CN113277675A - Biochemical treatment device for phenol-containing wastewater and method and application thereof - Google Patents
Biochemical treatment device for phenol-containing wastewater and method and application thereof Download PDFInfo
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F9/00—Multistage treatment of water, waste water or sewage
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- 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
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- 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
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- 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
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- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C02F2101/345—Phenols
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Abstract
The invention relates to the field of biochemical treatment of wastewater, in particular to a biochemical treatment device for phenolic wastewater and a method and application thereof. The device for treating the high-phenol-content wastewater by a biochemical method is formed by adopting an adjusting tank, a primary air flotation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air flotation tank, a pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank, so that the aims of detoxifying, modifying, biochemically treating and discharging the wastewater up to the standard are fulfilled. When the device and the method are used for treating the phenol-containing wastewater, phenols can be reduced to be below 0.25mg/L, and COD can be reduced to be below 40 mg/L.
Description
Technical Field
The invention relates to the field of biochemical treatment of wastewater, in particular to a biochemical treatment device for phenolic wastewater and a method and application thereof.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Along with industrial development and environmental protection requirements, industrial wastewater needs to be treated to reach a discharge standard and then discharged, corresponding sewage treatment devices need to be constructed in a matched manner in order to meet production requirements of industrial devices taking drainage of chemical plants and coking plants and phenol and phenolic aldehyde as raw materials, the sewage treatment units of the type are also difficult to face, and in order to reduce the influence on an activated sludge biochemical system, the sewage needs to be detoxified and modified, so that the biodegradability of the sewage is improved, and the standard discharge of biochemical treatment can be ensured.
The inventor researches and discovers that the oxidation steps of the treatment method of the phenolic wastewater are few, the oxidation mode is single, and harmful substances in the wastewater cannot be fully decomposed. And the treatment method of the phenol-containing wastewater only relates to a biological method or a chemical method, the treatment mode is simple, and the effect is to be improved.
Disclosure of Invention
The invention provides a biochemical treatment device for phenolic wastewater and a method and application thereof, aiming at solving the problem that the existing phenolic wastewater treatment method is not thorough in treatment, and the biochemical treatment device for phenolic wastewater adopts a regulating tank, a primary air floatation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air floatation tank, a pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank to form a biochemical treatment device for treating high-phenolic wastewater, so that the aims of detoxifying, modifying and discharging the wastewater after biochemical treatment to reach the standard are achieved. When the device and the method are used for treating the phenol-containing wastewater, phenols can be reduced to be below 0.25mg/L, and COD can be reduced to be below 40 mg/L.
Specifically, the invention is realized by the following technical scheme:
the invention provides a biochemical treatment device for phenolic wastewater, which comprises a regulating tank, a primary air floatation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air floatation tank, a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank which are connected in sequence.
The invention provides a biochemical treatment method of phenolic wastewater, which comprises the steps of adjusting homogenization, primary adsorption impurity removal, ozone preoxidation, hydrolytic acidification, contact oxidation, secondary adsorption impurity removal, ozone hydrogen peroxide two-dimensional advanced oxidation and activated carbon adsorption.
In a third aspect of the present invention, there is provided an apparatus for treating wastewater, comprising a biochemical treatment apparatus for wastewater containing phenol.
In a fourth aspect of the present invention, there is provided an application of a biochemical treatment apparatus and/or a biochemical treatment method for phenol-containing wastewater in the field of phenol-containing wastewater or wastewater treatment.
One or more embodiments of the present invention have the following advantageous effects:
1) the device for treating the high-phenol-content wastewater by the biochemical method is formed by adopting an adjusting tank, a primary air flotation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air flotation tank, a pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank, and can be used for treating the high-phenol-content wastewater, wherein phenols can be reduced to be below 0.25mg/L, and COD can be reduced to be below 40 mg/L.
2) Through designing a two-stage air floatation tank, the air floatation tank is matched with an ozone oxidation device, a hydrolytic acidification device and a contact oxidation device, the purposes of physical impurity removal, biochemical reaction and physical impurity removal are realized, and the treatment is more thorough than that by using a chemical method or a physical method singly.
3) Choose for use syllogic ozone pre-oxidation device, through design rivers direction of motion, the reaction time of extension phenol-containing waste water in ozone pre-oxidation pond, during rivers got into each ozone pre-oxidation section simultaneously, rivers downstream, ozone upward movement, rivers and ozone's motion in opposite directions increase the contact time and the area of rivers and ozone, help going on of ozone oxidation reaction. In combination with the requirements of the phenol-containing wastewater on the ozone content in different stages, the residual ozone in the second ozone pre-oxidation reaction section can also enter the first ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section for reaction, so that the utilization rate of the ozone is improved.
4) The top of the pulse hydrolysis acidification tank is provided with a pulse water tank, the water tank is subjected to pulse stirring at intervals of 2 minutes, and activated sludge adsorbed on the flexible filler in the hydrolysis acidification tank is impacted to fall off, so that the filler plate in the water tank is prevented from being bonded.
5) The sludge contains flora for degrading phenolic substances, and is introduced from the sludge in the sludge collection tank to the pulse hydrolysis acidification tank and the contact oxidation tank at proper time according to the sludge concentration in the pulse hydrolysis acidification tank and the contact oxidation tank, so that the sludge concentration in the pulse hydrolysis acidification tank and the contact oxidation tank is improved, and the treatment capacity of pollutants is improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. Embodiments of the invention are described in detail below with reference to the attached drawing figures, wherein:
FIG. 1 is a schematic view of an apparatus for biochemical treatment of phenol-containing wastewater according to example 1 of the present invention;
FIG. 2 is a schematic view of an ozone pre-oxidation tank according to example 1 of the present invention;
FIG. 3 is a schematic view of a pulse hydrolysis acidification tank according to example 1 of the present invention;
FIG. 4 is a schematic view of a contact oxidation cell according to example 1 of the present invention;
FIG. 5 is a schematic view of a biological activated carbon cell according to example 1 of the present invention;
wherein: 1. a wastewater tank, 2, a regulating tank, 3, a first-stage air floatation tank, 4, an ozone pre-oxidation tank and 5
A pulse hydrolysis acidification tank, 6, a contact oxidation tank, 7, a secondary air flotation tank, 8, a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank, 9, a biological activated carbon tank, 10, a clean water tank, 11, a sludge collection tank, 12, a sludge tank, 13, a mother liquor tank, 14, an ozone inlet, 15, a first ozone pre-oxidation reaction section, 16, a second ozone pre-oxidation reaction section, 17, a third ozone pre-oxidation reaction section, 18, a first aerator, 19, a second aerator, 20, a third aerator, 21, a first pipeline, 22, a mixer, 23, a second pipeline, 24, a tail gas collection device, 25, a medicament inlet, 26, a plug flow air device, 27, a first flexible filler zone, 28, a pulse water tank, 29, a pneumatic valve, 30, an oxidation-reduction potential monitor, 31, an air inlet, 32, a fourth aerator, 33, a water cap, 34, a second flexible filler zone, 35, a second flexible filler zone, The device comprises an online dissolved oxygen value monitoring device 36, a liquid level meter 37, a water inlet partition wall 38, a perforated aeration device 39, an air inlet 40 and a grid.
Detailed Description
The invention will be further illustrated with reference to the following specific examples. It should be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. The experimental procedures, in which specific conditions are not noted in the following examples, are generally carried out according to conventional conditions or according to conditions recommended by the manufacturers.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In addition, any methods and materials similar or equivalent to those described herein can be used in the methods of the present invention. The preferred embodiments and materials described herein are intended to be exemplary only.
It is to be understood that the terms "upper", "lower", "horizontal", "top", "bottom", and the like are used in an orientation or positional relationship indicated on the drawings for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are not to be construed as limiting the present invention.
The invention provides a biochemical treatment device for phenolic wastewater and a method and application thereof, aiming at solving the problem that the existing phenolic wastewater treatment method is not thorough in treatment, and the biochemical treatment device for phenolic wastewater adopts a regulating tank, a primary air floatation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air floatation tank, a pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank to form a biochemical treatment device for treating high-phenolic wastewater, so that the aims of detoxifying, modifying and discharging the wastewater after biochemical treatment to reach the standard are achieved.
Specifically, the invention is realized by the following technical scheme:
the invention provides a biochemical treatment device for phenolic wastewater, which comprises a regulating tank, a primary air floatation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air floatation tank, a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank which are connected in sequence.
In one or more embodiments of the invention, the conditioning tank is connected to a wastewater tank or wastewater inlet;
the phenol-containing wastewater changes along with the change of production conditions in the discharge process, and the conditions of non-uniform water quality and unstable water quantity exist. In order to ensure that the treatment process works normally and is not influenced by the peak flow or the peak concentration change of the wastewater, the wastewater is required to have stable water quantity and uniform water quality before treatment, and the water quality and the water quantity must be adjusted.
Preferably, the pulse hydrolysis acidification tank is connected with the sludge collection tank through two pipelines, the sludge collection tank conveys the sludge to the pulse hydrolysis acidification tank, the sludge contains flora for degrading phenols, and the flora is decomposed in the pulse hydrolysis acidification tank, so that the sludge concentration of the pulse hydrolysis acidification tank is improved, and the pollutant treatment capacity is improved. When the sludge is excessive, the activated sludge adsorbed on the flexible filler in the hydrolytic acidification is impacted and dropped off by pulse vibration, so that the filler plates in the water tank are prevented from being bonded, and the dropped activated sludge is conveyed to the sludge collection tank.
Preferably, the contact oxidation pond is connected with the sludge collection pond through two pipelines, the sludge collection pond conveys the sludge to the contact oxidation pond, the sludge contains flora for degrading phenols, and the flora is decomposed in the contact oxidation pond, so that the sludge concentration of the contact oxidation pond is improved, and the pollutant treatment capacity is improved. And when the sludge is excessive, controlling the activated sludge to be conveyed to the sludge collecting tank.
Preferably, the secondary air flotation tank is connected with the sludge collection tank through a pipeline, sludge floated by the secondary air flotation tank is conveyed to the sludge concentration tank through a sludge pump, and the sludge is concentrated and then enters the sludge drying equipment for further dehydration and then is subjected to incineration treatment.
Preferably, the sludge collection tank is connected with the sludge tank and the mother liquor tank, and the mother liquor tank is connected with the pulse hydrolysis acidification tank and is used for adjusting the pH value.
In one or more embodiments of the present invention, the first-stage air flotation tank adopts a shallow dissolved air flotation tank to adsorb the suspended organic matters with larger particles by using air bubbles.
Preferably, one end of the ozone pre-oxidation tank is connected with the primary air flotation tank, the other end of the ozone pre-oxidation tank is connected with the pulse hydrolysis acidification tank, the ozone pre-oxidation tank comprises a first ozone pre-oxidation reaction section, a second ozone pre-oxidation reaction section and a third ozone pre-oxidation reaction section, and a first aerator, a second aerator and a third aerator are respectively arranged at the bottoms of the first ozone pre-oxidation reaction section, the second ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section.
Preferably, the first aerator and the second aerator are connected with an ozone inlet.
During rivers got into each ozone pre-oxidation section, rivers downstream, ozone upward movement, rivers and ozone's relative motion increase rivers and ozone's contact time and area, help ozone oxidation reaction's going on.
Preferably, a mixer, preferably a venturi mixer, is arranged at the joint of the primary air flotation tank and the ozone pre-oxidation tank.
Preferably, the second ozone pre-oxidation reaction section is connected with the mixer through a first pipeline and is connected with a third aerator of a third ozone pre-oxidation reaction section through a second pipeline.
In combination with the requirements of the phenol-containing wastewater on the ozone content in different stages, the residual ozone in the second ozone pre-oxidation reaction section can also enter the first ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section for reaction, so that the utilization rate of the ozone is improved.
Preferably, be equipped with two at least parallel baffles between first ozone pre-oxidation reaction section and the second ozone pre-oxidation reaction section, the division baffle is vertical to be placed, is close to a certain distance of baffle lower part distance ozone pre-oxidation pond bottom of first ozone pre-oxidation reaction section, and a certain distance of baffle upper portion distance ozone pre-oxidation pond top that is close to the second ozone pre-oxidation reaction section.
Preferably, at least two parallel isolation baffles are arranged between the second ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section, the isolation baffles are vertically arranged, the lower part of the baffle close to the second ozone pre-oxidation reaction section is away from the bottom of the ozone pre-oxidation tank, and the upper part of the baffle close to the third ozone pre-oxidation reaction section is away from the top of the ozone pre-oxidation tank. The reaction time of the phenol-containing wastewater in the ozone pre-oxidation tank is prolonged by designing the water flow direction.
Preferably, a tail gas collecting device is connected above the third ozone pre-oxidation reaction section.
In one or more embodiments of the invention, the top of the pulse hydrolysis acidification tank is provided with a pulse water tank and a pneumatic valve, and the pulse water tank is connected with the medicament inlet. The pulse water tank carries out pulse stirring on the water tank every 2 minutes, and activated sludge adsorbed on the flexible filler in the hydrolytic acidification is impacted to fall off, so that the filler plate in the water tank is prevented from being bonded.
Preferably, the bottom of the pulse hydrolysis acidification tank is provided with a flow pushing device, a first flexible packing area is arranged above the flow pushing device, and the upper part of the first flexible packing area is connected with the contact oxidation tank through a pipeline.
The gas pushing device further disturbs the flexible filler in the hydrolysis acidification tank, and hardening is avoided.
The water inlet of the pulse hydrolysis acidification tank is directly inserted into the bottom of the pulse hydrolysis acidification tank, through the continuous increase of water quantity, the phenol-containing wastewater is subjected to adsorption and hydrolysis acidification treatment under the action of activated sludge through the first flexible filler region, and the treated wastewater enters the contact oxidation tank.
Preferably, the first flexible filler is elastic filler;
preferably, the top of the pulse hydrolysis acidification tank is also provided with an oxidation-reduction potential monitor and a tail gas collecting device;
preferably, one end of the pulse hydrolysis acidification is connected with the ozone pre-oxidation tank and the sludge collection tank, and the other end of the pulse hydrolysis acidification is connected with the contact oxidation tank;
preferably, the lower part of the contact oxidation pond is provided with at least one water cap, at least one fourth aerator is arranged above the water cap, the fourth aerator is connected with the air inlet, and a second flexible filler area is arranged above the fourth aerator.
The waste water that gets into the contact oxidation pond is earlier through the water cap, and the gas contact who produces with the fourth aerator is mixed after that, and the fourth aerator is towards aquatic towards oxygen, keeps the dissolved oxygen in the contact oxidation pond at certain extent, promotes the oxidative decomposition of fungus crowd in the flexible filler district of second, goes out water and sets up L type play mill weir, makes the velocity of flow on every rivers section equal, avoids appearing the condition that appears the short-term flow in the filler, and even velocity of flow also can keep the biochemical system in whole pond to move evenly simultaneously.
Preferably, the second flexible filler is elastic filler;
preferably, the contact oxidation pond is also provided with an online dissolved oxygen value monitoring device and a liquid level meter which are connected with a tail gas collecting device;
preferably, a water inlet partition wall is arranged at the water inlet end of the contact oxidation pond, a water through hole is formed in the position, 0.3m away from the bottom of the pond, of the wall, and the flow velocity of the water through hole is controlled to be 0.4-0.6 m/s, preferably 0.5 m/s;
preferably, one end of the contact oxidation tank is connected with the pulse hydrolysis acidification tank and the sludge collection tank, and the other end of the contact oxidation tank is connected with the secondary air flotation tank;
preferably, an effluent weir is arranged at the contact oxidation tank opening, and the effluent weir is an L-shaped effluent weir.
In one or more embodiments of the invention, an ozone aerator is arranged at the bottom of the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond, and a hydrogen peroxide adding port is arranged above the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond;
preferably, the pH value in the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond is 9-12, and preferably 9.5;
the hydrogen peroxide is decomposed into hydroxyl under the alkaline condition to generate oxidation.
Furthermore, the hydrogen peroxide in the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank is added at multiple points, so that the uniformity in the tank is ensured.
Furthermore, the hydrogen peroxide in the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank is positioned above the ozone aerator by adopting a multi-point feeding pipeline so as to ensure that the effect of the oxidation reaction in the tank is better.
And further, the effluent of the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation pond enters a biological activated carbon filter for further biochemical treatment and filtration treatment, so that the effluent reaches a first-level a standard and then is discharged after reaching the standard.
Preferably, activated carbon is arranged in the biological activated carbon tank, and the specific surface area of the activated carbon is preferably 200m2/g；
Preferably, the upper part of the biological activated carbon pool is provided with a grid, the grid consists of grid bars with intervals of 2 cm, the perforating aeration device is arranged below the grid and is horizontally arranged, the diameter of a perforation is 2-4mm, the direction of an opening is 45 degrees downwards in an inclined mode, and the diameter of the perforation is preferably 4 mm;
preferably, the activated carbon is positioned on a grid with the grid bar spacing of 2 cm;
preferably, the biological activated carbon tank is also provided with an air inlet connected with a perforation aeration device;
preferably, the bottom of the biological activated carbon pool is connected with a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation pool, and the top of the biological activated carbon pool is connected with a clean water pool;
preferably, a filter screen is arranged among the adjusting tank, the primary air flotation tank, the ozone pre-oxidation tank, the pulse hydrolysis acidification tank, the contact oxidation tank, the secondary air flotation tank, the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank and the biological activated carbon tank.
The invention provides a biochemical treatment method of phenolic wastewater, which comprises the steps of adjusting homogenization, primary adsorption impurity removal, ozone preoxidation, hydrolytic acidification, contact oxidation, secondary adsorption impurity removal, ozone hydrogen peroxide two-dimensional advanced oxidation and activated carbon adsorption.
In one or more embodiments of the invention, the phenol-containing wastewater enters the regulating tank to be regulated and homogenized, and the water source from the sewage treatment has water quality fluctuation, enters the homogenizing tank to be uniformly mixed, and then enters the post-system.
Preferably, the first-stage air floatation adopts a shallow dissolved air floatation tank, the particle size of bubbles in the shallow dissolved air floatation tank is controlled to be 5-10 micrometers, the particle size of the bubbles is reduced, and the flotation effect is improved.
Preferably, the ozone pre-oxidation step comprises a first ozone pre-oxidation reaction, a second ozone pre-oxidation reaction section and a third ozone pre-oxidation reaction;
preferably, the rubber diaphragms of the first aerator, the second aerator and the third aerator are made of EPDM (ethylene-propylene-diene monomer) materials, and the diameter of bubbles is controlled to be 2-3 mm;
in one or more embodiments of the invention, the hydrolytic acidification is pulsed hydrolytic acidification, pulsed water tanks pulse stir the pool every 2 minutes;
preferably, the flow rate of the pneumatic valve is 0.4-0.5 m/s, preferably 0.4 m/s;
preferably, the hydrolysis acidification time is 18-24 hours, preferably 21 hours;
preferably, the contact oxidation reaction time is 3-8 hours, preferably 5 hours;
preferably, sludge generated by hydrolytic acidification, contact oxidation and secondary adsorption impurity removal is collected, and the sludge is activated sludge and contains flora for degrading phenolic substances.
In a third aspect of the present invention, there is provided an apparatus for treating wastewater, comprising a biochemical treatment apparatus for wastewater containing phenol.
In a fourth aspect of the present invention, there is provided an application of a biochemical treatment apparatus and/or a biochemical treatment method for phenol-containing wastewater in the field of phenol-containing wastewater or wastewater treatment.
The present invention is described in further detail below with reference to specific examples, which are intended to be illustrative of the invention and not limiting.
Example 1
As shown in figure 1, the biochemical treatment device for the phenolic wastewater comprises a regulating tank 2, a primary air flotation tank 3, an ozone pre-oxidation tank 4, a pulse hydrolysis acidification tank 5, a contact oxidation tank 6, a secondary air flotation tank 7, a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank 8 and a biological activated carbon tank 9 which are connected in sequence. The adjusting tank 2 is connected with the wastewater tank 1 or a wastewater inlet, the biological activated carbon tank 9 is connected with the clean water tank 10, the pulse hydrolysis acidification tank 5 is connected with the sludge collection tank 11 through two pipelines, the contact oxidation tank 6 is connected with the sludge collection tank 11 through two pipelines, and the secondary air flotation tank 7 is connected with the sludge collection tank 11 through one pipeline. The sludge collecting tank 11 is connected with the sludge tank 12 and the mother liquor tank 13, and the mother liquor tank 13 is connected with the pulse hydrolysis acidification tank 5.
The first-stage air floatation tank 3 adopts a shallow layer dissolved air floatation tank to adsorb the suspended organic matters with larger particles by using air bubbles.
As shown in fig. 2, one end of the ozone pre-oxidation tank 4 is connected with the first-stage air flotation tank 3, the other end is connected with the pulse hydrolysis acidification tank 5, the ozone pre-oxidation tank 4 comprises a first ozone pre-oxidation reaction section 15, a second ozone pre-oxidation reaction section 16 and a third ozone pre-oxidation reaction section 17, the bottom of the first ozone pre-oxidation reaction section 15, the bottom of the second ozone pre-oxidation reaction section 16 and the bottom of the third ozone pre-oxidation reaction section 17 are respectively provided with a first aerator 18, a second aerator 19 and a third aerator 20, the first aerator 18 and the second aerator 19 are connected with an ozone inlet 14,
a mixer 22 is arranged at the joint of the first-stage air flotation tank 3 and the ozone pre-oxidation tank 4, the second ozone pre-oxidation reaction section 16 is connected with the mixer 22 through a first pipeline 21 and is connected with a third aerator 20 of the third ozone pre-oxidation reaction section 17 through a second pipeline 23.
Be equipped with the baffle of two at least parallels between first ozone pre-oxidation reaction section 15 and the second ozone pre-oxidation reaction section 16, the vertical placing of division baffle, the baffle lower part that is close to first ozone pre-oxidation reaction section 15 is apart from one section distance in ozone pre-oxidation pond 4 bottom, and the baffle upper portion that is close to second ozone pre-oxidation reaction section 16 is apart from one section distance in ozone pre-oxidation pond 4 top. At least two parallel isolation baffles are arranged between the second ozone pre-oxidation reaction section 16 and the third ozone pre-oxidation reaction section 17, the isolation baffles are vertically arranged, the lower part of the baffle close to the second ozone pre-oxidation reaction section 16 is away from the bottom of the ozone pre-oxidation tank 4, and the upper part of the baffle close to the third ozone pre-oxidation reaction section 17 is away from the top of the ozone pre-oxidation tank 4. The design can make the water flow enter the first ozone pre-oxidation reaction section 15 from the upper part of the first ozone pre-oxidation reaction section 15, move towards the ozone of the first aerator 18, move in an S shape from the lower part of the first ozone pre-oxidation reaction section 15, enter the second ozone pre-oxidation reaction section 16 from the upper part of the second ozone pre-oxidation reaction section 16, move towards the ozone of the second aerator 19, move in an S shape from the lower part of the second ozone pre-oxidation reaction section 16, enter the third ozone pre-oxidation reaction section 17 from the upper part of the third ozone pre-oxidation reaction section 17, and move towards the ozone of the third aerator 20.
The upper part of the third ozone pre-oxidation reaction section 17 is connected with a tail gas collecting device 24.
As shown in fig. 3, the pulse hydrolysis acidification 5 one end is connected with the ozone pre-oxidation pond 4 and the sludge collection pond 11, the other end is connected with the contact oxidation pond 6, the top of the pulse hydrolysis acidification pond 5 is provided with a pulse water tank 28 and a pneumatic valve 29, the pulse water tank 28 is connected with a medicament inlet 25, the bottom of the pulse hydrolysis acidification pond 5 is provided with a plug flow gas device 26, a first flexible filler area 27 is arranged above the plug flow gas device 26, the upper part of the first flexible filler area 27 is connected with the contact oxidation pond 6 through a pipeline, the first flexible filler area 27 adopts elastic filler, the top of the pulse hydrolysis acidification pond 5 is further provided with an oxidation-reduction potential monitor 30 and a tail gas collection device 24.
As shown in fig. 4, at least one water cap 33 is arranged at the lower part of the contact oxidation pond 6, at least one fourth aerator 32 is arranged above the water cap 33, the fourth aerator 32 is connected with the air inlet 31, a second flexible filler area 34 is arranged above the fourth aerator 32, the second flexible filler area 34 adopts elastic filler, and the contact oxidation pond 6 is also provided with an online dissolved oxygen value monitoring device 35 and a liquid level meter 36 which are connected with the tail gas collecting device 24.
The end of intaking in the contact oxidation pond sets up into water partition wall 37, and the partition wall 37 that intakes shelters from water and does not directly get into in the side and pack, and the water hole is opened apart from the bottom of the pool 0.3 meters to the partition wall 37 that intakes, and the control is crossed the water hole velocity of flow and is 0.4 ~ 0.6 meters/second, 6 one end in contact oxidation pond is connected with pulse hydrolysis acidification pond 5 and mud collecting pit 11, and the other end is connected with second grade air supporting pond 7, 6 second flexible filler district 34 tops in contact oxidation pond are close to second grade air supporting pond 7 and locate to set up L type play water weir.
An ozone aerator is arranged at the bottom of the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond 8, a hydrogen peroxide adding port is arranged above the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond 8, and the pH value in the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond 8 is 9-12.
As shown in figure 5, the biological activated carbon pool 9 is internally provided with activated carbon, and the specific surface area of the activated carbon is preferably 200m2The upper part of the biological activated carbon pool 9 is provided with a grid 40, the grid 40 is composed of grid bars at intervals of 2 cm, a perforation aeration device 38 is arranged below the grid, the perforation aeration device 38 is horizontally arranged, the perforation diameter is 4mm, the opening direction is 45 degrees downwards in a slant mode, the activated carbon is positioned on the grid 40 with the interval of 2 cm, the biological activated carbon pool 9 is further provided with an air inlet 39 connected with the perforation aeration device 38, the bottom of the biological activated carbon pool 9 is connected with the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation pool 8, and the top of the biological activated carbon pool is connected with the clean water pool 10.
The wastewater from the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond 8 enters from the bottom of the biological activated carbon pond 9, is respectively contacted and reacted with air and activated carbon along with the rising of the liquid level, so as to further remove harmful substances in the wastewater, and the treated wastewater enters into the clean water pond 10 from the top of the biological activated carbon pond 9.
A filter screen is arranged between the adjusting tank 2, the primary air flotation tank 3, the ozone pre-oxidation tank 4, the pulse hydrolysis acidification tank 5, the contact oxidation tank 6, the secondary air flotation tank 7, the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank 8, the biological activated carbon tank 9 and the clean water tank 10.
The working process is as follows: the phenol-containing wastewater is discharged from a wastewater tank 1, enters an adjusting tank 2 for water quality adjustment and homogenization, then enters a primary air flotation tank 3, the primary air flotation tank 3 adopts a shallow air-dissolved air flotation tank to adsorb suspended organic matters with larger particles by using bubbles, the wastewater with reduced COD sequentially enters an ozone pre-oxidation reaction tank 4, and phenols in the wastewater are attenuated and modified by strong oxidation effect of ozone. The ozone pre-oxidation reaction tank 4 adopts a three-section structure, water flow enters the first ozone pre-oxidation reaction section 15 from the upper part of the first ozone pre-oxidation reaction section 15, moves towards ozone of the first aerator 18, flows out from the lower part of the first ozone pre-oxidation reaction section 15, moves in an S shape, enters the second ozone pre-oxidation reaction section 16 from the upper part of the second ozone pre-oxidation reaction section 16, moves towards ozone of the second aerator 19, flows out from the lower part of the second ozone pre-oxidation reaction section 16, moves in an S shape, enters the third ozone pre-oxidation reaction section 17 from the upper part of the third ozone pre-oxidation reaction section 17, and moves towards ozone of the third aerator 20. The residual ozone that second ozone pre-oxidation reaction section 16 produced on the one hand gets into blender 22 through first pipeline 21, carries out preliminary mixing and preliminary oxidation with waste water, and on the other hand is connected with third aerator 20 through first pipeline 23, and the design can carry out preliminary treatment to waste water at first ozone pre-oxidation reaction section 15 like this, carries out further processing to waste water at third ozone pre-oxidation reaction section 17.
After the phenol-containing wastewater moves from the ozone pre-oxidation reaction tank 4 to the pulse hydrolysis acidification tank 5, a pulse water tank 28 is arranged at the top of the pulse hydrolysis acidification tank 5, the water tank is subjected to pulse stirring at intervals of 2 minutes, and activated sludge adsorbed on the flexible filler in the hydrolysis acidification tank is impacted and falls off, so that the phenomenon that the filler plate in the water tank is blocked is avoided. The water inlet and the water outlet of the pulse water tank 28 are provided with electric switch valves which are interlocked with the liquid level of the pulse hydrolysis acidification pool 5. When the 5 th position of the pulse hydrolysis acidification tank reaches the high position, the water inlet valve is automatically interlocked and the water outlet valve is closed at the same time. The flow velocity of the air hole valve 29 of the pulse water tank 28 is 0.4-0.5 m/s, the volume of the pulse hydrolysis acidification tank 5 is determined according to the designed water quantity of sewage, and the water flushing time of a single tank is 1-4 minutes, so that the pulse stirring effect of the hydrolysis acidification tank is ensured. The retention time of the wastewater in the hydrolysis acidification tank is 18-24 hours, and the wastewater enters the contact oxidation tank 6 after exiting the pulse hydrolysis acidification tank 5.
An air inlet is arranged above the pulse water tank 28, and an air outlet is arranged above the pulse hydrolysis acidification pool 5, so that the pulse effect is guaranteed.
The wastewater entering the contact oxidation tank 6 flows to the water cap area from the water through hole 0.3m away from the bottom of the water inlet partition wall 37, then contacts and mixes with the gas, enters the second flexible filler area 34 for oxidation reaction, and flows out of the water outlet weir, wherein the water outlet weir can ensure that the flow velocity on each water flow section is equal, the condition of short flow in the filler area is avoided, and meanwhile, the uniform flow velocity can also keep the biochemical system in the whole water tank to run uniformly.
The effluent of the contact oxidation tank 6 enters a secondary air flotation tank 7, suspended matters carried in the effluent of the contact oxidation tank are removed by the secondary air flotation tank 7, and a shallow air flotation tank is used for replacing a secondary sedimentation tank.
And then the wastewater flows out of the secondary air flotation tank 7 and enters a pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation tank 8 to carry out ozone and hydrogen peroxide two-dimensional advanced oxidation reaction. Then the wastewater enters a biological activated carbon tank 9 for adsorption reaction, and is filtered and enters a clean water tank 10.
Example 2
A biochemical treatment method of phenol-containing wastewater comprises the steps of adjusting homogenization, first-stage adsorption impurity removal, ozone pre-oxidation, hydrolytic acidification, contact oxidation, second-stage adsorption impurity removal, ozone and hydrogen peroxide two-dimensional advanced oxidation and activated carbon adsorption.
The phenol-containing wastewater enters an adjusting tank to be adjusted and homogenized, water from sewage treatment has water quality fluctuation, the water enters a homogenizing tank to be uniformly mixed and then enters a rear system, a shallow dissolved air flotation tank is adopted in primary air flotation, and the bubble particle size of the shallow dissolved air flotation tank is controlled to be 5-10 microns.
The ozone pre-oxidation step comprises a first ozone pre-oxidation reaction, a second ozone pre-oxidation reaction section and a third ozone pre-oxidation reaction, rubber sheets of the first aerator, the second aerator and the third aerator are made of EPDM materials, and the diameter of bubbles is controlled to be 2-3 mm.
The hydrolysis acidification is pulse hydrolysis acidification, the pulse water tank performs pulse stirring on the water pool every 2 minutes, the flow rate of the pneumatic valve is 0.4 m/s, the hydrolysis acidification time is 21 hours, and the contact oxidation reaction time is 5 hours.
Collecting sludge generated by hydrolytic acidification, contact oxidation and secondary adsorption impurity removal, wherein the sludge is activated sludge and contains flora for degrading phenolic substances. The activated sludge can also supplement active flora for the steps of hydrolytic acidification and contact oxidation.
Example 3
A biochemical treatment method of phenol-containing wastewater comprises mixing 100m3Conveying the waste water with phenol content of 65mg/L and COD of 600mg/L to a conditioning tank by a pump, homogenizing the waste water, then feeding the waste water into a first-stage shallow dissolved air flotation tank to adsorb suspended organic matters with larger particles by utilizing bubbles in the shallow dissolved air flotation tank to suspended matters in the waste water, feeding the waste water with COD of 480mg/L after reducing suspended matters in the waste water into an ozone pre-oxidation reaction tank, attenuating and modifying phenols in the waste water by strong oxidation of ozone to improve the biodegradability of the waste water, feeding the waste water into a pulse hydrolysis acidification tank after the phenol content is reduced to 40mg/L or about 360mg/L, wherein a pulse water tank is arranged at the top of the pulse hydrolysis acidification tank, and is provided with an electric valve to stir the water tank in a pulse mode every 2 minutes to impact and drop active sludge adsorbed on flexible fillers in the hydrolysis acidification tank so as to avoid filler plates in the water tank from being solidified, the retention time of the wastewater in the hydrolysis acidification tank is 21 hours, the phenol content of the wastewater is reduced to 32mg/L COD (chemical oxygen demand) which is about 330mg/L, the wastewater is discharged from the pulse hydrolysis acidification tank and enters the advection contact oxidation tank, the water inlet end of the advection contact oxidation tank is provided with a water inlet partition wall, the water with a water hole at the bottom enters the flexible filler region, the flexible filler region is provided with a perforated aeration pipe, oxygen is flushed into the water, the dissolved oxygen in the contact oxidation tank is kept in a certain range, the discharged water is provided with a water outlet weir, the flow velocity on each water flow section is equal, the short flow condition in the filler is avoided, meanwhile, the uniform flow velocity can also keep the uniform operation of a biochemical system in the whole water tank, the retention time of the wastewater in the contact oxidation tank is 5 hours, the phenol content of the discharged water from the contact oxidation tank is 0.6mg/L, and the COD is 60 mg/L. The effluent of the contact oxidation tank enters a secondary shallow air flotation tank, suspended matters carried in the effluent of the contact oxidation tank are removed by the secondary air flotation tank, sludge floated by the air flotation tank is conveyed to a sludge concentration tank by a sludge pump, concentrated and then enters a sludge drying device for further dehydration and then is subjected to incineration treatment, and simultaneously, the sludge is introduced to a pulse hydrolysis acidification tank and connected with the pulse hydrolysis acidification tank from the secondary shallow air flotation tank in due time according to the sludge concentration in the pulse hydrolysis acidification tank and the contact oxidation tankThe catalytic oxidation tank improves the sludge concentration of the pulse hydrolysis acidification tank and the catalytic oxidation tank and improves the treatment capacity of pollutants. And the effluent of the second-stage shallow air flotation tank enters a second-stage ozone oxidation water tank, the oxidation effect of ozone and hydrogen peroxide on the phenol-containing water is utilized to reduce the phenol content to be below 0.3mg/L, COD is reduced to be below 50mg/L, the effluent enters a biological activated carbon tank for further biochemical treatment and adsorption, the phenol content is reduced to be below 0.2mg/L, and the COD is reduced to 40mg/L so that the effluent of the wastewater reaches the standard and is discharged.
Example 4
Will be 150m3The waste water containing 110mg/L phenol and 900mg/L COD is pumped into a tempering tank, the waste water enters a first-level shallow dissolved air flotation tank after homogenization to adsorb suspended organic matters with larger particles by utilizing bubbles in the shallow dissolved air flotation tank to suspended matters in the waste water, the waste water with 750mg/L COD after reducing suspended matters in the waste water enters an ozone pre-oxidation reaction tank, phenols in the waste water are attenuated and modified by strong oxidation of ozone to improve the biodegradability of the waste water, the phenol content is reduced to 60mg/L and about 690mg/L, the waste water enters a pulse hydrolysis acidification tank, a pulse water tank is arranged at the top of the pulse hydrolysis acidification tank, an electric valve is arranged to carry out pulse stirring on the water tank every 2 minutes to impact and drop active sludge adsorbed on flexible COD in the hydrolysis acidification, and a filler plate in the water tank is avoided being bonded, the retention time of the wastewater in the hydrolysis acidification tank is 22 hours, the phenol content of the wastewater is reduced to 40mg/L COD (chemical oxygen demand) and then the wastewater enters a laminar flow contact oxidation tank after exiting from the pulse hydrolysis acidification tank, a water inlet partition wall is arranged at the water inlet end of the laminar flow contact oxidation tank, water with a water hole at the bottom enters a flexible filler region, the flexible filler region is provided with a perforated aeration pipe, oxygen is flushed into the water, the dissolved oxygen in the contact oxidation tank is kept within a certain range, an effluent weir is arranged for effluent, the flow rate on each water flow section is equal, the short flow condition in the filler is avoided, meanwhile, the uniform flow rate can also keep the uniform operation of a biochemical system in the whole water tank, the retention time of the wastewater in the contact oxidation tank is 7 hours, the phenol content of the effluent of the contact oxidation tank is 0.6mg/L, and the COD is 60 mg/L. The effluent of the contact oxidation tank enters a second-stage shallow air flotation tank, and the second-stage air flotation tank is utilized to remove the clamp in the effluent of the contact oxidation tankThe suspended solids in the belt, the sludge floated by the air flotation tank are conveyed to a sludge concentration tank through a sludge pump, and enter a sludge drying device for further dehydration after concentration, and are subjected to incineration treatment, and simultaneously, the sludge is introduced to the pulse hydrolysis acidification tank and the contact oxidation tank from the secondary shallow air flotation tank in due time according to the sludge concentration in the pulse hydrolysis acidification tank and the contact oxidation tank, so that the sludge concentration of the pulse hydrolysis acidification tank and the contact oxidation tank is improved, and the treatment capacity on pollutants is improved. And the effluent of the second-stage shallow air flotation tank enters a second-stage ozone oxidation water tank, the oxidation effect of ozone and hydrogen peroxide on the phenol-containing water is utilized to reduce the phenol content to be below 0.32mg/L, COD is reduced to be below 53mg/L, the effluent enters a biological activated carbon tank for further biochemical treatment and adsorption, the phenol content is reduced to be below 0.25mg/L, and the COD is reduced to 42mg/L so that the effluent of the wastewater reaches the standard and is discharged.
Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The biochemical treatment device for the phenolic wastewater is characterized by comprising an adjusting tank, a primary air flotation tank, an ozone pre-oxidation tank, a pulse hydrolysis acidification tank, a contact oxidation tank, a secondary air flotation tank, a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank and a biological activated carbon tank which are sequentially connected.
2. The biochemical treatment apparatus for phenol-containing wastewater according to claim 1, wherein the regulating reservoir is connected to a wastewater reservoir or a wastewater inlet;
preferably, the pulse hydrolysis acidification tank is connected with the sludge collection tank through two pipelines;
preferably, the contact oxidation tank is connected with the sludge collecting tank through two pipelines
Preferably, the secondary air flotation tank is connected with the sludge collection tank through a pipeline;
preferably, the sludge collection tank is connected with a sludge tank and a mother liquor tank, and the mother liquor tank is connected with the pulse hydrolysis acidification tank.
3. The biochemical treatment device for phenolic wastewater as recited in claim 1, wherein the primary floatation tank employs a shallow dissolved air floatation tank to adsorb suspended organic matters with larger particles by using air bubbles;
preferably, one end of the ozone pre-oxidation tank is connected with the primary air flotation tank, the other end of the ozone pre-oxidation tank is connected with the pulse hydrolysis acidification tank, the ozone pre-oxidation tank comprises a first ozone pre-oxidation reaction section, a second ozone pre-oxidation reaction section and a third ozone pre-oxidation reaction section, and a first aerator, a second aerator and a third aerator are respectively arranged at the bottoms of the first ozone pre-oxidation reaction section, the second ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section;
preferably, the first aerator and the second aerator are connected with an ozone inlet;
preferably, a mixer, preferably a venturi mixer, is arranged at the joint of the primary air flotation tank and the ozone pre-oxidation tank;
preferably, the second ozone pre-oxidation reaction section is connected with the mixer through a first pipeline and is connected with a third aerator of a third ozone pre-oxidation reaction section through a second pipeline;
preferably, at least two parallel partition plates are arranged between the first ozone pre-oxidation reaction section and the second ozone pre-oxidation reaction section, the isolation baffle plates are vertically arranged, the lower part of the baffle plate close to the first ozone pre-oxidation reaction section is away from the bottom of the ozone pre-oxidation tank by a certain distance, and the upper part of the baffle plate close to the second ozone pre-oxidation reaction section is away from the top of the ozone pre-oxidation tank by a certain distance;
preferably, at least two parallel isolation baffles are arranged between the second ozone pre-oxidation reaction section and the third ozone pre-oxidation reaction section, the isolation baffles are vertically arranged, the lower part of the baffle close to the second ozone pre-oxidation reaction section is away from the bottom of the ozone pre-oxidation tank by a certain distance, and the upper part of the baffle close to the third ozone pre-oxidation reaction section is away from the top of the ozone pre-oxidation tank by a certain distance;
preferably, a tail gas collecting device is connected above the third ozone pre-oxidation reaction section.
4. The biochemical treatment device for phenolic wastewater according to claim 1, wherein a pulse water tank and a pneumatic valve are arranged at the top of the pulse hydrolysis acidification tank, and the pulse water tank is connected with the chemical inlet;
preferably, the bottom of the pulse hydrolysis acidification tank is provided with a flow pushing device, a first flexible filler area is arranged above the flow pushing device, and the upper part of the first flexible filler area is connected with the contact oxidation tank through a pipeline;
preferably, the first flexible filler is elastic filler;
preferably, the top of the pulse hydrolysis acidification tank is also provided with an oxidation-reduction potential monitor and a tail gas collecting device;
preferably, one end of the pulse hydrolysis acidification is connected with the ozone pre-oxidation tank and the sludge collection tank, and the other end of the pulse hydrolysis acidification is connected with the contact oxidation tank;
preferably, the lower part of the contact oxidation pond is provided with at least one water cap, at least one fourth aerator is arranged above the water cap, the fourth aerator is connected with the air inlet, and a second flexible filler area is arranged above the fourth aerator;
preferably, the second flexible filler is elastic filler;
preferably, the contact oxidation pond is also provided with an online dissolved oxygen value monitoring device and a liquid level meter which are connected with a tail gas collecting device;
preferably, a water inlet partition wall is arranged at the water inlet end of the contact oxidation pond, a water through hole is formed in the position, 0.3m away from the bottom of the pond, of the wall, and the flow velocity of the water through hole is controlled to be 0.4-0.6 m/s, preferably 0.5 m/s;
preferably, one end of the contact oxidation tank is connected with the pulse hydrolysis acidification tank and the sludge collection tank, and the other end of the contact oxidation tank is connected with the secondary air flotation tank;
preferably, an effluent weir is arranged at the contact oxidation tank opening, and the effluent weir is an L-shaped effluent weir.
5. The biochemical treatment device for the phenolic wastewater according to claim 1, wherein an ozone aerator is arranged at the bottom of the pressure-bearing ozone-hydrogen peroxide two-dimensional advanced oxidation tank, and a hydrogen peroxide feeding port is arranged above the pressure-bearing ozone-hydrogen peroxide two-dimensional advanced oxidation tank;
preferably, the pH value in the pressure-bearing ozone and hydrogen peroxide two-dimensional advanced oxidation pond is 9-12, and preferably 9.5;
preferably, activated carbon is arranged in the biological activated carbon tank, and the specific surface area of the activated carbon is preferably 200m2/g；
Preferably, the upper part of the biological activated carbon pool is provided with a grid, the grid consists of grid bars with intervals of 2 cm, the perforating aeration device is arranged below the grid and is horizontally arranged, the diameter of a perforation is 2-4mm, the direction of an opening is 45 degrees downwards in an inclined mode, and the diameter of the perforation is preferably 4 mm;
preferably, the activated carbon is positioned on a grid with the grid bar spacing of 2 cm;
preferably, the biological activated carbon tank is also provided with an air inlet connected with a perforation aeration device;
preferably, the bottom of the biological activated carbon pool is connected with a pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation pool, and the top of the biological activated carbon pool is connected with a clean water pool;
preferably, a filter screen is arranged among the adjusting tank, the primary air flotation tank, the ozone pre-oxidation tank, the pulse hydrolysis acidification tank, the contact oxidation tank, the secondary air flotation tank, the pressure-bearing ozone hydrogen peroxide two-dimensional advanced oxidation tank and the biological activated carbon tank.
6. The biochemical treatment method of phenol-containing wastewater based on the biochemical treatment device of phenol-containing wastewater according to any one of claims 1 to 5, characterized by comprising the steps of adjusting homogenization, primary adsorption impurity removal, ozone pre-oxidation, hydrolytic acidification, contact oxidation, secondary adsorption impurity removal, ozone hydrogen peroxide two-dimensional advanced oxidation, and activated carbon adsorption.
7. The biochemical treatment method of phenolic wastewater as claimed in claim 6, wherein the phenolic wastewater enters a regulating tank for regulating and homogenizing;
preferably, the primary air floatation adopts a shallow dissolved air floatation tank, and the particle size of bubbles in the shallow dissolved air floatation tank is controlled to be 5-10 microns;
preferably, the ozone pre-oxidation step comprises a first ozone pre-oxidation reaction, a second ozone pre-oxidation reaction section and a third ozone pre-oxidation reaction;
preferably, the rubber diaphragms of the first aerator, the second aerator and the third aerator are made of EPDM (ethylene-propylene-diene monomer) materials, and the diameter of the bubbles is controlled to be 2-3 mm.
8. The biochemical treatment method of phenolic wastewater according to claim 6, wherein the hydrolytic acidification is pulse hydrolytic acidification, and the pulse water tank performs pulse agitation on the water pool every 2 minutes;
preferably, the flow rate of the pneumatic valve is 0.4-0.5 m/s, preferably 0.4 m/s;
preferably, the hydrolysis acidification time is 18-24 hours, preferably 21 hours;
preferably, the contact oxidation reaction time is 3-8 hours, preferably 5 hours;
preferably, sludge generated by hydrolytic acidification, contact oxidation and secondary adsorption impurity removal is collected, and the sludge is activated sludge and contains flora for degrading phenolic substances.
9. An apparatus for treating wastewater, comprising the apparatus for biochemical treatment of phenol-containing wastewater according to any one of claims 1 to 5.
10. Use of the apparatus for biochemical treatment of phenol-containing wastewater according to any one of claims 1 to 5 and/or the method for biochemical treatment of phenol-containing wastewater according to any one of claims 6 to 8 in the field of phenol-containing wastewater or wastewater treatment.
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