WO2019011023A1 - 一种复合式臭氧气浮一体化装置 - Google Patents

一种复合式臭氧气浮一体化装置 Download PDF

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Publication number
WO2019011023A1
WO2019011023A1 PCT/CN2018/082901 CN2018082901W WO2019011023A1 WO 2019011023 A1 WO2019011023 A1 WO 2019011023A1 CN 2018082901 W CN2018082901 W CN 2018082901W WO 2019011023 A1 WO2019011023 A1 WO 2019011023A1
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cylinder
pipe
center
zone
integrated device
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PCT/CN2018/082901
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English (en)
French (fr)
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金鹏康
金鑫
王锐
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西安建筑科技大学
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Priority to US16/619,678 priority Critical patent/US10814337B2/en
Publication of WO2019011023A1 publication Critical patent/WO2019011023A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1431—Dissolved air flotation machines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/02—Froth-flotation processes
    • B03D1/028—Control and monitoring of flotation processes; computer models therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1406—Flotation machines with special arrangement of a plurality of flotation cells, e.g. positioning a flotation cell inside another
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/145—Feed mechanisms for reagents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
    • C01B13/10—Preparation of ozone
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D2203/00—Specified materials treated by the flotation agents; Specified applications
    • B03D2203/008—Water purification, e.g. for process water recycling
    • 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
    • C02F1/006—Water distributors either inside a treatment tank or directing the water to several treatment tanks; Water treatment plants incorporating these distributors, with or without chemical or biological tanks
    • 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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • 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
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Definitions

  • Ozone is a kind of active small molecule with strong oxidizing property, and its redox potential is 2.07V, which is second only to fluorine.
  • Ozone is widely used in feedwater treatment and sewage treatment of micro-polluted source water.
  • Air floatation has the characteristics of efficient separation of suspended solids in water, simple operation and low operating cost.
  • the combination of the two, synergistic use of ozone oxidation characteristics and air flotation separation characteristics has created ozone floatation technology.
  • the equipment has various functions such as water inlet, chemical injection, ozone air, drainage, exhaust and slagging, and has various functions such as ozonation, coagulation and air flotation.
  • the shape of the traditional equipment is limited. Convenience of operation.
  • the object of the present invention is to provide a composite ozone-air-floating integrated device, which utilizes a special structure of three layers of a central cylinder, an intermediate cylinder and a container wall to realize partition ozonation, air flotation separation and Automatic slagging and other functions, with the advantages of quick installation, simple operation and high processing efficiency.
  • a composite ozone air flotation integrated device comprises a coaxial cylinder 6, an intermediate cylinder 7 and a central cylinder 8, the cylinder 6 and the central cylinder 8 are co-bottomed, the cylinder 6 and the intermediate cylinder 7 are co-topped, and the intermediate cylinder 7 It is disposed on the support channel 4 between the cylinder 6 and the center cylinder 8.
  • the top of the center cylinder 8 is located in the intermediate cylinder 7, and the top of the center cylinder 8 is open.
  • the upper part of the cylinder 6 is provided with a drain pipe 14, and the top is provided with a drain pipe 14
  • the inner cylinder exhaust pipe 12 and the slag discharge pipe 9, the upper portion of the intermediate cylinder 7 is provided with an outer cylinder exhaust pipe 13, the lower portion of the central cylinder 8 and the inlet pipe 15, the dissolved gas inlet pipe 1, and the connecting inner cylinder venting the drain pipe 16
  • an annular aeration tube 5 with an aeration inner wire head 18 is disposed at a lower position between the cylinder body 6 and the intermediate cylinder 7, and the annular aeration tube 5 is connected to the intake pipe 25, and the lower portion of the cylinder body 6 is connected
  • the cylinder venting pipe 2 is connected, a contact zone A is formed in the center cylinder 8, an air flotation separation zone B is formed in the upper part of the intermediate cylinder 7, and a slag zone C is formed at the top of the intermediate cylinder 7, in the cylinder 6 and the center cylinder
  • the lower region between 8 forms a sl
  • the bottom of the cylinder 6 has a bottom plate 26, and the top has a top cover 11, wherein the bottom plate 26 is disposed on the equipment base 27, the top cover 11 is a conical top, and the inner cylinder exhaust pipe 12 is connected to the top cover 11.
  • the bottom of the cylinder 6 is a conical bucket 3, and the angle of the cone exit of the conical bucket 3 is 30° to 45°.
  • the upper part of the intermediate tube 7 is connected to the top by the scum guiding body 10, and the slag guiding body 10 has a tapered outer flaring structure, and the inclination angle of the center line of the tapered outlet is 80° to 85°, and the outer tube
  • the exhaust pipe 13 is connected to the scum guiding body 10.
  • the center of the center cylinder 8 is provided with a central cylinder guide swash plate 22, which is a tapered outer flaring, and the inclination angle of the center line of the tapered outlet is 40° to 50°.
  • the upper portion of the cylinder 6 is provided with a zigzag weir 19 around the intermediate cylinder 7, and a drain 14 is provided at the bottom of the weir 19.
  • the inlet pipe 15 is connected to the feed water pump and the coagulant dosing pump outlet pipe, and the inlet pipe 15 conveys raw water to the center cylinder 8 in a tangential manner, and the dissolved gas inlet device 21 is provided with an ozone-dissolving air release device 21 at the end of the dissolved gas inlet pipe 1. .
  • the inner cylinder exhaust pipe 12 and the outer cylinder exhaust pipe 13 are connected to an exhaust manifold having an exhaust electric valve 24 through an exhaust tee 23, and the drain pipe 14 is provided with an outlet electric valve 20, the inner cylinder
  • the venting drain pipe 16 is provided with a central cylinder venting electric valve 17, and the outer cylinder venting sump 2 is provided with a sump venting electric valve 28.
  • the exhaust electric valve 24, the outlet electric valve 20, the center cylinder venting electric valve 17, and the sump venting electric valve 28 are connected to the time relay, and are automatically opened and closed according to the set interval time.
  • the inlet pipe 15 is connected to the inlet pump and the coagulant dosing pump outlet pipe.
  • the volume ratio of the contact zone A, the precipitation zone D, the slag collection zone C, the ozone oxidation zone E and the air flotation separation zone B is 1:5:5:15:20.
  • the tops of the inner cylinder exhaust pipe 12 and the outer cylinder exhaust pipe 13 are about 0.9 to 1.2 m higher than the top of the slag discharge pipe 9.
  • the water inlet pipe 15 of the invention tangentially enters the water, improves the hydrocyclone strength, can increase the three-phase contact and mixing of the gas, solid and liquid, and increases the reaction efficiency while increasing the volumetric loading rate of the device.
  • the device features a three-layer composite structure, which divides the reactor space into three layers: inner, middle and outer. Each layer has corresponding functions according to the water treatment process and does not interfere with each other.
  • the whole device is composed of a scum removal area, an air flotation separation area and a sludge sedimentation area from top to bottom, and the functions of each division are clear.
  • the operation of the ozone flotation equipment can be divided into water inlet, slagging, liquid level reduction, re-influent water, etc., and the device inlet water pump, the exhaust electric valve 24, and the outlet water electric valve 20 are controlled by a time relay or a PLC.
  • the exhaust electric valve 24 and the outlet electric valve 20 are controlled in linkage, and are in an open or closed state.
  • the operation of the slag discharge is alternated by opening and closing the valve.
  • the inner cylinder and the bottom of the tank are deposited with sludge, which is controlled by the mud-water interface meter.
  • the central valve is evacuated by the control center cylinder and the electric valve 28 is automatically drained.
  • the present invention changes the mode of the multi-stage ozone flotation by the U-shaped tube of the original high-efficiency ozone flotation device, and completes four processes of reaction, separation, oxidation and precipitation through the inner, middle and outer three-layer structures.
  • the inflow water runs in a swirling upward direction, so that the system consumes the lowest energy and the gas, water and the medicament are uniformly mixed.
  • the invention uniformly distributes into the central cylinder through the mixing process to complete the oxidation reaction process. While the organic matter is oxidized and removed, the suspended matter can also be carried by the microbubbles to the top and discharged through the slag discharge pipe.
  • FIG. 1 is a schematic view showing the structure of a composite ozone flotation integrated device of the present invention.
  • Figure 2 is a structural view of a bottom planar pipe in the present invention.
  • Figure 4 is a structural view of a top planar pipe in the present invention.
  • the system includes a casing, an inlet and outlet unit, an ozone flotation unit, an ozone oxidation unit, a slagging system, a sludge discharging system, and the like.
  • the housing includes a barrel 6, a top cover 11, a bottom plate 26, a device base 27, and the like.
  • the inlet and outlet unit unit includes an inlet pipe 15, a dissolved gas inlet pipe 1, a drain pipe 1, and the like.
  • the ozone flotation unit includes a center cylinder 8, a dissolved ozone air release unit 21, an intermediate cylinder 7, and the like.
  • the ozone oxidation unit includes an intake pipe 25, an annular aeration pipe 5, and the like.
  • the cylinder 6, the intermediate cylinder 7 and the central cylinder 8 are coaxially arranged, the cylinder 6 and the central cylinder 8 are co-bottomed, and are co-located with the intermediate cylinder 7, and the upper portion of the intermediate cylinder 7 passes through the scum to guide the vertebral body 10 and the top.
  • the cover 11 is connected, and the scum guiding body 10 has a tapered outer flare structure, and the inclination angle of the center line of the tapered outlet is 80° to 85°.
  • the intermediate cylinder 7 is disposed on the support channel 4 between the cylinder 6 and the center cylinder 8, and supports the channel 4 to support the water flow.
  • the top of the center cylinder 8 is located in the middle cylinder 7, and the center cylinder 8 is provided with a central cylinder swash plate 22 at the top thereof, and the swash plate 22 has a tapered outer flaring, and the inclination angle of the center line of the tapered outlet is 40° to 50°. .
  • the drain pipe 14 is connected to the upper portion of the cylinder 6, the top cover 11 is a conical top, the inner cylinder exhaust pipe 12 is connected to the side of the top cover 11, the slag discharge pipe 9 is connected to the apex position of the top cover 11, and the outer cylinder is exhausted.
  • the tube 13 is connected to the scum guiding body 10, and the bottom of the barrel 6 is a conical bucket 3 with a dip angle of 30° to 45° on the center line of the conical outlet, an inlet pipe 15, a dissolved gas inlet pipe 1 and
  • the inner cylinder venting drain pipe 16 is connected to the center cylinder 8 through the conical draining bucket 3, and the outer cylinder venting mud discharging pipe 2 is connected to the bottom of the conical draining hopper 3.
  • the inlet pipe 15 is connected to the inlet water pump and the coagulant dosing pump outlet pipe, and delivers the raw water to the center cylinder 8 in a tangential manner.
  • the dissolved gas inlet pipe 1 is provided with an ozone-dissolving air release device 21 at the end of the dissolved gas inlet pipe 1, and the inner cylinder is emptied of the mud discharge pipe. 16 is located below the water inlet pipe 15.
  • the inner cylinder exhaust pipe 12 and the outer cylinder exhaust pipe 13 are connected to the exhaust manifold with the exhaust electric valve 24 through the exhaust tee 23, and the drain pipe 14 is provided with a water outlet electric valve 20, and the inner cylinder is vented on the drain pipe 16
  • a central cylinder venting electric valve 17 is provided, and an outer venting venting pipe 2 is provided with a sump venting electric valve 28.
  • the exhaust electric valve 24, the outlet electric valve 20, the center cylinder venting electric valve 17, and the sump venting electric valve 28 are connected to the time relay, and are automatically opened and closed according to the set interval time.
  • the volume ratio of the contact zone A, the precipitation zone D, the slag collection zone C, the ozone oxidation zone E and the air flotation separation zone B is 1:5:5:15:20, and the inner cylinder exhaust pipe 12 and the outer cylinder exhaust pipe 13 top ratio
  • the top of the slag discharge pipe 9 is about 0.9 to 1.2 m high.
  • the inlet pipe 15 is tangentially influent, and the influent flows through the wall of the cylinder in the narrow region of the central cylinder 8 to form a vortex flow.
  • the reflux water mixed with ozone, air and coagulant entering from the dissolved gas inlet pipe 1 is thoroughly mixed with the raw water, and the coagulant is coagulated to capture the suspended particles, and after the reaction, enters the upper air flotation separation zone through the deflecting swash plate 22.
  • ozone and air form a large amount of microbubbles. Ozone microbubbles have a large surface area and oxidize organic matter in raw water.
  • the ozonolysis produces a large amount of hydroxyl radicals, which can further remove the refractory organic matter in the raw water.
  • a part of the oxidation product is a hydrophobic substance, which is separated by small particles of the coagulant floc by the coagulation air flotation.
  • Ozone enters the annular aeration tube 5 through the intake pipe 25, and the aeration inner wire head 18 performs aeration.
  • the ozone oxidation zone is located in the outer ring of the device. Although the radius is relatively small but the volume is large, the longer hydraulic retention time provides better conditions for the full reaction of ozone.
  • the effluent turbidity is very low, and the ozone in the oxidation unit is mainly consumed by removing organic matter, which improves the ozone utilization rate.

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Biotechnology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Inorganic Chemistry (AREA)
  • General Engineering & Computer Science (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Physical Water Treatments (AREA)

Abstract

一种复合式臭氧气浮一体化装置，包括同轴的筒体（6）、中间筒（7）和中心筒（8），筒体（6）与中心筒（8）共底，筒体（6）与中间筒（7）共顶，中间筒（7）设置在筒体（6）与中心筒（8）之间的支撑槽钢（4）上，中心筒（8）顶部位于中间筒（7）中，且中心筒（8）顶部敞口，筒体（6）的上部设置有排水管（14），顶部设置有内筒排气管（12）和排渣管（9），中间筒（7）的上部设置有外筒排气管（13），中心筒（8）的下部与进水管（5）、溶气进水管（1）以及连接内筒放空排泥管（16）连接，在筒体（6）与中间筒（7）之间的下部位置设置有带曝气内丝头（18）的环形曝气管（5），环形曝气管（5）与进气管（25）连接，筒体（6）的下部与连接外筒放空排泥管（2）连接，该装置为三层结构，实现分区臭氧化、气浮分离和自动排渣等功能，具有安装快捷、操作简单和处理效率高等优点。

Description

一种复合式臭氧气浮一体化装置 技术领域
本发明属于污/废水技术领域，涉及污/废水深度处理，特别涉及一种复合式臭氧气浮一体化装置。
背景技术
臭氧是一种活泼小分子，具有很强氧化性，其氧化还原电位为2.07V，仅次于氟。臭氧广泛应用于微污染水源水的给水处理和污水处理。气浮具有高效分离水中悬浮物的特点，操作简单，运行费用低。两者结合，协同利用臭氧氧化特性和气浮分离特性，创造出了臭氧气浮技术。在实际应用过程中，由于设备具有进水、进药剂、进臭氧空气、排水、排气和排渣等多种管道，有臭氧化、混凝和气浮等多种功能，传统设备的外形限制了操作的便利性。另外，在罐体内混凝和气浮反应后，生成絮凝污泥大部分会被溶气携带到顶部排渣口排出。在运行的间歇期和水流扰动时，总有部分浮渣会沉积到罐体底部。沉积在罐底的积泥会随水流携带到出水口，降低出水有机物和悬浮物去除效率，影响了臭氧气浮装置的正常运行。受限于现有溶气技术，臭氧发生器产生的臭氧存在较大程度的浪费。同时，竖流式臭氧气浮装置为了保证其气浮效果使得其高度过高，对加工、安装及调试造成了很多不便。
发明内容
为了克服上述现有技术的缺点，本发明的目的在于提供一种复合式臭氧气浮一体化装置，利用中心筒、中间筒和容器壁三层的特殊结构，实现分区臭氧化、气浮分离和自动排渣等功能，具有安装快捷、操作简单和处理效率高等优点。
为了实现上述目的，本发明采用的技术方案是：
一种复合式臭氧气浮一体化装置，包括同轴的筒体6、中间筒7和中心筒8， 筒体6与中心筒8共底，筒体6与中间筒7共顶，中间筒7设置在筒体6与中心筒8之间的支撑槽钢4上，中心筒8顶部位于中间筒7中，且中心筒8顶部敞口，筒体6的上部设置有排水管14，顶部设置有内筒排气管12和排渣管9，中间筒7的上部设置有外筒排气管13，中心筒8的下部与进水管15、溶气进水管1以及连接内筒放空排泥管16连接，在筒体6与中间筒7之间的下部位置设置有带曝气内丝头18的环形曝气管5，环形曝气管5与进气管25连接，筒体6的下部与连接外筒放空排泥管2连接，在中心筒8中形成接触区A，在中间筒7的上部形成气浮分离区B，在中间筒7的顶部形成排渣区C，在筒体6与中心筒8之间的下部区域形成污泥沉淀区D，在筒体6与中间筒7之间的下部区域形成臭氧氧化区E。
所述筒体6的底部有底板26，顶部有顶盖11，其中，底板26设置在设备基座27上，顶盖11为锥形顶，内筒排气管12连接在顶盖11上，所述筒体6的底部为锥形排泥斗3，锥形排泥斗3锥形出口中心线上倾角为30°～45°。
所述中间筒7的上部通过浮渣导流椎体10与顶部连接，浮渣导流椎体10为锥形外扩口结构，锥形出口中心线上倾角为80°～85°，外筒排气管13连接在浮渣导流椎体10上。
所述中心筒8的顶部设置有中心筒导流斜板22，所述导流斜板22为锥形外扩口，锥形出口中心线上倾角为40°～50°。
所述筒体6上部环绕中间筒7设置有锯齿形的溢流堰19，排水管14设置在溢流堰19的底部。
所述进水管15和进水泵、混凝剂加药泵出水管相连，进水管15以切向形式向中心筒8输送原水，所述溶气进水管1的端部设置溶臭氧空气释放器21。
所述内筒排气管12和外筒排气管13通过排气三通23连接带排气电动阀24的排气总管，所述排水管14上设置有出水电动阀20，所述内筒放空排泥管16上设置有中心筒排空电动阀17，所述外筒放空排泥管2上设置有集泥斗排空电动阀28。
所述排气电动阀24、出水电动阀20、中心筒排空电动阀17和集泥斗排空 电动阀28连接时间继电器，根据设定间隔时间自动启闭。
所述进水管15和进水泵、混凝剂加药泵出水管相连。
所述筒体(6)、中间筒(7)和中心筒(8)的高度比为10：6.5～8：4～5，筒体(6)的直径、中间筒(7)的底部直径、中心筒(8)的直径为5：(3～3.5)：(1～1.5)。
所述接触区A、沉淀区D、集渣区C、臭氧氧化区E和气浮分离区B体积比为1:5:5:15:20。内筒排气管12和外筒排气管13顶部比排渣管9顶部高约0.9～1.2m。
与现有技术相比，本发明的有益效果表现在：
1、进水管切向喷口结构
本发明进水管15切向进水，提高了水力旋流强度，能增加气、固和液三相接触与混合，提高反应效率的同时增大设备容积负荷率。
2、中心筒、中间筒和筒壁复合结构
装置特征三层筒复合结构，将反应器空间区分为内、中和外三层，每一层根据水处理流程具有对应功能，互不干扰。装置整体从上到下由浮渣清除区、气浮分离区和污泥沉淀区等组成，各分区功能明确。
3、浮渣排放程序控制
臭氧气浮设备操作按顺序可分为进水、排渣、降液位、再进水等，装置进水泵、排气电动阀24、出水电动阀20由时间继电器或PLC控制。其中排气电动阀24、出水电动阀20联动控制，同时处于开或关状态。通过阀门开闭实现工作与排渣的交替运行。
4、底部沉积污泥自清渣系统
内筒和罐体底部沉积污泥，由泥水界面仪控制，在泥面接近底部高度的50％时，通过控制中心筒排空电动阀17和集泥斗排空电动阀28自动排泥。
综上，本发明改变了原有高效臭氧气浮装置依靠U形管进行多级臭氧气浮的模式，通过内、中和外三层结构的完成反应、分离、氧化和沉淀等四个过程。本发明提供的切向进水方式，进水呈旋流向上运行，使得系统能耗最低且气、 水和药剂混合均匀。本发明在投加臭氧与混凝剂后，通过混合过程均匀分布到中心筒中，完成氧化反应过程，在有机物被氧化去除的同时，悬浮物质也能被微气泡携带到顶部通过排渣管排出。
附图说明
图1是本发明复合式臭氧气浮一体化装置结构示意图。
图2是本发明中底层平面管道结构图。
图3是本发明中中层平面管道结构图。
图4是本发明中顶层平面管道结构图。
具体实施方式
下面结合附图对本发明的内容进行描述，以下的描述仅是示范性和解释性的，不应对本发明的保护范围有任何限制作用。
如图1、图2、图3和图4所示，所述系统包括壳体、进出水单元、臭氧气浮单元、臭氧氧化单元、排渣系统、排泥系统等。
壳体包括筒体6、顶盖11、底板26及设备基座27等。
进出水单元单元包括进水管15、溶气进水管1和排水管1等。
臭氧气浮单元包括中心筒8、溶臭氧空气释放器21、中间筒7等。
臭氧氧化单元包括进气管25、环形曝气管5等。
排渣系统包括内筒排气管12、外筒排气管13、排渣管9等。
排泥系统包括外筒放空排泥管2、内筒放空排泥管16等。
具体地，筒体6、中间筒7和中心筒8同轴设置，筒体6与中心筒8共底，与中间筒7共顶，中间筒7的上部通过浮渣导流椎体10与顶盖11连接，浮渣导流椎体10为锥形外扩口结构，锥形出口中心线上倾角为80°～85°。中间筒7设置在筒体6与中心筒8之间的支撑槽钢4上，支撑槽钢4起支撑作用，不影响水流通过。中心筒8顶部位于中间筒7中，且中心筒8顶部设置有中心筒导流斜板22，导流斜板22为锥形外扩口，锥形出口中心线上倾角为40°～50°。
排水管14连接在筒体6的上部，顶盖11为锥形顶，内筒排气管12连接在顶盖11的侧面，排渣管9连接在顶盖11的顶点位置，外筒排气管13连接在浮 渣导流椎体10上，筒体6的底部为锥形出口中心线上倾角为30°～45°的锥形排泥斗3，进水管15、溶气进水管1以及内筒放空排泥管16穿过锥形排泥斗3连接至中心筒8，外筒放空排泥管2连接在锥形排泥斗3底部。进气管25穿过筒体6连接环形曝气管5，环形曝气管5为耐臭氧氧化的钛合金材质，其上均匀布置有曝气内丝头18，曝气内丝头18选用钛合金曝气头，环形曝气管5环绕设置在筒体6与中间筒7之间的下部位置。
其中，筒体6上还设置有人孔，供观察反应过程使用，筒体6上部环绕中间筒7设置有锯齿形的溢流堰19，排水管14可设置在溢流堰19的底部。进水管15和进水泵、混凝剂加药泵出水管相连，以切向形式向中心筒8输送原水，溶气进水管1的端部设置溶臭氧空气释放器21，内筒放空排泥管16位于进水管15的下方位置。
内筒排气管12和外筒排气管13通过排气三通23连接带排气电动阀24的排气总管，排水管14上设置有出水电动阀20，内筒放空排泥管16上设置有中心筒排空电动阀17，外筒放空排泥管2上设置有集泥斗排空电动阀28。排气电动阀24、出水电动阀20、中心筒排空电动阀17和集泥斗排空电动阀28连接时间继电器，根据设定间隔时间自动启闭。
最终，在中心筒8中形成接触区A，在中间筒7的上部形成气浮分离区B，在中间筒7的顶部形成排渣区C，在筒体6与中心筒8之间的下部区域形成污泥沉淀区D，在筒体6与中间筒7之间的下部区域形成臭氧氧化区E。接触区A、沉淀区D、集渣区C、臭氧氧化区E和气浮分离区B体积比为1:5:5:15:20，内筒排气管12和外筒排气管13顶部比排渣管9顶部高约0.9～1.2m。
本发明臭氧气浮原理：
进水管15切向进水，进水在中心筒8狭小区域通过筒壁导流形成涡旋流。从溶气进水管1进入的混合有臭氧、空气和混凝剂的回流水与原水充分混合，混凝剂混凝捕捉悬浮颗粒，反应后通过导流斜板22进入装置上部气浮分离区。在溶臭氧空气释放器21作用下，臭氧和空气形成大量微气泡。臭氧微气泡具有巨大表面积，氧化原水中有机物。在混凝剂的催化作用下，臭氧分解产生大量 羟基自由基，能将原水中难降解有机物进一步去除。氧化产物中的一部分是疏水性物质，通过混凝气浮作用而被混凝剂絮体小颗粒捕捉得以分离。
本发明臭氧氧化原理：
臭氧通过进气管25进入环形曝气管5，曝气内丝头18进行曝气。一方面臭氧氧化区位于设备外环，虽然半径占比较小但体积占比大，较长的水力停留时间为臭氧充分反应提供了较好条件。另一方面，经过前段臭氧气浮处理，出水浊度很低，氧化单元中的臭氧主要因为去除有机物而被消耗，这就提高了臭氧利用率。
本发明排渣原理：
通过时间继电器控制出水电动阀20和排气电动阀24的启闭状态，实现液位上升与下降，保证排渣与运行的状态正常进行。
本发明排泥原理：
外筒放空排泥管2和内筒放空排泥管16连接时间继电器，根据设定间隔时间分别开闭中心筒排空电动阀17和集泥斗排空电动阀28，将锥形排泥斗3和中心筒8内积泥排出。设备内排泥液位高压差大便于积泥外排。
利用上述装置进行污水深度处理的流程如下：
1、正常运行时，出水电动阀20和排气电动阀24同时打开，中心筒排空电动阀17和集泥斗排空电动阀28同时关闭，进水管15中的原水和溶气回流管1中的溶臭氧水在中心筒8内的反应区A充分混合，溶臭氧空气释放器释放大量微小臭氧气泡。混合水向上进入气浮分离区B，浮渣在微气泡作用下上浮到集渣区C，水流固液分离后的原水向下从中心筒8和中间筒7之间转向进入氧化区E，从氧化区E顶部经锯齿形的溢流堰19流出经排水管14排出。
2、在中心筒8内，微小气泡中的臭氧氧化水中有机物，微小颗粒被混凝剂捕捉形成絮体，絮体被微气泡携带到集渣区C进行固液分离。
3、在排渣模式下，出水电动阀20和排气电动阀24同时关闭，中心筒排空电动阀17和集泥斗排空电动阀28同时关闭，装置内液位持续上升，直到将浮渣经排渣管9排出完全。此后，关闭进水泵，打开出水电动阀20和排气电动阀 24，液位持续下降到溢流堰19的槽口中心线后，打开进水泵，开始正常工作。此后，通过电动阀的启闭，实现处理与排渣的周期性运行。
4、当底部沉淀区D空间积累泥量，泥水界面上升到锥形排泥斗3深度的60％时，开启集泥斗排空电动阀28，排空锥形排泥斗3内积泥。当中心筒8底部积泥过多时，打开中心筒排空电动阀17，排出中心筒8内积泥。
综上所述，本发明通过中心筒8、中间筒7和筒体6将设备分为反应区A、气浮分离区B和臭氧氧化区E，横向布置和电动阀的组合使用，使得设备具有了高效臭氧利用、渣水高效分离和自排渣自清泥等优势。

Claims (10)

  1. 一种复合式臭氧气浮一体化装置，其特征在于，包括同轴的筒体(6)、中间筒(7)和中心筒(8)，筒体(6)与中心筒(8)共底，筒体(6)与中间筒(7)共顶，中间筒(7)设置在筒体(6)与中心筒(8)之间的支撑槽钢(4)上，中心筒(8)顶部位于中间筒(7)中，且中心筒(8)顶部敞口，筒体(6)的上部设置有排水管(14)，顶部设置有内筒排气管(12)和排渣管(9)，中间筒(7)的上部设置有外筒排气管(13)，中心筒(8)的下部与进水管(15)、溶气进水管(1)以及连接内筒放空排泥管(16)连接，在筒体(6)与中间筒(7)之间的下部位置设置有带曝气内丝头(18)的环形曝气管(5)，环形曝气管(5)与进气管(25)连接，筒体(6)的下部与连接外筒放空排泥管(2)连接，在中心筒(8)中形成接触区A，在中间筒(7)的上部形成气浮分离区B，在中间筒(7)的顶部形成排渣区C，在筒体(6)与中心筒(8)之间的下部区域形成污泥沉淀区D，在筒体(6)与中间筒(7)之间的下部区域形成臭氧氧化区E。
  2. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述筒体(6)的底部有底板(26)，顶部有顶盖(11)，其中，底板(26)设置在设备基座(27)上，顶盖(11)为锥形顶，内筒排气管(12)连接在顶盖(11)上，所述筒体(6)的底部为锥形排泥斗(3)，锥形排泥斗(3)锥形出口中心线上倾角为30°～45°。
  3. 根据权利要求1或2所述复合式臭氧气浮一体化装置，其特征在于，所述中间筒(7)的上部通过浮渣导流椎体(10)与顶部连接，浮渣导流椎体(10)为锥形外扩口结构，锥形出口中心线上倾角为80°～85°，外筒排气管(13)连接在浮渣导流椎体(10)上。
  4. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述中心筒(8)的顶部设置有中心筒导流斜板(22)，所述导流斜板(22)为锥形外 扩口，锥形出口中心线上倾角为40°～50°。
  5. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述筒体(6)上部环绕中间筒(7)设置有锯齿形的溢流堰(19)，排水管(14)设置在溢流堰(19)的底部。
  6. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述进水管(15)和进水泵、混凝剂加药泵出水管相连，进水管(15)以切向形式向中心筒(8)输送原水，所述溶气进水管(1)的端部设置溶臭氧空气释放器(21)。
  7. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述内筒排气管(12)和外筒排气管(13)通过排气三通(23)连接带排气电动阀(24)的排气总管，所述排水管(14)上设置有出水电动阀(20)，所述内筒放空排泥管(16)上设置有中心筒排空电动阀(17)，所述外筒放空排泥管(2)上设置有集泥斗排空电动阀(28)。
  8. 根据权利要求7所述复合式臭氧气浮一体化装置，其特征在于，所述排气电动阀(24)、出水电动阀(20)、中心筒排空电动阀(17)和集泥斗排空电动阀(28)连接时间继电器，根据设定间隔时间自动启闭。
  9. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述接触区A、沉淀区D、集渣区C、臭氧氧化区E和气浮分离区B体积比为1:5:5:15:20，内筒排气管12和外筒排气管13顶部比排渣管9顶部高约0.9～1.2m。
  10. 根据权利要求1所述复合式臭氧气浮一体化装置，其特征在于，所述筒体(6)、中间筒(7)和中心筒(8)的高度比为10：6.5～8：4～5，筒体(6)的直径、中间筒(7)的底部直径、中心筒(8)的直径为5：(3～3.5)：(1～1.5)。
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