CN119118448A - A green and low-carbon garbage leachate concentrate treatment system and method - Google Patents

A green and low-carbon garbage leachate concentrate treatment system and method Download PDF

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Publication number
CN119118448A
CN119118448A CN202411541659.8A CN202411541659A CN119118448A CN 119118448 A CN119118448 A CN 119118448A CN 202411541659 A CN202411541659 A CN 202411541659A CN 119118448 A CN119118448 A CN 119118448A
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ozone
catalytic
oxidation reaction
reaction tower
rods
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CN119118448B (en
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赵义武
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Xuanang Ecological Environment Construction Co ltd
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Xuanang Ecological Environment Construction Co ltd
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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
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F1/5281—Installations for water purification using chemical agents
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • 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
    • 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
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/06—Contaminated groundwater or leachate
    • 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
    • C02F2201/782—Ozone generators
    • 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
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • 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]
    • 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
    • C02F2301/04—Flow arrangements
    • C02F2301/046—Recirculation with an external loop
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/02—Specific form of oxidant
    • C02F2305/023—Reactive oxygen species, singlet oxygen, OH radical

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

The invention relates to a treatment system of green low-carbon landfill leachate concentrated solution, which comprises a flocculation sedimentation tank, a sand filter and an ozone advanced oxidation device which are sequentially connected, wherein the concentrated solution of landfill leachate firstly enters the flocculation sedimentation tank, is subjected to dosing flocculation sedimentation, then enters the sand filter, the effluent of the sand filter enters the ozone advanced oxidation device for treatment and is discharged, the ozone advanced oxidation device comprises an oxidation reaction tower, an atomization spraying device is arranged in the tower, a film hanging catalysis device is arranged below the atomization spraying device, the atomization spraying device sprays the inflow water downwards in the form of mist droplets to react with continuous phase ozone, the film hanging catalysis device comprises a plurality of catalysis rods, ozone catalyst coatings are coated on the surfaces of the catalysis rods, and the fallen water droplets form a liquid film on the catalysis rods and are further subjected to catalytic degradation. The invention uses continuous ozone gas phase to contact with discontinuous waste water liquid drop, improves gas-liquid mass transfer coefficient and oxidation efficiency, and improves ozone utilization rate and oxidation effect.

Description

Treatment system and method for green low-carbon landfill leachate concentrated solution
Technical Field
The invention relates to the technical field of environmental protection, in particular to a system and a method for treating green low-carbon landfill leachate concentrate.
Background
Domestic garbage can generate a large amount of percolate in landfill, incineration and other treatment processes, the current garbage percolate treatment generally adopts a technical mode of front-end biochemical and rear-end double-membrane treatment, and a certain amount of concentrated solution (nanofiltration concentrated solution and reverse osmosis concentrated solution) is generated in the rear-end treatment process, and the concentrated solution is required to be further treated. However, the concentrated solution of landfill leachate is still a polluted wastewater which is high in salt content, high in organic matter content and difficult to degrade, and is difficult to treat by biochemical and common physicochemical methods, so that the concentrated solution has become a great problem in the current garbage disposal process. Ozone has higher oxidation potential (2.07V) in a standard state, is a common oxidant, and can generate more oxidizing substances such as hydroxyl radicals (OH) and the like than ozone after being decomposed in water, so that organic pollutants in the water can be effectively removed. Hydroxyl free radical (OH) is used as a non-selective strong oxidant, the oxidation potential is 2.8V, the reaction rate constant of the oxidation reaction between the hydroxyl free radical and organic molecules can reach 10 6-109L·mol-1·s-1, and a plurality of organic pollutants which are difficult to biochemically degrade can be effectively removed through the oxidation of the OH. Although the ozone advanced oxidation technology is generally applied, has the advantages of convenient application, no secondary pollution, good oxidation effect and the like, in the practical application process, the technical problems of low ozone utilization rate and poor waste water oxidation effect still exist.
The reaction of ozone gas and pollutant in waste water belongs to a gas-liquid two-phase reaction system. At present, a bubbling reaction tower (a bubbling reaction tank) and a filler reactor are two main types of ozone oxidation reactors, and the reactors are mainly used for promoting the effects of gas-liquid mass transfer and reaction by controlling the size of ozone gas bubbles and selecting proper fillers. But is limited by the defect that the mass transfer rate of pollutant in a continuous liquid phase is not high, the reaction efficiency of the existing reactor is further improved, a novel reaction contact mode needs to be explored, a breakthrough is expected to be obtained in the mass transfer rate, a novel high-efficiency reactor is developed on the basis, the ozone oxidation efficiency is further exerted, and the improvement of the treatment effect of the whole landfill leachate treatment process is of key significance.
Disclosure of Invention
First, the technical problem to be solved
In view of the above-mentioned shortcomings and disadvantages of the prior art, the present invention provides a system and a method for treating a green low-carbon landfill leachate concentrate, which comprise an ozone advanced oxidation device, and by changing a gas-liquid contact mode, the gas-liquid mass transfer coefficient and the oxidation efficiency of ozone on organic matters are improved, so as to solve the technical problem that the oxidation effect of ozone oxidation on landfill leachate is poor in the prior art.
(II) technical scheme
The invention provides a treatment system of green low-carbon landfill leachate concentrated solution, which comprises a flocculation sedimentation tank, a sand filter and an ozone advanced oxidation device which are sequentially connected, wherein the concentrated solution of landfill leachate firstly enters the flocculation sedimentation tank, is subjected to flocculation sedimentation by adding medicines, then supernatant enters the sand filter, and effluent of the sand filter enters the ozone advanced oxidation device for treatment and is discharged;
the ozone advanced oxidation device comprises an oxidation reaction tower, wherein at least one group of film hanging catalytic devices are arranged in the oxidation reaction tower, a group of atomization spraying devices are arranged above each group of film hanging catalytic devices at intervals, a gas-liquid separation device is arranged at a position, close to the top of the oxidation reaction tower, a gas recovery pipeline is connected with the top of the oxidation reaction tower, ozone recovered from the top of the oxidation reaction tower is introduced from an ozone inlet at the bottom of the oxidation reaction tower, a water collecting tank is further arranged at the bottom of the oxidation reaction tower, a water outlet pipe is arranged in the water collecting tank, the water outlet pipe is connected with a circulating main pipe and an outer water outlet pipe, the circulating main pipe is communicated with a plurality of groups of circulating branch pipes, each group of circulating branch pipes is respectively correspondingly connected with one group of atomization spraying devices, and the circulating main pipe is also communicated with a water inlet;
The membrane hanging catalytic device comprises a plurality of catalytic rods, an ozone catalyst coating is coated on the surfaces of the catalytic rods, and the catalytic rods are arranged to form the membrane hanging catalytic device.
According to the preferred embodiment of the invention, the atomizing spray device comprises a plurality of atomizing nozzles, wherein the atomizing nozzles are solid conical nozzles and can be used for treating wastewater into liquid drops with the diameter of 100-1000 mu m, the cross section of each catalytic rod is circular, elliptic, calabash-shaped or liquid drop-shaped, the equivalent diameter of each catalytic rod is 1-5cm, and the cross section of each catalytic rod is elliptic, and the long axis direction of the cross section of each catalytic rod is arranged along the vertical direction.
According to the preferred embodiment of the invention, the catalytic rods of the film-forming catalytic device are divided into two or more layers and are arranged with layer spacing, single-layer catalytic rods are arranged in parallel and form rod spacing between the two catalytic rods, two adjacent layers of catalytic rods are arranged in a staggered manner, so that one layer of catalytic rods is just positioned in the rod spacing of the other layer of catalytic rods, or two adjacent layers of catalytic rods are arranged in a crossed manner, so that one layer of catalytic rods just crosses with the other layer of catalytic rods. The crossing angle is not limited, and is preferably 15 to 90 degrees, more preferably 45 to 90 degrees.
According to the preferred embodiment of the invention, three groups of film-forming catalytic devices and three groups of atomizing spraying devices are arranged in the oxidation reaction tower from bottom to top, and each catalytic rod of the film-forming catalytic devices is fixedly arranged on a mounting bracket on the inner wall of the oxidation reaction tower. Preferably, the vertical distance between the uppermost catalytic rod of the single-group film-forming catalytic device and the lower edge of the atomizing nozzle of the corresponding group of atomizing spray devices above the uppermost catalytic rod is 15cm-30cm, the single-layer catalytic rods are arranged in parallel, the rod distance between the two catalytic rods is 3-10 times (preferably 4 times) the diameter of the catalytic rods, and the layer distance between the two catalytic rods is 1-3 catalytic rods. Preferably, the catalytic rod is made of stainless steel or plastic, and the ozone catalyst coating on the surface of the catalytic rod is MnO 2.
According to the preferred embodiment of the invention, a group of micro bubbling reaction components are further arranged between at least one group of atomizing spraying devices and the film hanging catalytic device, each micro bubbling reaction component comprises a porous supporting net which is arranged on the inner wall of the oxidation reaction tower, bubbling pipes are arranged on the porous supporting net, two ends of each bubbling pipe are flares, the middle of each bubbling pipe is provided with a throat pipe, the upper end opening of each bubbling pipe faces to an atomizing nozzle of the atomizing spraying device, the lower end opening faces to the film hanging catalytic device, organic matter capturing coatings and ozone catalytic coatings are coated on the inner wall of each bubbling pipe, and the two coatings are alternately arranged in a spot mode, so that hollows are formed between the bubbling pipes. Ozone introduced from the bottom of the oxidation reaction tower reaches the lower part of the atomizing nozzle from the hollowed-out position to form an ozone continuous phase, and a reinforced oxidation place is formed inside the bubbling pipe. Preferably, the upper end of the bubbling pipe is 5-10cm away from the lower edge of an atomizing nozzle of the atomizing spray device, the lower edge is 1-4cm away from the upper edge of the uppermost catalytic rod of the single group of film-forming catalytic devices, the diameter of a throat pipe of the bubbling pipe is 0.5-3cm, and the length of the throat pipe is 5-20cm.
According to a preferred embodiment of the invention, each set of circulation branches comprises two or more circulation branches, each circulation branch being connected to at least three atomising nozzles. Preferably, the flow rate of the individual atomizing nozzles is 10 to 30L/min (preferably 20L/min) and the operating pressure is 0.5 to 1bar (preferably 0.7 bar). Preferably, each group of the circulation branch pipes comprises two circulation branch pipes, the two circulation branch pipes are arranged in parallel, and each circulation branch pipe is provided with 3 atomizing nozzles which are distributed along the width direction of the oxidation reaction tower.
According to a preferred embodiment of the invention, the gas-liquid separation device is formed by a group of obliquely installed corrugated plates, the distance between adjacent corrugated plates is 1-10mm, preferably 1.5-3mm, and the corrugated plates are coated with an ozone catalyst coating. Preferably, the corrugated plate is made of plastic or stainless steel, and the ozone catalyst coating on the surface of the corrugated plate is MnO 2. The ozone catalyst coating on the surface of the corrugated plate has an ozone catalytic effect and a hydrophilic effect, and improves the gas-water separation effect and the organic matter degradation efficiency.
According to the preferred embodiment of the invention, the distance from the bottom of the gas-liquid separation device to the upper edge of the atomizing nozzle of the uppermost atomizing spray device is 10-15cm, and the distance from the top of the gas-liquid separation device to the top of the oxidation reaction tower is 25-30cm.
According to the preferred embodiment of the invention, the ozone advanced oxidation device further comprises an ozone generator, wherein the ozone generator is positioned outside the oxidation reaction tower, an ozone on-line detector is arranged on the gas recovery pipeline and is communicated with a controller of the ozone generator, and when the ozone on-line detector detects that the concentration of ozone in the gas recovery pipeline is insufficient, the ozone generator is controlled to be started to supplement new ozone into the oxidation reaction tower.
According to the preferred embodiment of the invention, the gas recovery pipeline is connected with the exhaust fan and the compressor, the ozone on-line detector is positioned at the front end of the compressor, the exhaust fan is used for extracting ozone gas collected at the top of the oxidation reaction tower, the ozone gas is processed by the compressor and then is introduced from the ozone inlet at the bottom of the oxidation reaction tower, and the ozone generator is used for introducing ozone into the oxidation reaction tower through the gas permeability pipe or is used for introducing the ozone into the oxidation reaction tower together after being combined with gas compressed by the compressor. In addition, an ozone on-line detector can be arranged in the middle of the tower body of the oxidation reaction tower, and is communicated with a controller of an ozone generator, and when the insufficient concentration of ozone in the oxidation reaction tower is detected, the ozone generator is controlled to be started so as to supplement new ozone into the oxidation reaction tower.
According to the preferred embodiment of the invention, the water outlet pipe is connected with the circulating main pipe and the outer drain pipe through a three-way pipe, the circulating main pipe is connected with water inlet, the water inlet is continuously introduced into the wastewater to be treated, the outer drain pipe continuously discharges the wastewater after treatment, part of water in the water collecting tank is sprayed into the oxidation reaction tower through the circulating main pipe and the water inlet after being mixed and then sprayed into the oxidation reaction tower through the circulating branch pipe and the atomization spraying device, and the other part of water in the water collecting tank is discharged outside through the outer drain pipe.
The circulating main pipe is provided with a pressure gauge, and the joint of the circulating main pipe and each group of circulating branch pipes is provided with an independent control valve, so that the atomization spraying device in the oxidation reaction tower can be automatically controlled to work according to the quality of wastewater to be treated (mainly the COD of the inlet water).
According to the preferred embodiment of the invention, the top of the oxidation reaction tower is provided with a pressure reducing valve and a pressure gauge, and the pressure of the oxidation reaction tower is relieved through the pressure reducing valve when the pressure exceeds a set value.
According to the preferred embodiment of the invention, the oxidation reaction tower shell is made of plastic or stainless steel or glass fiber reinforced plastic, or the oxidation reaction tower shell is a concrete structure. Preferably, the bottom of the oxidation reaction tower is a tapered bottom to constitute the water collection tank.
In a second aspect, the invention provides a method for treating green low-carbon landfill leachate concentrate, which comprises the steps of treating the landfill leachate concentrate by adopting the system, and comprises the following steps:
the concentrated solution of the landfill leachate is subjected to flocculation sedimentation, sand filtration and ozone advanced oxidation treatment, and firstly enters a flocculation sedimentation tank, after flocculation sedimentation by adding medicines, supernatant fluid enters a sand filtration filter, and effluent of the sand filtration filter enters an ozone advanced oxidation device for treatment and then is discharged;
wherein the pH of the wastewater entering the oxidation reaction tower is regulated to 6.0-7.0, the ozone concentration in the oxidation reaction tower is controlled to be 5-10mg/L, preferably 5mg/L, 6mg/L, 7mg/L, 8mg/L, 9mg/L or 10mg/L, the pressure in the oxidation reaction tower is 0.1-1.0 mPa, preferably 0.1mPa, 0.2mPa, 0.3mPa, 0.4mPa, 0.5mPa or 1.0mPa.
The pressure in the oxidation reaction tower is moderately increased, so that the degradation reaction rate can be effectively improved. When the pressure exceeds the standard, the pressure is reduced through a pressure reducing valve at the top of the oxidation reaction tower so as to maintain the safe operation of the oxidation reaction tower.
(III) beneficial effects
The invention has the following technical effects:
1. The current common gas-liquid contact mode is that ozone gas bubbles into wastewater, the wastewater liquid phase is a continuous phase and the ozone gas is a discontinuous phase. Compared with the traditional bubbling reaction tower (bubbling reaction tank) and a filling reactor, the invention changes the traditional gas-liquid contact mode of ozone oxidation, uses ozone as a continuous phase and wastewater as a discontinuous phase, disperses the wastewater into small particle forms (small liquid drops) by using the atomizing spray device and disperses the wastewater into continuous ozone gas, reduces the particle size of the wastewater particles by dispersing measures, shortens the diffusion path of pollutant molecules in the liquid phase to a gas-liquid interface, and improves the apparent mass transfer rate of the liquid film side of the gas-liquid interface. Although the side diffusion path of the ozone is larger than that of the conventional gas-liquid contact mode, the gas-liquid apparent mass transfer rate of the oxidation process is obviously improved compared with that of the conventional gas-liquid contact mode because the gas-phase molecular diffusion rate is far greater than that of the liquid-phase molecular diffusion rate. The invention takes the gas phase as a continuous phase, simultaneously reduces the particle size of wastewater particles as much as possible (reduces the path length of diffusion of pollutant molecules in the liquid phase to a gas-liquid interface), greatly improves the gas-liquid mass transfer coefficient and the gas-liquid interface area, further improves the contact probability of ozone molecules and pollutants in the liquid phase, and finally achieves the aim of increasing the oxidation reaction rate.
2. The invention further provides a film-forming catalytic device below the atomizing spray device, the film-forming catalytic device consists of a plurality of catalytic rods with ozone catalytic coatings on the surfaces, liquid drops are adhered on the surfaces of the catalytic rods by utilizing the curved surfaces of the catalytic rods to form a spread liquid film, the diffusion path of ozone molecules to organic molecules in the liquid film is shortened, and the ozone catalytic coating (MnO 2) on the surfaces of the catalytic rods is used for carrying out catalytic degradation on the organic molecules in the wastewater, so that the catalytic efficiency is improved, and degradation on the organic molecules difficult to degrade is facilitated.
The invention further improves the mass transfer rate of ozone molecules and the solubility in aqueous solution by setting the gas concentration of ozone in the oxidation reaction tower and the air pressure intensity in the oxidation reaction tower, thereby further increasing the oxidation reaction rate.
3. The invention further provides a gas-liquid separation device which is formed by a group of corrugated plates which are obliquely arranged at intervals, the corrugated plates are provided with ozone catalyst coatings, the hydrophilia of the ozone catalyst coatings is utilized to enable wastewater to be attached to the surface and converged into large liquid drops, the effective separation of gas and liquid is realized, the recycled ozone is circulated and introduced from the bottom of the oxidation reaction tower, the efficient utilization of ozone is realized, and the ozone waste is avoided. The concentration of ozone in the recovery pipeline is monitored in the ozone recovery process, and when the concentration is reduced, an ozone generator can be started to supplement new ozone gas so as to maintain the concentration and the pressure of the ozone gas in the oxidation reaction tower.
4. Further, the invention is provided with a group of micro bubbling reaction components in the atomizing spraying device and the film-forming catalytic device, which can slow down the downward movement speed of the wastewater, the atomizing spraying device sprays tiny liquid drops (100-1000 μm), the liquid drops react with the ozone of the continuous phase, wherein the organic matters are partially degraded, the organic matters which are not degraded and the liquid drops fall into the bubbling pipe together, ozone gas molecules moving upwards from the bottom of the bubbling pipe and the wastewater moving downwards are in contact with each other in the throat pipe and bubble, the organic matters are degraded intensively under the catalysis of the ozone catalytic coating, and for some organic matters which are difficult to degrade, the flow speed of the wastewater is greatly slowed down when passing through the throat pipe, so that the organic matters of the larger molecules are absorbed by the organic matter capturing coating in the throat pipe and are degraded intensively under the ozone bubbling effect for a long time. The invention combines two mass transfer modes of continuous gas phase ozone/vaporific wastewater, micro bubbling and the like, thereby greatly improving the ozone utilization efficiency and the degradation effect of ozone on organic matters in the wastewater.
Drawings
FIG. 1 is a flow chart of the treatment of a green low carbon landfill leachate concentrate according to the present invention.
Fig. 2 is a schematic view showing the overall structure of the advanced ozone oxidation unit of example 1.
Fig. 3 is a schematic view of a membrane formation catalyst device and a circulation branch pipe in the ozone advanced oxidation unit of example 1.
Fig. 4 is a schematic view of a circulation branch pipe in the ozone advanced oxidation unit of example 1.
Fig. 5 is a schematic structural view of an ozone advanced oxidation unit according to embodiment 2.
Detailed Description
The invention will be better explained by the following detailed description of the embodiments with reference to the drawings.
Example 1
FIG. 1 is a flow chart showing the treatment of a green low carbon landfill leachate concentrate according to the present invention. The garbage percolate concentrate is obtained from concentrate obtained by front-end biochemical and back-end double-membrane treatment, and comprises nanofiltration concentrate and reverse osmosis concentrate. Firstly, the landfill leachate concentrated solution enters a flocculation sedimentation tank, after flocculation sedimentation by adding drugs, supernatant fluid enters a sand filter, and effluent of the sand filter enters an ozone advanced oxidation device and reaches an emission standard after advanced oxidation treatment.
Referring to fig. 2, a schematic diagram of an advanced ozone oxidation device according to a preferred embodiment of the present invention is shown, wherein the advanced ozone oxidation device includes an oxidation reaction tower, and the whole advanced ozone oxidation device is rectangular (or may be cylindrical), and the bottom is a four-sided cone to form a water collecting tank (or may be conical). The height of the water collecting tank is 0.5m, and the cone angle of the water collecting tank is 90 degrees. The total height of the oxidation reaction tower body is set to be 3.5m, the length is 1.5m, and the width is 1m. The whole oxidation reaction tower is closed, and a pressure reducing valve 9 and a pressure gauge 11-1 are arranged at the top of the tower body. The oxidation reaction tower is made of plastic (in other embodiments, stainless steel or concrete construction). The oxidation reaction tower is provided with three groups of film hanging catalytic devices 2, the three groups of film hanging catalytic devices 2 are arranged at intervals in the height direction, an atomization spraying device 1 is arranged above each group of film hanging catalytic devices 2 at intervals, and three groups of atomization spraying devices 1 are arranged in the oxidation reaction tower. The atomizing spray device 1 comprises a plurality of atomizing nozzles 101, the flow rate of the single atomizing nozzle 101 is 20L/min, the operating pressure is 0.7bar, the atomizing nozzle 101 is a solid conical nozzle, and the wastewater can be processed into liquid drops with the diameter of 100-1000 mu m.
The atomization spraying device 1 is connected with a circulating branch pipe positioned outside the oxidation reaction tower, the circulating branch pipe is connected with a circulating main pipe, the lower end of the circulating main pipe is connected with a three-way valve 4, one end of the three-way valve 4 is connected with an outer drain pipe 41, the other end of the three-way valve is connected with a water outlet pipe 42 of the oxidation reaction tower, a circulating pump 3 is arranged on the water outlet pipe 42, and the water outlet pipe 42 is connected with a water outlet of a water collecting tank at the bottom of the oxidation reaction tower. Wherein the water outlet pipe 42, the outer water outlet pipe 41, the circulating pump 3, the circulating main pipe, the circulating branch pipe and the like form a wastewater inlet and outlet water and circulating device. The circulating main pipe is also communicated with the water to be treated, so that the water is converged with the circulating water at the bottom of the oxidation reaction tower and then is conveyed to the atomization spraying device 1 through the circulating branch pipe. The pressure gauge 11-2 is arranged on the circulating main pipe, the connection part of the circulating main pipe and each group of circulating branch pipes is provided with an independent control valve, and the number of groups of atomizing spray devices 1 working in the oxidation reaction tower can be regulated by using the control valves. The water outlet pipe 42 is connected with the circulating main pipe and the outer water outlet pipe 41 through the three-way valve 4, the circulating main pipe is connected with water inlet, the water inlet is continuously introduced into the wastewater to be treated, the outer water outlet pipe 41 is continuously used for discharging the wastewater after treatment, part of water in the water collecting tank of the oxidation reaction tower is sprayed into the oxidation reaction tower through the circulating branch pipe and the atomization spraying device 1 after being mixed with the water inlet through the circulating main pipe, and the other part of water in the water collecting tank is discharged outside through the outer water outlet pipe 41, so that the ozone advanced oxidation of continuous water inlet/water outlet is formed.
The film-forming catalytic device 2 comprises a plurality of catalytic rods 21, wherein the cross section of each catalytic rod 21 is circular, elliptical, gourd-shaped or droplet-shaped, and if the cross section of each catalytic rod is elliptical, the long axis direction of the cross section of each catalytic rod is arranged along the vertical direction. In the present embodiment, as shown in FIG. 3, the cross section of the catalytic rod 21 is a circle having a diameter of 5 cm. The catalytic rods 21 in each film-forming catalytic device 2 are distributed in multiple layers, each layer comprises a plurality of dry catalytic rods 21, and the dry catalytic rods are made of stainless steel, as shown in fig. 3, 5 catalytic rods are arranged on the uppermost layer, 6 catalytic rods are arranged on the second layer, and 5 catalytic rods are arranged on the third layer. The single-layer catalytic rods are uniformly arranged, the distance between the catalytic rods is about 4 times the diameter of the catalytic rods, the catalytic rods 21 between adjacent layers are staggered, and the distance between the layers is about 2 times the diameter of the catalytic rods. Staggered means that one layer of catalytic rods is located exactly within the rod spacing of another layer of catalytic rods, as shown in fig. 3. The surface of the catalytic rod 21 is coated with a layer of MnO 2, which has ozone catalytic activity. The catalytic rod 21 is mounted and fixed to the mounting bracket 10 on the inner wall of the oxidation reaction tower. Three groups of catalytic rods are arranged in the oxidation reaction tower of the embodiment, and each group of catalytic rods forms a film-forming catalytic device 2. The distance between the uppermost catalytic rod of the film-forming catalytic device 2 and the lower edge of the atomizing nozzle 101 at the upper part thereof is 18cm. The droplets ejected from the atomizing spray device 1 slide along the curved catalytic rod 21 in the falling process, and a layer of liquid film is formed on the surface of the catalytic rod 21. The liquid film is contacted with continuous ozone gas, and the surface of the catalytic rod 21 is provided with MnO 2, so that the oxidation speed and the oxidation strength of the ozone on organic matters in the wastewater can be catalyzed.
As shown in fig. 4, since the number of the set groups of the atomizing spray device 1 is 3, the number of the set groups of the circulation branch pipes in this embodiment is also 3, and each set of the circulation branch pipes includes 2 circulation branch pipes, and each circulation branch pipe is provided with 3 atomizing nozzles 101.3 groups of circulation branch pipes are prepared at intervals in height, each group of circulation branch pipes comprises 2 circulation branch pipes, and 3 atomizing nozzles 101,6 and 101 are arranged on one circulation branch pipe to form an atomizing spray device 1. In the present embodiment, the number of atomizing nozzles 101 is 18. Each group of circulating branch pipes is provided with an independent valve, and the water inflow of each circulating branch pipe can be respectively regulated.
The position that is close to the top at the oxidation reaction tower is equipped with gas-liquid separation device 6, and gas-liquid separation device 6 comprises the buckled plate of a set of slope installation, and the buckled plate material is plastics, and the clearance between two adjacent buckled plates is 2mm. As shown in fig. 2, the corrugated plate is installed in such a manner that the extending direction of the corrugation of the corrugated plate coincides with the tilting direction of the corrugated plate. The corrugated plate is coated with a layer of catalyst material, and the catalyst is MnO 2. The distance from the bottom of the gas-liquid separation device 6 to the upper edge of the uppermost atomizing nozzle 101 was 10cm, and the distance from the top of the gas-liquid separation device 6 to the top of the oxidation reaction tower was 25cm.
The top of the oxidation reaction tower is provided with a gas recovery pipeline 71 above the gas-liquid separation device 6, and an exhaust fan 7 is arranged on the gas recovery pipeline 71 and is used for recycling ozone collected at the top of the oxidation reaction tower. The lower part of the gas recovery pipeline 71 is connected with a compressor 8, the recovered ozone is pressurized and concentrated and then is returned to an ozone inlet 81 at the bottom of the oxidation reaction tower, and the ozone is introduced into the oxidation reaction tower through the ozone inlet 81. The ozone inlet 81 is located in the oxidation reaction tower above the liquid surface of the water collection tank and below the lowest layer of the film formation catalyst device 2. An ozone on-line detector 12 is further provided on the gas recovery line 71 at the front end of the compressor 8 for detecting the concentration of ozone in the gas recovery line 71, and when the concentration of ozone is low, new ozone needs to be replenished into the oxidation reaction tower.
Specifically, an ozone generator 5 is further arranged outside the oxidation reaction tower and connected with the bottom of the oxidation reaction tower through a vent pipe 51, and the position of the vent pipe 51 inside the oxidation reaction tower is located between the liquid surface of the water collecting tank and the bottom catalytic film forming device 2. The ozone on-line detector 12 on the gas recovery pipeline 71 is in signal connection with the controller of the ozone generator 5, the controller calculates the fresh ozone amount to be supplemented according to the detection value (concentration) of the ozone on-line detector 12, the volume of the oxidation reaction tower, the set ozone concentration value and the like, and controls the ozone generator 5 to work according to the calculation result and generates the ozone of the required amount, the generated ozone is sent into the oxidation reaction tower through the breather pipe 51, or the generated new ozone is communicated with the gas recovery pipeline 71, the new ozone and the recovered ozone are combined and then compressed through the compressor 8, and the concentration is increased and then the ozone is introduced into the oxidation reaction tower through the ozone inlet 81.
The treatment process of the ozone advanced oxidation unit of this embodiment is as follows:
The pH value of the effluent of the sand filter is regulated to be between 6.0 and 7.0, the effluent is converged with the circulating wastewater from the water collecting tank through a connecting circulating main pipe, the effluent enters an oxidation reaction tower through a circulating branch pipe, tiny liquid drops with the diameter of 100-1000 mu m are formed in a dispersing mode through an atomization spraying device 1, the liquid drops are in descending trend on the whole under the dual effects of self gravity and ascending gas, in the descending process, the liquid drops are firstly contacted with continuous ozone atmosphere, pollutants in the liquid drops are subjected to oxidation reaction with ozone molecules and derived hydroxyl free radicals to realize degradation, and simultaneously a large number of liquid drops are attached to the surfaces of catalytic rods 21 of a catalytic film hanging device 2 in the descending process to form a thin liquid film, and the pollutants in the liquid film and the ozone molecules are contacted with an ozone catalyst MnO 2 on the surfaces of the catalytic rods 21 to further oxidize under the catalytic effect of the catalyst so as to realize further degradation of the pollutants. The liquid drops finally fall into a water collecting tank at the bottom of the oxidation reaction tower, and are circularly sprayed into water mist and oxidized by ozone under the action of a circulating pump 3. The outlet pipe 4 is connected with the circulating pump 3, the outlet end of the circulating pump 3 is connected with the three-way valve 4, the three-way valve 4 is connected with the circulating main pipe, the circulating main pipe is also connected with water inlet, and the three-way valve 4 is also connected with the outer drain pipe 41. The inflow water is continuously input with water of which the pH is adjusted to 6.0-7.0, and the outer drain pipe 41 is continuously discharged. The water part of the water collecting tank is discharged outside, and the part of the water is diluted and sprayed into the oxidation reaction tower by the circulating branch pipe and the atomization spraying device 1 in the form of atomized liquid drops.
Ozone gas generated by the ozone generator 5 is introduced from the bottom of the oxidation reaction tower, the ozone inlet flow is adjustable, ozone starts to rise from the bottom of the oxidation reaction tower, the ozone contacts with waste water drops and a liquid film on the surface of the catalytic rod 21 in the rising process, and pollutants in the waste water react with ozone molecules, hydroxyl free radicals and other derivative oxides, so that organic matter degradation is realized. And part of liquid drops can be entrained in the gas in the rising process, the gas with the liquid drops finally realizes gas-liquid separation through the gas-liquid separation device 6, the separated water phase flows back downwards along the surface of the corrugated plate, the gas continuously rises, and the reflowed liquid phase wastewater contacts with a catalyst MnO 2 and ozone on the surface of the corrugated plate, so that the organic matters are further oxidized and degraded.
Ozone-containing gas separated from the top of the oxidation reaction tower reenters the bottom of the oxidation reaction tower through a gas recovery pipeline 71, an exhaust fan 7, a compressor 8 and the like, thereby realizing the recycling of the ozone gas and improving the ozone utilization rate. The flow specification of the exhaust fan 7 and the compressor 8 is 10m 3/min. The gas recovery pipeline 71 is provided with an ozone on-line detector 12, the ozone on-line detector 12 is arranged at the front end of the compressor 8 and is used for monitoring the concentration of recovered ozone in real time, the ozone on-line detector 12 is also connected with a controller of the ozone generator 5, and the start and stop of the ozone generator 5 are controlled in real time according to the detected concentration of ozone to maintain the ozone gas in the oxidation reaction tower at a set level, such as 5mg/L-10mg/L. During the operation of the oxidation reaction tower, excessive gas is discharged through the pressure reducing valve 9 at the top of the oxidation reaction tower, and the gas pressure in the oxidation reaction tower is maintained between 0.1 and 1.0mPa.
Compared with the conventional bubbling ozone oxidation reaction which uses wastewater as a continuous phase and ozone as a disperse phase, the embodiment is changed into a gas-liquid contact mode which uses ozone as a continuous phase and wastewater as a disperse phase, and meanwhile, a film-forming catalytic device 2 consisting of a catalytic rod 21 array is arranged, so that a gas-liquid-solid three-phase reaction system is formed inside the oxidation reaction tower.
The ozone advanced oxidation device of the embodiment can realize high-efficiency degradation of pollutants in wastewater. According to the invention, the atomization spraying device 1 is used for processing wastewater into tiny liquid drops, so that the mass transfer path of pollutants in a liquid phase is reduced, the area of a gas-liquid contact interface is increased, and the contact probability of ozone molecules and oxidized derivatives thereof with the pollutants is increased, thereby increasing the apparent mass transfer rate of the gas-liquid. The catalytic rods 21 of the film-forming catalytic device 2 play a heterogeneous catalytic role in the degradation reaction of pollutants. The surface of the catalytic rod 21 can provide a larger gas-liquid contact surface, increasing the gas-liquid mass transfer rate and the reaction rate. Finally, the gas-liquid separation device 6 not only can realize gas-liquid separation, but also has the surface MnO 2 with hydrophilicity, can be used for adhering and converging waste water drops into large drops, improves the gas-liquid separation efficiency, and can further utilize the surface catalyst to play a role in catalytic degradation on the adhered waste water and pollutants. In the running process of the ozone advanced oxidation device, the pressure (such as 0.1mPa-1.0 mPa) in the oxidation reaction tower is moderately increased, so that the degradation reaction rate can be further improved. The ozone utilization rate can be improved by utilizing components such as the gas recovery pipeline, the exhaust fan, the compressor and the like, and the ozone waste is avoided. The on-line ozone detector 12 is arranged on the gas recovery pipeline, and is automatically and cooperatively controlled with the ozone generator 5, so that the ozone preparation cost can be saved, the high ozone concentration is maintained in the oxidation reaction tower, the ozone concentration is maintained within a set value range, and the degradation effect of organic matters in the wastewater is ensured.
Example 2
In this embodiment, an advanced ozone oxidation device is further improved based on the embodiment 1, as shown in fig. 5, a group of micro bubbling reaction components 13 are further arranged between the two groups of atomizing spraying devices 1 and the film-forming catalytic device 2. The micro bubbling reaction component 13 comprises a porous supporting net 131 arranged on the inner wall of the oxidation reaction tower, bubbling pipes 132 are arranged in part of holes of the porous supporting net, 6 bubbling pipes are arranged on each layer corresponding to the number of the atomizing nozzles 101, and two ends of each bubbling pipe 132 are flared and the middle is provided with a throat. The upper end opening of the bubbling pipe faces to the atomizing nozzle 101 of the atomizing spray device 1, and the lower end opening faces to the film hanging catalytic device 2. The inner wall of the bubbling tube 132 is coated with an organic matter capturing coating and an ozone catalytic coating, the two coatings are alternately arranged in a spot form, and a hollow part is arranged between the bubbling tube 132 and the bubbling tube 132, so that ozone can move from the lower side to one side of the atomizing spray device 1. Ozone introduced from the bottom of the oxidation reaction tower reaches the lower part of the atomizing nozzle 101 from the hollowed-out position to form an ozone continuous phase, and the inside of the bubbling pipe 132 forms an enhanced oxidation place. The upper end of the bubbling pipe 132 is 5cm away from the lower edge of the atomizing nozzle 101 of the atomizing spray device, the lower edge is 2cm away from the upper edge of the uppermost catalytic rod of the single group of film-forming catalytic devices, the diameter of the throat pipe of the bubbling pipe is 2cm, and the length of the throat pipe is 7cm. The ozone catalytic coating can be MnO 2, the organic matter capturing coating can be hydrophobic silane coupling agent (aminopropyl triethoxysilane, APTES) coating, the silane coupling agent is sprayed on the surface of the MnO 2 coating in an irregular spot form of 0.5-1cm 2, and the exposed surfaces of the two coatings respectively account for about 50% of the inner wall surface of the bubbling tube 132. The hydrophilic end of the silane coupling agent is connected with MnO 2, and the hydrophobic end of the silane coupling agent faces outwards, so that organic molecules in water can be captured, and the organic molecules in the wastewater can be retained. In this embodiment, by setting the micro bubbling reaction component 13, the contact mode of the continuous ozone gas phase and the discontinuous wastewater is organically combined with the traditional bubbling reaction contact mode, so as to avoid that organic molecules difficult to degrade quickly fall down to the water collecting tank along with water drops, and the inner wall of the bubbling pipe 132 is coated with an organic capturing coating, so that the organic difficult to degrade is retained, and the degradation rate of organic matters in the wastewater after one-time circulation can be further improved. The advanced ozone oxidation device of the embodiment can reduce the COD of the wastewater to a set value in a shorter time.
Application example 1
The reverse osmosis concentrated solution of the landfill leachate is treated by using the system of the embodiment 1, and the water quality condition of entering an ozone advanced oxidation device is CODcr,450mg/L, NH 4 -N (ammonia nitrogen) 15mg/L and salinity 15g/L.
The treatment conditions are that the water inflow rate is 2m 3/h, the pH value is regulated to 6.5, the gas flow rate of an ozone generator is 20L/min, the ozone concentration is 5mg/L, the wastewater circulation flow rate is controlled to be 20m 3/h, the circulating gas flow rate is controlled to be 5m 3/min, and the ozone concentration in an oxidation reaction tower is controlled to be 10mg/L. The continuous oxidative degradation treatment was carried out using the ozone advanced oxidation apparatus of example 1, and the gas pressure in the oxidation reaction column was controlled to be 0.1mPa, 0.2mPa, 0.4mPa, 0.5mPa and 1.0mPa. And under different pressure conditions, sampling and detecting the effluent respectively. Run continuously for 1 month, sample 1 time a day and take the average.
TABLE 1 CODcr detection values of advanced oxidation effluent under different gas pressures
Reaction pressure/mPa 0.1 0.2 0.4 0.5 1.0
CODcr/mg/L of effluent 70 58 48 43 40
As can be seen from Table 1, the effluent CODcr has a good removal effect, and can reach the first level standard of Integrated wastewater discharge Standard (GB 8978-1996), and when the pressure of the reaction tower is controlled to be more than 0.4mPa, the effluent CODcr can meet the first level A standard of pollutant discharge Standard (GB 18918-2002) of urban wastewater treatment plant.
Application example 2
The continuous oxidative degradation treatment was carried out using the ozone advanced oxidation apparatus of example 2 on the basis of application example 1, and the internal gas pressure of the oxidation reaction column was controlled to be 0.1mPa, 0.2mPa, 0.4mPa, 0.5mPa, 1.0mPa. The quality of the inlet water and the set treatment conditions were the same as in application example 1. And under different pressure conditions, sampling and detecting the effluent respectively. Run continuously for 1 month, sample 1 time a day and take the average.
TABLE 2 CODcr detection values of advanced oxidation effluent under different gas pressures
Reaction pressure/mPa 0.1 0.2 0.4 0.5 1.0
CODcr/mg/L of effluent 67 55 44 40 36
As can be seen from Table 2, the effluent CODcr has a good removal effect, and can reach the first level standard of Integrated wastewater discharge Standard (GB 8978-1996), and when the pressure of the reaction tower is controlled to be more than 0.4mPa, the effluent CODcr can meet the first level A standard of pollutant discharge Standard (GB 18918-2002) of urban wastewater treatment plant.
Application example 3
The reverse osmosis concentrated solution of the landfill leachate is treated by using the system of the embodiment 1, and the water quality condition of entering an ozone advanced oxidation device is CODcr,450mg/L, NH 4 -N (ammonia nitrogen) 15mg/L and salinity 15g/L.
The treatment conditions are that the water inflow rate is 2m 3/h, the pH value is regulated to 6.5, the gas flow rate of an ozone generator is 20L/min, the wastewater circulation flow rate is controlled to be 20m 3/h, the circulating gas flow rate is 5m 3/min, and the air pressure in the oxidation reaction tower is controlled to be 0.5mPa. The advanced ozone oxidation device in example 1 was used for continuous oxidative degradation treatment, and the concentration of ozone in the oxidation reaction tower was controlled to 5mg/L, 7.5mg/L and 10mg/L. Under the condition of different ozone concentrations, the effluent is sampled and detected respectively. Run continuously for 1 month, sample 1 time a day and take the average.
TABLE 3 CODcr detection values of advanced oxidation effluent at different ozone concentrations
Ozone concentration mg/L in reaction tower 5 7.5 10
CODcr/mg/L of effluent 75 49 45
As shown in Table 3, the effluent CODcr has good removal effect, and can reach the first level standard of Integrated wastewater discharge Standard (GB 8978-1996), and when the concentration of ozone in the reaction tower is controlled to be more than 7.5mg/L, the effluent CODcr can meet the first level A standard of pollutant discharge Standard of urban wastewater treatment plant (GB 18918-2002).
In conclusion, the ozone advanced oxidation device has the advantages of high mass transfer efficiency, high ozone recycling rate, capability of realizing accurate control of concentration of each phase in a reaction system and reaction conditions, and the like, thereby realizing efficient treatment of wastewater containing organic matters, and having the characteristics of environmental protection and low carbon.
It should be noted that the above embodiments are merely for illustrating the technical solution of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the above embodiments, it should be understood by those skilled in the art that the technical solution described in the above embodiments may be modified or some or all of the technical features may be equivalently replaced, and these modifications or substitutions do not make the essence of the corresponding technical solution deviate from the scope of the technical solution of the embodiments of the present invention.

Claims (10)

1.一种绿色低碳垃圾渗滤液浓缩液的处理系统，其特征在于，包括依次连接的絮凝沉淀池、砂滤过滤器和臭氧高级氧化装置；垃圾渗滤液的浓缩液首先进入絮凝沉淀池，通过加药絮凝沉降后，上清液进入砂滤过滤器，砂滤过滤器的出水进入臭氧高级氧化装置处理后排放；1. A green and low-carbon landfill leachate concentrate treatment system, characterized in that it comprises a flocculation sedimentation tank, a sand filter and an ozone advanced oxidation device connected in sequence; the landfill leachate concentrate first enters the flocculation sedimentation tank, after flocculation and sedimentation by adding drugs, the supernatant enters the sand filter, and the effluent of the sand filter enters the ozone advanced oxidation device for treatment and then is discharged; 所述臭氧高级氧化装置包括氧化反应塔；在氧化反应塔内设有至少一组挂膜催化装置，且每组挂膜催化装置上方间隔一定距离设有一组雾化喷淋装置；在氧化反应塔靠近塔顶的位置设有气液分离装置；氧化反应塔的塔顶连接气体回收管路，气体回收管路将从塔顶回收的臭氧从塔底的臭氧入口通入；在氧化反应塔的塔底还设有汇水槽，汇水槽中设有出水管，出水管连接循环主管和外排水管，所述循环主管连通若干组循环支管，各组循环支管分别对应连接一组所述雾化喷淋装置；所述循环主管还与进水相连通；臭氧入口在氧化反应塔内的位置高于汇水槽的液面且低于最下层的挂膜催化装置；The ozone advanced oxidation device comprises an oxidation reaction tower; at least one group of film-forming catalytic devices is arranged in the oxidation reaction tower, and a group of atomizing spray devices is arranged above each group of film-forming catalytic devices at a certain distance; a gas-liquid separation device is arranged near the top of the oxidation reaction tower; the top of the oxidation reaction tower is connected to a gas recovery pipeline, and the gas recovery pipeline passes the ozone recovered from the top of the tower into the ozone inlet at the bottom of the tower; a water collection tank is also arranged at the bottom of the oxidation reaction tower, and a water outlet pipe is arranged in the water collection tank, and the water outlet pipe is connected to a circulation main pipe and an external drainage pipe, and the circulation main pipe is connected to a plurality of groups of circulation branch pipes, and each group of circulation branch pipes is respectively connected to a group of the atomizing spray devices; the circulation main pipe is also connected to the water inlet; the position of the ozone inlet in the oxidation reaction tower is higher than the liquid level of the water collection tank and lower than the bottom film-forming catalytic device; 其中，雾化喷淋装置用于将待臭氧处理的废水以雾状液滴的形式向下喷洒；所述挂膜催化装置包含多根催化棒，各催化棒表面覆有臭氧催化剂涂层；所述多根催化棒排列以形成所述挂膜催化装置。Among them, the atomizing spray device is used to spray the wastewater to be treated with ozone downward in the form of mist droplets; the film-forming catalytic device comprises a plurality of catalytic rods, each of which is covered with an ozone catalyst coating; the plurality of catalytic rods are arranged to form the film-forming catalytic device. 2.根据权利要求1所述的处理系统，其特征在于，所述雾化喷淋装置包含雾化喷嘴，所述雾化喷嘴为实心锥形喷嘴，能将废水处理成直径在100-1000μm的液滴；所述催化棒的截面呈圆形、椭圆形、葫芦形或液滴形，每根催化棒的等效直径为1-5cm；截面为椭圆形的催化棒，其截面长轴方向沿竖直方向设置。2. The treatment system according to claim 1 is characterized in that the atomizing spray device comprises an atomizing nozzle, which is a solid conical nozzle and can treat wastewater into droplets with a diameter of 100-1000 μm; the cross-section of the catalytic rod is circular, elliptical, gourd-shaped or droplet-shaped, and the equivalent diameter of each catalytic rod is 1-5 cm; the cross-section of the catalytic rod is elliptical, and the major axis direction of the cross-section is arranged along the vertical direction. 3.根据权利要求1或2所述的处理系统，其特征在于，所述挂膜催化装置的催化棒分成两层或两层以上进行布置且具有层间距；单层催化棒平行排列且两个催化棒之间形成棒间距；相邻两层催化棒交错排列，使一层催化棒恰好位于另一层催化棒的棒间距内；或者相邻两层催化棒交叉排列，使一层催化棒恰好与另一层催化棒形成交叉。3. The treatment system according to claim 1 or 2 is characterized in that the catalytic rods of the biofilm catalytic device are arranged in two or more layers and have an interlayer spacing; the single-layer catalytic rods are arranged in parallel and a rod spacing is formed between the two catalytic rods; the catalytic rods of two adjacent layers are arranged in a staggered manner so that the catalytic rods of one layer are exactly located within the rod spacing of the catalytic rods of the other layer; or the catalytic rods of two adjacent layers are arranged in a cross-arrangement so that the catalytic rods of one layer are exactly crossed with the catalytic rods of the other layer. 4.根据权利要求3所述的处理系统，其特征在于，在所述氧化反应塔内从下至上设有三组挂膜催化装置和三组雾化喷淋装置；所述挂膜催化装置的各催化棒安装固定在氧化反应塔内壁的安装托架上；单组挂膜催化装置的最上层催化棒与其上方对应的一组雾化喷淋装置的雾化喷嘴下沿的垂直距离为15cm-30cm；单层催化棒平行排列且两个催化棒之间的棒间距为3-10倍催化棒直径；两层催化棒的层间距为1-3根催化棒直径。4. The treatment system according to claim 3 is characterized in that three groups of film-forming catalytic devices and three groups of atomizing spray devices are arranged from bottom to top in the oxidation reaction tower; each catalytic rod of the film-forming catalytic device is installed and fixed on the mounting bracket of the inner wall of the oxidation reaction tower; the vertical distance between the topmost catalytic rod of a single group of film-forming catalytic devices and the lower edge of the atomizing nozzle of a group of atomizing spray devices corresponding thereto is 15cm-30cm; the single-layer catalytic rods are arranged in parallel and the rod spacing between two catalytic rods is 3-10 times the diameter of the catalytic rods; the interlayer spacing between two layers of catalytic rods is 1-3 catalytic rod diameters. 5.根据权利要求2所述的处理系统，其特征在于，在至少一组雾化喷淋装置和挂膜催化装置之间还设有一组微型鼓泡反应组件；微型鼓泡反应组件包括一个安装在氧化反应塔内壁的多孔支撑网，多孔支撑网上设置鼓泡管，鼓泡管的两端为扩口且中间设为喉管；鼓泡管的上端开口朝向雾化喷淋装置的雾化喷嘴，下端开口朝向挂膜催化装置；鼓泡管内壁涂覆有机物捕捉涂层和臭氧催化涂层；两种涂层以斑点形式交替设置，鼓泡管与鼓泡管之间为镂空；鼓泡管的喉管直径为0.5-3cm，喉管长度为5-20cm。5. The treatment system according to claim 2 is characterized in that a group of micro-bubbling reaction components are further provided between at least one group of atomizing spray devices and the biofilm catalytic device; the micro-bubbling reaction component comprises a porous support net installed on the inner wall of the oxidation reaction tower, a bubbling tube is arranged on the porous support net, both ends of the bubbling tube are expanded and the middle is arranged as a throat; the upper end opening of the bubbling tube faces the atomizing nozzle of the atomizing spray device, and the lower end opening faces the biofilm catalytic device; the inner wall of the bubbling tube is coated with an organic matter capture coating and an ozone catalytic coating; the two coatings are alternately arranged in the form of spots, and the space between the bubbling tubes is hollow; the throat diameter of the bubbling tube is 0.5-3cm, and the throat length is 5-20cm. 6.根据权利要求3所述的处理系统，其特征在于，每一组循环支管包含两根或两根以上循环支管，每根循环支管连接至少三个雾化喷嘴；单个雾化喷嘴的流量10-30L/min，运行压力0.5-1bar；雾化喷嘴沿氧化反应塔的宽度方向分布。6. The treatment system according to claim 3 is characterized in that each group of circulation branches comprises two or more circulation branches, each circulation branch is connected to at least three atomizing nozzles; the flow rate of a single atomizing nozzle is 10-30 L/min, and the operating pressure is 0.5-1 bar; the atomizing nozzles are distributed along the width direction of the oxidation reaction tower. 7.根据权利要求1所述的处理系统，其特征在于，所述气液分离装置由一组倾斜安装的波纹板构成，相邻波纹板之间的间距为1-10mm，所述波纹板上涂覆有臭氧催化剂涂层。7. The treatment system according to claim 1 is characterized in that the gas-liquid separation device is composed of a group of obliquely installed corrugated plates, the spacing between adjacent corrugated plates is 1-10 mm, and the corrugated plates are coated with an ozone catalyst coating. 8.根据权利要求1所述的处理系统，其特征在于，所述臭氧高级氧化装置还包括臭氧发生器，所述臭氧发生器位于氧化反应塔外部；在所述气体回收管路上臭氧在线检测仪；所述臭氧在线检测仪与臭氧发生器的控制器连通；当臭氧在线检测仪检测到气体回收管路中臭氧浓度不足时，控制臭氧发生器开启以补充新的臭氧至氧化反应塔内；或者在氧化反应塔的塔身中间位置设置臭氧在线检测仪，所述臭氧在线检测仪与臭氧发生器的控制器连通，当检测到氧化反应塔内的臭氧浓度不足时，控制臭氧发生器开启以补充新的臭氧至氧化反应塔内。8. The treatment system according to claim 1 is characterized in that the ozone advanced oxidation device also includes an ozone generator, which is located outside the oxidation reaction tower; an ozone online detector is provided on the gas recovery pipeline; the ozone online detector is connected to the controller of the ozone generator; when the ozone online detector detects that the ozone concentration in the gas recovery pipeline is insufficient, the ozone generator is controlled to be turned on to replenish new ozone into the oxidation reaction tower; or an ozone online detector is arranged in the middle of the tower body of the oxidation reaction tower, the ozone online detector is connected to the controller of the ozone generator, and when it is detected that the ozone concentration in the oxidation reaction tower is insufficient, the ozone generator is controlled to be turned on to replenish new ozone into the oxidation reaction tower. 9.根据权利要求1所述的处理系统，其特征在于，所述出水管以三通管连接所述循环主管和外排水管，循环主管与进水连接，进水连续通入待处理的废水，外排水管连续外排处理后的废水；汇水槽中的一部分水通过循环主管和进水混合后经循环支管及雾化喷淋装置喷洒至氧化反应塔中，汇水槽的另一部分水则通过外排水管外排出去。9. The treatment system according to claim 1 is characterized in that the outlet pipe is connected to the circulation main pipe and the external drainage pipe by a three-way pipe, the circulation main pipe is connected to the water inlet, the water inlet continuously passes the wastewater to be treated, and the external drainage pipe continuously discharges the treated wastewater; a part of the water in the water collection tank is mixed with the water inlet through the circulation main pipe and sprayed into the oxidation reaction tower through the circulation branch pipe and the atomizing spray device, and the other part of the water in the water collection tank is discharged through the external drainage pipe. 10.一种绿色低碳垃圾渗滤液浓缩液的处理方法，其特征在于，采用权利要求1-9任一项所述的处理系统对垃圾渗滤液浓缩液进行处理，包括：10. A method for treating green and low-carbon landfill leachate concentrate, characterized in that the landfill leachate concentrate is treated by using the treatment system according to any one of claims 1 to 9, comprising: 将垃圾渗滤液的浓缩液进行絮凝沉淀、砂滤和臭氧高级氧化处理；垃圾渗滤液的浓缩液首先进入絮凝沉淀池，通过加药絮凝沉降后，上清液进入砂滤过滤器，砂滤过滤器的出水进入臭氧高级氧化装置处理后排放；其中，将进入氧化反应塔的废水pH调节至6.0-7.0，控制氧化反应塔内臭氧浓度为5-10mg/L，氧化反应塔内的压力为0.1mPa-1.0mPa。The concentrated liquid of the landfill leachate is subjected to flocculation sedimentation, sand filtration and ozone advanced oxidation treatment; the concentrated liquid of the landfill leachate first enters the flocculation sedimentation tank, and after flocculation and sedimentation by adding drugs, the supernatant enters the sand filter, and the effluent of the sand filter enters the ozone advanced oxidation device for treatment and then discharged; wherein, the pH value of the wastewater entering the oxidation reaction tower is adjusted to 6.0-7.0, the ozone concentration in the oxidation reaction tower is controlled to be 5-10 mg/L, and the pressure in the oxidation reaction tower is 0.1 mPa-1.0 mPa.
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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN203602393U (en) * 2013-11-20 2014-05-21 苏州世纪正源环保科技有限公司 Wet catalytic oxidation waste liquid treatment system
CN203833777U (en) * 2014-05-28 2014-09-17 江苏维尔利环保科技股份有限公司 Treatment device for ozone oxidation treatment leachate nanofiltration concentrated solution
CN203971653U (en) * 2014-07-04 2014-12-03 中节能六合天融环保科技有限公司 A kind of gas-liquid reallocation and subparticle capturing device that is applicable to single tower double circulation desulphurization tower
US20140353259A1 (en) * 2011-12-16 2014-12-04 Sven Strunk Oxidation Method, Nozzle and System for Treating Waste Water
CN104193055A (en) * 2014-09-18 2014-12-10 中国科学院生态环境研究中心 Reclaimed water reusing device integrating ultrafiltration membrane filtration and photocatalytic reaction
CN106238041A (en) * 2016-07-28 2016-12-21 天津大学 The preparation method of the catalyst that volatile organic matter ozonisation is decomposed it is catalyzed under a kind of room temperature
CN215048980U (en) * 2021-07-06 2021-12-07 荆州市中环环境治理有限公司 Medical waste disposal sewage two-stage ozone oxidation treatment system
CN113952949A (en) * 2021-09-14 2022-01-21 青岛创启迈沃环境科技有限公司 Preparation method of hydrophobic normal-temperature decomposition ozone catalyst
CN221217581U (en) * 2023-12-22 2024-06-25 青岛中通臭氧科技有限公司 COD degradation device for sewage and wastewater

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140353259A1 (en) * 2011-12-16 2014-12-04 Sven Strunk Oxidation Method, Nozzle and System for Treating Waste Water
CN203602393U (en) * 2013-11-20 2014-05-21 苏州世纪正源环保科技有限公司 Wet catalytic oxidation waste liquid treatment system
CN203833777U (en) * 2014-05-28 2014-09-17 江苏维尔利环保科技股份有限公司 Treatment device for ozone oxidation treatment leachate nanofiltration concentrated solution
CN203971653U (en) * 2014-07-04 2014-12-03 中节能六合天融环保科技有限公司 A kind of gas-liquid reallocation and subparticle capturing device that is applicable to single tower double circulation desulphurization tower
CN104193055A (en) * 2014-09-18 2014-12-10 中国科学院生态环境研究中心 Reclaimed water reusing device integrating ultrafiltration membrane filtration and photocatalytic reaction
CN106238041A (en) * 2016-07-28 2016-12-21 天津大学 The preparation method of the catalyst that volatile organic matter ozonisation is decomposed it is catalyzed under a kind of room temperature
CN215048980U (en) * 2021-07-06 2021-12-07 荆州市中环环境治理有限公司 Medical waste disposal sewage two-stage ozone oxidation treatment system
CN113952949A (en) * 2021-09-14 2022-01-21 青岛创启迈沃环境科技有限公司 Preparation method of hydrophobic normal-temperature decomposition ozone catalyst
CN221217581U (en) * 2023-12-22 2024-06-25 青岛中通臭氧科技有限公司 COD degradation device for sewage and wastewater

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
上海市纺织科学研究院编译: "印染工业废水处理", 31 December 1974, 轻工业出版社, pages: 187 *

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