阅读说明：本技术 一种气水循环的臭氧催化氧化污水处理装置 (Ozone catalytic oxidation sewage treatment device with air-water circulation ) 是由 不公告发明人 于 2021-08-24 设计创作，主要内容包括：本发明公开了一种气水循环的臭氧催化氧化污水处理装置,包括反应塔和自反应塔的下部进入反应塔的进水管；位于反应塔外部的所述进水管上沿污水进入方向依次设有进水射流泵和臭氧投加射流器,所述臭氧投加射流器还连通有臭氧投加管,进水管端部设有臭氧混合曝气头；反应塔内位于所述臭氧混合曝气头的上部设有臭氧催化床层,所述臭氧催化床层内设有多个水汽循环曝气头,多个水汽循环曝气头同时连接有延伸至所述反应塔外部的污水循环管,污水循环管向上延伸并连通催化床层上部的污水,所述污水循环管上还设有臭氧循环射流器。本发明的气水循环的臭氧催化氧化污水处理装置能够减少催化床层死区、增加催化剂与臭氧接触、提高臭氧利用率。(The invention discloses an ozone catalytic oxidation sewage treatment device with air-water circulation, which comprises a reaction tower and a water inlet pipe entering the reaction tower from the lower part of the reaction tower; a water inlet jet pump and an ozone adding jet device are sequentially arranged on the water inlet pipe positioned outside the reaction tower along the sewage inlet direction, the ozone adding jet device is also communicated with an ozone adding pipe, and an ozone mixing aeration head is arranged at the end part of the water inlet pipe; the ozone mixing aeration head is arranged on the upper portion of the ozone mixing aeration head in the reaction tower, a plurality of water vapor circulation aeration heads are arranged in the ozone catalysis bed, the water vapor circulation aeration heads are simultaneously connected with a sewage circulating pipe extending to the outside of the reaction tower, the sewage circulating pipe extends upwards and is communicated with sewage on the upper portion of the ozone mixing aeration head, and an ozone circulation ejector is further arranged on the sewage circulating pipe. The air-water circulating ozone catalytic oxidation sewage treatment device can reduce dead zones of catalytic beds, increase contact of a catalyst and ozone and improve the utilization rate of ozone.)

1. The utility model provides a sewage treatment plant of ozone catalytic oxidation of gas-water circulation which characterized in that: comprises a reaction tower and a water inlet pipe entering the reaction tower from the lower part of the reaction tower;

a water inlet jet pump and an ozone adding jet device are sequentially arranged on the water inlet pipe positioned outside the reaction tower along the sewage inlet direction, the ozone adding jet device is also communicated with an ozone adding pipe, and an ozone mixing aeration head is arranged at the end part of the water inlet pipe positioned inside the reaction tower;

an ozone catalytic bed layer is arranged on the upper portion of the ozone mixing aeration head in the reaction tower, a plurality of water vapor circulation aeration heads are arranged in the ozone catalytic bed layer, the water vapor circulation aeration heads are simultaneously connected with a sewage circulating pipe extending to the outside of the reaction tower, the sewage circulating pipe extends upwards and is communicated with sewage on the upper portion of the catalytic bed layer, and an ozone circulation ejector is further arranged on the sewage circulating pipe;

the sewage circulating pipe arranged in the reaction tower is communicated with a plurality of sewage circulating branch pipes which are arranged at intervals up and down, the plurality of sewage circulating branch pipes are arranged in parallel, and a plurality of water vapor circulating aeration heads are uniformly arranged on the plurality of sewage circulating branch pipes;

the top of the reaction tower is connected with an ozone circulating pipe, and the other end of the ozone circulating pipe is connected with the ozone circulating ejector.

2. The gas-water circulating ozone catalytic oxidation sewage treatment device of claim 1, wherein a circulating power pump is further arranged on the sewage circulating pipe at the upper part of the ozone circulating ejector.

3. The gas-water circulating ozone catalytic oxidation sewage treatment device of claim 1, wherein the upper part of the reaction tower is provided with a water outlet.

4. The gas-water circulating ozone catalytic oxidation sewage treatment device as claimed in claim 1, wherein a pressure relief valve is arranged at the top of the reaction tower.

5. The gas-water circulating ozone catalytic oxidation sewage treatment device of claim 1, wherein a support layer is attached to the lower part of the ozone catalytic bed layer.

6. The air-water circulating ozone catalytic oxidation sewage treatment device according to claim 5, wherein the support layer has a plate-like structure in which communication holes are uniformly formed.

7. The gas-water circulating ozone catalytic oxidation sewage treatment device of claim 5, wherein the ozone catalytic bed layer comprises a plurality of catalysts which are reserved with gaps and are arranged in a stacked mode, and the catalysts are spherical particles or columnar particles.

8. The gas-water circulating ozone catalytic oxidation sewage treatment device of claim 6, wherein the catalyst is a ferro-manganese catalyst.

Technical Field

The invention relates to the field of water pollution purification, in particular to an ozone catalytic oxidation sewage treatment device with air-water circulation.

Background

Ozone is a common oxidant, and can be converted into nontoxic oxygen after reacting with reducing substances, and no secondary pollution is caused. Therefore, the ozone oxidation process is widely applied to the field of organic wastewater treatment and the field of tap water pretreatment. Wherein, the ozone catalytic oxidation process has the highest efficiency.

At present, a reaction tank applied to ozone catalytic oxidation engineering is generally in a fixed bed form, a used catalyst is mainly high-density metal oxide pellets or a carrier type catalyst, sewage is easy to form channeling and dead zones in the fixed bed, only a small amount of catalyst can be contacted with the sewage and ozone, and the catalytic effect of the fixed bed is not obvious. On the other hand, the ozone gas has a high rising speed in water, and a considerable part of the ozone is discharged to the ozone destructor without being utilized, so that the ozone utilization rate is low, and the operation cost is increased. In addition, the fixed bed catalyst is easily covered by hardness ions in water, so that scaling occurs to influence catalytic activity, a backwashing device needs to be additionally arranged, the investment cost is increased due to the arrangement of the backwashing device, and the quality of effluent water can be influenced due to the shutdown backwashing process. Therefore, reducing dead zones of the catalytic bed, increasing contact between the catalyst and sewage, improving the utilization rate of ozone and reducing the arrangement of a backwashing device are important means for improving the water treatment process of catalytic oxidation of ozone.

Disclosure of Invention

The invention aims to overcome the defects of the prior art and provide the air-water circulating ozone catalytic oxidation sewage treatment device which can reduce dead zones of a catalytic bed layer, increase contact between a catalyst and sewage and improve the utilization rate of ozone.

In order to realize the aim, the invention provides an ozone catalytic oxidation sewage treatment device with air-water circulation, which comprises a reaction tower and a water inlet pipe entering the reaction tower from the lower part of the reaction tower;

a water inlet jet pump and an ozone adding jet device are sequentially arranged on the water inlet pipe positioned outside the reaction tower along the sewage inlet direction, the ozone adding jet device is also communicated with an ozone adding pipe, and an ozone mixing aeration head is arranged at the end part of the water inlet pipe positioned inside the reaction tower;

an ozone catalytic bed layer is arranged on the upper portion of the ozone mixing aeration head in the reaction tower, a plurality of water vapor circulation aeration heads are arranged in the ozone catalytic bed layer, the water vapor circulation aeration heads are simultaneously connected with a sewage circulating pipe extending to the outside of the reaction tower, the sewage circulating pipe extends upwards and is communicated with sewage on the upper portion of the catalytic bed layer, and an ozone circulation ejector is further arranged on the sewage circulating pipe;

the top of the reaction tower is connected with an ozone circulating pipe, and the other end of the ozone circulating pipe is connected with the ozone circulating ejector.

As a preferable scheme, a circulating power pump is further arranged on the sewage circulating pipe positioned at the upper part of the ozone circulating ejector.

Preferably, the upper part of the reaction tower is provided with a water outlet.

Preferably, a pressure relief valve is arranged at the top of the reaction tower.

As a preferred scheme, the lower part of the ozone catalytic bed layer is provided with a bearing layer in a bonding way.

Preferably, the support layer has a plate-like structure in which communication holes are uniformly formed.

Preferably, the ozone catalytic bed layer comprises a plurality of catalysts which are reserved with gaps and are arranged in a stacking mode and are spherical particles or columnar particles.

Preferably, the catalyst is a ferro-manganese catalyst.

Preferably, the sewage circulating pipe arranged in the reaction tower is communicated with a plurality of sewage circulating branch pipes which are arranged at intervals up and down, the plurality of sewage circulating branch pipes are arranged in parallel, and the plurality of water vapor circulating aeration heads are uniformly arranged on the plurality of sewage circulating branch pipes.

Compared with the prior art, the invention has the beneficial effects that:

the sewage of the ozone catalytic oxidation sewage treatment device with air-water circulation enters from the water inlet pipe by using the water inlet jet pump, and the ozone enters the ozone adding jet device through the ozone adding pipe and is fully mixed with the sewage, and then enters the reaction tower through the ozone mixing aeration head; the sewage level gradually rises, after the contact reaction of the ozone catalytic bed layer, the sewage on the upper part of the reaction tower enters the ozone circulating ejector through the sewage circulating pipe and enters the reaction tower from the water vapor circulating aeration head arranged in the catalytic bed layer, and the sewage is uniformly contacted with the ozone catalytic bed layer again, so that the reaction efficiency is improved, and meanwhile, the catalytic bed layer is continuously back-washed with certain strength to maintain the cleanness of the surface of the catalyst. When the pressure in the reaction tower reaches a certain value, redundant trace ozone is discharged from the pressure release valve and then discharged into the atmosphere after passing through the tail gas destructor.

The ozone catalytic oxidation sewage treatment device with gas-water circulation can perform secondary circulation on the unused tail gas, improve the ozone utilization rate, reduce the ozone concentration of the tail gas and reduce the scale and investment of a tail gas destruction device.

The water vapor circulation aeration head is arranged in the ozone catalyst bed layer, so that on one hand, the local water flow acceleration can be improved through the water amount of the internal circulation, the expansion rate of the catalyst bed layer can reach more than 5 percent, the catalyst bed layer is converted from a complete fixed bed to a micro fluidized bed, the reaction dead zone in the fixed bed is reduced, on the other hand, the water vapor mixed flow can form certain strength cleaning on the surface of the catalyst in the fixed bed, the salt scale accumulation on the surface of the catalyst is prevented, and the service life of the catalyst is prolonged; meanwhile, the generation of channeling of the fixed bed layer can be reduced, the dead zone of the fixed bed layer reaction is reduced, and the multiphase contact in the catalytic bed layer is increased.

In the prior art, because the particles or the columnar catalyst is in a static state in a water body, when the water body contains certain calcium, magnesium, carbonate and other anions and cations, the long-time adsorption and aggregation effect can generate a scaling phenomenon on the surface of the catalyst and between the particles, further shield active sites of the catalyst, reduce the activity of the catalyst, increase the head loss, and have to adopt periodic backwashing to flush catalyst bed layers, thereby increasing the operation and energy consumption without end; the invention can utilize the ozone tail gas to continuously wash the catalytic bed layer with certain intensity without additionally arranging a back washing module.

Drawings

FIG. 1 is a schematic structural diagram of an ozone catalytic oxidation sewage treatment device with air-water circulation, provided by the invention;

FIG. 2 is a comparison of COD degradation effects of different systems;

figure 3 is a comparison of ozone utilization for different systems.

In the figure, 1, a water inlet jet pump; 2. an ozone adding ejector; 3. an ozone adding pipe; 4. a support layer; 5. an ozone mixing aeration head; 6. an ozone catalytic bed layer; 7. a water vapor circulation aeration head; 8. a circulating power pump; 9. an ozone circulating ejector; 10. a pressure relief valve; 11. an ozone circulation pipe; 12. a water outlet; 13. a reaction tower; 14. a water inlet pipe; 15. a sewage circulating pipe.

Detailed Description

The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.

In the description of the present invention, it is to be understood that the terms "upper", "lower", "left", "right", "top", "bottom", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. It should be understood that the terms "first", "second", etc. are used herein to describe various information, but the information should not be limited to these terms, which are only used to distinguish one type of information from another. For example, "first" information may also be referred to as "second" information, and similarly, "second" information may also be referred to as "first" information, without departing from the scope of the present invention.

The preferred embodiment of the ozone catalytic oxidation sewage treatment device with gas-water circulation of the invention, as shown in figure 1, comprises a reaction tower 13 and a water inlet pipe 14 which enters the reaction tower 13 from the lower part of the reaction tower 13; a water inlet jet pump 1 and an ozone adding jet device 2 are sequentially arranged on a water inlet pipe 14 positioned outside the reaction tower 1 along the sewage inlet direction, the ozone adding jet device 2 is also communicated with an ozone adding pipe 3, the ozone adding pipe 3 is communicated with ozone, and an ozone mixing aeration head 5 is arranged at the end part of the water inlet pipe 14 positioned inside the reaction tower 1; the sewage mixed with ozone is introduced into the lower portion of the reaction tower 1 through the water inlet pipe 14. An ozone catalytic bed layer 6 is arranged at the upper part of the ozone mixing aeration head 5 in the reaction tower 1, and the water level of the sewage is gradually increased after the sewage enters the lower part of the reaction tower 13 and is mixed and oxidized with the ozone in the ozone catalytic bed layer 6; a plurality of water vapor circulation aeration heads 7 are arranged in the ozone catalytic bed layer 6, the water vapor circulation aeration heads 7 are simultaneously connected with a sewage circulating pipe 15 extending to the outside of the reaction tower 13, the sewage circulating pipe 15 extends upwards and is communicated with sewage on the upper part of the ozone catalytic bed layer 6, an ozone circulation ejector 9 is also arranged on the sewage circulating pipe 15, the sewage on the upper part of the reaction tower 13 enters the ozone circulation ejector 9 through the sewage circulating pipe 15, meanwhile, the top of the reaction tower 13 is connected with an ozone circulating pipe 11, the other end of the ozone circulating pipe 11 is connected with the ozone circulation ejector 9, so that the sewage enters the reaction tower 13 from the water vapor circulation aeration heads 7 arranged in the ozone catalytic bed layer 6 and is uniformly contacted with the ozone catalytic bed layer 6 again, thus, the ozone in tail gas can be recycled, the utilization rate of the ozone is improved, the reaction efficiency is improved, and the continuous backwashing with certain strength is carried out on the catalytic bed layer, the surface of the catalyst is kept clean.

The ozone catalytic oxidation sewage treatment device with gas-water circulation can perform secondary circulation on the unused tail gas, improve the ozone utilization rate, reduce the ozone concentration of the tail gas and reduce the scale and investment of a tail gas destruction device.

The second ozone mixing and circulating aeration head is arranged in the ozone catalytic bed layer 6, so that the local water flow acceleration can be improved through the water quantity of the internal circulation, the expansion rate of the catalytic bed layer reaches more than 5 percent, the catalytic bed layer is converted from a complete fixed bed to a micro fluidized bed, the reaction dead zone in the fixed bed is reduced, the multiphase contact in the catalytic bed layer is increased, and the pollutant removal rate is improved;

in the prior art, because the particles or the columnar catalyst is in a static state in a water body, when the water body contains certain calcium, magnesium, carbonate and other anions and cations, the long-time adsorption and aggregation effect can generate a scaling phenomenon on the surface of the catalyst and between the particles, further shield active sites of the catalyst, reduce the activity of the catalyst, increase the head loss, and have to adopt periodic backwashing to flush catalyst bed layers, thereby increasing the operation and energy consumption without end; the invention can utilize the ozone tail gas to continuously wash the ozone catalytic bed layer 6 with certain intensity without additionally arranging a back washing module.

Inside water vapor circulation aeration head 7 was laid in ozone catalytic bed layer 6, the reaction blind spot in the reducible fixed bed on the one hand, on the other hand water vapor mixing flow can form the washing of certain intensity to the catalyst surface in the fixed bed, prevents the accumulation of catalyst surface salt dirt, prolongs the life of catalyst.

Wherein, a circulating power pump 8 is also arranged on the sewage circulating pipe positioned at the upper part of the ozone circulating ejector 9 and is used for transmitting the sewage at the upper part of the reaction tower 13 into the sewage circulating pipe 15.

Wherein, the upper part of the reaction tower 1 is provided with a water outlet 12 for discharging the purified sewage out of the reaction tower 13.

Further, a pressure relief valve 10 is arranged at the top of the reaction tower 13, so that the pressure in the reaction tower 13 is prevented from being too high.

Wherein, the lower part of the ozone catalytic bed layer 6 is provided with a bearing layer 4 for bearing the catalyst in the ozone catalytic bed layer 6; in the present embodiment, the support layer 4 has a plate-like structure in which the communication holes are uniformly formed, but in other embodiments of the present application, the support layer 4 may have a net-like structure.

Further, the ozone catalytic bed layer 6 of this application includes that a plurality of reservation is gapped and pile up the catalyst of the globular granule or the column granule of arranging, reserves the clearance and is convenient for sewage to enter into in the clearance to make the reaction of catalyst and sewage more abundant. Illustratively, the catalyst in the examples of the present application is a ferro manganese catalyst.

Wherein, set up sewage circulating pipe 15 inside reaction tower 13 intercommunication have a plurality of sewage circulation branch pipes of interval arrangement from top to bottom, form the sewage circulation of layering and divide the pipe, a plurality of sewage circulation divide the pipe and arrange side by side, a plurality of steam circulation aeration heads 7 evenly set up on a plurality of sewage circulation divide the pipe to make the intraformational sewage of ozone catalytic bed carry out abundant reaction with catalyst and ozone.

In the application, sewage enters from a water inlet pipe 14 by using a water inlet jet pump 1, and ozone enters an ozone adding jet device 2 through an ozone adding pipe 3 and is fully mixed with the sewage, and then enters a reaction tower 13 through an ozone mixing aerator 5; the sewage water level gradually rises, after the contact reaction of the ozone catalytic bed layer 6, the sewage on the upper part of the reaction tower 13 enters the ozone circulation ejector 9 through the sewage circulation pipe 15, and enters the reaction tower 13 from the water vapor circulation aeration head 7 arranged in the ozone catalytic bed layer 6 to be uniformly contacted with the ozone catalytic bed layer 6 again, so that the reaction efficiency is improved, and meanwhile, the continuous backwashing with certain strength is carried out on the catalytic bed layer 6 to maintain the cleanness of the surface of the catalyst. When the pressure in the reaction tower 13 reaches a certain value, the redundant trace ozone is discharged into the atmosphere after passing through the tail gas destructor after being discharged from the pressure release valve.

For example, in the case of treating industrial wastewater, the initial COD of the wastewater is 136mg/L, the ozone dosage is 150mg/L, and the wastewater is treated by using an internal circulation microfluidization ozone catalytic oxidation wastewater treatment device.

As shown in figure 1, sewage enters from a water inlet jet pump 1, ozone enters an ozone adding jet device 2 through an ozone adding pipe 3, is fully mixed with the sewage, and then enters a reaction tower through an ozone mixing aerator 5. The sewage water level rises gradually, after the contact reaction of the ozone catalytic bed layer 6, partial sewage is pressurized by the circulating power pump 8, is mixed with the residual ozone passing through the ozone circulating ejector 9 again, enters the reaction tower from the water vapor circulating aeration head 7 which is uniformly arranged in the catalytic bed layer in a layered mode, is in uniform contact with the ozone catalyst again, enables the ozone catalytic bed layer to form microfluidization, improves the reaction efficiency, and meanwhile carries out continuous backwashing with certain strength on the catalytic bed layer to maintain the cleanness of the catalyst surface. When the pressure in the reaction tower reaches a certain value, redundant trace ozone is discharged into the atmosphere after passing through the tail gas destructor after being discharged from the pressure release valve 10. Measuring the COD of the effluent and the concentration of the residual ozone in the gas.

In addition, adopt sewage treatment plant among the prior art to handle industrial sewage, specific flow is: sewage enters from the water inlet jet pump, ozone enters the jet device through the ozone adding pipe and is fully mixed with the sewage, and then the ozone enters the reaction tower through the ozone mixing aeration head. The water level of the sewage is gradually raised, and the sewage is directly drained after the contact reaction of the ozone catalytic bed layer. The water vapor circulation module does not work. Measuring the COD of the effluent and the concentration of the residual ozone in the gas.

Fig. 2 and 3 are graphs showing changes in COD removal rate and ozone utilization rate of the sewage treatment apparatus of the present embodiment and the prior art, respectively, after the sewage treatment apparatus of the present embodiment and the prior art continuously operates for 60 days, and it can be seen from the graphs that the initial COD removal rate of the present embodiment is 56.2%, and the initial COD removal rate of the prior art is only 43.2%, and it can be seen that the COD removal effect is significantly improved after the steam-water circulation aeration head microfluidizes the catalytic bed. On the other hand, the ozone utilization rate of the embodiment of the present application is as high as 93.1%, while the ozone utilization rate of the prior art is only 75.6%, which shows that the tail gas can be effectively recycled in the embodiment 1. After 60 days of operation, the COD degradation rate of the embodiment of the application is basically stabilized to be more than 50%, and the COD degradation rate in the prior art is reduced from 43.2% to 30.8%, which shows that the sewage treatment device adopting the embodiment of the application has the beneficial effects of cleaning the surface of the catalyst and improving the long-term use stability of the catalyst.

The above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and substitutions can be made without departing from the technical principle of the present invention, and these modifications and substitutions should also be regarded as the protection scope of the present invention.