WO2012142974A1 - 一种臭氧气浮高级氧化流体处理系统 - Google Patents
一种臭氧气浮高级氧化流体处理系统 Download PDFInfo
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- WO2012142974A1 WO2012142974A1 PCT/CN2012/074525 CN2012074525W WO2012142974A1 WO 2012142974 A1 WO2012142974 A1 WO 2012142974A1 CN 2012074525 W CN2012074525 W CN 2012074525W WO 2012142974 A1 WO2012142974 A1 WO 2012142974A1
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- WIPO (PCT)
- Prior art keywords
- ozone
- ultraviolet radiation
- treatment system
- inflow
- zone
- Prior art date
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 title claims abstract description 154
- 239000012530 fluid Substances 0.000 title claims abstract description 83
- 238000011282 treatment Methods 0.000 title claims abstract description 45
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 16
- 230000003647 oxidation Effects 0.000 title claims abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 84
- 230000005855 radiation Effects 0.000 claims abstract description 67
- 239000002245 particle Substances 0.000 claims abstract description 44
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 33
- 238000005188 flotation Methods 0.000 claims description 81
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 239000007864 aqueous solution Substances 0.000 claims description 33
- 230000001590 oxidative effect Effects 0.000 claims description 26
- 238000007667 floating Methods 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 14
- 239000000126 substance Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 6
- 238000005339 levitation Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 17
- 230000000694 effects Effects 0.000 description 16
- 238000000034 method Methods 0.000 description 10
- -1 hydroxyl radicals Chemical class 0.000 description 7
- 238000005273 aeration Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 235000020188 drinking water Nutrition 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000009360 aquaculture Methods 0.000 description 1
- 244000144974 aquaculture Species 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000003621 irrigation water Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000027756 respiratory electron transport chain Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
Definitions
- the invention relates to an ozone air flotation advanced oxidation fluid processing system, and belongs to the field of fluid processing. Background technique
- the scheme of using 0 3 /UV, 0 3 /H 2 0 2 alone is greatly affected by the solubility of ozone, and the treatment efficiency depends mainly on the solubility of 0 3 in water, while the conventional 0 3 / UV, 0 3 /H 2 0 2
- the method of increasing the solubility of 0 3 in water in the advanced oxidation system is a microporous aeration method, but the ozone bubbles released by the microporous aeration method are microscopic bubbles visible to the naked eye.
- the particle size is about 1mm, the bubble particle size is large, and the rising speed in the water is fast, so that the residence time in the reaction tank is short, and most of the ozone does not react and escapes the reactor. Accordingly, the microporous aeration way that the ozone dosing 0 3 / UV and 0 3 / H 2 0 2 in both systems 03 not sufficiently soluble in water, its solubility is low, so it does not make the added Ozone is fully dissolved and reacts with UV or 02 , and it cannot produce a large amount of hydroxyl radicals, so the utilization of ozone is very low, usually only about 10%.
- the ozone levitation advanced oxidizing fluid treatment system comprising a reaction tank, wherein: the upstream and downstream of the reaction tank are respectively provided with an inflow zone and an outflow zone, The inflow zone and the outflow zone are in communication with the reaction cell, and further comprise an ozone flotation device and a plurality of sets of ultraviolet radiation devices, the ultraviolet radiation device comprising an ultraviolet lamp tube and a ballast device thereof and an electric control system, the ultraviolet radiation device group and The ozone flotation device is installed in the inflow zone, and the air flotation device can atomize the ozone gas in the aqueous solution to form misty particles, fully dissolve in the water, and mix to form a supersaturated high pressure dissolved ozone aqueous solution, and the supersaturated high pressure dissolves.
- the aqueous ozone solution is contacted with the fluid to be treated in the inflow region under the irradiation of ultraviolet rays, and then flows into the reaction tank after the reaction, and continues to fully contact and react with the fluid to be treated, and finally flows out through the outflow region.
- the technical solution of the present invention may also be specifically characterized as follows:
- the optimal processing effect can be achieved by controlling the particle size.
- the bubble particle size can have at least three options:
- the air flotation device may have a particle diameter of 0.2 to 50 ⁇ m.
- the particle diameter of the air flotation device is preferably between 0.2 and 10 ⁇ m.
- the particle size of the air flotation device may be between 10 and 50 ⁇ m.
- the ozone flotation device is disposed at the bottom of the inflow zone.
- the ultraviolet radiation device group is disposed downstream of the ozone air flotation device.
- the ultraviolet lamp is a medium pressure ultraviolet lamp.
- a pilot wall with a closed bottom opening at the top of the UV-radiation device ensures that water flows from the bottom of the diversion wall into the UV-radiation zone.
- a diversion wall with a bottom closed top opening is provided downstream of the UV radiation device group to ensure that water flows from the top of the diversion wall into the reaction cell to extend the radiation path and the radiation time.
- a diversion wall is provided upstream and downstream of the ultraviolet radiation device to ensure that the water flows from the bottom of the upstream diversion wall into the ultraviolet radiation zone and the top of the downstream diversion wall into the reaction cell.
- the ultraviolet radiation device may adopt a modular structure, and each of the ultraviolet lamp modules includes a plurality of ultraviolet lamps.
- a plurality of ozone flotation devices and multi-stage ultraviolet radiation device groups can be arranged in the inflow region along the fluid flow direction according to actual needs.
- the present invention also provides the following scheme 2 and scheme 3:
- An ozone levitation advanced oxidizing fluid treatment system comprises a reaction tank, characterized in that: an upstream and a downstream of the reaction tank are respectively provided with an inflow zone and an outflow zone, and the inflow zone and the outflow zone are connected with the reaction cell,
- the ozone flotation device and the H 2 0 2 adding device are installed, the ozone air floating device is installed at the bottom of the inflow region, and the H 2 0 2 adding device is disposed upstream of the air floating device in the inflow region to be inflow Adding liquid H 2 O 2
- the air flotation device can atomize ozone gas into an atomized solution to form misty particles, fully dissolve in water, and mix with water to form a supersaturated high-pressure dissolved ozone aqueous solution, the supersaturated high-pressure dissolved ozone
- the aqueous solution is sufficiently contacted with the added liquid H 2 O 2 in the inflow zone to generate a large amount of hydroxyl radicals in contact with the
- the optimal processing effect can be achieved by controlling the particle size.
- the bubble particle size can have at least three options:
- the air flotation device may have a bubble particle size of between 0.2 and 50 ⁇ m.
- the particle size of the air flotation device is preferably between 0.2 and 10 ⁇ m.
- the air flotation device may have a bubble particle diameter of between 10 and 50 ⁇ m.
- An ozone levitation advanced oxidizing fluid treatment system comprises a reaction tank, characterized in that: an upstream and a downstream of the reaction tank are respectively provided with an inflow zone and an outflow zone, and the inflow zone and the outflow zone are connected with the reaction cell,
- the utility model comprises an ozone air floating device, an H 2 0 2 adding device and a plurality of ultraviolet radiation devices, wherein the ultraviolet radiation device comprises an ultraviolet lamp tube and a ballast device thereof and an electric control system, and the ozone air floating device is installed at a bottom of the inflow region.
- the H 2 0 2 adding device is disposed upstream of the inflow region to add liquid H 2 O 2 at the time of inflow, and the air flotation device can atomize the ozone gas in the aqueous solution to form misty particles, and fully dissolve in the In the water, mixing forms a supersaturated high-pressure dissolved ozone aqueous solution, and the supersaturated high-pressure dissolved ozone aqueous solution is sufficiently contacted with the added liquid H 2 0 2 in the inflow region under ultraviolet irradiation to generate a large amount of hydroxyl radicals and the fluid to be treated. After contacting and reacting, it flows into the reaction tank to continue to fully contact with the fluid to be treated, reacts to remove harmful substances therein, and finally flows out through the outflow zone.
- the optimal processing effect can be achieved by controlling the particle size.
- the bubble particle size can have at least three options:
- the air flotation device may have a bubble particle size of between 0.2 and 50 ⁇ m.
- the particle size of the air flotation device is preferably between 0.2 and 10 ⁇ m.
- the air flotation device may have a bubble particle diameter of between 10 and 50 ⁇ m.
- the 3 ⁇ 40 2 addition device is placed upstream of the inflow zone, and a liquid 3 ⁇ 40 2 can be added during the inflow of the system to allow the 3 ⁇ 40 2 to fully contact with the highly atomized ultramicrobubble 0 3 to generate more hydroxyl radicals.
- the air flotation device can atomize ozone gas in an aqueous solution to form misty particles, fully dissolve in water, and mix with water to form a supersaturated high-pressure dissolved ozone aqueous solution, and the atomized ultra-fine bubble has a small particle size.
- the long residence time in the water enables most of the ozone to fully contact and react with the fluid to be treated in the inflow zone and the reaction cell to reduce the escape of ozone from the reaction cell.
- the fluid mixed with the misty ozone particles flows from the bottom of the ultraviolet radiation zone and flows into the reaction cell from the top thereof, prolonging the water flow and the ozone particles and the water flow. And the UV contact time, so that the reaction is sufficient.
- the supersaturated high-pressure dissolved ozone aqueous solution is sufficiently contacted and reacted with the fluid to be treated under ultraviolet radiation to oxidize and decompose the pollutant.
- the ozone air flotation advanced oxidizing fluid treatment system of the invention can atomize ozone gas into a misty particle in an aqueous solution, fully dissolve in water, and mix to form a supersaturated high-pressure dissolved ozone aqueous solution, thereby instantaneously releasing a large amount of misty ozone.
- the bubble, the particle size of the mist-like ozone bubble is small, and the average particle diameter is 0. 2-50 um, which greatly increases the chance of reaction with UV or 02 and the contact time, and sufficiently improves the reaction efficiency;
- the high-concentration supersaturated mist-like ozone bubbles do not easily rise in water, so that the residence time in water will be greatly increased, and the small-sized bubbles greatly increase the solubility of ozone, increase the utilization rate of ozone, and greatly reduce The dosage of ozone significantly reduces operating costs;
- the high-concentration supersaturated misty ozone bubbles do not easily rise in water, so that the residence time in the water will be greatly increased, so that the depth of the reaction tank can be greatly reduced, so that the depth of the reaction tank can be reduced by 10 meters. Up to 2 meters, greatly reducing the construction cost and workload of the reaction tank.
- the supersaturated high-pressure dissolved ozone aqueous solution is sufficiently contacted with the added liquid H 2 0 2 in the inflow region to generate a large amount of hydroxyl radicals in contact with the fluid to be treated, and then reacted into the reaction tank to effectively degrade the fluid to be treated. Harmful substances in the middle.
- the COD (chemical oxygen demand) removal rate of the pollutants is about 50% before the air flotation process is used, and the air floatation process using 0 3 is used. After that, the COD removal rate can be increased to about 60%-95%.
- the concentration of COD in the treated wastewater is generally around 400, which does not meet the emission standards.
- the commonly used 0 2 / 0 3 process can only degrade it to about 200. After using the air floatation process of 0 3 , it can be reduced to about 60-80, which is much better than the emission standard (the emission standard is 100).
- Figure 1 is a front elevational view of a first embodiment of the ozone gas floatation advanced oxidation fluid treatment system of the present invention
- Figure 2 is a front elevational view of a second embodiment of the ozone flotation advanced oxidizing fluid treatment system of the present invention
- Figure 3 is a front elevational view of a third embodiment of the ozone flotation advanced oxidizing fluid treatment system of the present invention.
- 1 is the reaction cell
- 2 is the ozone flotation device
- 3 is the ultraviolet radiation device
- 301 is the purple
- 302 is an ultraviolet lamp
- 303 is a power supply and control system of the ultraviolet radiation device
- 4 is an inflow area
- 5 is an outflow area
- Wl, W2 are the upstream and downstream diversion walls of the ultraviolet radiation device
- 6 is the inflow tube
- 7 is the outflow tube
- 8 is the cover plate
- 9 is the 3 ⁇ 40 2 adding device.
- Embodiment 1 is a diagrammatic representation of Embodiment 1:
- the ozone air flotation advanced oxidation fluid processing system shown in this embodiment comprises a reaction cell 1, and further comprises a plurality of ozone air flotation devices 2 and a plurality of groups of ultraviolet radiation devices 3 and their ballast devices and electricity. Control System.
- the upstream and downstream of the reaction cell 1 are respectively provided with an inflow zone 4 and an outflow zone 5, and the inflow zone 4 and the outflow zone 5 are in communication with the reaction cell 1.
- the ultraviolet radiation device group 3 and the ozone air flotation device 2 are installed in the inflow region 4.
- the ozone flotation device is disposed at the bottom of the inflow region 4, and the ozone flotation device is connected to the ozone gas source, which is omitted in the figure of the embodiment.
- the air flotation device 2 can atomize the ozone gas to form a misty particle and thoroughly mix with the fluid to be treated to form a supersaturated high pressure dissolved ozone aqueous solution.
- the ultraviolet radiation device group 3 is disposed downstream of the ozone air floating device 2, and the supersaturated high-pressure dissolved ozone aqueous solution is contacted with the fluid to be treated in the inflow region 4 under the irradiation of the ultraviolet radiation device 3, and flows into the reaction pool after the reaction. 1.
- an ozone flotation device is also provided at the bottom of the radiating ultraviolet radiation region to increase the ozone content in the fluid, and a top closed and bottom open diversion is provided upstream of the ultraviolet radiation device.
- the wall W1 ensures that the water flows from the bottom of the diversion wall W1 into the ultraviolet radiation zone, and a diversion wall W2 which closes the upper opening at the bottom of the ultraviolet radiation device group is provided to ensure that the water flows from the top of the diversion wall into the reaction cell.
- the ozone gas After passing through the air flotation device, the ozone gas will be atomized to form misty particles and mixed with the fluid to be treated to form a supersaturated high-pressure dissolved ozone aqueous solution, which is in the inflow region under ultraviolet irradiation.
- the treatment fluid contacts and flows into the reaction cell 1 after the reaction. Since the high-pressure dissolved ozone remains in the fluid after passing through the ultraviolet radiation device 3, in order to improve the utilization of ozone and improve the treatment effect of the fluid, it is necessary to continue the ozone in the reaction cell 1.
- the fluid to be treated is in full contact, The reaction finally flows out through the outflow zone 5.
- the particle size of the air flotation device is generally controlled to be between 0.2 and 50 ⁇ m, preferably between 0.2 and 10 ⁇ m, or between 10 and 50 ⁇ m.
- the ultraviolet radiation device 3 can adopt a modular structure, and each of the ultraviolet lamp modules 301 includes a plurality of ultraviolet lamps 302.
- the ultraviolet lamp tube in this embodiment is a medium pressure ultraviolet lamp tube.
- a plurality of ozone air flotation devices and a second ultraviolet radiation device group are disposed.
- the multi-stage ultraviolet radiation device group may be arranged along the fluid flow direction in the inflow region according to actual needs, and the diversion walls W1 and W2 are respectively disposed in front of and behind each group of the ultraviolet radiation device to increase the synergistic effect of ozone and ultraviolet rays. And time to improve the reaction.
- the ultraviolet lamp tube 302 is horizontally mounted on the module. In practical applications, the ultraviolet lamp tube 302 can also be vertically mounted on the module.
- Embodiment 2 is a diagrammatic representation of Embodiment 1:
- Flotation ozone advanced oxidation fluid treatment system the present embodiment shown in Figure 2 comprises a reaction tank 1, further comprising a flotation device 2 and a plurality of ozone ⁇ 2 0 2 addition device 9.
- the upstream and downstream of the reaction cell 1 are provided with an inflow zone 4 and an outflow zone 5, respectively, and the inflow zone 4 and the outflow zone 5 are in communication with the reaction cell 1.
- a 3 ⁇ 40 2 adding device is disposed upstream of the inflow zone to add a liquid helium 2 0 2 at the inflow, the ozone flotation device 2 is installed at the bottom of the inflow zone 4, and the ozone flotation device is connected to the ozone gas source.
- This embodiment is omitted in the drawings.
- the air flotation device 2 can atomize ozone gas in an aqueous solution to form misty particles, fully dissolve in water, and mix to form a supersaturated high pressure dissolved ozone aqueous solution, and the supersaturated high pressure dissolved ozone aqueous solution is added in the inflow region 4
- the liquid ⁇ 2 0 2 is in full contact, and a large amount of hydroxyl radicals are generated in contact with the fluid to be treated, and the reaction flows into the reaction cell 1 to effectively degrade the harmful substances in the fluid to be treated.
- the bubble diameter of the air flotation device is controlled to be between 0.2 and 50 ⁇ m, and the particle diameter of the bubble is preferably between 0.2 and 10 ⁇ m.
- the pressurized dissolved ozone aqueous solution is contacted with the fluid to be treated in the inflow region, and then flows into the reaction cell 1 in the inflow region.
- the ozone and H 2 0 2 are continuously contacted and reacted with the fluid to be treated, and finally flow out through the outflow region 5. .
- Embodiment 3 is a diagrammatic representation of Embodiment 3
- the ozone flotation advanced oxidizing fluid treatment system shown in this embodiment comprises a reaction tank 1, and further comprises a plurality of ozone flotation devices 2 and a plurality of groups of ultraviolet radiation devices 3 and their ballast devices and electricity. Control System.
- the upstream and downstream of the reaction cell 1 are respectively provided with an inflow zone 4 and an outflow zone 5, and the inflow zone 4 and the outflow zone 5 are in communication with the reaction cell 1.
- an H 2 0 2 adding device 9 is disposed upstream of the inflow region to add liquid H 2 O 2 at the time of inflow,] the ultraviolet radiation
- the device group 3 and the ozone flotation device 2 are installed in the inflow region 4.
- the ozone flotation device is disposed at the bottom of the inflow region 4, and the ozone flotation device is connected to the ozone gas source, which is omitted in the figure of the embodiment.
- the air flotation device 2 can atomize ozone gas in an aqueous solution to form misty ultrafine bubbles, fully dissolve in water, and thoroughly mix to form a supersaturated high pressure dissolved ozone aqueous solution.
- the ultraviolet radiation device group 3 is disposed downstream of the ozone air floating device 2, and the supersaturated high-pressure dissolved ozone aqueous solution is contacted with the fluid to be treated in the inflow region 4 under the irradiation of the ultraviolet radiation device 3, and flows into the reaction pool after the reaction. 1.
- an ozone flotation device is also disposed at the bottom of the ultraviolet radiation region to increase the ozone content in the fluid, and a drain wall with a top closed and a bottom opening is disposed upstream of the ultraviolet radiation device.
- W1 ensures that the water flows from the bottom of the diversion wall W1 into the ultraviolet radiation zone, and a diversion wall W2 that closes the upper opening at the bottom of the ultraviolet radiation device group is provided to ensure that water flows from the top of the diversion wall into the reaction cell.
- the ozone gas After passing through the air flotation device, the ozone gas is atomized in an aqueous solution to form a misty ultrafine bubble, which is fully dissolved in water and mixed with water to form a misty supersaturated high-pressure dissolved ozone aqueous solution, and the supersaturated high-pressure dissolved ozone aqueous solution Under ultraviolet irradiation, it is sufficiently contacted with the added liquid H 2 0 2 in the inflow region to generate a large amount of hydroxyl radicals, which are then reacted with the fluid to be treated to remove harmful substances therein.
- the bubble diameter of the air flotation device is controlled to be between 0.2 and 50 ⁇ m, and the particle diameter of the bubble is preferably between 0.2 and 10 ⁇ m.
- the supersaturated high-pressure dissolved ozone aqueous solution is contacted with the fluid to be treated in the inflow region under ultraviolet irradiation, and flows into the reaction cell 1 after the reaction. Since the high-pressure dissolved ozone remains in the fluid after passing through the ultraviolet radiation device 3, in order to increase ozone In terms of utilization rate and improvement of the treatment effect of the fluid, it is necessary to continuously bring the ozone into contact with the fluid to be treated, react in the reaction tank 1, and finally flow out through the outflow zone 5.
- the ozone flotation advanced oxidizing fluid treatment system adopting the technical scheme of the invention can be widely applied to urban domestic sewage treatment, deep treatment of drinking water, recycled water, agricultural irrigation water, aquaculture water, toxic and harmful exhaust gas treatment and other treatments that need to be treated. In the fluid.
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Description
一种臭氧气浮髙级氧化流体处理系统 技术领域
本发明涉及一种臭氧气浮高级氧化流体处理系统， 属于流体处理领域。 背景技术
目前， 基于臭氧的高级氧化技术 （03/UV， 03/H202等） 越来越广泛地被 应用于饮用水处理过程中，但是连续的单独气态臭氧投加装置使得反应器内 臭氧利用效率很低， 大部分臭氧没有反应就逃逸出反应器。
就目前情况看， 单独使用 03/UV， 03/H202的方案受到臭氧溶解度的影响 很大， 其处理效率的高低主要取决于 03在水中的溶解度， 而常规的 03/UV， 03/H202高级氧化系统中提高 03在水中的溶解度的方法是采用微孔曝气的方 法，但微孔曝气法释放出的臭氧气泡是肉眼可见的微小气泡，其粒径大约在 lmm左右， 其气泡粒径大， 在水中上升速度快， 使其在反应池中的停留时间 短， 导致大部分臭氧还没有反应就逃逸出了反应器。 因此， 微孔曝气的方式 投加臭氧使 03/UV和 03/H202这两种系统中的 03在水中不能充分溶解，其溶解 度低， 因此其并不能使所加入的臭氧充分溶解并与 UV或 02反应， 不能够 产生大量的羟基自由基， 使臭氧的利用率很低， 通常只有 10%左右。 目前使 用微孔曝气的方式的 03/UV， 03/H202高级氧化系统中提高臭氧溶解度的通常 做法是使用 10m左右水深的反应池以延长臭氧气泡在反应池中的停留时间 以提高臭氧的溶解率， 但水深 10米的反应池的建造成本和运行成本高昂， 不实用。 因此需要一种成本低， 安全、 高效的系统来克服上述不足。 发明内容
本发明的技术方案一是这样实现的，所述一种臭氧气浮高级氧化流体处 理系统， 包含一个反应池， 其特征在于： 反应池的上游和下游分别设有进流 区和出流区，进流区和出流区与反应池连通，还包含臭氧气浮装置和若干组 紫外线辐射装置，紫外线辐射装置包含紫外线灯管及其镇流器装置和电控制 系统，所述紫外线辐射装置组和臭氧气浮装置安装在进流区内，所述气浮装 置能使臭氧气体在水溶液中雾化形成雾状颗粒，充分溶解在水中， 混合形成 过饱和高压溶解臭氧水溶液，所述过饱和高压溶解臭氧水溶液在紫外线照射 下在进流区内与待处理流体接触、反应后流入反应池中继续与待处理流体充 分接触、 反应， 最后经出流区流出。
为了更好的技术效果， 本发明的技术方案还可以具体为如下特征：
1. 根据不同的系统条件和处理结果的要求， 可以通过控制气泡粒径的 大小达到最佳的处理效果。 其气泡粒径至少可以有以下三种选择：
( 1 ) 所述气浮装置的气泡粒径可以为 0.2-50μιη之间。
(2) 所述气浮装置的气泡粒径优选为 0.2-10μιη之间。
(3 ) 所述气浮装置的气泡粒径也可以为 10-50μιη之间。
2.所述臭氧气浮装置设置在进流区底部。
3.紫外线辐射装置组设置在臭氧气浮装置的下游。
4.所述紫外线灯管为中压紫外线灯管。
5.紫外线辐射装置的上游设置一个顶部封闭底部开口的导流墙保证水 流从导流墙底部进入紫外线辐射区。
6.紫外线辐射装置组下游设置一个底部封闭顶部开口的导流墙保证水 流从导流墙顶部进入反应池以延长辐射路程和受辐射时间。
7.紫外线辐射装置的上游和下游各设置一个导流墙， 保证水流从上游导 流墙底部进入紫外线辐射区和下游导流墙顶部进入反应池。
8.所述紫外线辐射装置可以采用模块化结构， 每个紫外灯模块包含若干 支紫外线灯管。
9.可以根据实际需要在进流区中沿流体流动方向设置多个臭氧气浮装置 和多级紫外线辐射装置组。
为了更好地实现高级氧化气浮装置的效果， 本发明还提供如下方案二和 方案三：
方案二：
一种臭氧气浮高级氧化流体处理系统， 包含一个反应池， 其特征在于： 反应池的上游和下游分别设有进流区和出流区，进流区和出流区与反应池连 通， 还包含臭氧气浮装置和 H202添加装置， 所述臭氧气浮装置安装在进流 区内的底部， H202添加装置设置在进流区内气浮装置的上游以在进流时加 入液态的 H202，所述气浮装置能使臭氧气体在水溶液中雾化形成雾状颗粒， 充分溶解在水中， 与水混合形成过饱和高压溶解臭氧水溶液，所述过饱和高 压溶解臭氧水溶液在进流区内与加入的液态的 H202充分接触， 产生大量的 羟基自由基与待处理流体接触、反应后流入反应池以便有效降解待处理流体 中的有害物质。
根据不同的系统条件和处理结果的要求，可以通过控制气泡粒径的大小 达到最佳的处理效果。 其气泡粒径至少可以有以下三种选择：
1. 所述气浮装置的气泡粒径可以为 0.2-50μιη之间。
2. 所述气浮装置的气泡粒径优选为 0.2-10μιη之间。
3. 所述气浮装置的气泡粒径也可以为 10-50μιη之间。
方案三：
在方案一的基础上， 在系统进流区的上游设置 Η202添加装置。 其具体 描述如下：
一种臭氧气浮高级氧化流体处理系统， 包含一个反应池， 其特征在于： 反应池的上游和下游分别设有进流区和出流区，进流区和出流区与反应池连 通， 还包含臭氧气浮装置、 H202添加装置和若干组紫外线辐射装置， 紫外 线辐射装置包含紫外线灯管及其镇流器装置和电控制系统，臭氧气浮装置安 装在进流区内的底部， 所述 H202添加装置设置在进流区的上游以在进流时 加入液态的 H202， 所述气浮装置能使臭氧气体在水溶液中雾化形成雾状颗 粒， 充分溶解在水中， 混合形成过饱和高压溶解臭氧水溶液， 所述过饱和高 压溶解臭氧水溶液在紫外线照射下在进流区内与加入的液态的 H202充分接 触，产生大量的羟基自由基与待处理流体接触、反应后流入反应池中继续与 待处理流体充分接触、 反应以脱除其中的有害物质， 最后经出流区流出。
根据不同的系统条件和处理结果的要求，可以通过控制气泡粒径的大小 达到最佳的处理效果。 其气泡粒径至少可以有以下三种选择：
1. 所述气浮装置的气泡粒径可以为 0.2-50μιη之间。
2. 所述气浮装置的气泡粒径优选为 0.2-10μιη之间。
3. 所述气浮装置的气泡粒径也可以为 10-50μιη之间。
¾02添加装置设置在进流区的上游， 可以在系统进流过程加入液态的 ¾02，使 ¾02与高度雾化的超微气泡 03充分接触反应产生更多的羟基自由 基。
采用本发明的臭氧气浮高级氧化流体处理系统具有如下优点：
1.所述气浮装置能使臭氧气体在水溶液中雾化形成雾状颗粒， 充分溶解 在水中， 与水混合形成过饱和高压溶解臭氧水溶液， 雾化后的臭氧超微气泡 粒径小，在水中停留时间长， 能使大部分臭氧与待处理流体在进流区和反应 池中充分接触、 反应， 减少臭氧逃逸出反应池。
2.效率高， 臭氧利用率高， 通过在反应池上游的进水区中装设气浮装置
使臭氧气体形成雾状颗粒与流体充分接触后再流经紫外辐射装置，运用紫外 线辐射与臭氧相结合协同作用相互促进，在与流体的接触反应中产生大量活 性极强的自由基，大大提高臭氧的利用率。再通过自由基与有机化合物之间 的加合、 取代、 电子转移、 断键等， 使水体中的大分子难降解有机物氧化降 解为低毒或无毒的小分子物质， 大大提高流体的处理效果。
3.通过在臭氧气浮装置与紫外辐射装置之间设置导流墙使混有雾状臭 氧颗粒的流体从紫外辐射区的底部流入并从其顶部流进反应池，延长水流与 臭氧颗粒与水流及紫外线接触时间， 使其反应充分。
4.利用臭氧雾化和紫外线辐射进行高级氧化反应，实现对流体的深度处 理， 无需投加过氧化氢或其他催化剂， 高效而无二次污染； 并能有效降低运 行成本。
5.并且过饱和高压溶解臭氧水溶液在紫外线辐射下与待处理流体充分 接触、 反应， 使污染物氧化分解。
6.本发明的臭氧气浮高级氧化流体处理系统能使臭氧气体在水溶液中 雾化形成雾状颗粒，充分溶解在水中，混合形成过饱和高压溶解臭氧水溶液， 因此能够瞬间释放大量的雾状臭氧气泡，释放出的雾状臭氧气泡粒径小，平 均粒径在 0. 2-50um， 大大增加了与 UV或 02反应的机会和接触时间， 充分 提高反应效率；
7.并且， 高浓度过饱和的雾状臭氧气泡在水中不容易上升，使其在水中 的停留时间将大幅增加， 小粒径气泡使臭氧的溶解度大幅提高， 提高臭氧的 利用率， 大幅减小臭氧的投加量， 显著降低运行成本；
8.并且， 高浓度过饱和的雾状臭氧气泡在水中不容易上升，使其在水中 的停留时间将大幅增加， 因此可以大大减小反应池的深度， 使反应池的深度 可以由 10米降至 2米， 大大减少反应池的建造成本和工作量。
9.所述过饱和高压溶解臭氧水溶液在进流区内与加入的液态的 H202充 分接触，产生大量的羟基自由基与待处理流体接触、反应后流入反应池以便 有效降解待处理流体中的有害物质。
需要另外指出的是， 一般在利用高级氧化技术处理的过程中，在没有使 用气浮工艺前污染物 COD (化学需氧量） 的去除率在 50%左右， 而使用了 03的气浮工艺后， 其 COD的去除率可以提高至 60%-95%左右。
在污水处理特别是造纸废水的处理过程中，处理后的废水中 COD的浓度 一般在 400左右， 达不到排放的标准， 目前常用的 02/ 03工艺也只能将其 降解到 200左右， 而使用了 03的气浮工艺后， 可以使其降到 60-80左右， 大大优于排放标准 （排放标准为 100)。
而上述显著的效果仅仅在于改变了其曝气的方式由微孔曝气改为气浮， 结构简单易于实现， 投资成本低， 效果显著提高， 并且大大降低 03的使用 量，节约运行成本。是一种与常规的高级氧化系统有明显区别且效果显著的 新的高级氧化系统。 附图说明
图 1 是本发明的臭氧气浮高级氧化流体处理系统的第一个实施例的主 视图；
图 2 是本发明的臭氧气浮高级氧化流体处理系统的第二个实施例的主 视图；
图 3 是本发明的臭氧气浮高级氧化流体处理系统的第三个实施例的主 视图。
图中， 1为反应池， 2为臭氧气浮装置， 3为紫外线辐射装置， 301为紫
外灯模块， 302为紫外线灯管， 303为紫外线辐射装置的电源及控制系统， 4 为进流区， 5为出流区。 Wl、 W2为紫外线辐射装置上游和下游的导流墙， 6为进流管， 7为出流管， 8为盖板， 9为 ¾02添加装置。 具体实舫式
以下结合附图 1对本发明的第一个实施例进行详细描述。
实施例一：
如图 1所示，本实施例所示的臭氧气浮高级氧化流体处理系统包含一个 反应池 1， 还包含多个臭氧气浮装置 2和若干组紫外线辐射装置 3及其镇流 器装置和电控制系统。反应池 1的上游和下游分别设有进流区 4和出流区 5， 进流区 4和出流区 5与反应池 1连通。所述紫外线辐射装置组 3和臭氧气浮 装置 2安装在进流区 4内。所述臭氧气浮装置设置在进流区 4的底部，臭氧 气浮装置与臭氧气源连接，本实施例图中省略。所述气浮装置 2能使臭氧气 体雾化形成雾状颗粒与待处理流体充分混合形成过饱和高压溶解臭氧水溶 液。根据流向， 紫外线辐射装置组 3设置在臭氧气浮装置 2的下游， 所述过 饱和高压溶解臭氧水溶液在紫外线辐射装置 3照射下在进流区 4内与待处理 流体接触、 反应后流入反应池 1。 本实施例中， 为了更好的反应效果， 在辐 射紫外线辐射区的底部也设置臭氧气浮装置以增加流体中的臭氧含量，并且 在紫外线辐射装置的上游设置一个顶部封闭而底部开口的导流墙 W1 保证 水流从导流墙 W1底部进入紫外线辐射区，同时在紫外线辐射装置组下游设 置一个底部封闭上部开口的导流墙 W2保证水流从导流墙顶部进入反应池。 所述臭氧气体通过气浮装置后将被雾化形成雾状颗粒并与待处理流体混合 形成过饱和高压溶解臭氧水溶液，所述过饱和高压溶解臭氧水溶液在紫外线 照射下在进流区内与待处理流体接触、 反应后流入反应池 1， 由于通过紫外 线辐射装置 3后流体中还剩余高压溶解臭氧，因此为了提高臭氧的利用率和 提高流体的处理效果， 需在反应池 1中使臭氧继续与待处理流体充分接触、
反应， 最后经出流区 5流出。
为了良好的技术效果， 所述气浮装置的气泡粒径一般控制在 0.2-50μιη 之间， 最好是气泡粒径为 0.2-10μιη之间， 也可以为 10-50μιη之间。
所述紫外线辐射装置 3可以采用模块化结构，每个紫外灯模块 301包含 若干支紫外线灯管 302。 本实施例中的紫外线灯管为中压紫外线灯管。
本实施例中设置多个臭氧气浮装置和二级紫外线辐射装置组。可以根据 实际需要在进流区中沿流体流动方向设置多级紫外线辐射装置组，相应地在 每组紫外线辐射装置的前下游各设置导流墙 W1和 W2, 以增加臭氧和紫外 线的协同作用路程和时间， 提高反应效果。
本实施例中紫外线灯管 302水平安装在模块上，在实际应用中紫外线灯 管 302灯管也可以竖直地安装在模块上。
实施例二：
以下结合附图 2对本发明的第二个实施例进行详细描述。
如图 2所示，本实施例所示的臭氧气浮高级氧化流体处理系统包含一个 反应池 1，还包含多个臭氧气浮装置 2和 Η202添加装置 9。反应池 1的上游 和下游分别设有进流区 4和出流区 5，进流区 4和出流区 5与反应池 1连通。 在进流区的上游设置 ¾02添加装置以在进流时加入液态的 Η202，所述臭氧 气浮装置 2安装在进流区 4内的底部，臭氧气浮装置与臭氧气源连接，本实 施例图中省略。所述气浮装置 2能使臭氧气体在水溶液中雾化形成雾状颗粒， 充分溶解在水中，混合形成过饱和高压溶解臭氧水溶液，所述过饱和高压溶 解臭氧水溶液在进流区 4内与加入的液态的 Η202充分接触， 产生大量的羟 基自由基与待处理流体接触、反应后流入反应池 1能有效降解待处理流体中 的有害物质。 为了良好的技术效果， 所述气浮装置的气泡粒径控制在 0.2-50μιη之间， 并且所述气泡粒径最好在为 0.2-10μιη之间。 所述过饱和高
压溶解臭氧水溶液在进流区内与待处理流体接触、 反应后流入反应池 1， 反 应池 1中使臭氧、 H202继续与待处理流体充分接触、 反应， 最后经出流区 5 流出。
实施例三：
以下结合附图 3对本发明的第三个实施例进行详细描述。
如图 3所示，本实施例所示的臭氧气浮高级氧化流体处理系统包含一个 反应池 1， 还包含多个臭氧气浮装置 2和若干组紫外线辐射装置 3及其镇流 器装置和电控制系统。反应池 1的上游和下游分别设有进流区 4和出流区 5， 进流区 4和出流区 5与反应池 1连通。 【新增： 与实施例一中不同的是， 本 实施例中在进流区的上游设置 H202添加装置 9 以在进流时加入液态的 H202，】，所述紫外线辐射装置组 3和臭氧气浮装置 2安装在进流区 4内。所 述臭氧气浮装置设置在进流区 4的底部，臭氧气浮装置与臭氧气源连接，本 实施例图中省略。所述气浮装置 2能使臭氧气体在水溶液中雾化形成雾状超 微气泡， 充分溶解在水中， 充分混合形成过饱和高压溶解臭氧水溶液。根据 流向， 紫外线辐射装置组 3设置在臭氧气浮装置 2的下游，所述过饱和高压 溶解臭氧水溶液在紫外线辐射装置 3照射下在进流区 4内与待处理流体接触、 反应后流入反应池 1。 本实施例中， 为了更好的反应效果， 在紫外线辐射区 的底部也设置臭氧气浮装置以增加流体中的臭氧含量，并且在紫外线辐射装 置的上游设置一个顶部封闭而底部开口的导流墙 W1保证水流从导流墙 W1 底部进入紫外线辐射区，同时在紫外线辐射装置组下游设置一个底部封闭上 部开口的导流墙 W2保证水流从导流墙顶部进入反应池。所述臭氧气体通过 气浮装置后将在水溶液中被雾化形成雾状超微气泡，其充分溶解在水中， 与 水混合形成雾状过饱和高压溶解臭氧水溶液，所述过饱和高压溶解臭氧水溶 液在紫外线照射下在进流区内与加入的液态的 H202充分接触反应， 产生大 量的羟基自由基，再与待处理流体反应以脱除其中的有害物质。为了良好的
技术效果， 所述气浮装置的气泡粒径控制在 0.2-50μιη之间， 并且所述气泡 粒径最好在 0.2-10μιη之间。 所述过饱和高压溶解臭氧水溶液在紫外线照射 下在进流区内与待处理流体接触、 反应后流入反应池 1， 由于通过紫外线辐 射装置 3后流体中还剩余高压溶解臭氧，因此为了提高臭氧的利用率和提高 流体的处理效果，需在反应池 1中使臭氧继续与待处理流体充分接触、反应， 最后经出流区 5流出。
采用本发明技术方案的臭氧气浮高级氧化流体处理系统能够广泛地应 用在城市生活污水处理、 饮用水的深度处理、 循环回用水、 农业灌溉用水、 养殖用水、 有毒有害废气处理和其他需要处理的流体中。
Claims
权利要求：
1 一种臭氧气浮高级氧化流体处理系统， 包含一个反应池， 其特征在于： 还包含臭氧气浮装置 （2) 和若干组紫外线辐射装置 （3 )， 紫外线辐射 装置（3 )包含紫外线灯管（302)及其镇流器装置和电控制系统， 反应 池的上游和下游分别设有进流区和出流区， 进流区 （4) 和出流区 （5 ) 与反应池（1 )连通， 所述紫外线辐射装置组和臭氧气浮装置（2)安装 在进流区 （4) 内， 所述气浮装置能使臭氧气体在水溶液中雾化形成雾 状颗粒， 充分溶解在水中， 混合形成过饱和高压溶解臭氧水溶液， 所述 过饱和高压溶解臭氧水溶液在紫外线照射下在进流区 （4) 内与待处理 流体接触、 反应后流入反应池 （1 ) 中继续与待处理流体充分接触、 反 应， 最后经出流区 （5 ) 流出。
2 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述紫外线辐射装置组设置在臭氧气浮装置 （2) 的下游。
3 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述紫外线辐射装置上安装的紫外线灯管 （302) 为中压紫外线灯管。
4 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述臭氧气浮装置 （2) 设置在进流区 （4) 底部。
5 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述紫外线辐射装置的上游设置一个导流墙保证水流从导流墙底部进入 紫外线辐射区。
6 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述紫外线辐射装置组下游设置一个导流墙保证水流从导流墙顶部进入 反应池中以延长辐射路程。
7 如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所
述紫外线辐射装置的上游和下游各设置一个导流墙 （Wl， W2), 保证 水流从上游导流墙 （W1 ) 底部进入紫外线辐射区和下游导流墙 （W2) 顶部进入反应池 （1 )。
如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：在 进流区 （4) 中沿流体流动方向设置多个臭氧气浮装置和多级紫外线辐 射装置组。
如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述紫外线辐射装置（3 )采用模块化结构， 每个紫外灯模块（301 )包含 若干支紫外线灯管 （302)。
如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述气浮装置雾化成的雾状颗粒的气泡粒径为 0.2-50um之间。
如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述气浮装置雾化成的雾状颗粒的气泡粒径为 10-50um之间。
如权利要求 1所述的臭氧气浮高级氧化流体处理系统，其特征在于：所 述气浮装置雾化成的雾状颗粒的气泡粒径为 0.2-10um之间。
一种臭氧气浮高级氧化流体处理系统， 包含一个反应池， 其特征在于： 反应池的上游和下游分别设有进流区和出流区，进流区和出流区与反应 池连通， 还包含臭氧气浮装置和 H202添加装置， 所述臭氧气浮装置安 装在进流区内的底部， H202添加装置设置在进流区内气浮装置的上游 以在进流时加入液态的 H202， 所述气浮装置能使臭氧气体在水溶液中 雾化形成雾状颗粒，充分溶解在水中，混合形成过饱和高压溶解臭氧水 溶液， 所述过饱和高压溶解臭氧水溶液在进流区内与加入的液态的 H202充分接触， 产生大量的羟基自由基与待处理流体接触、 反应后流 入反应池以便有效降解待处理流体中的有害物质。
如权利要求 13所述的臭氧气浮高级氧化流体处理系统， 其特征在于： 所述进流区中设置至少一组导流墙，每组导流墙沿流体流动方向包括一 个上游导流墙和一个下游导流墙，所述上游导流墙的底部设有开口，所 述下游导流墙的顶部设有开口以保证水流从上游导流墙底部进入而从 下游导流墙顶部流出以延长路程。
一种臭氧气浮高级氧化流体处理系统， 包含一个反应池， 其特征在于： 反应池的上游和下游分别设有进流区和出流区，进流区和出流区与反应 池连通， 还包含臭氧气浮装置、 H202添加装置和若干组紫外线辐射装 置，紫外线辐射装置包含紫外线灯管及其镇流器装置和电控制系统，臭 氧气浮装置安装在进流区内的底部， 所述 H202添加装置设置在进流区 的上游以在进流时加入液态的 H202， 所述气浮装置能使臭氧气体在水 溶液中雾化形成雾状颗粒， 充分溶解在水中， 混合形成过饱和高压溶解 臭氧水溶液，所述过饱和高压溶解臭氧水溶液在紫外线照射下在进流区 内与加入的液态的 H202充分接触， 产生大量的羟基自由基与待处理流 体接触、反应后流入反应池中继续与待处理流体充分接触、反应以脱除 其中的有害物质， 最后经出流区流出。
如权利要求 15所述的臭氧气浮高级氧化流体处理系统， 其特征在于： 所述紫外线辐射装置的上游设置一个导流墙保证水流从导流墙底部进 入紫外线辐射区。
如权利要求 15所述的臭氧气浮高级氧化流体处理系统， 其特征在于： 所述紫外线辐射装置组下游设置一个导流墙保证水流从导流墙顶部进 入反应池中以延长辐射路程。
如权利要求 15所述的臭氧气浮高级氧化流体处理系统， 其特征在于： 所述紫外线辐射装置的上游和下游各设置一个导流墙 （Wl， W2) , 保
证水流从上游导流墙（Wl)底部进入紫外线辐射区和下游导流墙（W2) 顶部进入反应池 （1)。
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| CN201120134865U CN202148212U (zh) | 2011-04-22 | 2011-04-22 | 一种臭氧气浮高级氧化流体处理系统 |
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