气排气瞬时负压；发电机调控组件3078通过调节发电励磁或发电电流，能够改变发电功输出，从而调节排气排放阻力，适应排气排放设备做功工况。
当采用排气余热发电时，且排气温度连续高于200摄氏度时，向介质气化腔30711注入水，水吸收排气的热量形成高温高压的蒸气，同时产生蒸气动力，继续加速推动介质腔动力扇307222，使介质腔动力扇307222和排气腔动力扇307232转动更快，力矩更大。通过调节发动电流或励磁电流平衡排气排放设备做功和排气背压平衡；通过调节向介质气化腔30711注入的水量，适应排气温度变化，从而恒定排气温度。
当制动发电时，排气排放设备的压气通过排气腔动力扇307232，并推动排气腔动力扇307232转动，从而将压力转变为发电机旋转动力，通过调节发电电流或励磁电流，改变阻力 大小，实现制动和制动力缓释。
当电动制动时，排气排放设备的压气通过排气腔动力扇307232，推动排气腔动力扇307232正向转动，开启电动机，输出反向转动力矩，通过涡扇轴30721传递到介质腔动力扇307222和排气腔动力扇307232上，形成强烈反推阻力，将能耗转变为腔体热量，同时使排气排放设备的制动力增加，强制制动。
介质传输单元3074包括反推涵道。当蒸气制动时，连续压气制动蓄积热量通过蒸气，产生更大推力，并通过反推涵道，将蒸气输出到介质腔动力扇307222上，强制介质腔动力扇307222和排气腔动力扇307232反转，实现制动发动同时进行。
实施例56
如图52所示，本实施例在上述实施例55的基础上，其介质气化腔30711位于排气通过腔30712中；且介质腔涡扇组件30722位于介质气化腔30711中，并具体位于介质气化腔30711的后端处；排气腔涡扇组件30723位于排气通过腔30712中，并具体位于排气通过腔30712的后端处。介质腔涡扇组件30722和排气腔涡扇组件30723均安装在涡扇轴30721上。本实施例中排气腔涡扇组件30723位于介质腔涡扇组件30722的后方。这样，流经排气通过腔30712的排气将直接作用于排气腔涡扇组件30723，以带动排气腔涡扇组件30723及涡扇轴30721转动；同时，当排气流经排气通过腔30712时，将与介质气化腔30711中的液体进行换热，并使介质气化腔30711中的液体形成蒸气，该蒸气的压力作用于介质腔涡扇组件30722，以带动介质腔涡扇组件30722及涡扇轴30721转动，从而进一步加快推动涡扇轴30721转动；涡扇轴30721转动时将带动与其相连接的发电机转子30732一起转动，进而利用发电单元3073实现发电。另外，介质气化腔30711中的蒸气在向后流经介质腔涡扇组件30722后，将流入介质循环回路3076，并经介质循环回路3076中的冷凝器30761冷凝为液体后，再重新注入介质气化腔30711，以实现换热介质的循环回收利用。排气通过腔30712中的排气在流经排气腔涡扇组件30723后排放至大气。
另外，本实施例中介质气化腔30711的侧壁上设有弯折段307111，该弯折段307111能有效增加介质气化腔30711与排气通过腔30712的接触面积，即换热面积。本实施例中弯折段307111的截面呈锯齿状。
实施例57
为提高排气排放设备的热效率，需要把排气热能和背压回收换能，达到高效率，既要燃油直接带动发电机，也要尾热高效转换为电能，这样燃油热效率可以提高15％-20％。对于混动排气排放设备来说，在节省燃油同时可以为电池组件充更多的电，燃油转换为电能的效率 可以达到70％以上。
具体地，在排气排放设备的排气口，安装上述实施例55或实施例56中排气降温装置，开启燃油型排气排放设备，排气进入排气通过腔30712，在排气背压作用下，经排气腔导流扇307231调整方向，直接推动排气腔动力扇307232旋转，从而在涡扇轴30721上产生旋转扭矩。由于存在转动惯量介质腔动力扇307222和排气腔动力扇307232继续旋转时，将产生抽气，使排气处于瞬时负压，这样，排气阻力极低，有利于排气排放设备继续排气并做功。同样燃油供给和输出负载情况下，提升排气排放设备转速3％-5％左右。
排气排放设备排气温度会因为翘片导热集聚在介质气化腔30711，当集聚温度大于水的沸点温度时，将水注入介质气化腔30711，水瞬间汽化，体积急剧膨胀，通过介质腔导流扇导向，推动介质腔动力扇307222及涡扇轴30721进一步加速旋转，产生更大的转动惯量和转矩。继续提升排气排放设备转速，而燃油并没有增加，负载也没有减轻，获得的额外转速提升10％-15％。在转速因回收背压和温度提升同时，排气排放设备动力输出将增加，根据排气温度差异，提高功率输出13％-20％左右，对于提高燃油经济性、减少排气排放设备体积来说，非常有帮助。
实施例58
本实施例将实施例55或实施例56中的排气降温装置应用于一台13升柴油型排气排放设备上，该柴油型排气排放设备的排气温度为650摄氏度，流量约4000立方米/小时，排气热量约80千瓦左右。同时，本实施例使用水为换热介质，本排气降温装置可以回收20千瓦电能，可以用于驱动电器。因此，本实施例中排气降温装置既可以提高燃油经济性，还可以把排气温度降低到露点以下，有利于需要低温环境的静电除尘、湿电除尘及臭氧脱硝排气净化工艺的实施；同时实现了排气排放设备变扭连续高效制动和强制连续制动。
具体地，本实施例的排气降温装置直接连接在一台13升柴油型排气排放设备的排气口，并通过在本排气降温装置的出口、即上述排气通过腔30712的出口连接电场装置、排气湿电除尘和臭氧脱硝系统，就能够实现尾热发电、排气降温、制动、除尘、脱硝等。本实施例中排气降温装置安装在电场装置的前方。
其中，本实施例使用3寸的介质腔动力扇307222和排气腔动力扇307232，并使用10kw高速直流发电电动机，电池组件采用48v300ah动力电池组，使用发电电动手动切换开关。初始状态时，排气排放设备怠速运转，转速小于750转，排气排放设备输出功率10％左右，通过排气排放设备排气推动排气腔动力扇307232旋转，转速在2000转左右，实现排气压力直接换能；排气腔动力扇307232以及涡扇轴30721的转动惯量使排气排气瞬时负压；由于排气 腔动力扇307232转动，在排气管道内产生瞬时负压-80kp左右，通过调节发电电流，改变发电功输出，从而调节排气排放阻力，适应做功工况，获得发电功率0.1-1.2kw。
当带负载30％时，排气排放设备转速上升到1300转，排气温度连续高于300摄氏度，向介质气化腔30711注入水，排气温度下降到200摄氏度，产生大量高温高压蒸气，吸收排气温度同时产生蒸气动力，由于介质腔导流扇和喷口限制，喷到介质腔动力扇上的蒸气压力继续加速推动介质腔动力扇转动，使介质腔动力扇及涡扇轴转动更快，力矩更大，带动发电机高速大扭矩旋转，通过调节发动电流或励磁电流平衡发动做功和排气背压平衡，获得发电量1kw-3kw，通过调节注入水量，适应排气温度变化，达到恒定排气温度目的，从而获得连续排气温度150摄氏度。低温排气有利于后续电场装置回收颗粒物和臭氧脱硝，达到环保目的。
当排气排放设备停止供油时，通过涡扇轴30721拖动排气排放设备压气，压气通过排气管路到达排气腔动力扇307232，推动排气腔动力扇307232，将压力转变为涡扇轴30721旋转动力，在涡扇轴30721上同时安装的发电机，通过调节发电电流，改变通过涡扇的排气量，从而改变排气阻力大小，实现制动和制动力缓释，可以获得3-10kw左右的制动力，同时回收1-5kw的发电量。
当发电机切换到电动制动模式时，发电机瞬间变成电动机，等于驾驶员快速踏下制动踏板。这时压气通过排气腔动力扇307232，推动排气腔动力扇307232正向转动。开启电动机，输出反向转动力矩，通过涡扇轴30721传递到介质腔动力扇307222和排气腔动力扇307232上，形成强烈反推阻力，进一步增加制动效果。大量压气做功将能耗转变为高温气体，使腔体热量蓄积，同时使制动力增加，强制制动。强制制动功率15-30kw。这种制动可以间歇发电，发电功率3-5kw左右。
当使用电动反推制动同时间歇发电时，突然需要紧急制动，可以停止发电，将制动热量产生蒸气用于制动，连续压气制动蓄积热量传递给介质气化腔中的水，介质气化腔中产生的蒸气通过反推涵道，输出到介质腔动力扇307222上，且蒸气反推介质腔动力扇307222，强制介质腔动力扇307222和排气腔动力扇307232反转，实现强制制动，可产生制动功率30kw以上。
综上所述，本发明有效克服了现有技术中的种种缺点而具高度产业利用价值。
上述实施例仅例示性说明本发明的原理及其功效，而非用于限制本发明。任何熟悉此技术的人士皆可在不违背本发明的精神及范畴下，对上述实施例进行修饰或改变。因此，举凡所属技术领域中具有通常知识者在未脱离本发明所揭示的精神与技术思想下所完成的一切等效修饰或改变，仍应由本发明的权利要求所涵盖。

Claims (13)

  1. 一种排气处理系统，其特征在于，包括臭氧净化系统；所述臭氧净化系统包括臭氧量控制装置，用于控制臭氧量以致有效氧化排气中待处理的气体组分，所述臭氧量控制装置包括控制单元。
  2. 根据权利要求1所述的排气处理系统，其特征在于，所述臭氧量控制装置还包括臭氧处理前排气组分检测单元，用于检测臭氧处理前排气组分含量。
  3. 根据权利要求2中的任一项所述的排气处理系统，其特征在于，所述控制单元根据所述臭氧处理前排气组分含量控制混合反应所需臭氧量。
  4. 根据权利要求3所述的排气处理系统，其特征在于，所述臭氧处理前排气组分检测单元选自以下检测单元中至少一个：
    第一挥发性有机化合物检测单元，用于检测臭氧处理前排气中挥发性有机化合物含量；
    第一CO检测单元，用于检测臭氧处理前排气中CO含量；
    第一氮氧化物检测单元，用于检测臭氧处理前排气中氮氧化物含量。
  5. 根据权利要求4所述的排气处理系统，其特征在于，所述控制单元根据至少一个所述臭氧处理前排气组分检测单元的输出值控制混合反应所需臭氧量。
  6. 根据权利要求5中的任一项所述的排气处理系统，其特征在于，所述控制单元用于按照预设的数学模型控制混合反应所需臭氧量。
  7. 根据权利要求5所述的排气处理系统，其特征在于，所述控制单元用于按照理论估计值控制混合反应所需臭氧量。
  8. 根据权利要求7中的任一项所述的排气处理系统，其特征在于，所述理论估计值为：臭氧通入量与排气中待处理物的摩尔比为2～10。
  9. 根据权利要求1所述的排气处理系统，其特征在于，所述臭氧量控制装置包括臭氧处理后排气组分检测单元，用于检测臭氧处理后排气组分含量。
  10. 根据权利要求9所述的排气处理系统，其特征在于，所述控制单元根据所述臭氧处理后排气组分含量控制混合反应所需臭氧量。
  11. 根据权利要求10所述的排气处理系统，其特征在于，所述臭氧处理后排气组分检测单元选自以下检测单元中至少一个：
    第一臭氧检测单元，用于检测臭氧处理后排气中臭氧含量；
    第二挥发性有机化合物检测单元，用于检测臭氧处理后排气中挥发性有机化合物含量；
    第二CO检测单元，用于检测臭氧处理后排气中CO含量；
    第二氮氧化物检测单元，用于检测臭氧处理后排气中氮氧化物含量。
  12. 根据权利要求11所述的排气处理系统，其特征在于，所述控制单元根据至少一个所述臭氧处理后排气组分检测单元的输出值控制臭氧量。
  13. 根据权利要求1至12中的任一项所述的排气处理系统，其特征在于，所述除尘系统包括除尘系统入口、除尘系统出口、电场装置；所述电场装置包括电场装置入口、电场装置出口、除尘电场阴极和除尘电场阳极，所述除尘电场阴极和所述除尘电场阳极用于产生电离除尘电场。
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JP2022509337A (ja) 2022-01-20
EP3871756A4 (en) 2022-06-29
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WO2020083212A1 (zh) 2020-04-30
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WO2020083207A1 (zh) 2020-04-30
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EP3872312A4 (en) 2022-01-05
US20220054974A1 (en) 2022-02-24
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