CN112159026A - Treatment method for industrial sewage difficult to degrade - Google Patents
Treatment method for industrial sewage difficult to degrade Download PDFInfo
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- VTEIFHQUZWABDE-UHFFFAOYSA-N 2-(2,5-dimethoxy-4-methylphenyl)-2-methoxyethanamine Chemical compound COC(CN)C1=CC(OC)=C(C)C=C1OC VTEIFHQUZWABDE-UHFFFAOYSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/285—Treatment of water, waste water, or sewage by sorption using synthetic organic sorbents
-
- 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
- C02F1/722—Oxidation by peroxides
-
- 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
- C02F2303/00—Specific treatment goals
- C02F2303/16—Regeneration of sorbents, filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/26—Reducing the size of particles, liquid droplets or bubbles, e.g. by crushing, grinding, spraying, creation of microbubbles or nanobubbles
-
- 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
- C02F2305/026—Fenton's reagent
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Engineering & Computer Science (AREA)
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- Water Supply & Treatment (AREA)
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- Organic Chemistry (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The invention discloses a method for treating industrial sewage difficult to degrade, which comprises the following steps: the industrial sewage sequentially enters a regulating tank and an air floatation tank, and micro-nano bubbles are adopted in the air floatation tank to remove granular stickies in the sewage; mixing the sewage discharged by the air floatation tank with desorption liquid generated by adsorption regeneration, and then carrying out heat exchange and temperature rise; carrying out sludge-free Fenton catalytic reaction on the heated sewage, and then carrying out biochemical treatment by adopting an A2/O + MBR process; and (3) performing resin adsorption treatment on the sewage subjected to biochemical treatment, and mixing desorption liquid generated by adsorption regeneration with the sewage discharged by the air floatation tank. The treatment method disclosed by the invention combines the technical advantages of a sludge-free Fenton method, a biochemical method and an adsorption resin, can effectively remove pollutants in sewage, is high in discharged water quality, can realize stable standard reaching of discharged water, and is low in cost.
Description
Technical Field
The invention relates to an industrial sewage treatment method, in particular to a degradation-resistant industrial sewage treatment method.
Background
The industrial sewage discharged from pharmaceutical, chemical and coal industries contains many chemical substances which are harmful to human body besides BOD, nitrogen, phosphorus and other pollutants. Because the COD of the sewage is high, difficult to degrade and high in toxicity, and the sewage is difficult to degrade by a conventional biochemical process, the sewage is generally treated by combining chemical, physical and biological processes.
Since biochemical methods have cost advantages in reducing COD, most of the prior art has centered on biochemical methods for pretreatment and post-treatment. In order to improve the biochemical performance of sewage, the sewage is generally pretreated by an oxidation medicament, iron-carbon micro-electrolysis and an advanced oxidation process at present, the iron-carbon micro-electrolysis decomposes organic matters in the sewage by utilizing a galvanic cell reaction, the pH of the sewage needs to be adjusted, the oxidation capability is poor, and the long-time operation stability is poor. The advanced oxidation process mainly comprises electrochemical oxidation, ozone catalytic oxidation and Fenton reaction, and the electrochemical oxidation has the defects of low conversion efficiency, poor electrode stability and the like at present. Ozone has certain oxidizing power, but the oxidation potential is lower, and catalytic oxidation is generally carried out by utilizing a catalyst, but the ozone has low preparation efficiency and low gas-liquid mass transfer efficiency, so that the treatment cost is higher, and tail gas generated by ozone treatment sewage needs to be treated to avoid secondary pollution. The conventional Fenton method has strict requirements on the pH value of sewage, adopts iron salt as a catalyst, has low catalytic efficiency and generates a large amount of sludge.
After the sewage is biochemically treated, pollutants which are difficult to biochemically degrade are also in tail water, and if the pollutants are directly discharged, the pollutants can exist in the nature for a long time.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to solve the technical problem of providing a method for treating the degradation-resistant industrial sewage with high treatment effect and low cost, and the process has higher operation stability.
The technical scheme is as follows: the invention relates to a method for treating refractory industrial sewage, which comprises the following steps:
(1) the industrial sewage sequentially enters a regulating tank and an air floatation tank, and micro-nano bubbles are adopted in the air floatation tank to remove granular stickies in the sewage;
(2) mixing the sewage discharged by the air floatation tank with desorption liquid generated by adsorption regeneration, and then carrying out heat exchange and temperature rise;
(3) carrying out sludge-free Fenton catalytic reaction on the heated sewage, and then carrying out biochemical treatment by adopting an A2/O + MBR process;
(4) and performing resin adsorption treatment on the sewage subjected to biochemical treatment, mixing desorption liquid generated by adsorption regeneration with the sewage discharged by the air floatation tank, performing heat exchange, raising the temperature, and then entering a Fenton reactor for final treatment.
In the step (2), the heat exchange temperature rise is realized by exchanging heat with tail gas generated by mud-free Fenton in a tail gas absorber, and then the temperature rise is realized through a heat exchanger.
Preferably, in the step (2), the mixing is performed in a pipeline mixer, and the heat exchange temperature rise is performed in a tail gas absorber to exchange heat with tail gas generated by mud-free Fenton to reduce the temperature of the tail gas, and then the temperature rise is performed through a heat exchanger. The bottom of the tail gas absorber is provided with an aeration disc, and tail gas generated by mud-free Fenton enters sewage through the aeration disc and is in direct contact with the sewage for heat exchange.
The bottom of the tail gas absorber is provided with an aeration disc, and tail gas generated by mud-free Fenton enters sewage through the aeration disc and is in direct contact with the sewage for heat exchange.
In the step (3), the mud-free Fenton catalytic reaction is carried out in a vertical reaction tower. Stainless steel wire net ripple packs are laid inside the vertical reaction tower, and the mud-free Fenton catalytic packs are placed among ripples. Hydrogen peroxide is added into the vertical reaction tower through multiple points, and the double oxidation is mixed with the sewage by adopting a nozzle. The hydrogen peroxide pressure is 0.2-0.4 MPa. Steam enters the vertical reaction tower through multiple points, a valve is arranged on the pipeline, and the opening and closing of the steam valve are controlled through the temperature in the reaction kettle. The steam is mixed with the sewage by a nozzle. In the step (3), the temperature of the sewage is maintained to be not lower than 80 ℃ in the mud-free Fenton catalytic reaction.
In the mud-free Fenton reaction, the hydroxyl free radicals generated by hydrogen peroxide under the catalytic action are utilized to decompose organic pollutants in the sewage, the COD in the sewage is reduced, and the biodegradability of the sewage is improved. Sewage flowing out of the sludge-free Fenton process enters a biochemical unit, sewage treatment is carried out by adopting an A2/O + MBR process, contaminants such as C, N, P in the sewage are removed by utilizing active microorganisms, the solid-liquid separation is carried out by utilizing a membrane, the occupied area of the system is reduced, and the water quality is improved. The sewage after biochemical treatment enters the adsorption resin, and the organic matters incapable of being degraded by microorganisms in the sewage are removed by adsorption by utilizing the adsorption capacity of the resin, so that the sewage can be stably discharged up to the standard, and the toxicity is low.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages: the system can be started quickly by combining the technical advantages of the sludge-free Fenton method, the biochemical method and the adsorption resin, pollutants in sewage can be effectively removed, the water quality of the discharged water is high, and the discharged water can stably reach the standard; the cost is low, the utilization efficiency of the hydrogen peroxide is high, and the overall operation cost is low; the heat is recovered through the heat exchanger, so that the overall steam consumption of the system is low; the biochemical tail water is adsorbed by using the adsorption resin, the content of the biochemical substances difficult to decompose in the discharged water is low, and the desorption liquid enters the Fenton reactor to completely decompose the biochemical substances difficult to decompose.
Drawings
FIG. 1 is a block diagram of a process flow of the present invention;
FIG. 2 is a process flow diagram of the present invention;
FIG. 3 is a schematic diagram of a configuration of a mud-free Fenton reactor;
FIG. 4 is a schematic diagram of a tail gas absorber configuration.
Detailed Description
The technical solution of the present invention is further illustrated by the following examples.
Example 1
As shown in figures 1-4, the COD of raw water in acrylonitrile production sewage of a certain petrochemical enterprise is 2500mg/L, the sewage at 25 ℃ generated in the production process firstly enters an adjusting tank, and enters an air floatation tank after being buffered and adjusted to stabilize the water quality, large-particle pollutants in the sewage are removed by adopting micro-nano bubbles, and the COD is reduced to 2300 mg/L. And then the sewage is mixed with desorption liquid generated by a resin adsorption process through a pipeline mixer and enters a tail gas absorber. The bottom of the tail gas absorber is provided with an aeration disc, and tail gas generated by mud-free Fenton enters sewage through the aeration disc and is in direct contact with the sewage for heat exchange. The temperature of the sewage is increased to 28 ℃, the temperature of the tail gas is reduced, the water vapor is condensed, and the non-condensable gas is discharged. The sewage enters a heat exchanger to exchange heat with the sewage discharged from the sludge-free Fenton reactor, the temperature is further increased to 65 ℃, and the sewage after temperature increase enters the sludge-free Fenton reactor; and (4) the cooled sewage enters a biochemical reactor, and a biochemical unit adopts an A2/O + MBR process to perform sewage treatment.
Sewage enters the mud-free Fenton reactor after heat is recovered by the heat exchanger, the mud-free Fenton reactor is of a tower structure, the sewage enters the reactor from the bottom of the reactor, steam feed ports 1, 2, 3 and 4 are formed in the side wall of the reactor, and the steam feed port 1 heats the sewage to 80 ℃. Set up the valve on steam heating mouth 2, 3, 4 pipelines, be equipped with the thermometer above the heating mouth, through the temperature control valve switch who sets for: when the temperature is lower than 80 ℃, the steam valve is opened, steam enters the reactor, and the temperature of the sewage is increased. When the temperature is higher than 85 ℃, the valve is closed. Steam is mixed with sewage through the injection of a nozzle after entering the reactor through a feed inlet, and the steam is saturated steam water at 120 ℃. Hydrogen peroxide feed inlets 1, 2, 3 and 4 are arranged on the opposite sides of the steam feed inlets, and the utilization efficiency of hydrogen peroxide is improved by adding hydrogen peroxide at multiple points. Hydrogen peroxide enters the reactor through the feed inlet and then is mixed with sewage through the nozzle, and the pressure of a hydrogen peroxide jet orifice is 0.2 Mpa. Stainless steel wire net ripple packs are laid in the reactor, and the mud-free Fenton catalytic packs are placed between the wave troughs of the ripples. The top of the reactor is provided with a sewage discharge port and a tail gas outlet, and a demister is arranged below the tail gas outlet in order to reduce liquid mixed in the tail gas. After Fenton treatment, the COD of the sewage is reduced to 500 mg/L.
After the sewage is subjected to biochemical treatment by an A2/O + MBR process, COD is reduced to 50mg/L, the drained water of a biochemical system enters into adsorption resin, the organic matters which cannot be degraded by microorganisms in the sewage are removed by adsorption by utilizing the adsorption capacity of the resin, the COD of the sewage is reduced to 15mg/L, the toxicity is reduced, and the stable standard-reaching discharge of the sewage can be realized.
The adsorption resin is subjected to adsorption saturation, then the desorption agent is used for regeneration on site, desorption liquid and sewage discharged by the air floatation tank are mixed and then enter a Fenton reactor for final treatment, and the treated water quality, steam and hydrogen peroxide consumption are shown in Table 1.
Table 1 treated water quality, steam and hydrogen peroxide consumption of example 1
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 2500mg/L | 2300mg/L | 500mg/L | 50mg/L | 15mg/L | 27kg/t | 60kg/t |
Example 2
The industrial sewage in the embodiment is the sewage containing pyridine pesticide, the temperature of the sewage is heated to 85 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.4Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the consumption of the treated water, the steam and the hydrogen peroxide is shown in the table 2.
Table 2 treated water quality, steam and hydrogen peroxide consumption of example 2
Example 3
The industrial sewage in the embodiment is coal chemical industry sewage, the temperature of the sewage is heated to 83 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.3Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the consumption of the treated water, the steam and the hydrogen peroxide is shown in Table 3.
Table 3 water quality, steam and hydrogen peroxide consumption of the treatment of example 3
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 4200mg/L | 4100mg/L | 830mg/L | 50mg/L | 18mg/L | 33kg/t | 87kg/t |
Example 4
The industrial sewage in the embodiment is printing and dyeing sewage, the temperature of the sewage is heated to 85 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.2Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the consumption of the treated water, the steam and the hydrogen peroxide is shown in Table 4.
Table 4 treatment water quality, steam and hydrogen peroxide consumption of example 4
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 6000mg/L | 5300mg/L | 650mg/L | 50mg/L | 16mg/L | 36kg/t | 88kg/t |
Example 5
The industrial sewage in the embodiment is the sewage produced in the chemical fiber production, the temperature of the sewage is heated to 83 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.4Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the consumption of the treated water, the steam and the hydrogen peroxide is shown in the table 5.
Table 5 treatment water quality, steam and hydrogen peroxide consumption of example 5
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 5000mg/L | 4600mg/L | 550mg/L | 55mg/L | 18mg/L | 33kg/t | 86kg/t |
Example 6
The industrial sewage in the embodiment is BDO-containing medical sewage, the temperature of the sewage is heated to 85 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.3Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the water quality, steam and hydrogen peroxide consumption are shown in Table 6.
Table 6 treated water quality, steam and hydrogen peroxide consumption of example 6
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 4500mg/L | 4000mg/L | 500mg/L | 60mg/L | 16mg/L | 36kg/t | 82kg/t |
Example 7
The industrial sewage in the embodiment is coking sewage, the temperature of the sewage is heated to 83 ℃ by the steam feed inlet 1, the pressure of the hydrogen peroxide injection orifice is 0.2Mpa, other operation steps, reagents, devices and detection methods are the same as those in the embodiment 1, and the consumption of the treated water, the steam and the hydrogen peroxide is shown in Table 7.
Table 7 treated water quality, steam and hydrogen peroxide consumption of example 7
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 5000mg/L | 4700mg/L | 530mg/L | 50mg/L | 17mg/L | 32kg/t | 85kg/t |
Comparative example 1
In the comparative example, the sewage does not pass through the A2/O + MBR process, and other operation steps, reagents, devices and detection methods are the same as those of the example 1.
As shown in Table 8, in acrylonitrile production sewage of a petrochemical enterprise, COD in raw water was 2500mg/L, COD after air flotation was 2300mg/L, COD was reduced to 250mg/L after sludge-free Fenton treatment, and COD was reduced to 230mg/L after resin adsorption.
Table 8 treated water quality, steam and hydrogen peroxide consumption of comparative example 1
| COD of raw water | Air-float COD | Fenton COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 2500mg/L | 2300mg/L | 250mg/L | 230mg/L | 27kg/t | 100kg/t |
Comparative example 2
In the comparative example, the wastewater was not subjected to the resin adsorption method, and the other operation steps, reagents, apparatuses and detection methods were the same as those in example 1.
As shown in Table 9, in acrylonitrile production sewage of a petrochemical enterprise, COD in raw water was 2500mg/L, COD after air flotation was 2200mg/L, COD was reduced to 500mg/L after sludge-free Fenton treatment, and COD was reduced to 50mg/L after adsorption with resin.
TABLE 9 treated Water quality, steam and Hydrogen peroxide consumption of comparative example 2
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Steam consumption | Consumption of hydrogen peroxide |
| 2500mg/L | 2300mg/L | 500mg/L | 50mg/L | 27kg/t | 60kg/t |
Comparative example 3
In the comparative example, the temperature of the wastewater in the mud-free Fenton catalytic reaction was maintained at 75 ℃, and other operation steps, reagents, devices and detection methods were the same as those of example 1.
As shown in Table 10, in acrylonitrile production sewage of a petrochemical enterprise, COD in raw water was 2500mg/L, COD after air flotation was 2200mg/L, COD was reduced to 500mg/L after sludge-free Fenton treatment, and COD was reduced to 50mg/L after adsorption with resin.
TABLE 10 treated Water quality, steam and Hydrogen peroxide consumption of comparative example 3
Comparative example 4
In the comparative example, the temperature of the wastewater in the mud-free Fenton catalytic reaction was maintained at 90 ℃, and other operation steps, reagents, devices and detection methods were the same as those of example 1.
As shown in Table 11, in acrylonitrile production sewage of a petrochemical enterprise, COD in raw water was 2500mg/L, COD after air flotation was 2200mg/L, COD was reduced to 500mg/L after sludge-free Fenton treatment, and COD was reduced to 50mg/L after adsorption with resin.
TABLE 11 treated Water quality, steam and Hydrogen peroxide consumption of comparative example 4
| COD of raw water | Air-float COD | Fenton COD | Biochemical COD | Resin adsorption of COD | Steam consumption | Consumption of hydrogen peroxide |
| 2500mg/L | 2300mg/L | 500mg/L | 50mg/L | 15mg/L | 46kg/t | 60kg/t |
Claims (10)
1. A method for treating industrial sewage difficult to degrade is characterized by comprising the following steps:
(1) the industrial sewage sequentially enters a regulating tank and an air floatation tank, and micro-nano bubbles are adopted in the air floatation tank to remove granular stickies in the sewage;
(2) mixing the sewage discharged by the air floatation tank with desorption liquid generated by adsorption regeneration, and then carrying out heat exchange and temperature rise;
(3) carrying out sludge-free Fenton catalytic reaction on the heated sewage, and then carrying out biochemical treatment by adopting an A2/O + MBR process;
(4) and performing resin adsorption treatment on the sewage subjected to biochemical treatment, mixing desorption liquid generated by adsorption regeneration with the sewage discharged by the air floatation tank, performing heat exchange, raising the temperature, and then entering a Fenton reactor for final treatment.
2. The method for treating refractory industrial sewage according to claim 1, wherein: in the step (2), the heat exchange temperature rise is heat exchange with tail gas generated by mud-free Fenton in a tail gas absorber, and then the temperature rise is carried out through a heat exchanger.
3. The method for treating refractory industrial sewage according to claim 2, wherein: the bottom of the tail gas absorber is provided with an aeration disc, and tail gas generated by mud-free Fenton enters sewage through the aeration disc and is in direct contact with the sewage for heat exchange.
4. The method for treating refractory industrial sewage according to claim 1, wherein: in the step (3), the mud-free Fenton catalytic reaction is carried out in a vertical reaction tower.
5. The method for treating refractory industrial sewage according to claim 4, wherein: stainless steel wire net ripple packs are laid inside the vertical reaction tower, and the mud-free Fenton catalytic packs are placed among ripples.
6. The method for treating refractory industrial sewage according to claim 4, wherein: hydrogen peroxide is added into the vertical reaction tower through multiple points, and the double oxidation is mixed with the sewage by adopting a nozzle.
7. The method for treating refractory industrial sewage according to claim 6, wherein: the hydrogen peroxide pressure is 0.2-0.4 MPa.
8. The method for treating refractory industrial sewage according to claim 4, wherein: steam enters the vertical reaction tower through multiple points, a valve is arranged on the pipeline, and the opening and closing of the steam valve are controlled through the temperature in the reaction kettle.
9. The method for treating refractory industrial sewage according to claim 8, wherein: the steam is mixed with the sewage by a nozzle.
10. The method for treating refractory industrial sewage according to claim 1, wherein: in the step (3), the temperature of the sewage is maintained to be not lower than 80 ℃ in the mud-free Fenton catalytic reaction.
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| CN202010830857.1A CN112159026A (en) | 2020-08-18 | 2020-08-18 | Treatment method for industrial sewage difficult to degrade |
| BE20215424A BE1027967B1 (en) | 2020-08-18 | 2021-05-27 | Process for the treatment of poorly degradable industrial waste water |
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| BE1027967A1 (en) | 2021-08-02 |
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