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WO2020083169A1 - 一种发动机尾气臭氧净化系统和方法 - Google Patents

一种发动机尾气臭氧净化系统和方法 Download PDF

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Publication number
WO2020083169A1
WO2020083169A1 PCT/CN2019/112145 CN2019112145W WO2020083169A1 WO 2020083169 A1 WO2020083169 A1 WO 2020083169A1 CN 2019112145 W CN2019112145 W CN 2019112145W WO 2020083169 A1 WO2020083169 A1 WO 2020083169A1
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WIPO (PCT)
Prior art keywords
ozone
electrode
exhaust gas
present
electrocoagulation
Prior art date
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PCT/CN2019/112145
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English (en)
French (fr)
Inventor
唐万福
王大祥
奚勇
Original Assignee
上海必修福企业管理有限公司
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Publication of WO2020083169A1 publication Critical patent/WO2020083169A1/zh

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    • F01N2560/00—Exhaust systems with means for detecting or measuring exhaust gas components or characteristics
    • F01N2560/05—Exhaust systems with means for detecting or measuring exhaust gas components or characteristics the means being a particulate 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
    • F01N2900/00—Details of electrical control or of the monitoring of the exhaust gas treating apparatus
    • F01N2900/06—Parameters used for exhaust control or diagnosing
    • F01N2900/14—Parameters used for exhaust control or diagnosing said parameters being related to the exhaust gas
    • F01N2900/1402—Exhaust gas composition
    • 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
    • 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
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T10/00—Road transport of goods or passengers
    • Y02T10/10—Internal combustion engine [ICE] based vehicles
    • Y02T10/12—Improving ICE efficiencies

Definitions

  • the invention belongs to the field of environmental protection and relates to an engine exhaust ozone purification system and method.
  • the engine's environmental pollution mainly comes from the exhaust product of the engine, that is, the engine exhaust.
  • the conventional technical route is to use the oxidation catalyst DOC to remove the hydrocarbons THC and CO, and at the same time oxidize the low-valent NO to the high-valent NO 2 ; after the DOC, the particulate matter PM is filtered by the diesel particulate trap DPF; after the diesel particulate trap DPF, urea is injected, and the urea is decomposed into ammonia gas NH 3 in the exhaust gas, and the subsequent selectivity of NH 3 A selective catalytic reduction reaction with NO 2 occurs on the catalyst SCR to produce nitrogen N 2 and water.
  • an object of the present invention is to provide an engine exhaust ozone purification system and method for solving at least one of the problems of the prior art exhaust gas purification in which a large amount of urea is added and the exhaust gas purification effect is generally.
  • the study of the present invention found that the high-valent nitrogen oxides produced by the reaction of ozone with nitrogen oxides in the exhaust gas are not the final products, and there are enough VOCs in the exhaust gas to generate enough water to fully react with the high-valent nitrogen oxides. Nitric acid, therefore, the use of ozone to treat engine exhaust makes ozone more effective in removing NO X , with unexpected technical effects.
  • the invention provides an engine exhaust ozone purification system and method.
  • the engine exhaust ozone purification system includes a reaction field for mixing and reacting the ozone stream and the exhaust stream without adding a large amount of urea, and the purification effect is good.
  • Example 1 provided by the present invention: an engine exhaust ozone purification system.
  • Example 2 provided by the present invention: including the above example 1, wherein the engine exhaust ozone purification system includes a reaction field for mixing and reacting the ozone stream with the exhaust stream.
  • Example 3 provided by the present invention: including the above example 2, wherein the reaction field includes a pipe.
  • Example 4 provided by the present invention: including the above example 2 or 3, wherein the reaction field includes a reactor.
  • Example 5 provided by the present invention includes the above Example 4, wherein the reactor has a reaction chamber, and tail gas and ozone are mixed and reacted in the reaction chamber.
  • Example 6 provided by the present invention: including the above example 4 or 5, wherein the reactor includes a plurality of honeycomb-shaped cavities for providing a space where tail gas and ozone are mixed and reacted; between the honeycomb-shaped cavities There is a gap for passing cold medium to control the reaction temperature of exhaust gas and ozone.
  • Example 7 provided by the present invention: including any one of the above Examples 4 to 6, wherein the reactor includes several carrier units, and the carrier units provide a reaction site.
  • Example 8 provided by the present invention: including any one of the above Examples 4 to 7, wherein the reactor includes a catalyst unit for promoting an oxidation reaction of exhaust gas.
  • Example 9 provided by the present invention: including any one of the above examples 2 to 8, wherein the reaction field is provided with an ozone inlet, and the ozone inlet is selected from a nozzle, a spray grid, a nozzle, a swirl nozzle, At least one of the vents provided with a venturi tube.
  • Example 10 provided by the present invention includes any one of the above examples 2 to 9, wherein the reaction field is provided with an ozone inlet, the ozone enters the reaction field through the ozone inlet to contact with the exhaust gas, the ozone inlet
  • Example 11 provided by the present invention includes any one of the above examples 2 to 10, wherein the reaction field includes an exhaust pipe, a heat storage device, or a catalyst.
  • Example 12 provided by the present invention: including any one of the above Examples 2 to 11, wherein the temperature of the reaction field is -50-200 ° C.
  • Example 13 provided by the present invention: including the above Example 12, wherein the temperature of the reaction field is 60-70 ° C.
  • Example 14 provided by the present invention includes any one of the above examples 1 to 13, wherein the exhaust gas ozone purification system further includes an ozone source for providing an ozone stream.
  • Example 15 provided by the present invention includes the above example 14, wherein the ozone source includes a storage ozone unit and / or an ozone generator.
  • Example 16 provided by the present invention: including the above example 15, 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 light 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 light
  • 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 light 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 17 provided by the present invention includes the above Example 15, 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 18 provided by the present invention includes the above Example 17, 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 19 provided by the present invention includes the above Example 18, 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 20 provided by the present invention includes the above Example 18, 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 dielectric 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 21 provided by the present invention includes any one of the above examples 17 to 20, 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 22 provided by the present invention includes the above Example 21, wherein the alkaline earth metal element is selected from at least one of magnesium, strontium and calcium.
  • Example 23 provided by the present invention includes the above Example 21, wherein the transition metal element is selected from at least one of titanium, manganese, zinc, copper, iron, nickel, cobalt, yttrium, and zirconium.
  • Example 24 provided by the present invention includes the above example 21, wherein the fourth main group metal element is tin.
  • Example 25 provided by the present invention includes the above example 21, wherein the precious metal element is selected from at least one of platinum, rhodium, palladium, gold, silver, and iridium.
  • Example 26 provided by the present invention includes the above Example 21, wherein the lanthanide rare earth element is selected from at least one of lanthanum, cerium, praseodymium, and samarium.
  • Example 27 provided by the present invention: including the above Example 21, wherein the compound of the metal element M is selected from at least one of oxides, sulfides, sulfates, phosphates, carbonates, and perovskites .
  • Example 28 provided by the present invention includes the above Example 21, wherein the porous material is selected from at least one of molecular sieve, diatomaceous earth, zeolite, and carbon nanotubes.
  • Example 29 provided by the present invention: including the above example 21, wherein the layered material is selected from at least one of graphene and graphite.
  • Example 30 provided by the present invention includes any one of the above examples 1 to 29, wherein the exhaust gas 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 31 provided by the present invention includes the above Example 30, wherein the control unit controls the amount of ozone required for the mixed reaction according to the content of the exhaust gas component before ozone treatment.
  • Example 32 provided by the present invention includes the above example 30 or 31, wherein the ozone amount control device further includes an exhaust gas component detection unit before ozone treatment, for detecting the content of the exhaust gas component before ozone treatment.
  • Example 33 provided by the present invention includes the above Example 32, wherein the exhaust gas component detection unit before ozone treatment includes a first nitrogen oxide detection unit for detecting the content of nitrogen oxides in the exhaust gas before ozone treatment.
  • Example 34 provided by the present invention includes the above example 32 or 33, wherein the exhaust gas component detection unit before ozone treatment includes a first CO detection unit for detecting the CO content in the exhaust gas before ozone treatment.
  • Example 35 provided by the present invention includes any one of the above examples 32 to 34, wherein the exhaust gas component detection unit before ozone treatment includes a first volatile organic compound detection unit for detecting exhaust gas before ozone treatment Medium volatile organic compound content.
  • Example 36 provided by the present invention: including any one of the above examples 33 to 35, wherein the control unit controls the amount of ozone required for the mixed reaction according to the output value of at least one exhaust gas component detection unit before ozone treatment .
  • Example 37 provided by the present invention includes any one of the above examples 30 to 36, wherein the control unit is used to control the amount of ozone required for the mixed reaction according to a preset mathematical model.
  • Example 38 provided by the present invention includes any one of the above examples 30 to 37, wherein the control unit is used to control the amount of ozone required for the mixed reaction according to a theoretical estimated value.
  • Example 39 provided by the present invention: including any one of the above Example 38, wherein the theoretical estimated value is: the molar ratio of ozone flux to the to-be-processed material in the exhaust gas is 2-10.
  • Example 40 provided by the present invention includes any one of the above examples 30 to 39, wherein the 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.
  • Example 41 provided by the present invention includes any one of the above examples 30 to 40, wherein the ozone quantity control device includes an ozone-treated tail gas component detection unit for detecting the content of the tail gas component after ozone treatment.
  • Example 42 provided by the present invention includes the above Example 41, wherein the ozone-treated tail gas component detection unit includes a first ozone detection unit for detecting the ozone content in the tail gas after ozone treatment.
  • Example 43 provided by the present invention includes the above example 41 or 42, wherein the post-ozone treatment tail gas component detection unit includes a second nitrogen oxide detection unit for detecting the nitrogen oxide content in the tail gas after ozone treatment.
  • Example 44 provided by the present invention: including any one of the above examples 41 to 43, wherein the ozone-treated tail gas component detection unit includes a second CO detection unit for detecting the CO content in the ozone-treated tail gas .
  • Example 45 provided by the present invention: including any one of the above examples 41 to 44, wherein the post-ozone treatment exhaust gas component detection unit includes a second volatile organic compound detection unit for detecting the post-ozone treatment exhaust gas Medium volatile organic compound content.
  • Example 46 provided by the present invention includes any one of the above examples 42 to 45, wherein the control unit controls the amount of ozone according to at least one output value of the ozone-treated exhaust gas composition detection unit.
  • Example 47 provided by the present invention includes any one of the above examples 1 to 46, wherein the exhaust gas ozone purification system further includes a denitration device for removing the mixed reaction product of the ozone stream and the exhaust gas stream Nitric acid.
  • Example 48 provided by the present invention includes the above Example 47, 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 49 provided by the present invention includes the above example 48, wherein the first electrode is a solid, a liquid, a gas molecular group, a plasma, a conductive mixed state substance, a biological natural mixed conductive substance, or an object is artificially formed A combination of one or more forms in a conductive substance.
  • Example 50 provided by the present invention includes the above example 48 or 49, wherein the first electrode is solid metal, graphite, or 304 steel.
  • Example 51 provided by the present invention includes any one of the above examples 48 to 50, wherein the first electrode has a dot shape, a linear shape, a mesh shape, an orifice shape, a plate shape, a needle rod shape, a ball cage Shaped, box-shaped, tubular, natural form material, or processed form material.
  • Example 52 provided by the present invention: including any one of the above examples 48 to 51, wherein the first electrode is provided with a front through hole.
  • Example 53 provided by the present invention includes the above example 52, wherein the shape of the front through hole is polygon, circle, ellipse, square, rectangle, trapezoid, or rhombus.
  • Example 54 provided by the present invention: includes the above example 52 or 53, wherein the diameter of the front through hole is 0.1-3 mm.
  • Example 55 provided by the present invention includes any one of the above examples 48 to 54, 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 56 provided by the present invention: including any one of the above examples 48 to 55, wherein the second electrode is provided with a rear through hole.
  • Example 57 provided by the present invention includes the above example 56, wherein the rear through hole is polygonal, circular, elliptical, square, rectangular, trapezoidal, or rhombic.
  • Example 58 provided by the present invention includes the above example 56 or 57, wherein the diameter of the rear through hole is 0.1-3 mm.
  • Example 59 provided by the present invention: includes any one of the above examples 48 to 58, wherein the second electrode is made of a conductive substance.
  • Example 60 provided by the present invention: including any one of the above examples 48 to 59, wherein the surface of the second electrode has a conductive substance.
  • Example 61 provided by the present invention includes any one of the above examples 48 to 60, wherein there is an electrocoagulation electric field between the first electrode and the second electrode, and 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 62 provided by the present invention includes any one of the above examples 48 to 61, wherein the first electrode is linear and the second electrode is planar.
  • Example 63 provided by the present invention: includes any one of the above examples 48 to 62, wherein the first electrode is perpendicular to the second electrode.
  • Example 64 provided by the present invention: including any one of the above examples 48 to 63, wherein the first electrode is parallel to the second electrode.
  • Example 65 provided by the present invention: including any one of the above examples 48 to 64, wherein the first electrode is curved or arc-shaped.
  • Example 66 provided by the present invention includes any one of the above examples 48 to 65, wherein the first electrode and the second electrode are both planar, and the first electrode is parallel to the second electrode.
  • Example 67 provided by the present invention includes any one of the above examples 48 to 66, wherein the first electrode uses a wire mesh.
  • Example 68 provided by the present invention: including any one of the above examples 48 to 67, wherein the first electrode is planar or spherical.
  • Example 69 provided by the present invention: including any one of the above examples 48 to 68, wherein the second electrode is curved or spherical.
  • Example 70 provided by the present invention includes any one of the above examples 48 to 69, 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 71 provided by the present invention: including any one of the above examples 48 to 70, 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 72 provided by the present invention includes any one of the above examples 48 to 71, 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 73 provided by the present invention: including the above example 71 or 72, wherein the voltage of the power supply is 5-50KV.
  • Example 74 provided by the present invention includes any one of the above examples 71 to 73, wherein the voltage of the power supply is less than the initial halo voltage.
  • Example 75 provided by the present invention: including any one of the above examples 71 to 74, wherein the voltage of the power supply is 0.1kv-2kv / mm.
  • Example 76 provided by the present invention includes any one of the above examples 71 to 75, wherein the voltage waveform of the power supply is a DC waveform, a sine wave, or a modulation waveform.
  • Example 77 provided by the present invention includes any one of the above examples 71 to 76, 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 78 provided by the present invention includes any one of the above examples 48 to 77, 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 79 provided by the present invention includes any one of the above examples 48 to 78, wherein there are two second electrodes, and the first electrode is located between the two second electrodes.
  • Example 80 provided by the present invention: includes any one of the above examples 48 to 79, wherein the distance between the first electrode and the second electrode is 5-50 mm.
  • Example 81 provided by the present invention includes any one of the above examples 48 to 80, wherein the first electrode and the second electrode constitute an adsorption unit, and there are a plurality of the adsorption units.
  • Example 82 provided by the present invention includes the above example 81, in which 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 83 includes any one of the above examples 48 to 82, 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 84 provided by the present invention includes the above example 83, wherein the electrocoagulation inlet is circular, and the diameter of the electrocoagulation inlet is 300-1000 mm, or 500 mm.
  • Example 85 provided by the present invention includes the above example 83 or 84, wherein the electrocoagulation outlet is circular, and the diameter of the electrocoagulation outlet is 300-1000 mm, or 500 mm.
  • Example 86 provided by the present invention: including any one of the above examples 83 to 85, 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.
  • Example 87 provided by the present invention includes the above example 86, wherein the outline size of the first housing portion gradually increases from the electrocoagulation inlet to the electrocoagulation outlet.
  • Example 88 provided by the present invention includes the above-mentioned example 86 or 87, wherein the first housing portion has a straight tubular shape.
  • Example 89 provided by the present invention: including any one of the above examples 86 to 88, 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 90 provided by the present invention includes any one of the above examples 86 to 89, wherein the outline size of the third housing portion gradually decreases from the electrocoagulation inlet to the electrocoagulation outlet direction.
  • Example 91 provided by the present invention: includes any one of the above examples 86 to 90, wherein the cross sections of the first housing portion, the second housing portion, and the third housing portion are all rectangular.
  • Example 92 provided by the present invention includes any one of the above examples 83 to 91, 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 93 provided by the present invention includes any one of the above examples 48 to 92, wherein the first electrode is connected to the electrocoagulation case through an electrocoagulation insulator.
  • Example 94 provided by the present invention includes the above example 93, wherein the material of the electrocoagulation insulating member is insulating mica.
  • Example 95 provided by the present invention includes the above example 93 or 94, wherein the electrocoagulation insulator is in the shape of a column or a tower.
  • Example 96 provided by the present invention: includes any one of the above examples 48 to 95, 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 97 provided by the present invention includes any one of the above examples 48 to 96, 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 98 provided by the present invention includes any one of the above examples 48 to 97, 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 99 provided by the present invention includes any one of the above examples 47 to 98, wherein the denitration device includes a condensation unit for condensing the ozone-treated tail gas to achieve gas-liquid separation.
  • Example 100 provided by the present invention includes any one of the above examples 47 to 99, wherein the denitration device includes a rinsing unit for rinsing the exhaust gas after ozone treatment.
  • Example 101 includes the above example 100, wherein the denitration device further includes an eluent unit for providing an eluent to the eluent unit.
  • Example 102 provided by the present invention: includes the above example 101, wherein the eluent in the eluent unit includes water and / or alkali.
  • Example 103 provided by the present invention: including any one of the above examples 47 to 102, wherein the denitration device further includes a denitration liquid collection unit for storing the nitric acid aqueous solution and / or nitrate aqueous solution removed in the tail gas .
  • Example 104 provided by the present invention: includes the above example 103, 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 105 provided by the present invention includes any one of the above examples 1 to 104, wherein the exhaust gas ozone purification system further includes an ozone digester for digesting ozone in the exhaust gas treated by the reaction field.
  • Example 106 provided by the present invention includes the above example 105, wherein the ozone digester is selected from at least one of an ultraviolet ozone digester and a catalytic ozone digester.
  • Example 107 provided by the present invention includes any one of the above examples 1 to 106, wherein the exhaust gas ozone purification system further includes a first denitration device for removing nitrogen oxides in the exhaust gas; the reaction field It is used to mix and react the tail gas processed by the first denitration device with the ozone stream, or to mix and react the tail gas with the ozone stream before being processed by the first denitration device.
  • the exhaust gas ozone purification system further includes a first denitration device for removing nitrogen oxides in the exhaust gas; the reaction field It is used to mix and react the tail gas processed by the first denitration device with the ozone stream, or to mix and react the tail gas with the ozone stream before being processed by the first denitration device.
  • Example 108 provided by the present invention includes the above example 107, 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 109 provided by the present invention: includes any one of the above examples 1 to 108, wherein it further includes an engine.
  • Example 110 provided by the present invention: an exhaust gas ozone purification method, comprising the following steps: mixing and reacting an ozone stream with an exhaust stream.
  • Example 111 provided by the present invention: includes the exhaust gas ozone purification method described in Example 110, wherein the exhaust gas stream includes nitrogen oxides and volatile organic compounds.
  • Example 112 provided by the present invention: includes the exhaust gas ozone purification method described in Example 110 or 111, wherein in the low temperature section of the exhaust gas, the mixing reaction of the ozone stream and the exhaust gas stream.
  • Example 113 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 110 to 112, wherein the mixing reaction temperature of the ozone stream and the exhaust gas stream is -50 to 200 ° C.
  • Example 114 provided by the present invention: The exhaust gas ozone purification method described in Example 113, wherein the mixing reaction temperature of the ozone stream and the exhaust gas stream is 60-70 ° C.
  • Example 115 includes the exhaust gas ozone purification method according to any one of Examples 110 to 114, wherein the mixing method of the ozone stream and the exhaust stream is selected from Venturi mixing, positive pressure mixing, insertion mixing, At least one of dynamic mixing and fluid mixing.
  • Example 116 provided by the present invention: includes the exhaust gas ozone purification method described in Example 115, wherein when the mixing mode of the ozone stream and the exhaust gas stream is positive pressure mixing, the pressure of the ozone inlet gas is greater than the pressure of the exhaust gas.
  • Example 117 provided by the present invention includes the exhaust gas ozone purification method described in Example 110, wherein, before the ozone stream and the exhaust gas stream are mixed and reacted, the exhaust gas stream velocity is increased and the ozone stream is mixed using the Venturi principle.
  • Example 118 provided by the present invention includes the exhaust gas ozone purification method described in Example 110, wherein the mixing method of the ozone stream and the exhaust gas stream is selected from the reverse flow of the exhaust gas outlet, the mixing in the front section of the reaction field, the front and rear insertion of the dust collector, and the denitration At least one of mixing back and forth of the device, mixing back and forth of the catalytic device, mixing back and forth of the washing device, mixing back and forth of the filtering device, mixing back and forth of the muffler device, mixing in the exhaust pipe, mixing externally by the adsorption device and mixing back and forth of the condensation device.
  • Example 119 provided by the present invention includes the exhaust gas ozone purification method described in Example 110, wherein the reaction field in which the ozone stream and the exhaust gas stream are mixed and reacted includes pipes and / or reactors.
  • Example 120 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 110 to 119, wherein the reaction field includes an exhaust pipe, a regenerator device, or a catalyst.
  • Example 121 provided by the present invention includes the exhaust gas ozone purification method described in Example 120, wherein the exhaust gas ozone purification method further includes at least one of the following technical features:
  • 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 tail 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 tail gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing a cold medium to control the tail gas and Ozone reaction temperature;
  • 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 the tail 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 to contact the exhaust gas.
  • the ozone inlet is formed in at least one of the following directions: opposite to the direction of the exhaust gas flow, and The direction is perpendicular, tangential to the direction of exhaust gas flow, the direction of insertion exhaust gas flow, and multiple directions are in contact with the exhaust gas.
  • Example 122 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 110 to 121, wherein the ozone stream is provided by a storage ozone unit and / or an ozone generator.
  • Example 123 provided by the present invention includes the exhaust gas ozone purification method described in Example 122, wherein the ozone generator includes a surface discharge ozone generator, a power frequency arc ozone generator, a high frequency induction ozone generator, a low One or more combinations of air pressure ozone generator, ultraviolet ozone generator, electrolyte ozone generator, chemical agent ozone generator and 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 One or more combinations of air pressure ozone generator, ultraviolet ozone generator, electrolyte ozone generator, chemical agent ozone generator and radiation irradiation particle generator.
  • Example 124 provided by the present invention includes the exhaust gas ozone purification method described in Example 122, wherein the ozone stream providing method: under the action of an electric field and an oxidation catalytic bond cracking selective catalyst, a gas containing oxygen generates ozone, A selective catalyst for oxidative catalytic bond cleavage is supported on the electrode forming the electric field.
  • Example 125 provided by the present invention: The exhaust gas ozone purification method including Example 124, wherein the electrode includes a high-voltage electrode or an electrode provided with a barrier medium layer, and when the electrode includes a high-voltage electrode, the oxidation catalysis A selective catalyst for bond cleavage is supported on the surface of the high-voltage electrode. When the electrode includes a high-voltage electrode for the barrier medium layer, the selective catalyst for bond cleavage of the oxidation catalyst is supported on the surface of the barrier medium layer.
  • Example 126 provided by the present invention includes the exhaust gas ozone purification method described in Example 124, wherein when the electrode includes a high-voltage electrode, the thickness of the oxidation catalytic bond cracking selective catalyst is 1 to 3 mm; when the When the electrode includes a high-voltage electrode that blocks the dielectric layer, the loading of the selective catalyst for oxidative catalytic bond cleavage includes 1 to 10 wt% of the blocking dielectric layer.
  • Example 127 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 124 to 126, wherein the oxidation catalytic bond cracking selective catalyst 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 128 provided by the present invention: includes the exhaust gas ozone purification method described in Example 127, wherein the alkaline earth metal element is selected from at least one of magnesium, strontium, and calcium.
  • Example 129 provided by the present invention includes the exhaust gas ozone purification method described in Example 127, wherein the transition metal element is selected from at least one of titanium, manganese, zinc, copper, iron, nickel, cobalt, yttrium, and zirconium Species.
  • Example 130 provided by the present invention includes the exhaust gas ozone purification method described in Example 127, wherein the fourth main group metal element is tin.
  • Example 131 provided by the present invention includes the exhaust gas ozone purification method described in Example 127, wherein the precious metal element is selected from at least one of platinum, rhodium, palladium, gold, silver, and iridium.
  • Example 132 provided by the present invention: includes the exhaust gas ozone purification method described in Example 127, wherein the lanthanide rare earth element is selected from at least one of lanthanum, cerium, praseodymium, and samarium.
  • Example 133 provided by the present invention: includes the exhaust gas ozone purification method described in Example 127, wherein the compound of the metal element M is selected from oxides, sulfides, sulfates, phosphates, carbonates, and calcium titanium At least one of the mines.
  • Example 134 provided by the present invention includes the exhaust gas ozone purification method described in Example 127, wherein the porous material is selected from at least one of molecular sieve, diatomaceous earth, zeolite, and carbon nanotubes.
  • Example 135 provided by the present invention includes the exhaust gas ozone purification method described in Example 127, wherein the layered material is selected from at least one of graphene and graphite.
  • Example 136 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 124 to 126, wherein the electrode is loaded with an oxygen double catalytic bond cracking selective catalyst by a method of impregnation and / or spraying.
  • Example 137 provided by the present invention includes the exhaust gas ozone purification method described in Example 136, which includes the following steps:
  • 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.
  • Example 138 provided by the present invention includes the exhaust gas ozone purification method described in Example 136, which includes the following steps:
  • 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.
  • Example 139 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 110 to 138, which includes: controlling the amount of ozone in the ozone stream so as to effectively oxidize the gas component to be treated in the exhaust gas.
  • Example 140 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 110 to 139, wherein controlling the amount of ozone in the ozone stream to achieve the following removal efficiency:
  • Nitrogen oxide removal efficiency 60-99.97%
  • Example 141 provided by the present invention includes the exhaust gas ozone purification method described in Example 139 or 140, which includes: detecting the content of exhaust gas components before ozone treatment.
  • Example 142 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 139 to 141, wherein the amount of ozone required for the mixing reaction is controlled according to the content of the exhaust gas component before the ozone treatment.
  • Example 143 provided by the present invention includes the exhaust gas ozone purification method described in Example 141 or 142, wherein the content of the exhaust gas component before the ozone treatment is selected from at least one of the following:
  • Example 144 provided by the present invention includes the exhaust gas ozone purification method described in Example 143, wherein the amount of ozone required for the mixed reaction is controlled according to at least one output value that detects the content of the exhaust gas component before ozone treatment.
  • Example 145 provided by the present invention: The exhaust gas ozone purification method according to any one of Examples 139 to 144, wherein the amount of ozone required for the mixed reaction is controlled according to a preset mathematical model.
  • Example 146 provided by the present invention: The exhaust gas ozone purification method according to any one of Examples 139 to 145, wherein the amount of ozone required for the mixed reaction is controlled according to a theoretical estimated value.
  • Example 147 provided by the present invention includes the method for purifying ozone in exhaust gas as described in Example 146, wherein the theoretical estimated value is: the molar ratio of ozone flux to the material to be treated in the exhaust gas is 2-10.
  • Example 148 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 139 to 147, which includes: detecting the content of exhaust gas components after ozone treatment.
  • Example 149 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 139 to 148, wherein the amount of ozone required for the mixing reaction is controlled according to the content of the exhaust gas component after the ozone treatment.
  • Example 150 provided by the present invention includes the exhaust gas ozone purification method described in Example 148 or 149, wherein the content of the exhaust gas component after the ozone treatment is detected is selected from at least one of the following:
  • Example 151 provided by the present invention includes the exhaust gas ozone purification method described in Example 150, wherein the amount of ozone is controlled according to at least one output value that detects the content of exhaust gas components after ozone treatment.
  • Example 152 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 110 to 151, wherein the exhaust gas ozone purification method further includes the following steps: removing mixed reaction products of the ozone stream and the exhaust gas stream Nitric acid.
  • Example 153 provided by the present invention: includes the exhaust gas ozone purification method described in Example 152, wherein 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 applies an attractive force to the charged nitric acid mist, so that the nitric acid mist moves toward the second electrode until the nitric acid mist adheres to On the second electrode.
  • Example 154 provided by the present invention includes the exhaust gas ozone purification method described in Example 153, wherein the first electrode introduces electrons into a nitric acid mist, and the electrons are transferred between mist droplets between the first electrode and the second electrode, Charge more droplets.
  • Example 155 provided by the present invention includes the exhaust gas ozone purification method described in Example 153 or 154, wherein the first electrode and the second electrode conduct electrons through a nitric acid mist and form an electric current.
  • Example 156 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153-155, wherein the first electrode charges the nitric acid mist by contact with the nitric acid mist.
  • Example 157 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153-156, wherein the first electrode charges the nitric acid mist by means of energy fluctuation.
  • Example 158 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153-157, wherein 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.
  • Example 159 provided by the present invention: includes the exhaust gas ozone purification method described in Example 158, wherein water droplets on the second electrode flow into the collection tank under the action of gravity.
  • Example 160 provided by the present invention: includes the exhaust gas ozone purification method described in Example 158 or 159, wherein when the gas flows, the blowing water droplets flow into the collection tank.
  • Example 161 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153-160, wherein the first electrode is a solid, a liquid, a gas molecular group, a plasma, a conductive mixed-state substance, a biological body Naturally mixed conductive substances, or objects are artificially processed to form a combination of one or more forms of conductive substances.
  • the first electrode is a solid, a liquid, a gas molecular group, a plasma, a conductive mixed-state substance, a biological body Naturally mixed conductive substances, or objects are artificially processed to form a combination of one or more forms of conductive substances.
  • Example 162 includes the exhaust gas ozone purification method according to any one of Examples 153-161, wherein the first electrode is solid metal, graphite, or 304 steel.
  • Example 163 includes the exhaust gas ozone purification method according to any one of Examples 153-162, wherein the first electrode is dot-shaped, wire-shaped, mesh-shaped, orifice-shaped, plate-shaped, needle-rod-shaped , Ball cage, box, tube, natural form material, or processed form material.
  • Example 164 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 153-163, wherein the first electrode is provided with a front through hole.
  • Example 165 includes the exhaust gas ozone purification method of Example 164, wherein the shape of the front through hole is polygon, circle, ellipse, square, rectangle, trapezoid, or diamond.
  • Example 166 provided by the present invention: includes the exhaust gas ozone purification method described in Example 164 or 165, wherein the pore diameter of the front through hole is 0.1-3 mm.
  • Example 167 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153-166, wherein the second electrode is in the form of a multi-layer mesh, mesh, orifice, tube, barrel, Ball cage, box shape, plate shape, particle accumulation layer shape, bent plate shape, or panel shape.
  • Example 168 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 167, wherein a rear through hole is provided on the second electrode.
  • Example 169 provided by the present invention includes the exhaust gas ozone purification method of Example 168, wherein the rear through hole is polygonal, circular, elliptical, square, rectangular, trapezoidal, or rhombic.
  • Example 170 provided by the present invention includes the exhaust gas ozone purification method described in Example 168 or 169, wherein the diameter of the rear through hole is 0.1-3 mm.
  • Example 171 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 170, wherein the second electrode is made of a conductive substance.
  • Example 172 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 153 to 171, wherein the surface of the second electrode has a conductive substance.
  • Example 173 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 153 to 172, wherein an electrocoagulation electric field is provided between the first electrode and the second electrode, and the electrocoagulation electric field is a point surface A combination of one or more electric fields in the electric field, line-area electric field, mesh-area electric field, dot-barrel electric field, wire-barrel electric field, or wire-barrel electric field.
  • Example 174 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 173, wherein the first electrode is linear and the second electrode is planar.
  • Example 175 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 153 to 174, wherein the first electrode is perpendicular to the second electrode.
  • Example 176 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 175, wherein the first electrode is parallel to the second electrode.
  • Example 177 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 176, wherein the first electrode is curved or arc-shaped.
  • Example 178 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 177, wherein the first electrode and the second electrode are both planar, and the first electrode and the second electrode Parallel.
  • Example 179 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 178, wherein the first electrode uses a wire mesh.
  • Example 180 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 179, wherein the first electrode is planar or spherical.
  • Example 181 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 180, wherein the second electrode is curved or spherical.
  • Example 182 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 153 to 181, wherein the first electrode is dot-shaped, linear, or mesh-shaped, and 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.
  • Example 183 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 182, wherein the first electrode is electrically connected to one electrode of the power supply, and the second electrode is connected to the other of the power supply The electrodes are electrically connected.
  • Example 184 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 183, 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 connection.
  • Example 185 provided by the present invention includes the exhaust gas ozone purification method described in Example 183 or 184, wherein the voltage of the power supply is 5-50KV.
  • Example 186 provided by the present invention: including the exhaust gas ozone purification method according to any one of Examples 183 to 185, wherein the voltage of the power source is less than the initial halo voltage.
  • Example 187 provided by the present invention: including the exhaust gas ozone purification method of any one of Examples 183 to 186, wherein the voltage of the power source is 0.1 kv-2 kv / mm.
  • Example 188 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 183 to 187, wherein the voltage waveform of the power supply is a DC waveform, a sine wave, or a modulated waveform.
  • Example 189 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 183 to 188, 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 190 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 189, 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 at the The left end of the left end of the two electrodes.
  • Example 191 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 190, wherein there are two second electrodes, and the first electrode is located between the two second electrodes.
  • Example 192 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 191, wherein the distance between the first electrode and the second electrode is 5-50 mm.
  • Example 193 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 192, wherein the first electrode and the second electrode constitute an adsorption unit, and there are a plurality of adsorption units.
  • Example 194 provided by the present invention includes the exhaust gas ozone purification method described in Example 193, wherein all 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 195 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 153 to 194, wherein the first electrode is installed in an electrocoagulation housing, and the electrocoagulation housing has an electrocoagulation inlet and Electrocoagulation outlet.
  • Example 196 provided by the present invention includes the exhaust gas ozone purification method of Example 195, wherein the electrocoagulation inlet is circular, and the diameter of the electrocoagulation inlet is 300-1000 mm, or 500 mm.
  • Example 197 provided by the present invention includes the exhaust gas ozone purification method described in Example 195 or 196, wherein the electrocoagulation outlet is circular, and the diameter of the electrocoagulation outlet is 300-1000 mm, or 500 mm.
  • Example 198 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 195 to 197, wherein the electrocoagulation housing includes a first housing portion sequentially distributed from the electrocoagulation inlet to the electrocoagulation outlet In the second casing portion and the third casing portion, the electrocoagulation inlet is located at one end of the first casing portion, and the electrocoagulation outlet is located at one end of the third casing portion.
  • Example 199 provided by the present invention includes the exhaust gas ozone purification method described in Example 198, wherein the outline size of the first housing portion gradually increases from the electrocoagulation inlet to the electrocoagulation outlet.
  • Example 200 includes the exhaust gas ozone purification method described in Example 198 or 199, wherein the first housing portion has a straight tubular shape.
  • Example 201 includes the exhaust gas ozone purification method according to any one of Examples 198 to 200, wherein the second housing portion has a straight tube shape, and the first electrode and the second electrode are installed at the first In the second housing part.
  • Example 202 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 198 to 201, wherein the outline size of the third housing portion gradually decreases from the electrocoagulation inlet to the electrocoagulation outlet direction.
  • Example 203 provided by the present invention: includes the exhaust gas ozone purification method according to any one of Examples 198 to 202, wherein the cross sections of the first shell portion, the second shell portion, and the third shell portion are all present rectangle.
  • Example 204 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 195 to 203, wherein the material of the electrocoagulation shell is stainless steel, aluminum alloy, iron alloy, cloth, sponge, molecular sieve, activated carbon, Foam iron, or foam silicon carbide.
  • Example 205 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 204, wherein the first electrode is connected to the electrocoagulation case through an electrocoagulation insulator.
  • Example 206 provided by the present invention includes the exhaust gas ozone purification method described in Example 205, wherein the material of the electrocoagulation insulator is insulating mica.
  • Example 207 provided by the present invention includes the exhaust gas ozone purification method described in Example 205 or 206, wherein the electrocoagulation insulator is in the shape of a column or tower.
  • Example 208 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 207, wherein a cylindrical front connection portion is provided on the first electrode, and the front connection portion is Condensation insulation is fixed.
  • Example 209 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 208, wherein the second electrode is provided with a cylindrical rear connection portion, and the rear connection portion is Condensation insulation is fixed.
  • Example 210 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 153 to 209, wherein the first electrode is located in the electrocoagulation flow channel; the gas with nitric acid mist flows along the electrocoagulation flow channel, and Flowing through the first electrode; the ratio of the cross-sectional area of the first electrode to the cross-sectional area of the electrocoagulation flow channel is 99% -10%, or 90-10%, or 80-20%, or 70-30%, or 60 ⁇ 40%, or 50%.
  • Example 211 provided by the present invention includes the exhaust gas ozone purification method described in any one of Examples 152 to 210, wherein the method for removing nitric acid in the mixed reaction product of the ozone stream and the exhaust gas stream: combining the ozone stream with The tail gas stream mixes the reaction product and condenses.
  • Example 212 provided by the present invention includes the exhaust gas ozone purification method described in any one of Examples 152 to 211, wherein the method for removing nitric acid in the mixed reaction product of the ozone stream and the exhaust gas stream: combining the ozone stream with The tail gas stream mixes the reaction product for rinsing.
  • Example 213 provided by the present invention includes the exhaust gas ozone purification method described in Example 212, wherein the method for removing nitric acid in the mixed reaction product of the ozone stream and the exhaust gas stream further includes: to the ozone stream and the exhaust gas stream The mixed reaction products provide eluent.
  • Example 214 provided by the present invention includes the method for purifying ozone in exhaust gas as described in Example 213, wherein the eluent is water and / or alkali.
  • Example 215 provided by the present invention includes the exhaust gas ozone purification method described in any one of Examples 152 to 214, wherein the method for removing nitric acid in the mixed reaction product of the ozone stream and the exhaust gas stream further includes: storing the exhaust gas The removed nitric acid aqueous solution and / or nitrate aqueous solution.
  • Example 216 provided by the present invention includes the exhaust gas ozone purification method described in Example 215, wherein when an aqueous solution of nitric acid is stored, an alkaline solution is added to form nitrate with nitric acid.
  • Example 217 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 110 to 216, wherein the exhaust gas ozone purification method further includes the following step: performing ozone digestion on the exhaust gas from which nitric acid has been removed.
  • Example 218 provided by the present invention includes the exhaust gas ozone purification method described in Example 217, wherein the ozone digestion is selected from at least one of ultraviolet digestion and catalytic digestion.
  • Example 219 provided by the present invention includes the exhaust gas ozone purification method according to any one of Examples 110 to 218, wherein the exhaust gas ozone purification method further includes the following steps: removing nitrogen oxides from the exhaust gas for the first time; The tail gas stream after one-time removal of nitrogen oxides is mixed and reacted with the ozone stream, or, before the first removal of nitrogen oxides in the tail gas, it is mixed and reacted with the ozone stream first.
  • Example 220 provided by the present invention: includes the exhaust gas ozone purification method described in Example 219, wherein the first removal of nitrogen oxides in the exhaust gas is selected from a non-catalytic reduction method, a selective catalytic reduction method, and a non-selective method At least one of a catalytic reduction method, an electron beam denitration method, and the like.
  • Figure 1 is a schematic diagram of the engine exhaust ozone purification system.
  • 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 engine exhaust ozone purification system according to Embodiment 1 of the present invention.
  • FIG. 6 is a plan view of the reaction field in the engine exhaust ozone purification system of Embodiment 1 of the present invention.
  • FIG. 7 is a schematic diagram of the ozone amount control device of the present invention.
  • Embodiment 8 is a schematic structural diagram of an electrocoagulation device in Embodiment 9 of the present invention.
  • Embodiment 9 is a left side view of the electrocoagulation device in Embodiment 9 of the present invention.
  • Embodiment 10 is a perspective view of an electrocoagulation device in Embodiment 9 of the present invention.
  • Example 11 is a schematic structural diagram of an electrocoagulation device in Example 10 of the present invention.
  • Embodiment 12 is a top view of an electrocoagulation device in Embodiment 10 of the present invention.
  • FIG. 13 is a schematic structural diagram of an electrocoagulation device in Embodiment 11 of the present invention.
  • Embodiment 14 is a schematic structural diagram of an electrocoagulation device in Embodiment 12 of the present invention.
  • Embodiment 15 is a schematic structural diagram of an electrocoagulation device in Embodiment 13 of the present invention.
  • FIG. 16 is a schematic structural diagram of an electrocoagulation device in Embodiment 14 of the present invention.
  • FIG. 17 is a schematic structural diagram of an electrocoagulation device in Embodiment 15 of the present invention.
  • Embodiment 16 is a schematic structural diagram of an electrocoagulation device in Embodiment 16 of the present invention.
  • Embodiment 19 is a schematic structural diagram of an electrocoagulation device in Embodiment 17 of the present invention.
  • Embodiment 18 is a schematic structural diagram of an electrocoagulation device in Embodiment 18 of the present invention.
  • FIG. 21 is a schematic structural diagram of an electrocoagulation device in Embodiment 19 of the present invention.
  • FIG. 22 is a schematic structural diagram of an electrocoagulation device in Embodiment 20 of the present invention.
  • Embodiment 23 is a schematic structural diagram of an electrocoagulation device in Embodiment 21 of the present invention.
  • Embodiment 24 is a schematic structural diagram of an electrocoagulation device in Embodiment 22 of the present invention.
  • the engine exhaust ozone purification system includes a reaction field for mixing and reacting the ozone stream with the exhaust stream. For example: treating the exhaust gas of the automobile engine 210, using the water in the exhaust gas and the exhaust gas pipeline 220 to generate an oxidation reaction, oxidizing the organic volatile matter in the exhaust gas to carbon dioxide and water; and harmlessly collecting sulfur and nitrate.
  • the exhaust gas ozone purification system may further include an external ozone generator 230, which supplies ozone to the exhaust gas 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 the positive or negative pressure into the reaction field, such as the exhaust gas channel.
  • 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, and nitrogen
  • the removal rate of oxygen compounds 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 compound removal rate is 99%. Power consumption increased to 30w / g.
  • the ozone produced by the ultraviolet lamp produces 11-195 nanometer wavelength ultraviolet rays by gas discharge, and directly irradiates the air around the lamp to produce ozone, high-energy ions, and high-energy particles, which pass 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 gas 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%, and then nitrogen Oxygen compound gas concentration drops, nitrogen oxides removal rate is 70%; when the molar ratio of 185 nanometer ultraviolet ozone stream to tail gas stream is greater than 10, the VOCs removal rate is more than 95%, then the nitrogen oxide compound gas concentration decreases and nitrogen oxides removal The 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 tail gas stream is 5, the VOCs removal rate is over 89%, and then When the nitrogen oxide gas concentration decreases, 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, nitrogen oxides The compound removal rate was 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 tail 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 tail gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing a cold medium to control the tail gas and Ozone reaction temperature;
  • 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 the tail 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, and the ozone enters the reaction field through the ozone inlet to contact the exhaust gas, and the ozone inlet is formed in at least one of the following directions: the direction opposite to the flow of the exhaust gas, and the The direction is perpendicular, tangent to the direction of the exhaust gas flow, insert the exhaust gas flow direction, and multiple directions are in contact with the exhaust gas; the opposite direction to the exhaust gas flow is to enter in the opposite direction, increase the reaction time, reduce the volume; the flow with the exhaust gas
  • the direction is vertical and uses the Venturi effect; it is tangent to the direction of exhaust gas flow for easy mixing; insert 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 engine exhaust ozone purification system further includes an ozone source for providing 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 tail gas stream to subject the tail gas 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.
  • 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, generating 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 engine exhaust ozone purification system further includes an ozone amount control device for controlling the amount of ozone so as to effectively oxidize the gas component to be treated in the exhaust gas.
  • the ozone amount control device includes a control unit.
  • the ozone amount control device further includes a tail gas component detection unit before ozone treatment, configured to detect the content of the tail gas component 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 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 gas 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 tail gas 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 tail gas component to ozone, and ozone can be increased when determining the amount of ozone required for the mixed reaction The amount of ozone is 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 to-be-processed material in the exhaust gas is 2-10.
  • 13L diesel engine can control ozone flux from 300 to 500g
  • 2L gasoline engine can control ozone flux from 5 to 20g.
  • the ozone quantity control device includes an exhaust gas component detection unit after ozone treatment, configured to detect the content of the exhaust gas component 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 exhaust gas component detection unit after ozone treatment.
  • the engine 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 realize gas-liquid separation.
  • the denitration device includes a rinsing unit for rinsing the exhaust gas after ozone treatment, for example, water and / or alkali for rinsing.
  • 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 tail 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 engine exhaust ozone purification system further includes an ozone digester, which 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, catalysis and the like.
  • the ozone digester is selected from at least one of an ultraviolet ozone digester and a catalytic ozone digester.
  • the engine exhaust ozone purification system further includes a first denitration device for removing nitrogen oxides in the exhaust gas; the reaction field is used for treating the exhaust gas processed by the first denitration device Mixed reaction with ozone stream, or used to mix and react tail gas with 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 of the engine 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 treatment of the first denitration device 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.
  • ozone When ozone is used to treat engine exhaust, ozone is most preferred to react with volatile organic compounds VOC and be oxidized into CO 2 and water, and then with nitrogen oxide compounds NO X to be oxidized into high-valent nitrogen oxides such as NO 2 and 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 gas VOC produces enough water to fully react with high-valent nitrogen oxides to generate nitric acid. Therefore, the use of ozone to treat engine exhaust makes ozone to remove NO X better. This effect is unexpected for those skilled in the art. Technical effect.
  • Engine 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.
  • An exhaust gas 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 gas stream may be engine exhaust gas, and the engine is generally a device that converts chemical energy of fuel into mechanical energy, which may specifically be an internal combustion engine or the like, and more specifically may be diesel engine exhaust gas 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.
  • the nitrogen oxides (NO x ) in the exhaust gas 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, which can 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 tail gas 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 gas 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. .
  • the reaction field in which the ozone stream and the tail gas 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 tail 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 tail gas and ozone are mixed and reacted; a gap is provided between the honeycomb-shaped cavities for passing a cold medium to control the tail gas and Ozone reaction temperature;
  • 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 the tail 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 to contact the exhaust gas.
  • the ozone inlet is formed in at least one of the following directions: opposite to the direction of the exhaust gas flow, and The direction is perpendicular, tangent to the direction of the exhaust gas flow, insert the exhaust gas flow direction, and multiple directions are in contact with the exhaust gas; the opposite direction to the exhaust gas flow is to enter in the opposite direction, increase the reaction time, reduce the volume; the flow with the exhaust gas
  • the direction is vertical and uses the Venturi effect; it is tangent to the direction of exhaust gas flow for easy mixing; insert 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 a 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 the active component obtained in step 1) is made into a slurry, supported 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 tail 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 gas components before ozone treatment.
  • the amount of ozone required for the mixed reaction is controlled according to the content of the exhaust gas component before the ozone treatment.
  • the content of the exhaust gas component before the 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 for detecting the content of the exhaust gas component 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 tail gas 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 tail gas component to ozone, and ozone can be increased when determining the amount of ozone required for the mixed reaction The amount of ozone is 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 to-be-processed material in the exhaust gas is 2 to 10, such as 5 to 6, 5.5 to 6.5, 5 to 7, 4.5 to 7.5, 4-8, 3.5-8.5, 3-9, 2.5-9.5, 2-10.
  • 13L diesel engine can control ozone flux from 300 to 500g
  • 2L gasoline engine can control ozone flux from 5 to 20g.
  • it includes: detecting the content of exhaust gas components after ozone treatment.
  • the amount of ozone required for the mixed reaction is controlled according to the content of the exhaust gas component after the ozone treatment.
  • the content of the exhaust gas component 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 gas components after ozone treatment.
  • the tail gas ozone purification method further includes the following steps: removing nitric acid from the mixed reaction product of the ozone stream and the tail 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 from a mixed reaction product of an ozone stream and a tail gas stream condensing the mixed reaction product of the ozone stream and the tail gas stream.
  • a method for removing nitric acid in a mixed reaction product of an ozone stream and a tail gas stream washing the mixed reaction product of the ozone stream and the tail gas stream.
  • the method for removing nitric acid from the mixed reaction product of the ozone stream and the tail gas stream further includes: providing an eluent to the mixed reaction product of the ozone stream and the tail gas stream.
  • the eluent is water and / or alkali.
  • the method for removing nitric acid from the mixed reaction product of the ozone stream and the tail gas stream further includes: storing the removed nitric acid aqueous solution and / or nitrate aqueous solution in the tail 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 nitric acid removal exhaust gas, 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 gas ozone purification method further includes the following steps: removing nitrogen oxides from the exhaust gas for the first time; mixing the exhaust gas stream with the ozone stream after the first nitrogen oxide removal, Alternatively, before the first removal of nitrogen oxides in the tail gas, it is mixed and reacted with the ozone stream.
  • the first removal of nitrogen oxides in the tail gas can be a method for denitrification in the prior art, for example: non-catalytic reduction method (such as ammonia denitration), selective catalytic reduction method (SCR: ammonia plus catalyst denitration), non- At least one of a selective catalytic reduction method (SNCR) and an electron beam denitration method.
  • non-catalytic reduction method such as ammonia denitration
  • SCR selective catalytic reduction method
  • SNCR non- At least one of a selective catalytic reduction method
  • An electron beam denitration method an electron beam denitration method.
  • the content of nitrogen oxides (NO x ) in the engine exhaust gas does not reach the standard after the first removal of nitrogen oxides in the exhaust gas, and can reach the latest standard after the first removal of the nitrogen oxides in the exhaust gas or after a mixed reaction with ozone .
  • 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. .
  • 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 may be one or more forms of solid, liquid, gas molecular cluster, plasma, conductive mixed state substance, biological natural mixed conductive substance, or artificially processed object to form conductive substance The combination.
  • 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 may be a multi-layer mesh, a mesh, an orifice, a tube, a barrel, a ball cage, a box, a plate, a particle accumulation layer, or a bent plate , Or panel-like.
  • 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 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 net barrel A combination of one or more electric fields in the electric field.
  • 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, specifically, it may be planar, 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 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 is electrically connected to one electrode of the power supply; the second electrode is electrically connected to the other electrode of the power supply. In an embodiment of the invention, 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 fluctuations, so that the first electrode can not contact 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.
  • movable particles such as fog droplets
  • the current formed by the moving charged particles For example, as the amount of electrons increases, movable particles, such as fog droplets, increase the current formed by the moving charged particles.
  • 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 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 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 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 adjusted arbitrarily to meet 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.
  • the power-on driving voltage of each power supply may be the same or different.
  • 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 electrocoagulation Mist of nitric acid flowing out from the 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 case is a conductor, the material may be 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. When 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.
  • An engine exhaust ozone purification system as shown in Figure 5, 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 to mix and react 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 electrocoagulating the engine exhaust gas after ozone treatment, and water containing nitric acid The 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 for digesting 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. 6, a plurality of honeycomb cavities 2021 are provided therein to provide a space where tail gas and ozone are mixed and reacted; gaps 2022 are provided between the honeycomb cavities , Used to pass 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 is used to treat industrial tail gas containing acid mist.
  • the inlet 3031 is connected to the port for discharging industrial exhaust gas.
  • 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 flow through one of the first electrodes 301 first.
  • the first electrode 301 transfers electrons to the acid mist, part of the acid mist is charged, and the second electrode 302 gives the charged acid mist
  • 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 this part of the acid mist continues to flow toward the outlet 3032.
  • both the inlet 3031 and the outlet 3032 are circular, the inlet 3031 may also be referred to as an air inlet, and the outlet 3032 may also be referred to as an air inlet.
  • the engine exhaust ozone purification system in Embodiment 1 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, and the ozone amount control device 209 includes a control unit 2091.
  • the ozone amount control device 209 further includes a tail gas component detection unit 2092 before ozone treatment, configured to detect the content of the tail gas component before ozone treatment.
  • the 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 20921 is used to detect the content of volatile organic compounds in the exhaust gas before ozone treatment, such as a volatile organic compound sensor;
  • 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 at least one output value of the exhaust gas component detection unit 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 to-be-processed material in the exhaust gas is 2-10.
  • the ozone quantity control device includes an exhaust gas component detection unit 2093 after ozone treatment, which is used to detect the content of the exhaust gas component after ozone treatment.
  • the 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 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 based on at least one output value of the exhaust gas composition detection unit after ozone treatment.
  • 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.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the water mist containing nitric acid; when the electrons are conducted to the water mist of nitric acid, the water mist of nitric acid is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the electrocoagulation device in this embodiment further includes an electrocoagulation housing 303 having an electrocoagulation inlet 3031 and an electrocoagulation outlet 3032, and the first electrode 301 and the second electrode 302 are both installed in the electrocoagulation housing 303.
  • the first electrode 301 is fixedly connected to the inner wall of the electrocoagulation case 303 through the electrocoagulation insulator 304, and the second electrode 302 is directly fixed to the electrocoagulation case 303.
  • the electrocoagulation insulator 304 has a column shape, which is also called an insulation column.
  • the electrocoagulation insulating member 304 may also have a tower shape or the like.
  • the electrocoagulation insulator 304 is mainly anti-pollution and anti-leakage.
  • both the first electrode 301 and the second electrode 302 are mesh-shaped, and both are between the electrocoagulation inlet 3031 and the electrocoagulation outlet 3032.
  • the first electrode 301 has a negative potential
  • the second electrode 302 has a positive potential.
  • the electrocoagulation housing 303 and the second electrode 302 have the same electric potential, and the electrocoagulation housing 303 also has an adsorption effect on the charged substances.
  • an electrocoagulation flow channel 3036 is provided in the electrocoagulation housing, the first electrode 301 and the second electrode 302 are both installed in the electrocoagulation flow channel 3036, and the cross-sectional area of the first electrode 301 and the electrocoagulation flow channel 3036
  • the cross-sectional area ratio is 99% -10%, or 90-10%, or 80-20%, or 70-30%, or 60-40%, or 50%.
  • the electrocoagulation device in this embodiment can also be used to treat industrial tail gas containing acid mist.
  • the electrocoagulation inlet 3031 is connected to the port for discharging industrial tail gas. As shown in FIG.
  • the working principle of the electrocoagulation device in this embodiment is as follows: industrial exhaust gas flows into the electrocoagulation shell 303 from the electrocoagulation inlet 3031 and flows out through the electrocoagulation outlet 3032; in this process, the industrial exhaust gas will flow through The first electrode 301, when the acid mist in the industrial exhaust gas contacts the first electrode 301, or when the distance from the first electrode 301 reaches a certain value, the first electrode 301 transmits electrons to the acid mist, the acid mist is charged, and the second The electrode 302 exerts an attractive force on the charged acid mist, and the acid mist moves toward the second electrode 302 and attaches to the second electrode 302.
  • the acid mist has the characteristics of easy charging and loss of electricity, a charged mist droplet
  • the second electrode 302 will lose power during the movement. At this time, other charged droplets will quickly transfer electrons to the lost droplets. This repeats, the droplets are continuously charged, and the second electrode 302 can continue to give
  • the mist droplets apply an adsorption force and cause the droplets to adhere to the second electrode 302, thereby achieving the removal of acid mist from industrial exhaust gas, preventing the acid mist from being directly discharged into the atmosphere and causing pollution to the atmosphere.
  • the first electrode 301 and the second electrode 302 constitute an adsorption unit.
  • the electrocoagulation device in this embodiment can remove 80% of the acid mist in the industrial exhaust gas, which greatly reduces the discharge of acid mist and has a significant environmental protection effect.
  • the three first connection parts 3011 are provided on the first electrode 301, and the three front connection parts 3011 pass three electrocoagulation insulators 304 and 3 on the inner wall of the electrocoagulation case 303, respectively.
  • the connecting parts are fixedly connected.
  • This connection form can effectively enhance the connection strength between the first electrode 301 and the electrocoagulation case 303.
  • the front connecting portion 3011 has a cylindrical shape. In other embodiments, the front connecting portion 3011 may also have a tower shape.
  • the electrocoagulation insulator 304 is cylindrical, and in other embodiments, the electrocoagulation insulator 304 may also be tower-shaped.
  • the rear connection portion is cylindrical, and in other embodiments, the electrocoagulation insulator 304 may also be tower-shaped.
  • the electrocoagulation housing 303 includes a first housing portion 3033, a second housing portion 3034, and a third housing portion that are sequentially distributed from the electrocoagulation inlet 3031 to the electrocoagulation outlet 3032 3035.
  • the electrocoagulation inlet 3031 is located at one end of the first housing portion 3033, and the electrocoagulation outlet 3032 is located at one end of the third housing portion 3035.
  • the outline size of the first housing portion 3033 gradually increases from the direction of the electrocoagulation inlet 3031 to the electrocoagulation outlet 3032, and the outline size of the third housing portion 3035 gradually decreases from the direction of the electrocoagulation inlet 3031 to the electrocoagulation outlet 3032.
  • the cross section of the second housing portion 3034 is rectangular.
  • the electro-coagulation housing 303 adopts the above structural design, so that the exhaust gas reaches a certain inlet flow rate at the electro-coagulation inlet 3031, and more mainly can make the air flow distribution more uniform, thereby making the medium in the exhaust gas, such as mist droplets, easier to The first electrode 301 is charged by the excitation.
  • the coagulation shell 303 is more convenient to encapsulate, reduces the amount of materials, and saves space. It can be connected by pipes, and it is also considered for insulation. Any electrocoagulation casing 303 that can achieve the above-mentioned effects is acceptable.
  • the electrocoagulation inlet 3031 and the electrocoagulation outlet 3032 are both circular.
  • the electrocoagulation inlet 3031 may also be called an air inlet, and the electrocoagulation outlet 3032 may also be called an air inlet.
  • the diameter of the electrocoagulation inlet 3031 is 300 mm to 1000 mm, specifically 500 mm. Meanwhile, in this embodiment, the diameter of the electrocoagulation inlet 3031 is 300 mm to 1000 mm, specifically 500 mm.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the electrocoagulation device in this embodiment further includes an electrocoagulation housing 303 having an electrocoagulation inlet 3031 and an electrocoagulation outlet 3032, and the first electrode 301 and the second electrode 302 are both installed in the electrocoagulation housing 303.
  • the first electrode 301 is fixedly connected to the inner wall of the electrocoagulation case 303 through the electrocoagulation insulator 304, and the second electrode 302 is directly fixed to the electrocoagulation case 303.
  • the electrocoagulation insulator 304 has a column shape, which is also called an insulation column.
  • the first electrode 301 has a negative potential
  • the second electrode 302 has a positive potential.
  • the electrocoagulation housing 303 and the second electrode 302 have the same electric potential, and the electrocoagulation housing 303 also has an adsorption effect on the charged substances.
  • the electrocoagulation device in this embodiment can also be used to treat industrial tail gas containing acid mist.
  • the electrocoagulation inlet 3031 may be connected to a port for discharging industrial exhaust gas.
  • the working principle of the electrocoagulation device in this embodiment is as follows: the industrial exhaust gas flows into the electrocoagulation shell 303 from the electrocoagulation inlet 3031, and flows out through the electrocoagulation outlet 3032; in this process, the industrial exhaust gas will flow first Via one of the first electrodes 301, when the acid mist in the industrial exhaust 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.
  • the acid mist is charged, and the second electrode 302 exerts an attractive force on the charged acid mist.
  • 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, The part of the acid mist continues to flow toward the electrocoagulation outlet 3032.
  • the electrocoagulation shell 303 applies an adsorption force to this part of the charged acid mist, so that this part of the charged acid mist adheres to the inner wall of the electrocoagulation shell 303, thereby greatly reducing the discharge of acid mist in industrial exhaust gas, and this embodiment
  • the processing device can go 90% of industrial exhaust gas mist, the mist removal effect is very significant.
  • the electrocoagulation inlet 3031 and the electrocoagulation outlet 3032 are both circular.
  • the electrocoagulation inlet 3031 may also be called an air inlet, and the electrocoagulation outlet 3032 may also be called an air inlet.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 has a needle shape, and the first electrode 301 has a negative potential.
  • the second electrode 302 is planar, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the second electrode 302 is specifically planar, and the first electrode 301 is perpendicular to the second electrode 302. In this embodiment, a linear electric field is formed between the first electrode 301 and the second electrode 302.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to nitric acid-containing water mist; 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 water mist.
  • the first electrode 301 is linear, and the first electrode 301 has a negative potential.
  • the second electrode 302 is planar, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the second electrode 302 is specifically planar, and the first electrode 301 is parallel to the second electrode 302. In this embodiment, a linear electric field is formed between the first electrode 301 and the second electrode 302.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 has a mesh shape, and the first electrode 301 has a negative potential.
  • the second electrode 302 is planar, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the second electrode 302 is specifically planar, and the first electrode 301 is parallel to the second electrode 302.
  • a mesh electric field is formed between the first electrode 301 and the second electrode 302.
  • the first electrode 301 is a mesh structure made of wire, and the first electrode 301 is composed of a wire mesh.
  • the area of the second electrode 302 is larger than the area of the first electrode 301.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 has a dot shape, and the first electrode 301 has a negative potential.
  • the second electrode 302 has a barrel shape, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the first electrode 301 is fixed by a metal wire or a metal needle.
  • the first electrode 301 is located at the geometrically symmetric center of the barrel-shaped second electrode 302. In this embodiment, a spot barrel electric field is formed between the first electrode 301 and the second electrode 302.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 is linear, and the first electrode 301 has a negative potential.
  • the second electrode 302 has a barrel shape, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the first electrode 301 is fixed by a metal wire or a metal needle.
  • the first electrode 301 is located on the geometric symmetry axis of the barrel-shaped second electrode 302.
  • a wire barrel electric field is formed between the first electrode 301 and the second electrode 302.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 has a mesh shape, and the first electrode 301 has a negative potential.
  • the second electrode 302 has a barrel shape, and the second electrode 302 has a positive potential.
  • the second electrode 302 is also called a collector.
  • the first electrode 301 is fixed by a metal wire or a metal needle.
  • the first electrode 301 is located at the geometrically symmetric center of the barrel-shaped second electrode 302. In this embodiment, a net barrel electrocoagulation electric field is formed between the first electrode 301 and the second electrode 302.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode 301 can conduct electrons to the nitric acid-containing water mist; when the electrons are conducted to the nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode 302 can apply attractive force to the charged water mist.
  • the first electrode 301 is located between the two second electrodes 302.
  • the length of the first electrode 301 in the left-right direction is greater than the length of the second electrode 302 in the left-right direction.
  • the left end of the first electrode 301 is located to the left of the second electrode 302.
  • the left end of the first electrode 301 and the left end of the second electrode 302 form a power line extending diagonally.
  • an asymmetric electrocoagulation electric field is formed between the first electrode 301 and the second electrode 302.
  • water mist low specific resistance substance
  • mist droplets enters between the two second electrodes 302 from the left. After a part of the droplets are charged, the left end of the first electrode 301 moves diagonally toward the left end of the second electrode 302, thereby forming a pulling action on the droplets.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode can conduct electrons to nitric acid-containing water mist; when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode can exert an attractive force on the charged water mist.
  • the first electrode and the second electrode constitute an adsorption unit 3010.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode can conduct electrons to nitric acid-containing water mist; when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode can exert an attractive force on the charged water mist.
  • the first electrode and the second electrode constitute an adsorption unit 3010.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode can conduct electrons to nitric acid-containing water mist; when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode can exert an attractive force on the charged water mist.
  • the first electrode and the second electrode constitute an adsorption unit 3010.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode can conduct electrons to nitric acid-containing water mist; when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode can exert an attractive force on the charged water mist.
  • the first electrode and the second electrode constitute an adsorption unit 3010.
  • this embodiment provides an electrocoagulation device, including:
  • the first electrode can conduct electrons to nitric acid-containing water mist; when electrons are conducted to nitric acid-containing water mist, the nitric acid-containing water mist is charged;
  • the second electrode can exert an attractive force on the charged water mist.
  • the first electrode and the second electrode constitute an adsorption unit 3010.
  • the present invention effectively overcomes various shortcomings in the prior art and has high industrial utilization value.

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Abstract

提供一种发动机尾气臭氧净化系统和方法。发动机尾气臭氧净化系统包括反应场（202），用于将臭氧流股与尾气流股混合反应，不需添加大量尿素，且净化效果佳。

Description

一种发动机尾气臭氧净化系统和方法 技术领域
本发明属于环保领域，涉及一种发动机尾气臭氧净化系统和方法。
背景技术
发动机对环境的污染主要来自发动机的排气产物即发动机尾气，目前对于柴油机尾气净化，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，现有技术对发动机尾气的净化需添加大量尿素，且净化效果一般。
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发动机尾气臭氧净化系统和方法，用于解决现有技术尾气净化需加大量尿素且净化尾气效果一般中至少一个问题。本发明研究发现臭氧和尾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，而且尾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，用臭氧来处理发动机尾气使得臭氧除NO X效果更好，具有预料不到的技术效果。
本发明提供一种发动机尾气臭氧净化系统及方法，所述发动机尾气臭氧净化系统包括反应场，用于将臭氧流股与尾气流股混合反应，不需添加大量尿素，且净化效果佳。
为实现上述目的及其他相关目的，本发明提供以下示例：
1.本发明提供的示例1：一种发动机尾气臭氧净化系统。
2.本发明提供的示例2：包括上述示例1，其中，所述发动机尾气臭氧净化系统包括反应场，用于将臭氧流股与尾气流股混合反应。
3.本发明提供的示例3：包括上述示例2，其中，所述反应场包括管道。
4.本发明提供的示例4：包括上述示例2或3，其中，所述反应场包括反应器。
5.本发明提供的示例5：包括上述示例4，其中，所述反应器具有反应腔室，尾气与臭氧在所述反应腔室混合并反应。
6.本发明提供的示例6：包括上述示例4或5，其中，所述反应器包括若干蜂窝状腔体， 用于提供尾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，控制尾气与臭氧的反应温度。
7.本发明提供的示例7：包括上述示例4至6中的任一项，其中，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。
8.本发明提供的示例8：包括上述示例4至7中的任一项，其中，所述反应器包括催化剂单元，所述催化剂单元用于促进尾气的氧化反应。
9.本发明提供的示例9：包括上述示例2至8中的任一项，其中，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。
10.本发明提供的示例10：包括上述示例2至9中的任一项，其中，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尾气进行接触，臭氧进口的设置形成如下方向中至少一种：与尾气流动的方向相反、与尾气流动的方向垂直、与尾气流动的方向相切、插入尾气流动方向、多个方向与尾气进行接触。
11.本发明提供的示例11：包括上述示例2至10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。
12.本发明提供的示例12：包括上述示例2至11中的任一项，其中，所述反应场的温度为-50-200℃。
13.本发明提供的示例13：包括上述示例12，其中，所述反应场的温度为60-70℃。
14.本发明提供的示例14：包括上述示例1至13中的任一项，其中，所述尾气臭氧净化系统还包括臭氧源，用于提供臭氧流股。
15.本发明提供的示例15：包括上述示例14，其中，所述臭氧源包括存储臭氧单元和/或臭氧发生器。
16.本发明提供的示例16：包括上述示例15，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。
17.本发明提供的示例17：包括上述示例15，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。
18.本发明提供的示例18：包括上述示例17，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。
19.本发明提供的示例19：包括上述示例18，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。
20.本发明提供的示例20：包括上述示例18，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％。
21.本发明提供的示例21：包括上述示例17至20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。
22.本发明提供的示例22：包括上述示例21，其中，所述碱土金属元素选自镁、锶和钙中的至少一种。
23.本发明提供的示例23：包括上述示例21，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。
24.本发明提供的示例24：包括上述示例21，其中，所述第四主族金属元素为锡。
25.本发明提供的示例25：包括上述示例21，其中，所述贵金属元素选自铂、铑、钯、金、银和铱中的至少一种。
26.本发明提供的示例26：包括上述示例21，其中，所述镧系稀土元素选自镧、铈、镨和钐中的至少一种。
27.本发明提供的示例27：包括上述示例21，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。
28.本发明提供的示例28：包括上述示例21，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。
29.本发明提供的示例29：包括上述示例21，其中，所述层状材料选自石墨烯和石墨中的至少一种。
30.本发明提供的示例30：包括上述示例1至29中的任一项，其中，所述尾气臭氧净化 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尾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。
31.本发明提供的示例31：包括上述示例30，其中，所述控制单元根据臭氧处理前尾气组分含量控制混合反应所需臭氧量。
32.本发明提供的示例32：包括上述示例30或31，其中，所述臭氧量控制装置还包括臭氧处理前尾气组分检测单元，用于检测臭氧处理前尾气组分含量。
33.本发明提供的示例33：包括上述示例32中，其中，所述臭氧处理前尾气组分检测单元包括第一氮氧化物检测单元，用于检测臭氧处理前尾气中氮氧化物含量。
34.本发明提供的示例34：包括上述示例32或33，其中，所述臭氧处理前尾气组分检测单元包括第一CO检测单元，用于检测臭氧处理前尾气中CO含量。
35.本发明提供的示例35：包括上述示例32至34中的任一项，其中，所述臭氧处理前尾气组分检测单元包括第一挥发性有机化合物检测单元，用于检测臭氧处理前尾气中挥发性有机化合物含量。
36.本发明提供的示例36：包括上述示例33至35中的任一项，其中，所述控制单元根据至少一个所述臭氧处理前尾气组分检测单元的输出值控制混合反应所需臭氧量。
37.本发明提供的示例37：包括上述示例30至36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。
38.本发明提供的示例38：包括上述示例30至37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。
39.本发明提供的示例39：包括上述示例38中的任一项，其中，所述理论估计值为：臭氧通入量与尾气中待处理物的摩尔比为2-10。
40.本发明提供的示例40：包括上述示例30至39中的任一项，其中，所述控制单元根据所述臭氧处理后尾气组分含量控制混合反应所需臭氧量。
41.本发明提供的示例41：包括上述示例30至40中的任一项，其中，所述臭氧量控制装置包括臭氧处理后尾气组分检测单元，用于检测臭氧处理后尾气组分含量。
42.本发明提供的示例42：包括上述示例41，其中，所述臭氧处理后尾气组分检测单元包括第一臭氧检测单元，用于检测臭氧处理后尾气中臭氧含量。
43.本发明提供的示例43：包括上述示例41或42，其中，所述臭氧处理后尾气组分检测单元包括第二氮氧化物检测单元，用于检测臭氧处理后尾气中氮氧化物含量。
44.本发明提供的示例44：包括上述示例41至43中的任一项，其中，所述臭氧处理后尾 气组分检测单元包括第二CO检测单元，用于检测臭氧处理后尾气中CO含量。
45.本发明提供的示例45：包括上述示例41至44中的任一项，其中，所述臭氧处理后尾气组分检测单元包括第二挥发性有机化合物检测单元，用于检测臭氧处理后尾气中挥发性有机化合物含量。
46.本发明提供的示例46：包括上述示例42至45中的任一项，其中，所述控制单元根据至少一个所述臭氧处理后尾气组分检测单元的输出值控制臭氧量。
47.本发明提供的示例47：包括上述示例1至46中的任一项，其中，所述尾气臭氧净化系统还包括脱硝装置，用于脱除臭氧流股与尾气流股混合反应产物中的硝酸。
48.本发明提供的示例48：包括上述示例47，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。
49.本发明提供的示例49：包括上述示例48，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。
50.本发明提供的示例50：包括上述示例48或49，其中，所述第一电极为固态金属、石墨、或304钢。
51.本发明提供的示例51：包括上述示例48至50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。
52.本发明提供的示例52：包括上述示例48至51中的任一项，其中，所述第一电极上设有前通孔。
53.本发明提供的示例53：包括上述示例52，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。
54.本发明提供的示例54：包括上述示例52或53，其中，所述前通孔的孔径为0.1-3毫米。
55.本发明提供的示例55：包括上述示例48至54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。
56.本发明提供的示例56：包括上述示例48至55中的任一项，其中，所述第二电极上设有后通孔。
57.本发明提供的示例57：包括上述示例56，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。
58.本发明提供的示例58：包括上述示例56或57，其中，所述后通孔的孔径为0.1-3毫米。
59.本发明提供的示例59：包括上述示例48至58中的任一项，其中，所述第二电极由导电物质制成。
60.本发明提供的示例60：包括上述示例48至59中的任一项，其中，所述第二电极的表面具有导电物质。
61.本发明提供的示例61：包括上述示例48至60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。
62.本发明提供的示例62：包括上述示例48至61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。
63.本发明提供的示例63：包括上述示例48至62中的任一项，其中，所述第一电极垂直于第二电极。
64.本发明提供的示例64：包括上述示例48至63中的任一项，其中，所述第一电极与第二电极相平行。
65.本发明提供的示例65：包括上述示例48至64中的任一项，其中，所述第一电极呈曲线状或圆弧状。
66.本发明提供的示例66：包括上述示例48至65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。
67.本发明提供的示例67：包括上述示例48至66中的任一项，其中，所述第一电极采用金属丝网。
68.本发明提供的示例68：包括上述示例48至67中的任一项，其中，所述第一电极呈平面状或球面状。
69.本发明提供的示例69：包括上述示例48至68中的任一项，其中，所述第二电极呈曲面状或球面状。
70.本发明提供的示例70：包括上述示例48至69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。
71.本发明提供的示例71：包括上述示例48至70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。
72.本发明提供的示例72：包括上述示例48至71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
73.本发明提供的示例73：包括上述示例71或72，其中，所述电源的电压为5-50KV。
74.本发明提供的示例74：包括上述示例71至73中的任一项，其中，所述电源的电压小于起始起晕电压。
75.本发明提供的示例75：包括上述示例71至74中的任一项，其中，所述电源的电压为0.1kv-2kv/mm。
76.本发明提供的示例76：包括上述示例71至75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。
77.本发明提供的示例77：包括上述示例71至76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。
78.本发明提供的示例78：包括上述示例48至77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。
79.本发明提供的示例79：包括上述示例48至78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。
80.本发明提供的示例80：包括上述示例48至79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。
81.本发明提供的示例81：包括上述示例48至80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。
82.本发明提供的示例82：包括上述示例81，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。
83.本发明提供的示例83：包括上述示例48至82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。
84.本发明提供的示例84：包括上述示例83，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。
85.本发明提供的示例85：包括上述示例83或84，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。
86.本发明提供的示例86：包括上述示例83至85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。
87.本发明提供的示例87：包括上述示例86，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。
88.本发明提供的示例88：包括上述示例86或87，其中，所述第一壳体部呈直管状。
89.本发明提供的示例89：包括上述示例86至88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。
90.本发明提供的示例90：包括上述示例86至89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。
91.本发明提供的示例91：包括上述示例86至90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。
92.本发明提供的示例92：包括上述示例83至91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。
93.本发明提供的示例93：包括上述示例48至92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。
94.本发明提供的示例94：包括上述示例93，其中，所述电凝绝缘件的材质为绝缘云母。
95.本发明提供的示例95：包括上述示例93或94，其中，所述电凝绝缘件呈柱状、或塔状。
96.本发明提供的示例96：包括上述示例48至95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。
97.本发明提供的示例97：包括上述示例48至96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。
98.本发明提供的示例98：包括上述示例48至97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％。
99.本发明提供的示例99：包括上述示例47至98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尾气进行冷凝，实现气液分离。
100.本发明提供的示例100：包括上述示例47至99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尾气进行淋洗。
101.本发明提供的示例101：包括上述示例100，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。
102.本发明提供的示例102：包括上述示例101，其中，所述淋洗液单元中淋洗液包括水和/或碱。
103.本发明提供的示例103：包括上述示例47至102中的任一项，其中，所述脱硝装置还包括脱硝液收集单元，用于存储尾气中脱除的硝酸水溶液和/或硝酸盐水溶液。
104.本发明提供的示例104：包括上述示例103，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。
105.本发明提供的示例105：包括上述示例1至104中的任一项，其中，所述尾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尾气中的臭氧。
106.本发明提供的示例106：包括上述示例105，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。
107.本发明提供的示例107：包括上述示例1至106中的任一项，其中，所述尾气臭氧净化系统还包括第一脱硝装置，用于脱除尾气中氮氧化物；所述反应场用于将经所述第一脱硝装置处理后的尾气与臭氧流股混合反应，或者，用于将尾气在经所述第一脱硝装置处理前先与臭氧流股混合反应。
108.本发明提供的示例108：包括上述示例107，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。
109.本发明提供的示例109：包括上述示例1至108中的任一项，其中，还包括发动机。
110.本发明提供的示例110：一种尾气臭氧净化方法，包括如下步骤：将臭氧流股与尾气流股混合反应。
111.本发明提供的示例111：包括示例110所述的尾气臭氧净化方法，其中，所述尾气流股包括氮氧化物和挥发性有机化合物。
112.本发明提供的示例112：包括示例110或111所述的尾气臭氧净化方法，其中，于尾气的低温段，臭氧流股与尾气流股的混合反应。
113.本发明提供的示例113：包括示例110至112任一项所述的尾气臭氧净化方法，其中，臭氧流股与尾气流股混合反应温度为-50～200℃。
114.本发明提供的示例114：包括示例113所述的尾气臭氧净化方法，其中，臭氧流股与 尾气流股混合反应温度为60～70℃。
115.本发明提供的示例115：包括示例110至114任一项所述的尾气臭氧净化方法，其中，臭氧流股与尾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。
116.本发明提供的示例116：包括示例115所述的尾气臭氧净化方法，其中，当臭氧流股与尾气流股的混合方式为正压混合时，臭氧进气的压力大于尾气的压力。
117.本发明提供的示例117：包括示例110所述的尾气臭氧净化方法，其中，在臭氧流股与尾气流股混合反应前，提高尾气流股流速，采用文丘里原理混入臭氧流股。
118.本发明提供的示例118：包括示例110所述的尾气臭氧净化方法，其中，臭氧流股与尾气流股混合方式选自尾气出口逆流通入、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、尾气管道内发生混入、吸附装置外置混入和凝露装置前后混入中至少一种。
119.本发明提供的示例119：包括示例110所述的尾气臭氧净化方法，其中，臭氧流股与尾气流股混合反应的反应场包括管道和/或反应器。
120.本发明提供的示例120：包括示例110至119任一项所述的尾气臭氧净化方法，其中，所述反应场包括排气管、蓄热体装置或催化器。
121.本发明提供的示例121：包括示例120所述的尾气臭氧净化方法尾气臭氧净化方法，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，尾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，用于提供尾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，控制尾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尾气的氧化反应；
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尾气进行接触，臭氧进口的设置形成如下方向中至少一种：与尾气流动的方向相反、与尾气流动的方向垂直、 与尾气流动的方向相切、插入尾气流动方向、多个方向与尾气进行接触。
122.本发明提供的示例122：包括示例110至121任一项所述的尾气臭氧净化方法，其中，所述臭氧流股由存储臭氧单元和/或臭氧发生器提供。
123.本发明提供的示例123：包括示例122所述的尾气臭氧净化方法，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。
124.本发明提供的示例124：包括示例122所述的尾气臭氧净化方法，其中，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。
125.本发明提供的示例125：包括示例124所述的尾气臭氧净化方法，其中，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负载于阻挡介质层的表面上。
126.本发明提供的示例126：包括示例124所述的尾气臭氧净化方法，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的负载量包括阻挡介质层的1～10wt％。
127.本发明提供的示例127：包括示例124至126任一项所述的尾气臭氧净化方法，其中，所述氧化催化键裂解选择性催化剂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。
128.本发明提供的示例128：包括示例127所述的尾气臭氧净化方法，其中，所述碱土金属元素选自镁、锶和钙中的至少一种。
129.本发明提供的示例129：包括示例127所述的尾气臭氧净化方法，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。
130.本发明提供的示例130：包括示例127所述的尾气臭氧净化方法，其中，所述第四主族金属元素为锡。
131.本发明提供的示例131：包括示例127所述的尾气臭氧净化方法，其中，所述贵金属元素选自铂、铑、钯、金、银和铱中的至少一种。
132.本发明提供的示例132：包括示例127所述的尾气臭氧净化方法，其中，所述镧系稀土元素选自镧、铈、镨和钐中的至少一种。
133.本发明提供的示例133：包括示例127所述的尾气臭氧净化方法，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。
134.本发明提供的示例134：包括示例127所述的尾气臭氧净化方法，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。
135.本发明提供的示例135：包括示例127所述的尾气臭氧净化方法，其中，所述层状材料选自石墨烯和石墨中的至少一种。
136.本发明提供的示例136：包括示例124至126任一项所述的尾气臭氧净化方法，其中，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。
137.本发明提供的示例137：包括示例136所述的尾气臭氧净化方法，其中，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。
138.本发明提供的示例138：包括示例136所述的尾气臭氧净化方法，其中，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。
139.本发明提供的示例139：包括示例110至138任一项所述的尾气臭氧净化方法，其中，包括：控制臭氧流股的臭氧量以致有效氧化尾气中待处理的气体组分。
140.本发明提供的示例140：包括示例110至139任一项所述的尾气臭氧净化方法，其中，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％。
141.本发明提供的示例141：包括示例139或140所述的尾气臭氧净化方法，其中，包括：检测臭氧处理前尾气组分含量。
142.本发明提供的示例142：包括示例139至141任一项所述的尾气臭氧净化方法，其中，根据所述臭氧处理前尾气组分含量控制混合反应所需臭氧量。
143.本发明提供的示例143：包括示例141或142所述的尾气臭氧净化方法，其中，检测臭氧处理前尾气组分含量选自以下至少一个：
检测臭氧处理前尾气中挥发性有机化合物含量；
检测臭氧处理前尾气中CO含量；
检测臭氧处理前尾气中氮氧化物含量。
144.本发明提供的示例144：包括示例143所述的尾气臭氧净化方法，其中，根据至少一个检测臭氧处理前尾气组分含量的输出值控制混合反应所需臭氧量。
145.本发明提供的示例145：包括示例139至144任一项所述的尾气臭氧净化方法，其中，按照预设的数学模型控制混合反应所需臭氧量。
146.本发明提供的示例146：包括示例139至145任一项所述的尾气臭氧净化方法，其中，按照理论估计值控制混合反应所需臭氧量。
147.本发明提供的示例147：包括示例146所述的于尾气臭氧净化方法，其中，所述理论 估计值为：臭氧通入量与尾气中待处理物的摩尔比为2～10。
148.本发明提供的示例148：包括示例139至147任一项所述的尾气臭氧净化方法，其中，包括：检测臭氧处理后尾气组分含量。
149.本发明提供的示例149：包括示例139至148任一项所述的尾气臭氧净化方法，其中，根据所述臭氧处理后尾气组分含量控制混合反应所需臭氧量。
150.本发明提供的示例150：包括示例148或149所述的尾气臭氧净化方法，其中，检测臭氧处理后尾气组分含量选自以下至少一个：
检测臭氧处理后尾气中臭氧含量；
检测臭氧处理后尾气中挥发性有机化合物含量；
检测臭氧处理后尾气中CO含量；
检测臭氧处理后尾气中氮氧化物含量。
151.本发明提供的示例151：包括示例150所述的尾气臭氧净化方法，其中，根据至少一个检测臭氧处理后尾气组分含量的输出值控制臭氧量。
152.本发明提供的示例152：包括示例110至151任一项所述的尾气臭氧净化方法，其中，所述尾气臭氧净化方法还包括如下步骤：脱除臭氧流股与尾气流股混合反应产物中的硝酸。
153.本发明提供的示例153：包括示例152所述的尾气臭氧净化方法，其中，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。
154.本发明提供的示例154：包括示例153所述尾气臭氧净化方法，其中，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。
155.本发明提供的示例155：包括示例153或154所述尾气臭氧净化方法，其中，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。
156.本发明提供的示例156：包括示例153-155任一项所述尾气臭氧净化方法，其中，第一电极通过与硝酸雾接触的方式使硝酸雾带电。
157.本发明提供的示例157：包括示例153-156任一项所述尾气臭氧净化方法，其中，第一电极通过能量波动的方式使硝酸雾带电。
158.本发明提供的示例158：包括示例153-157任一项所述尾气臭氧净化方法，其中，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。
159.本发明提供的示例159：包括示例158所述尾气臭氧净化方法，其中，第二电极上的 水滴在重力作用下流入收集槽。
160.本发明提供的示例160：包括示例158或159所述尾气臭氧净化方法，其中，气体流动时，将吹动水滴流入收集槽中。
161.本发明提供的示例161：包括示例153-160任一项所述尾气臭氧净化方法，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。
162.本发明提供的示例162：包括示例153-161任一项所述尾气臭氧净化方法，其中，所述第一电极为固态金属、石墨、或304钢。
163.本发明提供的示例163：包括示例153-162任一项所述尾气臭氧净化方法，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。
164.本发明提供的示例164：包括示例153-163任一项所述尾气臭氧净化方法，其中，所述第一电极上设有前通孔。
165.本发明提供的示例165：包括示例164所述尾气臭氧净化方法，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。
166.本发明提供的示例166：包括示例164或165所述尾气臭氧净化方法，其中，所述前通孔的孔径为0.1-3毫米。
167.本发明提供的示例167：包括示例153-166中任一项所述尾气臭氧净化方法，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。
168.本发明提供的示例168：包括示例153至167任一项所述尾气臭氧净化方法，其中，所述第二电极上设有后通孔。
169.本发明提供的示例169：包括示例168所述尾气臭氧净化方法，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。
170.本发明提供的示例170：包括示例168或169所述尾气臭氧净化方法，其中，所述后通孔的孔径为0.1-3毫米。
171.本发明提供的示例171：包括示例153至170任一项所述尾气臭氧净化方法，其中，所述第二电极由导电物质制成。
172.本发明提供的示例172：包括示例153至171任一项所述尾气臭氧净化方法，其中，所述第二电极的表面具有导电物质。
173.本发明提供的示例173：包括示例153至172任一项所述尾气臭氧净化方法，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。
174.本发明提供的示例174：包括示例153至173任一项所述尾气臭氧净化方法，其中，所述第一电极呈线状，所述第二电极呈面状。
175.本发明提供的示例175：包括示例153至174任一项所述尾气臭氧净化方法，其中，所述第一电极垂直于第二电极。
176.本发明提供的示例176：包括示例153至175任一项所述尾气臭氧净化方法，其中，所述第一电极与第二电极相平行。
177.本发明提供的示例177：包括示例153至176任一项所述尾气臭氧净化方法，其中，所述第一电极呈曲线状或圆弧状。
178.本发明提供的示例178：包括示例153至177任一项所述尾气臭氧净化方法，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。
179.本发明提供的示例179：包括示例153至178任一项所述尾气臭氧净化方法，其中，所述第一电极采用金属丝网。
180.本发明提供的示例180：包括示例153至179任一项所述尾气臭氧净化方法，其中，所述第一电极呈平面状或球面状。
181.本发明提供的示例181：包括示例153至180任一项所述尾气臭氧净化方法，其中，所述第二电极呈曲面状或球面状。
182.本发明提供的示例182：包括示例153至181任一项所述尾气臭氧净化方法，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。
183.本发明提供的示例183：包括示例153至182任一项所述尾气臭氧净化方法，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。
184.本发明提供的示例184：包括示例153至183任一项所述尾气臭氧净化方法，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。
185.本发明提供的示例185：包括示例183或184所述尾气臭氧净化方法，其中，所述电源的电压为5-50KV。
186.本发明提供的示例186：包括示例183至185任一项所述尾气臭氧净化方法，其中，所述电源的电压小于起始起晕电压。
187.本发明提供的示例187：包括示例183至186任一顶所述尾气臭氧净化方法，其中，所述电源的电压为0.1kv-2kv/mm。
188.本发明提供的示例188：包括示例183至187任一项所述尾气臭氧净化方法，其中，所述电源的电压波形为直流波形、正弦波、或调制波形。
189.本发明提供的示例189：包括示例183至188任一项所述尾气臭氧净化方法，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。
190.本发明提供的示例190：包括示例153至189任一项所述尾气臭氧净化方法，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。
191.本发明提供的示例191：包括示例153至190任一项所述尾气臭氧净化方法，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。
192.本发明提供的示例192：包括示例153至191任一项所述尾气臭氧净化方法，其中，所述第一电极和第二电极之间的距离为5-50毫米。
193.本发明提供的示例193：包括示例153至192任一项所述尾气臭氧净化方法，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。
194.本发明提供的示例194：包括示例193所述尾气臭氧净化方法，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。
195.本发明提供的示例195：包括示例153至194任一项所述尾气臭氧净化方法，其中，所述第一电极安装在电凝壳体中，所述电凝壳体具有电凝进口和电凝出口。
196.本发明提供的示例196：包括示例195所述尾气臭氧净化方法，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。
197.本发明提供的示例197：包括示例195或196所述尾气臭氧净化方法，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。
198.本发明提供的示例198：包括示例195至197任一项所述尾气臭氧净化方法，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。
199.本发明提供的示例199：包括示例198所述尾气臭氧净化方法，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。
200.本发明提供的示例200：包括示例198或199所述尾气臭氧净化方法，其中，所述第一壳体部呈直管状。
201.本发明提供的示例201：包括示例198至200任一项所述尾气臭氧净化方法，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。
202.本发明提供的示例202：包括示例198至201任一项所述尾气臭氧净化方法，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。
203.本发明提供的示例203：包括示例198至202任一项所述尾气臭氧净化方法，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。
204.本发明提供的示例204：包括示例195至203任一项所述尾气臭氧净化方法，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。
205.本发明提供的示例205：包括示例153至204任一项所述尾气臭氧净化方法，其中，所述第一电极通过电凝绝缘件与电凝壳体相连接。
206.本发明提供的示例206：包括示例205所述尾气臭氧净化方法，其中，所述电凝绝缘件的材质为绝缘云母。
207.本发明提供的示例207：包括示例205或206所述尾气臭氧净化方法，其中，所述电凝绝缘件呈柱状、或塔状。
208.本发明提供的示例208：包括示例153至207任一项所述尾气臭氧净化方法，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。
209.本发明提供的示例209：包括示例153至208任一项所述尾气臭氧净化方法，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。
210.本发明提供的示例210：包括示例153至209任一项所述尾气臭氧净化方法，其中，所述第一电极位于电凝流道中；带硝酸雾的气体沿电凝流道流动，并流经第一电极；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％。
211.本发明提供的示例211：包括示例152至210任一项所述的尾气臭氧净化方法，其中，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法：将臭氧流股与尾气流股混合反应产物进行冷凝。
212.本发明提供的示例212：包括示例152至211任一项所述的尾气臭氧净化方法，其中，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法：将臭氧流股与尾气流股混合反应产物进行淋洗。
213.本发明提供的示例213：包括示例212所述的尾气臭氧净化方法，其中，脱除臭氧流 股与尾气流股混合反应产物中的硝酸的方法还包括：向臭氧流股与尾气流股混合反应产物提供淋洗液。
214.本发明提供的示例214：包括示例213所述的于尾气臭氧净化方法，其中，所述淋洗液为水和/或碱。
215.本发明提供的示例215：包括示例152至214任一项所述的尾气臭氧净化方法，其中，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法还包括：存储尾气中脱除的硝酸水溶液和/或硝酸盐水溶液。
216.本发明提供的示例216：包括示例215所述的尾气臭氧净化方法，其中，当存储有硝酸水溶液时，加入碱液，与硝酸形成硝酸盐。
217.本发明提供的示例217：包括示例110至216任一项所述的尾气臭氧净化方法，其中，所述尾气臭氧净化方法还包括如下步骤：对脱除硝酸的尾气进行臭氧消解。
218.本发明提供的示例218：包括示例217所述的尾气臭氧净化方法，其中，所述臭氧消解选自紫外线消解和催化消解中的至少一种。
219.本发明提供的示例219：包括示例110至218任一项所述的尾气臭氧净化方法，其中，所述尾气臭氧净化方法还包括如下步骤：第一次脱除尾气中氮氧化物；第一次脱除氮氧化物后的尾气流股与臭氧流股混合反应，或者，在第一次脱除尾气中氮氧化物前先与臭氧流股混合反应。
220.本发明提供的示例220：包括示例219所述的尾气臭氧净化方法，其中，所述第一次脱除尾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。
附图说明
图1为发动机尾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显示为本发明实施例1发动机尾气臭氧净化系统的示意图。
图6显示为本发明实施例1发动机尾气臭氧净化系统中反应场的俯视图。
图7显示为本发明臭氧量控制装置的示意图。
图8为本发明实施例9中电凝装置的结构示意图。
图9为本发明实施例9中电凝装置的左视图。
图10为本发明实施例9中电凝装置的立体图。
图11为本发明实施例10中电凝装置的结构示意图。
图12为本发明实施例10中电凝装置的俯视图。
图13为本发明实施例11中电凝装置的结构示意图。
图14为本发明实施例12中电凝装置的结构示意图。
图15为本发明实施例13中电凝装置的结构示意图。
图16为本发明实施例14中电凝装置的结构示意图。
图17为本发明实施例15中电凝装置的结构示意图。
图18为本发明实施例16中电凝装置的结构示意图。
图19为本发明实施例17中电凝装置的结构示意图。
图20为本发明实施例18中电凝装置的结构示意图。
图21为本发明实施例19中电凝装置的结构示意图。
图22为本发明实施例20中电凝装置的结构示意图。
图23为本发明实施例21中电凝装置的结构示意图。
图24为本发明实施例22中电凝装置的结构示意图。
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。
于本发明一实施例中，所述发动机尾气臭氧净化系统包括反应场，用于将臭氧流股与尾气流股混合反应。例如：处理汽车发动机210的尾气，利用尾气中的水以及尾气管道220，产生氧化反应，将尾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。所述尾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给尾气管道220提供臭氧，如图1所示，图中箭头方向为尾气流动方向。
臭氧流股与尾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尾气通道中。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尾气通道。臭氧流股与尾气流股的摩尔比为2时，VOCs去除率50％；臭氧流股与尾气流股的摩尔比为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％；臭氧流股与尾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尾气通道中。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尾气通道。使用185纳米紫外线臭氧流股与尾气流股的摩尔比为2时，VOCs去除率40％；185纳米紫外线臭氧流股与尾气流股的摩尔比为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尾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尾气流股的摩尔比为2时，VOCs去除率45％；172纳米紫外线臭氧流股与尾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尾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，尾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，用于提供尾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，控制尾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尾气的氧化反应；
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尾气进行接触，臭氧进口的设置形成如下方向中至少一种：与尾气流动的方向相反、与尾气流动的方向垂直、与尾气流动的方向相切、插入尾气流动方向、多个方向与尾气进行接触；所述与尾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；所述与尾气流动的方向垂直，使用文氏效应；与尾气流动的方向相切，便于混合；插入尾气流动方向，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，所述发动机尾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，从而可以与尾气流股混合，使尾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，所述发动机尾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尾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尾气组分检测单元，用于检测臭氧处理前尾气组分含量。
于本发明一实施例中，所述控制单元根据所述臭氧处理前尾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，所述臭氧处理前尾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尾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尾气中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尾气中氮氧化物含量，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尾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尾气组分含量相关，通过上述含量及尾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：臭氧通入量与尾气中待处理物的摩尔比为2～10。例如：13L柴油发动机可控制臭氧通入量为300～500g；2L汽油发动机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尾气组分检测单元，用于检测臭氧处理后尾气组分含量。
于本发明一实施例中，所述控制单元根据所述臭氧处理后尾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，所述臭氧处理后尾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尾气中臭氧含量；
第二挥发性有机化合物检测单元，用于检测臭氧处理后尾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尾气中CO含量；
第二氮氧化物检测单元，用于检测臭氧处理后尾气中氮氧化物含量。
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尾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，所述发动机尾气臭氧净化系统还包括脱硝装置，用于脱除臭氧流股与尾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尾气进行冷凝，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尾气进行淋洗，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，用于存储尾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，所述发动机尾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尾气中的臭氧。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，所述发动机尾气臭氧净化系统还包括第一脱硝装置，用于脱除尾气中氮氧化物；所述反应场用于将经所述第一脱硝装置处理后的尾气与臭氧流股混合反应，或者，用于将尾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发动机尾气中氮氧化物(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尾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：臭氧处理发动机尾气中氮氧化物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，仍然不能从发动机尾气中脱除，即臭氧处理发动机尾气中氮氧化物NO X无效，但是，本申请人却发现臭氧和尾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，硝酸则更容易从发动机尾气中脱除，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发动机尾气中的VOC反应产生足够水和高价氮氧化物反应产生 硝酸。
用臭氧来处理发动机尾气时，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，而且尾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，用臭氧来处理发动机尾气使得臭氧除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。
臭氧处理发动机尾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。
一种尾气臭氧净化方法，包括如下步骤：将臭氧流股与尾气流股混合反应。
于本发明一实施例中，所述尾气流股包括氮氧化物和挥发性有机化合物。所述尾气流股可以是发动机尾气，所述发动机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，更具体可以是如柴油发动机尾气等。所述尾气流股中氮氧化物(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。所述尾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，尾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，于尾气的低温段，臭氧流股与尾气流股的混合反应。
于本发明一实施例中，臭氧流股与尾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，臭氧流股与尾气流股混合反应温度为60～70℃。
于本发明一实施例中，臭氧流股与尾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，当臭氧流股与尾气流股的混合方式为正压混合时，臭氧进气的压力大于尾气的压力。当臭氧流股进气的压力小于尾气流股的排压时，可同时使用文丘里混合方式。
于本发明一实施例中，在臭氧流股与尾气流股混合反应前，提高尾气流股流速，采用文丘里原理混入臭氧流股。
于本发明一实施例中，臭氧流股与尾气流股混合方式选自尾气出口逆流通入、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、尾气管道内发生混入、吸附装置外置混入和凝露装置前后混入中至少一种。可设于发动机尾气的低温段，避免臭氧的消解。
于本发明一实施例中，臭氧流股与尾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，尾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，用于提供尾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，控制尾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尾气的氧化反应；
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尾气进行接触，臭氧进口的设置形成如下方向中至少一种：与尾气流动的方向相反、与尾气流动的方向垂直、与尾气流动的方向相切、插入尾气流动方向、多个方向与尾气进行接触；所述与尾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；所述与尾气流动的方向垂直，使用文 氏效应；与尾气流动的方向相切，便于混合；插入尾气流动方向，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：
3)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；
4)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：
3)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；
4)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尾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：检测臭氧处理前尾气组分含量。
于本发明一实施例中，根据所述臭氧处理前尾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，检测臭氧处理前尾气组分含量选自以下至少一个：
检测臭氧处理前尾气中挥发性有机化合物含量；
检测臭氧处理前尾气中CO含量；
检测臭氧处理前尾气中氮氧化物含量。
于本发明一实施例中，根据至少一个检测臭氧处理前尾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尾气组分含量相关，通过上述含量及尾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：臭氧通入量与尾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 发动机可控制臭氧通入量为300～500g；2L汽油发动机可控制臭氧通入量为5～20g。
于本发明一实施例中，包括：检测臭氧处理后尾气组分含量。
于本发明一实施例中，根据所述臭氧处理后尾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，检测臭氧处理后尾气组分含量选自以下至少一个：
检测臭氧处理后尾气中臭氧含量；
检测臭氧处理后尾气中挥发性有机化合物含量；
检测臭氧处理后尾气中CO含量；
检测臭氧处理后尾气中氮氧化物含量。
于本发明一实施例中，根据至少一个检测臭氧处理后尾气组分含量的输出值控制臭氧量。
于本发明一实施例中，所述尾气臭氧净化方法还包括如下步骤：脱除臭氧流股与尾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，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法：将臭氧流股与尾气流股混合反应产物进行冷凝。
于本发明一实施例中，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法：将臭氧流股与尾气流股混合反应产物进行淋洗。
于本发明一实施例中，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法还包括：向臭氧流股与尾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，脱除臭氧流股与尾气流股混合反应产物中的硝酸的方法还包括：存储尾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，所述尾气臭氧净化方法还包括如下步骤：对脱除硝酸的尾气进行臭氧消解，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，所述尾气臭氧净化方法还包括如下步骤：第一次脱除尾气中氮氧化物；第一次脱除氮氧化物后的尾气流股与臭氧流股混合反应，或者，在第一次脱除尾气中氮氧化物前先与臭氧流股混合反应。
第一次脱除尾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。第一次脱除尾气中氮氧化物后的发动机尾气中氮氧化物(NO x)含量不达标，在第一次脱除尾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，所述第一次脱除尾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。当尾气流经电凝流道中的第一电极时，尾气中含硝酸的水雾、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，从而实现对尾气中硝酸液的去除。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。
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。
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尾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。
实施例1
一种发动机尾气臭氧净化系统，如图5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，用于将臭氧流股与尾气流股混合反应。
脱硝装置203，用于脱除臭氧流股与尾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发动机尾气进行电凝，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尾气中的臭氧。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6所示，内设有若干蜂窝状腔体2021，用于提供尾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，控制尾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11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尾气。本实施例中进口3031与排放工业尾气的口相连通。本实施例中电凝装置的工作原理如下：工业尾气由进口3031流入外壳303，并经出口3032流出；在此过程中，工业尾气将先流经其中一个第一电极301，当工业尾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尾气中酸雾的排放量，且本实施例中处理装置能去除工业尾气中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2
如图7所示，实施例1中发动机尾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尾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还包括臭氧处理前尾气组分检测单元2092，用于检测臭氧处理前尾气组分含量。所述控制单元根据所述臭氧处理前尾气组分含量控制混合反应所需臭氧量。
所述臭氧处理前尾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尾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尾气中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尾气中氮氧化物含量，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尾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：臭氧通入量与尾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尾气组分检测单元2093，用于检测臭氧处理后尾气组分含量。所述控制单元根据所述臭氧处理后尾气组分含量控制混合反应所需臭氧量。
所述臭氧处理后尾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尾气中臭氧含量；
第二挥发性有机化合物检测单元20932，用于检测臭氧处理后尾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尾气中CO含量；
第二氮氧化物检测单元20934，用于检测臭氧处理后尾气中氮氧化物含量。
所述控制单元根据至少一个所述臭氧处理后尾气组分检测单元的输出值控制臭氧量。
实施例3
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4
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CuO0.1g；MnO0.2g)
(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5
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6
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7
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8
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9
如图8至图10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8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尾气。当电凝装置用于处理含有酸雾的工业尾气时，本实施例中电凝进口3031与排放工业尾气的口相连通。如图8所示，本实施例中电凝装置的工作原理如下：工业尾气由电凝进口3031流入电凝壳体303，并经电凝出口3032流出；在此过程中，工业尾气将流经第一电极301，当工业尾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， 从而实现对工业尾气中酸雾的去除，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尾气中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10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9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，使尾气在电凝进口3031处达到一定的入口流速，更主要能使气流分布更加均匀，进而使尾气中的介质、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10
如图11和图12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11和图12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11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尾气。本实施例中电凝进口3031可与排放工业尾气的口相连通。如图11所示，本实施例中电凝装置的工作原理如下：工业尾气由电凝进口3031流入电凝壳体303，并经电凝出口3032流出；在此过程中，工业尾气将先流经其中一个第一电极301，当工业尾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尾气中酸雾的排放量，且本实施例中处理装置能去除工业尾气中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11
如图13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。
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12
如图14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。
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13
如图15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。
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14
如图16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。
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15
如图17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。
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16
如图18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。
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17
如图19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。
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18
如图20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，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19
如图21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，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20
如图22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，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21
如图23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，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22
如图24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，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。
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 (12)

  1. 一种发动机尾气臭氧净化系统，其特征在于，包括臭氧量控制装置，用于控制臭氧量以致有效氧化尾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所述的发动机尾气臭氧净化系统，其特征在于，所述臭氧量控制装置还包括臭氧处理前尾气组分检测单元，用于检测臭氧处理前尾气组分含量。
  3. 根据权利要求2中的任一项所述的发动机尾气臭氧净化系统，其特征在于，所述控制单元根据所述臭氧处理前尾气组分含量控制混合反应所需臭氧量。
  4. 根据权利要求3所述的发动机尾气臭氧净化系统，其特征在于，所述臭氧处理前尾气组分检测单元包括：
    第一挥发性有机化合物检测单元，用于检测臭氧处理前尾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尾气中CO含量；
    第一氮氧化物检测单元，用于检测臭氧处理前尾气中氮氧化物含量。
  5. 根据权利要求4所述的发动机尾气臭氧净化系统，其特征在于，所述控制单元根据至少一个所述臭氧处理前尾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中的任一项所述的发动机尾气臭氧净化系统，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所述的发动机尾气臭氧净化系统，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中的任一项所述的发动机尾气臭氧净化系统，其特征在于，所述理论估计值为：臭氧通入量与尾气中待处理物的摩尔比为2～10。
  9. 根据权利要求1所述的发动机尾气臭氧净化系统，其特征在于，所述臭氧量控制装置包括臭氧处理后尾气组分检测单元，用于检测臭氧处理后尾气组分含量。
  10. 根据权利要求9所述的发动机尾气臭氧净化系统，其特征在于，所述控制单元根据所述臭氧处理后尾气组分含量控制混合反应所需臭氧量。
  11. 根据权利要求10所述的发动机尾气臭氧净化系统，其特征在于，所述臭氧处理后尾气组分检测单元包括：
    第一臭氧检测单元，用于检测臭氧处理后尾气中臭氧含量；
    第二挥发性有机化合物检测单元，用于检测臭氧处理后尾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尾气中CO含量；
    第二氮氧化物检测单元，用于检测臭氧处理后尾气中氮氧化物含量。
  12. 根据权利要求11所述的发动机尾气臭氧净化系统，其特征在于，所述控制单元根据至少一个所述臭氧处理后尾气组分检测单元的输出值控制臭氧量。
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US20210403324A1 (en) 2021-12-30
EP3871757A4 (en) 2022-07-20
WO2020083165A1 (zh) 2020-04-30
JP2022505940A (ja) 2022-01-14
EP3872322A4 (en) 2021-12-22
WO2020083170A1 (zh) 2020-04-30
WO2020083168A1 (zh) 2020-04-30
EP3872319A1 (en) 2021-09-01
WO2020083162A1 (zh) 2020-04-30
JP2022505938A (ja) 2022-01-14
EP3872322A1 (en) 2021-09-01
JP2022512025A (ja) 2022-02-01
WO2020083164A1 (zh) 2020-04-30
US20210402352A1 (en) 2021-12-30
JP2022505944A (ja) 2022-01-14
CN112930433A (zh) 2021-06-08
US20210394196A1 (en) 2021-12-23
WO2020083171A1 (zh) 2020-04-30
EP3871757A1 (en) 2021-09-01
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