CN112919612A - Rotational flow gas-liquid uniform distribution type sewage treatment device, sewage treatment system and sewage treatment method - Google Patents
Rotational flow gas-liquid uniform distribution type sewage treatment device, sewage treatment system and sewage treatment method Download PDFInfo
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- CN112919612A CN112919612A CN202110089982.6A CN202110089982A CN112919612A CN 112919612 A CN112919612 A CN 112919612A CN 202110089982 A CN202110089982 A CN 202110089982A CN 112919612 A CN112919612 A CN 112919612A
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- 239000007788 liquid Substances 0.000 title claims abstract description 162
- 239000010865 sewage Substances 0.000 title claims abstract description 140
- 238000009827 uniform distribution Methods 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 14
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 85
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 56
- 230000003647 oxidation Effects 0.000 claims abstract description 55
- 230000003197 catalytic effect Effects 0.000 claims abstract description 51
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- 239000007791 liquid phase Substances 0.000 claims abstract description 23
- 230000007246 mechanism Effects 0.000 claims abstract description 18
- 239000011148 porous material Substances 0.000 claims abstract description 16
- 230000001174 ascending effect Effects 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 86
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 239000007921 spray Substances 0.000 claims description 16
- 238000002347 injection Methods 0.000 claims description 15
- 239000007924 injection Substances 0.000 claims description 15
- 230000009471 action Effects 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
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- 239000002912 waste gas Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims 1
- 238000004065 wastewater treatment Methods 0.000 claims 1
- 238000013461 design Methods 0.000 abstract description 6
- 230000000694 effects Effects 0.000 description 24
- 239000012071 phase Substances 0.000 description 17
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical group C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 3
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- 229920002521 macromolecule Polymers 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
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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
- 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
- C02F1/006—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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- 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
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/78—Details relating to ozone treatment devices
- C02F2201/784—Diffusers or nozzles for ozonation
-
- 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
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention relates to a rotational flow gas-liquid uniform distribution type sewage treatment device, a sewage treatment system and a sewage treatment method; the device comprises a tower body, wherein the bottom of the tower body is provided with a gas-liquid inlet, the top of the tower body is provided with a sewage outlet and a tail gas outlet, a bearing pore plate is arranged in the tower body, and the bearing pore plate divides the interior of the tower body into an upper catalytic oxidation chamber and a lower gas-liquid mixing chamber; a plurality of subdivided holes are formed in the bearing orifice plate, and a rotational flow gas-liquid uniform distribution mechanism is installed in the lower gas-liquid mixing chamber; a flow baffle plate is arranged in the upper catalytic oxidation chamber, one side of the flow baffle plate is provided with a downward bent hem, two adjacent flow baffle plates are arranged in a staggered manner, the circumferential side wall of each flow baffle plate is tightly attached to the inner wall of the tower body, a liquid phase ascending channel is arranged between the hem and the inner wall of the tower body, a plurality of air holes are circumferentially distributed on each flow baffle plate at intervals, and a catalyst is filled in the upper catalytic oxidation chamber; the technical problems of low efficiency and high running cost of the catalytic oxidation of ozone existing in the prior art are solved through the design of the rotational flow gas-liquid uniform distribution type sewage treatment device.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to a rotational flow gas-liquid uniform distribution type sewage treatment device, a sewage treatment system and a sewage treatment method.
Background
In recent years, with the rapid development of cities and industries, the discharge amount of municipal and industrial sewage is increasing day by day, and great pressure is brought to the whole sewage treatment system. In order to improve the environmental water quality and reduce the water environmental pollution load, the related laws of China have put forward higher requirements on the sewage discharge standard, and the traditional sewage treatment technology is difficult to meet the requirements in the past. On the basis, new water treatment technologies such as advanced oxidation and the like are rapidly developed. As one of advanced oxidation technologies, ozone (catalytic) oxidation is widely used in the fields of municipal and industrial sewage advanced treatment, sewage recycling, high-concentration difficult biochemical sewage treatment and the like due to good treatment effect, less secondary pollution and simple and convenient operation.
However, in the practical application process, the ozone catalytic oxidation technology still has some problems: 1) ozone dissolves inefficiency, and the mass transfer effect is poor, and traditional ozone catalytic oxidation reactor is controlled in the bubble size to the influence of gas-liquid mixture effect, lacks efficient gas-liquid mixing system for the mass transfer effect is poor, and ozone utilization ratio is lower. 2) Ozone catalytic oxidation reactor structure is too simple, and the style is single, and except basic gas-liquid redistribution (supporting) device, catalyst filling mode is simple gravity type and piles up, and because the existence of "wall flow" effect and gaseous "short circuit" phenomenon leads to the gas-liquid contact time short in the reaction process, and area of contact is abundant inadequately to make catalyst result of use relatively poor, catalytic oxidation is efficient, and the running cost is higher.
Chinese patent CN203625104U discloses an oil refining sewage ozone catalytic oxidation advanced treatment device, which adopts two catalytic oxidation towers connected in series. The first catalytic oxidation tower adopts high pressure, and the second adopts the ordinary pressure, mainly degrades macromolecule organic matter into the micromolecule through high pressure, high concentration ozone earlier, and reuse low pressure, low concentration ozone carry out the secondary oxidation, improves ozone dissolution, mass transfer efficiency through high pressure, high concentration ozone promptly to thereby improve catalytic oxidation efficiency through two towers series connection improvement gas-liquid contact time. The method can improve the treatment effect of pollutants to a certain extent, but the improvement of the ozone utilization rate is not obvious, the equipment investment and the operation cost are high, the operation is complex, and the method is not suitable for engineering application.
Chinese patent CN209922993U discloses an ozone advanced oxidation device, which adopts a separately arranged generation box to mix gas and liquid. The sewage to be treated pressurized by the high-pressure water pump enters the negative pressure oxidation area through the jet flow plate at a high speed, the generated negative pressure sucks ozone and finishes mixing, and then the ozone passes through the overflowing hole at a high speed, when the pressure suddenly decreases to reach a vapor pressure or even a negative value, partial vacuum is formed, the dissolved gas is released, and meanwhile, the fluid is vaporized. A large amount of bubbles are rapidly collapsed in a pressure stabilizing area, and the generated local high temperature and high pressure ensure that a large amount of ozone is converted into hydroxyl free radicals and pollutants are oxidized. The process is essentially characterized in that the mass transfer and reaction rate is improved by utilizing the hydrodynamic cavitation effect, but the hydrodynamic cavitation equipment has higher investment cost, huge operation energy consumption and over harsh cavitation conditions, and the ideal cavitation effect is difficult to realize in engineering application.
Therefore, in order to solve the above problems, the present invention provides a cyclone gas-liquid uniform distribution type sewage treatment device, a sewage treatment system and a sewage treatment method.
Disclosure of Invention
The invention aims to provide a rotational flow gas-liquid uniform distribution type sewage treatment device, a sewage treatment system and a sewage treatment method, and the technical problems of low ozone catalytic oxidation efficiency and high operation cost in the prior art are solved through the design of the rotational flow gas-liquid uniform distribution type sewage treatment device.
The invention provides a rotational flow gas-liquid uniform distribution type sewage treatment device, which comprises a tower body, wherein a gas-liquid inlet is formed in the bottom of the tower body, a sewage outlet and a tail gas outlet are formed in the top of the tower body, a bearing pore plate is arranged in the tower body, and the bearing pore plate divides the interior of the tower body into an upper catalytic oxidation chamber and a lower gas-liquid mixing chamber; a plurality of sub-divided holes are uniformly distributed on the bearing orifice plate, and a rotational flow gas-liquid uniform distribution mechanism communicated with a gas-liquid inlet is arranged in the lower gas-liquid mixing chamber; the upper catalytic oxidation cavity is internally and longitudinally provided with a plurality of flow baffle plates at intervals, one side of each flow baffle plate is provided with a folded edge which is bent downwards, two adjacent flow baffle plates are arranged in a staggered manner, the circumferential side wall of each flow baffle plate is tightly attached to the inner wall of the tower body, a liquid phase ascending channel is arranged between each folded edge and the inner wall of the tower body, a plurality of air holes are arranged on each flow baffle plate at intervals in the circumferential direction, the upper catalytic oxidation cavity is internally filled with a catalyst, and the filling height of the catalyst is higher than the mounting height of the flow.
Furthermore, the flow baffle is circular, and the aperture ratio is 0.5-5%; the distance between two adjacent flow baffles is 20-100 cm; the diameter of the air hole on each flow baffle is 1-6 mm; the cross section area of the flow baffle plate accounts for 80-89% of the cross section area of the catalytic oxidation chamber; the height of the folded edge is 1-10 cm.
Further, the rotational flow gas-liquid uniform distribution mechanism comprises a gas-liquid conveying pipe communicated with a gas-liquid inlet, a plurality of transversely-arranged injection pipes are arranged at the top of the gas-liquid conveying pipe at intervals in the circumferential direction, each injection pipe is communicated with the gas-liquid conveying pipe, a plurality of gas-liquid spray holes are arranged at intervals along the length direction of each injection pipe, and the gas-liquid spray holes are arranged obliquely downwards and form an included angle of 0-45 degrees with the horizontal plane.
Furthermore, the diameter of the gas-liquid spray holes is 1-10mm, and the distance between two adjacent gas-liquid spray holes is 4-20 cm.
Further, the diameter of the subdivided pores is 1-8 mm.
Furthermore, the aperture ratio of the bearing orifice plate is 1-10%.
Furthermore, the bottom of the tower body is also provided with an emptying hole, the emptying hole is connected with an emptying pipe, and the emptying pipe is communicated with a ball valve; the sewage outlet is communicated with the water outlet pipe.
The invention also provides a sewage treatment system which comprises an ozone source, a sewage regulating tank, a jet mixer, the rotational flow gas-liquid uniform distribution type sewage treatment device and an ozone tail gas processor, wherein the rotational flow gas-liquid uniform distribution type sewage treatment device is arranged at the bottom of the sewage regulating tank; wherein, the gas-liquid import of tower body passes through the gas-liquid export intercommunication of pipeline with jet mixer, and jet mixer's air inlet passes through pipeline and ozone gas source intercommunication, and jet mixer's inlet and sewage equalizing basin intercommunication, intercommunication have the sewage pump between sewage equalizing basin and jet mixer, and the tail gas export passes through pipeline and ozone tail gas treater intercommunication.
Furthermore, a flow regulating valve and a check valve are communicated on a pipeline for communicating the ozone source and the jet flow mixer.
The invention also provides a sewage treatment method based on the sewage treatment system, which comprises the following steps:
the sewage pump conveys the sewage in the sewage adjusting tank to the jet flow mixer, the ozone gas source generates ozone, the ozone is conveyed to the jet flow mixer through a pipeline, and the sewage and the ozone are mixed in the jet flow mixer to obtain mixed gas-liquid;
the jet mixer conveys mixed gas and liquid from a gas-liquid inlet of the tower body to the rotational flow gas-liquid uniform distribution mechanism through a pipeline, and the rotational flow gas-liquid uniform distribution mechanism uniformly mixes ozone and sewage in the lower gas-liquid mixing chamber and rises in a vortex manner;
the mixed gas and liquid enter the upper catalytic oxidation chamber after passing through the subdivided holes of the bearing pore plate, gas and liquid contact reaction is carried out under the action of a catalyst, unreacted gas is gathered below the flow baffle plate to form an air cushion layer under the action of the flow baffle plate and the folded edge, the gas cushion layer continuously diffuses upwards through the air holes arranged on the flow baffle plate, and the liquid phase is limited by the air cushion layer and transversely flows between two adjacent flow baffle plates; and enters the upper layer from the liquid phase ascending channel at one side, and continuously contacts and reacts with ozone under the action of a catalyst; the treated sewage is discharged through a water outlet pipe, and the waste gas enters an ozone tail gas processor through a tail gas outlet.
Compared with the prior art, the rotational flow gas-liquid uniform distribution type sewage treatment device provided by the invention has the following advantages:
1. according to the rotational flow gas-liquid uniform distribution type sewage treatment device provided by the invention, ozone and sewage can be uniformly distributed at the bottom of the lower gas-liquid mixing chamber in the tower body through the action of the rotational flow gas-liquid uniform distribution mechanism, an ascending rotational flow is formed, the gas-liquid uniform distribution effect is improved, the jet flow mixing effect is very excellent, and the shearing force of high-speed liquid flow can even control the bubble size to be in a micron order; under the same gas-water flow, the faster the rotational flow speed is, the more uniform the distribution of the mixed gas-liquid is, and the higher the gas-phase dissolution efficiency is; meanwhile, the rotational flow action prolongs the diffusion path of the gas phase in the reactor, increases the contact time of the gas phase and the liquid phase, and improves the gas phase dissolution efficiency.
2. The rotational flow gas-liquid uniform distribution type sewage treatment device provided by the invention is circular through the flow baffle; the distance between two adjacent flow baffles is 20-100 cm; the diameter of the air hole on each flow baffle is 1-6 mm; the cross section area of the flow baffle accounts for 80-89% of that of the catalytic oxidation chamber, so that gas-liquid two phases are fully contacted, and the sewage treatment effect is improved; through the low aperture ratio of the baffle plate and the arrangement of the hems, an air cushion layer can be formed below the baffle plate, so that the flow direction control of a liquid phase is realized, the liquid phase is guided to flow upwards in the reactor in a baffling manner, an ascending gas phase enters the air cushion layer and then re-enters the catalyst bed layer above the reactor through the redistribution of air holes in the baffle plate, after multi-stage baffling, multi-stage cross flow contact of gas and liquid phases is realized, and the ozone utilization rate and the ozone catalytic oxidation effect are greatly improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural view (front view) of the cyclone gas-liquid uniform distribution type sewage treatment device in the present invention;
FIG. 2 is a schematic structural view (top view) of the swirling flow gas-liquid uniform distribution mechanism in the present invention;
FIG. 3 is a schematic structural view (top view) of the baffle plate of the present invention;
FIG. 4 is a schematic view (front view) of the sewage treatment system according to the present invention.
Description of reference numerals:
1. a tower body; 101. a gas-liquid inlet; 102. a sewage outlet; 103. a tail gas outlet; 104. an upper catalytic oxidation chamber; 105. a lower gas-liquid mixing chamber; 2. a jet mixer; 3. a source of ozone; 4. a sewage adjusting tank; 5. supporting the orifice plate; 6. a rotational flow gas-liquid uniform distribution mechanism; 61. a gas-liquid delivery pipe; 62. an injection pipe; 621. gas-liquid spraying holes; 7. a flow baffle plate; 8. a liquid phase rising channel; 9. folding edges; 10. air holes; 11. emptying the pipe; 12. a ball valve; 13. a sewage pump; 14. a catalyst; 15. a flow regulating valve; 16. emptying holes; 17. an ozone tail gas processor; 18. a water outlet pipe; 19. a pressure gauge; 20. a safety valve; 21. a check valve.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the accompanying drawings, and it should be understood that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
As shown in fig. 1, 2, and 3, the rotational flow gas-liquid uniform distribution type sewage treatment device in this embodiment includes a tower body 1, a gas-liquid inlet 101 is disposed at the bottom of the tower body 1, a sewage outlet 102 and a tail gas outlet 103 are disposed at the top of the tower body 1, a support orifice plate 5 is disposed in the tower body 1, and the interior of the tower body 1 is divided into an upper catalytic oxidation chamber 104 and a lower gas-liquid mixing chamber 105 by the support orifice plate 5; a plurality of subdivided holes are uniformly distributed on the bearing orifice plate 5, and a rotational flow gas-liquid uniform distribution mechanism 6 communicated with a gas-liquid inlet 101 is arranged in the lower gas-liquid mixing chamber 105; a plurality of flow baffle plates 7 are longitudinally arranged in the upper catalytic oxidation chamber 104 at intervals, one side of each flow baffle plate 7 is provided with a folded edge 9 which is bent downwards, two adjacent flow baffle plates 7 are arranged in a staggered manner, the circumferential side wall of each flow baffle plate 7 is tightly attached to the inner wall of the tower body 1, a liquid phase ascending channel 8 is arranged between each folded edge 9 and the inner wall of the tower body 1, a plurality of air holes 10 are circumferentially arranged on each flow baffle plate 7 at intervals, the upper catalytic oxidation chamber 104 is filled with a catalyst 14, and the filling height of the catalyst 14 is higher than the mounting height of the flow baffle plate 7 which is close to the.
The invention provides a rotational flow gas-liquid uniform distribution type sewage treatment device, wherein a gas-liquid inlet 101 is formed in the bottom of a tower body 1, a sewage outlet 102 and a tail gas outlet 103 are formed in the top of the tower body 1, a bearing pore plate 5 is arranged in the tower body 1, and the bearing pore plate 5 divides the interior of the tower body 1 into an upper catalytic oxidation chamber 104 and a lower gas-liquid mixing chamber 105; a plurality of subdivided holes (not shown in the figure and not described in detail herein for the prior art) are uniformly distributed on the bearing orifice plate 5, and a rotational flow gas-liquid uniform distribution mechanism 6 communicated with a gas-liquid inlet 101 is installed in the lower gas-liquid mixing chamber 105; a plurality of flow baffle plates 7 are longitudinally distributed in the upper catalytic oxidation chamber 104 at intervals, one side of each flow baffle plate 7 is provided with a downward bent hem 9, two adjacent flow baffle plates 7 are arranged in a staggered manner, the circumferential side wall of each flow baffle plate 7 is tightly attached to the inner wall of the tower body 1, a liquid phase ascending channel 8 is arranged between each hem 9 and the inner wall of the tower body 1, namely, a liquid phase ascending channel is arranged between one side of the hem opposite to the inner wall of the tower body 1 and the inner wall of the tower body 1, a plurality of air holes 10 are distributed on each flow baffle plate 7 at intervals in the circumferential direction, a catalyst 14 is also filled in the upper catalytic oxidation chamber 104, the filling height of the catalyst 14 is higher than the mounting height of the flow baffle plate 7 close to the top of the tower body 1, gas and liquid entering from a gas-liquid inlet 101 enter a lower gas-liquid mixing chamber 105 through a rotational flow, the mixed gas and liquid enters the upper catalytic oxidation chamber 104 through the subdivided holes of the bearing orifice plate 5, and catalytic oxidation treatment on the sewage is realized under the action of the catalyst 14, the baffle plate 7 and the folded plate 9. Limited by the low aperture ratio of the baffle plate 7, the gas which is not completely reacted is gathered on the lower plate surface of the baffle plate 7 to form a gas cushion layer, thereby stopping the longitudinal rising of the sewage to be treated, enabling the sewage between two adjacent flow baffles to move transversely and rise from the liquid phase rising channel 8 on one side, further contact with the catalyst 14 on the upper layer, the gas which is not completely reacted slowly diffuses into the gap of the catalyst 14 on the upper layer from the air hole 10 to continuously perform catalytic oxidation on the sewage, the two adjacent baffle plates 7 are arranged in a staggered way, the sewage to be treated is baffled and ascended in the upper catalytic oxidation chamber 104, the contact area and time of gas phase and liquid phase are increased, thereby improving the dissolving effect of the ozone, greatly improving the catalytic oxidation effect of the ozone catalyst, thereby achieving the purposes of improving the sewage treatment effect, reducing the energy consumption and reducing the sewage treatment cost.
The catalyst is a mesoporous carbon-based ozone catalyst; the included angle between the baffle plate 7 and the folded edge 9 is 90 degrees.
As shown in fig. 3, the baffle plate 7 of the present embodiment is circular, and the aperture ratio is 0.5-5%; the distance between two adjacent flow baffles 7 is 20-100 cm; the diameter of the air hole 10 on each flow baffle 7 is 1-6 mm; the cross section area of the baffle plate 7 accounts for 80-89% of the cross section area of the upper catalytic oxidation chamber 104; the height of the folded edge 9 is 1-10 cm.
According to the invention, the flow baffle 7 is circular, and the aperture ratio is 0.5-5%; the distance between two adjacent flow baffles 7 is 20-100 cm; the diameter of the air hole 10 on each flow baffle 7 is 1-6 mm; the cross section area of the baffle plate 7 accounts for 80-89% of the cross section area of the upper catalytic oxidation chamber 104; the design that the height of hem 9 is 1-10cm can form the air cushion layer below the baffle 7 to realize the flow direction control to the liquid phase, guide the liquid phase baffling to rise in the reactor, and the gas phase that rises gets into air cushion layer and redistributes through the gas hole 10 on the baffle 7 and reentries the catalyst bed layer of top, after multistage baffling, multistage cross-flow contact is realized to gas-liquid two-phase, improves ozone utilization ratio and ozone catalytic oxidation effect by a wide margin.
As shown in fig. 2, the swirling flow gas-liquid distribution mechanism 6 of the present embodiment includes a gas-liquid delivery pipe 61 communicated with a gas-liquid inlet 101, a plurality of transversely arranged injection pipes 62 are circumferentially arranged at intervals at the top of the gas-liquid delivery pipe 61, each injection pipe 62 is communicated with the gas-liquid delivery pipe 61, a plurality of gas-liquid injection holes 621 are arranged at intervals along the length direction of the injection pipe 62, and the gas-liquid injection holes 621 are arranged obliquely downward, and form an included angle of 0 ° to 45 ° with the horizontal plane.
According to the invention, the rotational flow gas-liquid uniform distribution mechanism 6 comprises a gas-liquid conveying pipe 61 communicated with a gas-liquid inlet 101, a plurality of transversely distributed injection pipes 62 are distributed at intervals in the circumferential direction at the top of the gas-liquid conveying pipe 61, each injection pipe 62 is communicated with the gas-liquid conveying pipe 61, a plurality of gas-liquid spray holes 621 are distributed at intervals along the length direction of each injection pipe 62, the gas-liquid spray holes 621 are arranged obliquely downwards, and the included angle between each gas-liquid spray hole 621 and the horizontal plane is 0-45 degrees, so that gas-liquid two phases are uniformly mixed at the bottom of a lower gas-liquid mixing chamber 105, an ascending; the jet mixing effect is very excellent, and the shearing force of the high-speed liquid flow can even control the bubble size to be in a micron level; under the same gas-water flow, the faster the rotational flow speed is, the more uniform the distribution of the mixed gas-liquid is, and the higher the gas-phase dissolution efficiency is; meanwhile, the rotational flow action prolongs the diffusion path of the gas phase in the reactor, increases the contact time of the gas phase and the liquid phase, and improves the gas phase dissolution efficiency.
The diameter of the gas-liquid spray holes 621 is 1-10mm, preferably, the diameter of the gas-liquid spray holes 621 is 6.0mm, the distance between two adjacent gas-liquid spray holes 621 is 4-20cm, preferably, the distance between two adjacent gas-liquid spray holes 621 is 10.0 cm; the flow velocity of the mixed gas and liquid is ensured to meet the rotational flow requirement, and the uniform distribution is realized at the bottom of the lower gas and liquid mixing cavity 105.
The diameter of the subdivided holes is 1-8.0 mm; the design that the aperture ratio of the supporting pore plate 5 is 1-10% enables the mixed gas and liquid in the lower gas-liquid mixing chamber 105 to uniformly pass through the supporting pore plate 5 and perform catalytic oxidation reaction under the action of the upper catalyst 14.
The diameter of the subdivided pores in this embodiment is preferably 8.0 mm; the aperture ratio of the supporting orifice 5 is 4.2%.
As shown in fig. 1, the bottom of the tower body 1 of the embodiment is further provided with an evacuation hole 16, the evacuation hole 16 is connected with an evacuation pipe 11, and the evacuation pipe 11 is communicated with a ball valve 12; the waste water outlet 102 communicates with the outlet pipe 18.
The bottom of the tower body 1 is also provided with an emptying hole 16, the emptying hole 16 is connected with an emptying pipe 11, and the emptying pipe 11 is communicated with a ball valve 12; the waste outlet 102 is in communication with the outlet pipe 18 and is configured to be shut down for cleaning and maintenance, and the ball valve 12 is opened for emptying.
The invention also provides a sewage treatment system, which comprises an ozone source 3, a sewage regulating tank 4, a jet mixer 2, a rotational flow gas-liquid uniform distribution type sewage treatment device and an ozone tail gas processor 17, wherein the rotational flow gas-liquid uniform distribution type sewage treatment device is arranged at one side of the ozone source; wherein, the gas-liquid inlet 101 of the tower body 1 is communicated with the gas-liquid outlet of the jet mixer 2 through a pipeline, the gas inlet of the jet mixer 2 is communicated with the ozone gas source 3 through a pipeline, the liquid inlet of the jet mixer 2 is communicated with the sewage adjusting tank 4, a sewage pump 13 is communicated between the sewage adjusting tank 4 and the jet mixer 2, and the tail gas outlet 103 is communicated with the ozone tail gas processor 17 through a pipeline.
The device comprises an ozone source 3, a sewage adjusting tank 4, a jet mixer 2, a rotational flow gas-liquid uniform distribution type sewage treatment device and an ozone tail gas processor 17, wherein the rotational flow gas-liquid uniform distribution type sewage treatment device comprises a gas-liquid uniform distribution type sewage treatment device and a gas-liquid uniform distribution type ozone tail gas processor; wherein, the gas-liquid import 101 of tower body 1 passes through the gas-liquid export intercommunication of pipeline with jet mixer 2, the air inlet of jet mixer 2 passes through pipeline and ozone gas source 3 intercommunication, the inlet of jet mixer 2 and sewage equalizing basin 4 intercommunication, it has sewage pump 13 to communicate between sewage equalizing basin 4 and jet mixer 2, tail gas export 103 passes through the design of pipeline and ozone tail gas treater 17 intercommunication, can realize the catalytic oxidation treatment to sewage, and improve the sewage treatment effect, reduce energy consumption and sewage treatment cost.
The ozone tail gas treater/ozone tail gas destructor manufactured by Qingdao national forest environmental protection science and technology corporation is selected as the ozone tail gas treater of the invention, and other models of other brands can be selected as well, are not marked in the figure and are the existing devices, and are not described again.
As shown in fig. 4, the ozone source 3 and the jet mixer 2 of the present embodiment are connected to a line which is also connected to a flow control valve 15 and a check valve 18.
According to the ozone water supply device, the ozone flow can be flexibly adjusted by communicating the flow adjusting valve 15 and the check valve 18 with the pipeline communicated with the ozone gas source 3 and the jet flow mixer 2, the running cost is reduced to the maximum extent while the effluent water is ensured to reach the standard when the inflow water fluctuates, and the liquid can be effectively prevented from flowing backwards after the gas source equipment fails by virtue of the design of the check valve 16.
The top of the tower body 1 is also provided with a pressure gauge 19 and a safety valve 20, so that the internal pressure of the tower body 1 is monitored in real time, the excessive internal pressure of the tower body 1 is avoided, and the safe production is ensured.
The invention also provides a sewage treatment method based on the sewage treatment system, which comprises the following steps:
s1) the sewage pump 13 conveys the sewage in the sewage adjusting tank 4 to the jet flow mixer 2, the ozone gas source 3 generates ozone, the ozone is conveyed to the jet flow mixer 2 through a pipeline, and the sewage and the ozone are mixed in the jet flow mixer 2 to obtain mixed gas-liquid;
s2) the jet flow mixer 2 conveys the mixed gas and liquid from the gas and liquid inlet 101 of the tower body 1 to the rotational flow gas and liquid uniform distribution mechanism 6 through a pipeline, and the rotational flow gas and liquid uniform distribution mechanism 6 uniformly mixes the ozone and the sewage in the lower gas and liquid mixing chamber 105 and rises in a vortex manner;
s3) mixed gas and liquid enter the upper catalytic oxidation chamber 104 after passing through the subdivided holes of the bearing orifice plate 5, gas and liquid contact reaction is carried out under the action of the catalyst 14, unreacted gas is gathered under the flow baffle plate 7 to form a gas cushion layer under the action of the flow baffle plate 7 and the folded edge 9, and the gas continues to diffuse upwards through the gas holes 10 arranged on the flow baffle plate 7; the liquid phase is limited by the gas cushion layer, flows transversely between two adjacent flow baffles 7, enters the upper layer from the liquid phase ascending channel 8 at one side, and continuously reacts with ozone in a contact way under the action of the catalyst 14; the treated sewage is discharged through the water outlet pipe 18, and the waste gas enters the ozone tail gas processor 17 after passing through the tail gas outlet 103.
The sewage treatment system provided by the invention and a conventional upward flow catalytic oxidation reactor (HT type) are studied to meet the discharge requirement, mesoporous carbon-based ozone catalysts are filled in the sewage treatment system provided by the invention and the conventional upward flow catalytic oxidation reactor, the hydraulic retention time is 1h, the ozone adding amount is 600mg/L, four baffle plates 7 are arranged in the tower body 1, the distance between two adjacent baffle plates 7 is 0.3m, the COD of the treated sewage is 416mg/L and is lower than 500mg/L, the discharge requirement is met, and the specific numerical value is shown in Table 1.
By adopting the sewage treatment system, the gas-liquid distribution effect is good, and the size of the bubbles formed by shearing the gas phase by the high-speed liquid flow in the jet flow mixer 2 is between 200 and 400 mu m; after the mixed gas and liquid is sprayed out through the gas-liquid spray holes 621, obvious rotational flow is formed at the bottom of the tower body 1, the rotational flow speed is close to 2m/s, the local gas and liquid phases even reach an emulsified state, and the ozone dissolving efficiency is greatly improved; the ascending gas phase forms air cushion layers with different thicknesses of about 3-5cm below each layer of flow baffle 7, and the gas phase redistribution effect through the gas-liquid jet holes 621 is good. From the experimental results in table 1, compared with the conventional upflow catalytic oxidation reactor, under the same conditions, the sewage treatment system provided by the invention has a better sewage treatment effect, the COD removal rate is increased by nearly 39%, the ozone utilization rate is greatly increased, and the purpose of improving the sewage treatment effect is achieved while the treatment requirements of the enterprise are met.
The sewage treatment system is adopted to treat MBR effluent of a domestic sewage plant, the COD of the MBR effluent is 30-40mg/L, and the discharge requirement is that the COD of the MBR effluent is not higher than 20 mg/L; in order to meet the discharge requirement, the sewage treatment system and the conventional upflow catalytic oxidation reactor provided by the invention are examined, mesoporous carbon-based ozone catalysts are filled, the hydraulic retention time is 20min, the ozone adding amount is 25mg/L, and the test results are shown in Table 2.
From the experimental results shown in table 2, compared with the conventional upflow catalytic oxidation reactor, under the same conditions, the municipal sewage treatment effect of the sewage treatment system provided by the invention is better, the COD removal rate is improved by about 31%, the ozone utilization rate is greatly improved, and the discharge requirement of the sewage plant is met.
The sewage treatment system provided by the invention is adopted to treat the DF concentrated water of the domestic sewage plant, the COD of the DF concentrated water is 100-120mg/L, the DF concentrated water is required to be treated to be below 60mg/L and is mixed with DF produced water to be discharged, and the sewage treatment system and the conventional upward flow catalytic oxidation reactor provided by the invention are respectively considered on site. The hydraulic retention time of the two groups of experiments is 1h, and the ozone adding amount is 70 mg/L. The test data are shown in Table 3.
According to the experimental results shown in Table 3, the concentrated water treatment effect of the sewage treatment system provided by the invention under the same conditions is better than that of the conventional upflow catalytic oxidation reactor, the COD removal rate is improved by about 25%, the ozone utilization rate is improved, and the treatment result meets the requirements of the sewage plant.
TABLE 1 comparison of the results of sewage treatment in spinning production of a certain enterprise
TABLE 2 MBR effluent treatment results comparison in domestic sewage plants
TABLE 3 comparison of DF concentrated Water treatment results in domestic Sewage plants
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. The utility model provides a whirl gas-liquid equipartition formula sewage treatment plant which characterized in that: the device comprises a tower body (1), wherein a gas-liquid inlet (101) is formed in the bottom of the tower body (1), a sewage outlet (102) and a tail gas outlet (103) are formed in the top of the tower body (1), a bearing pore plate (5) is arranged in the tower body (1), and the bearing pore plate (5) divides the interior of the tower body (1) into an upper catalytic oxidation chamber (104) and a lower gas-liquid mixing chamber (105); a plurality of subdivided holes are uniformly distributed on the bearing pore plate (5), and a rotational flow gas-liquid uniform distribution mechanism (6) communicated with a gas-liquid inlet (101) is arranged in the lower gas-liquid mixing chamber (105); go up in catalytic oxidation chamber (104) longitudinal interval and laid a plurality of fender and flow board (7), keep off and flow board (7) one side and be equipped with hem (9) of buckling downwards, two adjacent fender and flow board (7) dislocation set, keep off and flow board (7) circumference lateral wall and tower body (1) inner wall and closely laminate, be equipped with liquid phase rising channel (8) between hem (9) and tower body (1) inner wall, a plurality of gas pockets (10) have been laid to circumference interval on each fender and flow board (7), it has catalyst (14) still to fill in catalytic oxidation chamber (104), catalyst (14) packing height is higher than with tower body (1) top next-door neighbour keep off and flow board (7) mounting height.
2. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 1, which is characterized in that: the flow baffle (7) is round, and the aperture ratio is 0.5-5%; the distance between two adjacent flow baffles (7) is 20-100 cm; the diameter of the air hole (10) on each flow baffle (7) is 1-6 mm; the cross section area of the flow baffle plate (7) accounts for 80-89% of the cross section area of the upper catalytic oxidation chamber (104); the height of the folded edge (9) is 1-10 cm.
3. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 2, wherein: the rotational flow gas-liquid uniform distribution mechanism (6) comprises a gas-liquid conveying pipe (61) communicated with a gas-liquid inlet (101), a plurality of transversely-distributed injection pipes (62) are arranged at the top of the gas-liquid conveying pipe (61) at intervals in the circumferential direction, each injection pipe (62) is communicated with the gas-liquid conveying pipe (61), a plurality of gas-liquid spray holes (621) are arranged at intervals along the length direction of each injection pipe (62), and the gas-liquid spray holes (621) are arranged obliquely downwards and form an included angle of 0-45 degrees with the horizontal plane.
4. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 3, wherein: the diameter of the gas-liquid spray hole (621) is 1-10 mm; the distance between two adjacent gas-liquid spray holes (621) is 4-20 cm.
5. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 4, wherein: the diameter of the subdivided pores is 1-8 mm.
6. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 5, wherein: the aperture ratio of the bearing orifice plate (5) is 1-10%.
7. The cyclone gas-liquid uniform distribution type sewage treatment device according to claim 6, wherein: the bottom of the tower body (1) is also provided with an emptying hole (16), the emptying hole (16) is connected with an emptying pipe (11), and the emptying pipe (11) is communicated with a ball valve (12); the sewage outlet (102) is communicated with the water outlet pipe (18).
8. A sewage treatment system is characterized in that: comprises an ozone source (3), a sewage adjusting tank (4), a jet mixer (2), a rotational flow gas-liquid uniform distribution type sewage treatment device as claimed in any one of claims 1-7 and an ozone tail gas treater (17); wherein, the gas-liquid export intercommunication of gas-liquid import (101) through pipeline and jet mixer (2) of tower body (1), the air inlet of jet mixer (2) passes through pipeline and ozone source (3) intercommunication, the inlet and the sewage equalizing basin (4) intercommunication of jet mixer (2), intercommunication has sewage pump (13) between sewage equalizing basin (4) and jet mixer (2), tail gas export (103) are through pipeline and ozone tail gas treater (17) intercommunication.
9. The wastewater treatment system according to claim 8, wherein: the pipeline for communicating the ozone source (3) and the jet flow mixer (2) is also communicated with a flow regulating valve (15) and a check valve (18).
10. A sewage treatment method based on the sewage treatment system according to claim 8 or 9, characterized in that: the method comprises the following steps:
the sewage pump (13) conveys the sewage in the sewage adjusting tank (4) to the jet flow mixer (2), the ozone source (3) generates ozone, the ozone is conveyed to the jet flow mixer (2) through a pipeline, and the sewage and the ozone are mixed in the jet flow mixer (2) to obtain mixed gas-liquid;
the jet flow mixer (2) conveys mixed gas and liquid from a gas-liquid inlet (101) of the tower body (1) to the rotational flow gas-liquid uniform distribution mechanism (6) through a pipeline, and the rotational flow gas-liquid uniform distribution mechanism (6) uniformly mixes ozone and sewage in the lower gas-liquid mixing chamber (105) and rises in a vortex manner;
mixed gas and liquid enter an upper catalytic oxidation chamber (104) after passing through subdivided holes of a bearing pore plate (5), gas and liquid contact reaction is carried out under the action of a catalyst (14), unreacted gas is gathered under a flow baffle plate (7) to form an air cushion layer under the action of the flow baffle plate (7) and a folded edge (9), and the gas continues to diffuse upwards through air holes (10) arranged on the flow baffle plate (7); the liquid phase is limited by the gas cushion layer, flows transversely between two adjacent flow baffles (7), enters the upper layer from the liquid phase ascending channel (8) on one side, and continues to contact and react with ozone under the action of the catalyst (14); the treated sewage is discharged through a water outlet pipe (18), and the waste gas enters an ozone tail gas processor (17) through a tail gas outlet (103).
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