CN210764696U - Reinforced up-flow type multiphase wastewater oxidation treatment system - Google Patents
Reinforced up-flow type multiphase wastewater oxidation treatment system Download PDFInfo
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- CN210764696U CN210764696U CN201920955660.3U CN201920955660U CN210764696U CN 210764696 U CN210764696 U CN 210764696U CN 201920955660 U CN201920955660 U CN 201920955660U CN 210764696 U CN210764696 U CN 210764696U
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Abstract
The utility model discloses a reinforce heterogeneous waste water oxidation treatment system of STREAMING, this processing system is including the heterogeneous waste water oxidation system of the STREAMING that meets in proper order, solid-liquid separation system, neutralization degasification system and flocculation and precipitation system. During treatment, wastewater firstly enters an up-flow multiphase wastewater oxidation system for oxidation treatment, then the wastewater is sent into a solid-liquid separation system for solid-liquid separation, the separated heterogeneous catalytic carrier is sent back to the up-flow multiphase wastewater oxidation system, then the wastewater is sent into a neutralization degassing system, the pH of the wastewater is adjusted to 5.5-7.5, stirring and degassing are carried out, finally the wastewater is sent into a flocculation precipitation system for mud-water separation, supernatant liquid is discharged, and precipitated iron mud is subjected to filter pressing and then is transported outside for harmless treatment. Adopt the utility model discloses processing system can improve heterogeneous waste water oxidation treatment system's treatment effect, reduces the fenton reagent quantity, effectively reduces the production of chemical sludge.
Description
Technical Field
The utility model relates to an organic wastewater treatment device, in particular to an intensified upflow multiphase wastewater oxidation treatment system.
Background
The existing technology for treating the wastewater difficult to be biochemically degraded comprises an ozone oxidation method, an activated carbon adsorption method, a Fenton oxidation method and the like, wherein the Fenton oxidation method (H) is adopted2O2/Fe2+) Is the most efficient, simple and economical method.
The combination of ferrous salt (such as ferrous sulfate) and hydrogen peroxide (hydrogen peroxide) is called Fenton reagent, which can effectively oxidize and remove refractory organic matters which can not be removed by the traditional wastewater treatment technology, and the essence is H2O2In Fe2+Generate hydroxyl free radical (OH) with high reactivity under the catalysis of the (C), and the OH can react with most organic mattersThe reactants react to degrade them.
In a broad sense, the Fenton method utilizes the action of a catalyst or electrochemistry, and the like, and passes H2O2To produce OH-treated organic matter. However, a large amount of Fe is required in the course of a simple Fenton oxidation method2+The amount of the iron mud added is added to maintain sufficient OH generation, and a large amount of iron mud is generated during the treatment process, thereby requiring additional treatment cost. There may also be some very refractory organics or residual organics that are not degraded. The traditional homogeneous Fenton iron mud is more, and the oxidation efficiency is low; the traditional heterogeneous Fenton catalyst has large loss, and iron mud newly generated in the production, processing and operation processes is attached with a plurality of metals to combine into the catalyst, so that the efficiency of the catalyst is reduced.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a reinforce heterogeneous waste water oxidation treatment system of STREAMING is provided, this processing system has combined homogeneous catalysis technique, carrier heterogeneous catalysis technique, ozone aeration catalysis technique, catalyzes the fenton reaction process fully to utilize remaining hydrogen peroxide solution secondary degradation to remain the organic matter, strengthened the throughput of traditional heterogeneous waste water treatment system of STREAMING.
The utility model discloses solve above-mentioned technical problem with following technical scheme:
the utility model discloses a reinforced upflow multiphase wastewater oxidation treatment system, which comprises an upflow multiphase wastewater oxidation system, a solid-liquid separation system, a neutralization degassing system and a flocculation precipitation system which are connected in sequence;
the upflow multiphase wastewater oxidation system comprises an upflow multiphase wastewater oxidation tower, the bottom of the upflow multiphase wastewater oxidation tower is provided with a water distribution cover, the inside of the upflow multiphase wastewater oxidation tower is filled with a heterogeneous catalysis carrier, the upper part of the upflow multiphase wastewater oxidation tower is provided with a solid-liquid separator, the water distribution cover and the solid-liquid separator are respectively positioned below and above the heterogeneous catalysis carrier, the upper part of the solid-liquid separator is provided with a water inlet A and a water inlet circulation tank connected with the water inlet A, the water inlet circulation tank is connected with the water distribution cover at the bottom through a circulation pipe, the circulation pipe is provided with a circulation pump;
the solid-liquid separation system comprises a cyclone separator, the upper part of the cyclone separator is provided with a water inlet B connected with a water outlet A of the up-flow multiphase wastewater oxidation tower, the bottom of the cyclone separator is provided with a sand discharge pipe, the inside of the cyclone separator is provided with a central pipe for upwards conveying wastewater, and the upper part of the central pipe is provided with a water outlet B;
the neutralization and degassing system comprises a neutralization tower and a degassing tower, wherein the bottoms of the neutralization tower and the degassing tower are respectively provided with a microporous aeration disc into which ozone air and pure oxygen can be introduced, the upper parts of the neutralization tower and the degassing tower are respectively provided with a gas-liquid two-phase separator, the upper part of the gas-liquid two-phase separator is connected with a gas-liquid separator through a pipeline, the gas-liquid separator is provided with a descending pipe extending into the lower part of the tower, the lower part of the neutralization tower is provided with a water inlet C connected with a water outlet B of the solid-liquid separation system, the upper part of the neutralization tower is provided with a water outlet C positioned above the gas-liquid two-phase separator, the bottom of the degassing tower is provided with a water inlet D connected with the water outlet C;
the flocculation sedimentation system comprises a flocculation sedimentation tank, the flocculation sedimentation tank is connected with a water outlet D of the degassing tower, a supernatant discharge port is arranged at the upper part of the flocculation sedimentation tank, and a sludge discharge port is arranged at the bottom of the flocculation sedimentation tank.
The gas discharge port of the gas-liquid separator is connected with two pipeline branches in a parallel connection mode, one branch is connected with the manganese dioxide filler, and the other branch is connected with the air inlet pipe of the microporous aeration disc through the booster fan.
Compared with the prior art, the utility model, following beneficial effect has:
1) the utility model can improve the capability of the oxidation system for catalyzing and degrading organic matters and reduce the dosage of Fenton medicament;
2) the utility model can better intercept the heterogeneous catalysis carrier in the system by adding the solid-liquid separation system, so that the heterogeneous catalysis carrier can continuously play a role;
3) the utility model discloses adopt the ozone of certain concentration and the air to mix jointly and expose to the sun in neutralization tower and degasser, when maintaining certain aeration quantity, the ozone that lets in can take place catalytic reaction with remaining hydrogen peroxide solution in the aquatic, takes place the secondary oxidation process, improves the treatment effect of system, and it remains to reduce the medicament.
Drawings
FIG. 1 is a schematic view of the operation of the enhanced upflow multiphase wastewater oxidation treatment system of the present invention.
FIG. 2 is a schematic structural diagram of an upflow multiphase wastewater treatment oxidation tower adopted in the reinforced upflow multiphase wastewater oxidation treatment system of the present invention.
FIG. 3 is a schematic diagram of a cyclone separator used in the enhanced upflow multiphase wastewater oxidation treatment system of the present invention.
FIG. 4 is a schematic diagram of the structure of the neutralization tower and the degassing tower which are used in the enhanced upflow multiphase wastewater oxidation treatment system.
FIG. 5 is a schematic structural view of a flocculation sedimentation tank used in the enhanced upflow multi-phase wastewater oxidation treatment system of the present invention.
In the figure: 1-an up-flow multiphase wastewater treatment oxidation tower; 2-water outlet A; 3-a water inlet circulation tank; 4-water inlet A; 5-a heterogeneous catalytic support; 6-a solid-liquid separator; 7-a circulation pipe; 8-a circulating pump; 9-water distribution cover; 10-a cyclone separator; 11-a central tube; 12-a sand discharge pipe; 13-a neutralization column; 14-a gas-liquid two-phase separator; 15-gas-liquid separator; 16-a downcomer; 17-a microporous aeration disc; 18-manganese dioxide filler; 19-a degasser column; 20-a flocculation sedimentation tank, 21-a water inlet B, 22-a water outlet B, 23-a water inlet C, 24-a water outlet C, 25-a water inlet D, 26-a water outlet D, 27-a supernatant discharge port, 28-a sludge discharge port and 29-a booster fan.
Detailed Description
In order to illustrate the treatment process of the present invention more clearly, the following non-limiting detailed description of the technical solution of the present invention is made with reference to the accompanying drawings and specific examples.
As shown in figure 1, the treatment system adopted by the treatment process of the utility model comprises an upflow multi-phase wastewater treatment system, a solid-liquid separation system, a neutralization and degassing system and a flocculation and precipitation system.
As shown in figure 2, heterogeneous waste water oxidation system of upflow includes heterogeneous waste water oxidation tower 1 of upflow, the bottom of heterogeneous waste water oxidation tower 1 of upflow is equipped with water distribution cover 9, inside is filled with heterogeneous catalysis carrier 5, upper portion is equipped with solid-liquid separator 6, water distribution cover 9 and solid-liquid separator 6 are located heterogeneous catalysis carrier 5's below and top respectively, solid-liquid separator 6's top is equipped with water inlet A4 and the water inlet circulation groove 3 that is connected with water inlet A4, water inlet circulation groove 3 is connected with the water distribution cover 9 of bottom through circulating pipe 7, install circulating pump 8 on this circulating pipe 7, solid-liquid separator 6's top is equipped with delivery port A2.
As shown in fig. 3, the solid-liquid separation system includes a cyclone separator 10, a water inlet B21 connected to a water outlet A2 of the upflow multiphase wastewater oxidation tower 1 is provided at an upper portion of the cyclone separator 10, a sand discharge pipe 12 is provided at a bottom portion of the cyclone separator 10, a central pipe 10 for upwardly transporting wastewater is provided inside the cyclone separator 10, and a water outlet B22 is provided at an upper portion of the central pipe 10.
As shown in fig. 4, the neutralization and degassing system comprises a neutralization tower 13 and a degassing tower 19, the bottoms of the neutralization tower 13 and the degassing tower 19 are respectively provided with a microporous aeration disc 17 into which ozone air and pure oxygen can be introduced, the upper parts of the neutralization tower 13 and the degassing tower 19 are respectively provided with a gas-liquid two-phase separator 14, the upper part of the gas-liquid two-phase separator 14 is connected with a gas-liquid separator 15 through a pipeline, the gas-liquid separator 15 is provided with a downcomer 16 extending into the lower parts of the neutralization tower 13 and the degassing tower 19, the lower part of the neutralization tower 13 is provided with a water inlet C23 connected with a water outlet B22 of the solid-liquid separation system, the upper part of the neutralization tower 13 is provided with a water outlet C24 positioned above the gas-liquid two-phase separator, the bottom of the degassing tower 19 is provided with a water inlet D25 connected with a water outlet C24, the upper part of the degassing tower 19 is provided with a water outlet D26 positioned, one of the pipeline branches is connected with the manganese dioxide filler 18, and the other pipeline branch is connected with the air inlet pipe of the microporous aeration disc 17 through a booster fan 29.
As shown in fig. 5, the flocculation sedimentation system comprises a flocculation sedimentation tank 20, the flocculation sedimentation tank 20 is connected with a water outlet D26 of the degassing tower 19, a supernatant discharge port 27 is arranged at the upper part of the flocculation sedimentation tank 20, and a sludge discharge port 28 is arranged at the bottom.
The utility model discloses strengthen heterogeneous waste water oxidation treatment system of STREAMING's concrete operation process as follows:
in the first step, the refractory organic wastewater first enters an upflow multiphase wastewater oxidation system, which comprises an upflow multiphase wastewater oxidation tower 1. The organic wastewater difficult to degrade firstly enters a water inlet circulating groove 3 at the top of an up-flow multiphase wastewater treatment oxidation tower 1 through a water inlet A4, and ferrous sulfate and H are added into the water inlet circulating groove 32O2The Fenton reagent and the homogeneous phase catalytic promoter are formed, waste water and the reagent are mixed and then enter a water distribution cover 9 at the bottom of an up-flow type multiphase waste water oxidation tower 1 through a circulating pipe 7, the waste water is subjected to oxidation treatment and then is subjected to solid-liquid separation through a solid-liquid separator 6, and then the waste water is discharged from a water outlet A2 and enters the next working procedure.
In the step, the wastewater is firstly mixed with a Fenton reagent to form OH with high reaction activity and react with organic molecules, a high molecular organic matter is oxidized and degraded into a small molecular organic matter, the Fenton reagent is fully contacted with a homogeneous phase catalytic promoter in a good fluidization state of a system, and more OH is generated under the catalytic action to participate in the reaction; metal element and Fe in homogeneous phase catalysis promoter2+And H2O2Produced Fe3+The heterogeneous catalyst is adsorbed on the surface of the heterogeneous catalyst carrier 5 in a crystallization or precipitation mode to form heterogeneous catalyst particles, and the heterogeneous catalyst particles and the homogeneous catalyst promoter act together, so that the treatment efficiency of the oxidation system is improved.
The adding amount of the Fenton medicament in the step is added according to the conventional requirement, and the heterogeneous catalytic carrier is added before the system is started, wherein the adding amount is 1/10-1/3 of the volume of the upflow type multiphase wastewater oxidation tower; the heterogeneous catalysis carrier is a spherical heterogeneous catalysis carrier with the diameter of 2-5 mm or a polyhedral heterogeneous catalysis carrier with the maximum diagonal distance of 2-5 mm, and is made of an inorganic carrier of ceramic, silicon dioxide or active alumina or an organic inert carrier of PVA and PVE.
The homogeneous phase catalysis promoter is a liquid homogeneous phase catalysis promoter, and contains but is not limited to cation trace elements of iron, manganese, cobalt and nickel, wherein the concentration of iron is 10-20 mg/L, the concentration of manganese is 5.0-15 mg/L, the concentration of cobalt is 1.0-3.0 mg/L, and the concentration of nickel is 0.5-1.0 mg/L.
In the operation process of the up-flow type multiphase wastewater oxidation tower, the homogeneous phase catalytic promoter is added for the first time according to 1-5 per mill of the treated water amount, and the homogeneous phase catalytic promoter is continuously added for 5-10 days to maintain the amount; and after each time of system sand discharge, continuously supplementing and maintaining according to 1-5 per mill of the treated water amount, and continuously adding for 3-5 days.
And secondly, sending the wastewater treated by the upflow multiphase wastewater oxidation system into a solid-liquid separation system, wherein the solid-liquid separation system can adopt a cyclone separator 10. Effluent of the upflow multiphase wastewater oxidation tower 1 enters a cyclone separator 10 through a water outlet A2, part of heterogeneous catalytic carriers 5 flowing into the cyclone separator 10 are enriched at the bottom of the cyclone separator 10 through the cyclone effect, and can be discharged through a sand discharge pipe 12 to be activated, regenerated and recycled after reaching a certain amount, and separated wastewater enters the next process after being discharged through a central pipe 10 and a water outlet B24.
The solid-liquid separation system can adopt a separation mode of fluid arresting by an inclined plate, an inclined pipe or an arresting net, and can also adopt a mode of cyclone centrifugal separation and gravity separation.
And thirdly, feeding the separated wastewater into a neutralization and degassing system which comprises a neutralization tower 13 and a degassing tower 19 which are connected. The method comprises the steps of firstly enabling wastewater to enter a neutralization tower 13, adding alkali liquor into the neutralization tower 13, simultaneously introducing mixed air containing 1-10% of ozone in mass concentration into the bottom of the neutralization tower 13 through a microporous aeration disc 17 and an air inlet pipe connected with the microporous aeration disc 17 for aeration stirring, adjusting the pH value of the wastewater to 5.5-7.5 for 15-25 min, then carrying out gas-liquid separation treatment on the wastewater through a gas-liquid two-phase separator 14, then sending the wastewater into a degassing tower 19, adding a PAM solution into the degassing tower 19, simultaneously introducing mixed air containing 1-10% of ozone in mass concentration into the bottom of the degassing tower 19 for gas stripping, wherein the treatment time is 20-30 min, then carrying out gas-liquid separation treatment on the wastewater through the gas-liquid two-phase separator 14, and then sending the wastewater into a flocculation precipitation system.
The gas-liquid two-phase separator 14 can collect carbon dioxide gas generated by the reaction and residual ozone gas which is not completely reacted. The gas-liquid separator 15 separates the wastewater mixed liquid from the gas stripping and the mixed gas of residual ozone or air and pure oxygen. Can set up ozone concentration and atmospheric pressure monitoring devices above vapour and liquid separator 15, when ozone concentration is higher in the vapour and liquid separator 15, carry the mist in the vapour and liquid separator to neutralization tower and degasification tower bottom through booster fan 29 and carry out aeration once more, make remaining ozone obtain make full use of, and take place advanced catalytic reaction with hydrogen peroxide solution, play the stirring effect to the liquid alkali that the neutralization tower added and the PAM solution that the degasification tower added simultaneously, can not satisfy the requirement of recycling until monitoring ozone concentration and the pressure in the vapour and liquid separator. When the mixed gas in the gas-liquid separator does not meet the reuse requirement, the mixed gas is discharged to a manganese dioxide filler 18 to absorb residual low-concentration ozone, so that the discharged mixed gas meets the discharge requirement.
The mass transfer efficiency can be improved through micropore aeration, and the residual hydrogen peroxide in the wastewater is catalytically decomposed under the aeration action of ozone to form nascent OH, so that the residual micromolecular organic matters are further reacted, and secondary oxidative degradation is realized.
Fourthly, the wastewater treated by the neutralization and degassing system is sent to a flocculation sedimentation system, the flocculation sedimentation system comprises a flocculation sedimentation tank 20, the wastewater enters the flocculation sedimentation tank 20 and is subjected to flocculation sedimentation with a fed flocculating agent in the tank, precipitated sludge (iron mud) is discharged from a sludge discharge port 28 after being concentrated by gravity, is subjected to dehydration and filter pressing and is then transported out for harmless treatment, and supernatant on the upper part of the sedimentation tank is discharged after reaching the standard through a supernatant discharge port 27; the treatment time of the flocculation sedimentation tank 20 is 2-3 hours.
The following are application examples of the treatment system of the present invention:
example 1
Adopt the utility model discloses processing system handles the biochemical effluent of a certain paper mill, former waste water COD365mg/L, and colourity is 80 times. The wastewater is sent into a water inlet circulating groove at the top of the oxidation tower by a lifting pump, and H is added into the water inlet circulating groove2O2And FeSO4·7H2And O. The dosage of the two medicaments is as follows: h2O2The mass ratio of the waste water to COD to be treated is 1.5:1, namely H2O2The dosage is 547.5mg/L, H2O2With Fe2+In a molar ratio of 5:1, i.e. FeSO4·7H2The dosage of O is 895 mg/L. Before the treatment system is started, silicon dioxide crystals with the maximum diagonal distance of 2mm and uniform width are added according to 1/5 of the volume of the reactor, and a liquid homogeneous phase promoter is added according to 1 per mill of the designed treatment water amount, wherein the liquid homogeneous phase promoter adopts FeSO4、CoCl2、NiSO4And MnCl2And (3) preparing a salt solution by dilution, wherein the mass concentration of Fe is 10mg/L, the mass concentration of Mn is 10mg/L, the mass concentration of Co is 2mg/L, and the mass concentration of Ni is 0.5mg/L, and continuously adding for 3 days.
And (2) separating the wastewater after the wastewater flows out of the oxidation tower and enters a cyclone separator for 3-5 min, then entering a neutralization tower for acid-base neutralization, adding liquid alkali into the neutralization tower, adjusting the pH to 6-7.5, carrying out ozone aeration stirring at the bottom of the neutralization tower during the period, reacting ozone with residual hydrogen peroxide in the wastewater, and degrading part of organic pollutants, wherein the retention time is 15-20 min at the period. And (3) introducing the neutralized wastewater into a degassing tower, introducing ozone into a micropore aeration disc at the bottom of the degassing tower, stirring and degassing for 20-30 min, adding 0.05mg/L of PAM to form flocs, and simultaneously performing advanced oxidation reaction on the ozone and residual hydrogen peroxide in the mixed solution to further degrade residual organic pollutants. And (3) allowing the degassed wastewater to enter a flocculation sedimentation tank, allowing the wastewater to stay in the flocculation sedimentation tank for 2-3 hours, performing sludge-water separation, discharging supernatant effluent, and performing external transportation harmless treatment after precipitated iron mud is subjected to filter pressing. The COD of the treated effluent is reduced to 50mg/L, and the chroma is reduced to 5 times.
Example 2
The treatment process of the utility model is adopted to treat the biochemical wastewater effluent of a certain starch factory, and the original wastewater COD472mg/L has 75 times of chroma. The wastewater is sent into a water inlet circulating groove at the top of the oxidation tower by a lifting pump, and H is added into the water inlet circulating groove2O2And FeSO4·7H2And O. The dosage of the two medicaments is as follows: h2O2The mass ratio of the waste water to COD to be treated is 1.8:1, namely H2O2The dosage is 850mg/L, H2O2With Fe2+In a 12:1 molar ratio, i.e. FeSO4·7H2The dosage of O is 579 mg/L. Adding a heterogeneous catalytic carrier according to 1/10 of the volume of the reactor before starting a treatment system, wherein the heterogeneous catalytic carrier is formed by mixing silicon dioxide crystals with the maximum diagonal distance of 2mm and active alumina balls with the diameter of 5mm according to the volume ratio of 1:3, adding a liquid homogeneous promoter according to 3 per mill of the designed treatment water quantity, and adopting FeSO as the liquid homogeneous catalytic promoter4、CoCl2、NiSO4And MnCl2And (3) preparing a salt solution by dilution, wherein the mass concentration of Fe is 10mg/L, the mass concentration of Mn is 10mg/L, the mass concentration of Co is 2mg/L, and the mass concentration of Ni is 0.5mg/L, and continuously adding for 3 days.
And (2) separating the wastewater after the wastewater flows out of the oxidation tower and enters a cyclone separator for 3-5 min, then entering a neutralization tower for acid-base neutralization, adding liquid alkali into the neutralization tower to adjust the pH value to 5.5-7.5, carrying out ozone aeration stirring at the bottom of the neutralization tower during the period, reacting ozone with residual hydrogen peroxide in the wastewater, and degrading part of organic pollutants, wherein the retention time is 20-25 min at the period. And (3) introducing the neutralized wastewater into a degassing tower, introducing ozone into a micropore aeration disc at the bottom of the degassing tower, stirring and degassing for 25-30 min, adding 0.05mg/L PAM to form flocs, and simultaneously performing advanced oxidation reaction on the ozone and residual hydrogen peroxide in the mixed solution to further degrade residual organic pollutants. And (3) allowing the degassed wastewater to enter a flocculation sedimentation tank, allowing the wastewater to stay in the flocculation sedimentation tank for 2-3 hours, performing sludge-water separation, discharging supernatant effluent, and performing external transportation harmless treatment after precipitated iron mud is subjected to filter pressing. The COD of the treated effluent is reduced to 56mg/L, and the chroma is reduced to 4.5 times.
It should be noted that the above-mentioned embodiments are only for illustrating the technical concept of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and to implement the present invention, and thus the protection scope of the present invention cannot be limited thereby. All equivalent changes and modifications made according to the spirit of the present invention should be covered by the protection scope of the present invention.
Claims (2)
1. The reinforced upflow multiphase wastewater oxidation treatment system is characterized by comprising an upflow multiphase wastewater oxidation system, a solid-liquid separation system, a neutralization and degassing system and a flocculation and precipitation system which are connected in sequence;
the upflow multiphase wastewater oxidation system comprises an upflow multiphase wastewater oxidation tower (1), wherein a water distribution cover (9) is arranged at the bottom of the upflow multiphase wastewater oxidation tower, a heterogeneous catalysis carrier (5) is filled in the upflow multiphase wastewater oxidation tower, a solid-liquid separator (6) is arranged at the upper part of the upflow multiphase wastewater oxidation tower, the water distribution cover (9) and the solid-liquid separator (6) are respectively positioned below and above the heterogeneous catalysis carrier (5), a water inlet A (4) and a water inlet circulation tank (3) connected with the water inlet A are arranged above the solid-liquid separator (6), the water inlet circulation tank is connected with the water distribution cover at the bottom through a circulation pipe (7), a circulation pump (8) is arranged on the circulation pipe, and a water outlet A (;
the solid-liquid separation system comprises a cyclone separator (10), the upper part of the cyclone separator is provided with a water inlet B (21) connected with a water outlet A (2) of the up-flow multiphase wastewater oxidation tower, the bottom of the cyclone separator is provided with a sand discharge pipe (12), a central pipe (11) for upwards conveying wastewater is arranged in the cyclone separator (10), and the upper part of the central pipe (11) is provided with a water outlet B (22);
the neutralization and degassing system comprises a neutralization tower (13) and a degassing tower (19), the bottoms of the neutralization tower and the degassing tower are respectively provided with a microporous aeration disc (17) into which ozone air and pure oxygen can be introduced, the upper parts of the neutralization tower and the degassing tower are respectively provided with a gas-liquid two-phase separator (14), the upper part of the gas-liquid two-phase separator is connected with a gas-liquid separator (15) through a pipeline, the gas-liquid separator (15) is provided with a descending pipe (16) extending into the lower part of the tower, the lower part of the neutralization tower is provided with a water inlet C (23) connected with a water outlet B (22) of the solid-liquid separation system, the upper part of the neutralization tower is provided with a water outlet C (24) positioned above the gas-liquid two-phase separator, the bottom of the degassing tower is provided with a water inlet D (25) connected with the water outlet C (24;
the flocculation sedimentation system comprises a flocculation sedimentation tank (20), the flocculation sedimentation tank (20) is connected with a water outlet D (26) of the degassing tower, a supernatant discharge port (27) is arranged at the upper part of the flocculation sedimentation tank (20), and a sludge discharge port (28) is arranged at the bottom.
2. The system for the enhanced upflow multiphase wastewater oxidation treatment according to claim 1, wherein the gas discharge port of the gas-liquid separator (15) is connected with two pipeline branches in parallel, one branch is connected with the manganese dioxide filler (18), and the other branch is connected with the gas inlet pipe of the microporous aeration disc (17) through a booster fan (29).
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| CN110316861A (en) * | 2019-06-24 | 2019-10-11 | 广西博世科环保科技股份有限公司 | Strengthen up flow type multiphase wastewater oxidation treatment process and processing system |
| CN112209489A (en) * | 2020-08-25 | 2021-01-12 | 广西博世科环保科技股份有限公司 | Preparation method of high-molecular catalytic water purifying agent for improving Fenton process treatment effect |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110316861A (en) * | 2019-06-24 | 2019-10-11 | 广西博世科环保科技股份有限公司 | Strengthen up flow type multiphase wastewater oxidation treatment process and processing system |
| CN112209489A (en) * | 2020-08-25 | 2021-01-12 | 广西博世科环保科技股份有限公司 | Preparation method of high-molecular catalytic water purifying agent for improving Fenton process treatment effect |
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