CN113149341A - Advanced treatment method for high-salinity wastewater - Google Patents
Advanced treatment method for high-salinity wastewater Download PDFInfo
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- 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
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- 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
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
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- C02F2101/00—Nature of the contaminant
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- C02F2305/06—Nutrients for stimulating the growth of microorganisms
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- 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
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- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention relates to the field of sewage treatment, and relates to a method for advanced treatment of high-salinity wastewater. The method comprises a pretreatment unit, a first-stage micron carrier fluidized bed, an ozone catalytic oxidation unit, a second-stage micron carrier fluidized bed, a reverse osmosis unit and an MVR unit, solves the problem of membrane fouling of the reverse osmosis unit, avoids the problem of pan pasting when the MVR unit treats membrane concentrated solution for desalination, realizes advanced treatment of biochemical effluent of high-salinity wastewater, and can discharge the effluent up to the standard.
Description
Technical Field
The invention relates to the field of sewage treatment, and relates to a method for advanced treatment of high-salinity wastewater.
Background
The high-salinity wastewater has the common characteristics of high COD, high total nitrogen, poor biodegradability and the like, and is difficult to discharge after reaching the standard by only using a biochemical method for treatment. Therefore, measures are needed to reduce the influence of the organic matters difficult to degrade on the growth of microorganisms so as to promote the biochemical treatment process.
China CN106927556 discloses a method for deeply treating high-salinity wastewater by an electrolytic method, which adopts a regulating reservoir, a lift pump, a primary electrolytic tank, a secondary electrolytic tank, a tertiary electrolytic tank and a sedimentation tank which are arranged in series for treatment. However, the process adopts a three-stage electrolysis device, the pH value needs to be adjusted to 2-3 in the process, and hydrogen peroxide and ferrous sulfate are added simultaneously, so that more sludge can be generated. Chinese patent CN105271608A discloses a non-membrane advanced treatment method for high-salinity wastewater, which comprises a physicochemical treatment unit, an electrochemical oxidation unit, a biochemical treatment unit and a filtration unit. The method has the advantages of strong impact resistance, economic and reliable operation, no generation of concentrated solution, simple operation and the like, but the flocculation treatment unit has unstable effect, the electrochemical treatment unit has low efficiency, a subsequent biochemical treatment unit is required, and the occupied area is large. Chinese patent CN 108675565A discloses a method for advanced treatment of high-salinity wastewater, which comprises the following steps: the method comprises a pretreatment unit, an UASB reaction unit, an AO reaction unit, an MBR reaction unit, a selective permeable membrane unit, a coagulation air flotation unit, an oxidation unit and an advanced oxidation unit, wherein the selective permeable membrane unit is selected, namely the COD (chemical oxygen demand) of the inlet water of the reverse osmosis system is controlled below 2000mg/L, the inlet water is inevitably subjected to membrane fouling and blocking irreversibly after long-term operation, the membrane flux cannot be recovered even if frequent chemical cleaning is carried out, and finally, the replacement of a reverse osmosis membrane element cannot be avoided, so that the operation cost is high; at present, the total salt of the high-salt wastewater is required to be controlled below 1600mg/l in many areas, reverse osmosis concentrated water of many high-salt wastewater projects is not desalted and is finally discharged along with the effluent, and the salt content cannot reach the discharge standard.
If the reverse osmosis concentrated water is desalted by MVR, the high organic matter content (namely high COD) in the concentrated water can be adhered to a wall hanging (commonly called a pasting pot) on the inner wall of an MVR system, so that the efficiency is reduced, the machine is frequently stopped for cleaning, and the salt is difficult to crystallize. Therefore, how to provide a high-salinity wastewater treatment method which has reliable process, low treatment cost, reverse osmosis membrane fouling prevention and desalting capability is an urgent problem to be solved.
Disclosure of Invention
Based on the problems in the prior art, the invention aims to provide a deep treatment method of high-salinity wastewater, which can realize standard discharge of effluent of the high-salinity wastewater, solve the problem of fouling and blocking of a reverse osmosis membrane and solve the problem of pot pasting during desalination of membrane concentrated solution treated by an MVR unit.
In order to realize the purpose of the invention, the technical scheme is as follows:
a high-salinity wastewater advanced treatment system comprises a pretreatment unit, a first-level micron carrier fluidized bed, an ozone catalytic oxidation unit, a second-level micron carrier fluidized bed, a reverse osmosis membrane unit and an MVR unit which are sequentially connected; the pretreatment unit is provided with a high-salinity wastewater inlet and a high-salinity wastewater outlet respectively, and the water outlet is connected with the primary micron carrier fluidized bed, the ozone catalytic oxidation unit, the secondary micron carrier fluidized bed and the reverse osmosis membrane unit in series; the reverse osmosis membrane unit is respectively provided with a separated water outlet and a concentrated water outlet, and the separated water outlet is directly connected with a standard water outlet; the concentrated water outlet is connected with the MVR unit in series.
The first-stage micron carrier fluidized bed is sequentially provided with an anoxic zone, an aerobic zone and a primary sedimentation tank; the second-level micron carrier fluidized bed is sequentially provided with an anoxic zone and an aerobic zone, and an MBR flat membrane used for sludge-water separation is arranged in the aerobic zone.
And the primary micron carrier fluidized bed and the secondary micron carrier fluidized bed are respectively provided with a device which can enable micron carriers added in the primary micron carrier fluidized bed and the secondary micron carrier fluidized bed to be capable of suspending and fluidizing.
The micron carrier is one or more of powdered activated carbon, activated zeolite and activated diatomite; the dosage is 50-1000 mg/l according to different water quality.
Methanol and/or glucose are added into the first-stage micron carrier fluidized bed and the second-stage micron carrier fluidized bed; the adding amount of the carbon source is calculated according to the COD/TN being more than or equal to 5.
The second-stage micron carrier fluidized bed is sequentially provided with an anoxic zone and an aerobic zone, and the aerobic zone is provided with an MBR flat sheet membrane as a mud-water separation facility.
The ozone catalytic oxidation unit is provided with an ozone generator and an ozone catalytic oxidation tower; the ozone catalytic oxidation tower is provided with an air inlet, an air outlet, a water inlet and a water outlet, and the water outlet of the ozone catalytic oxidation tower is connected to the secondary micron carrier fluidized bed through a pipeline; wherein, an ozone catalyst is added into the ozone catalytic oxidation tower.
The reverse osmosis unit adopts a seawater desalination reverse osmosis membrane.
A method for carrying out advanced treatment on high-salinity wastewater by using the system,
(1) pretreatment: introducing high-salinity wastewater to be treated into a pretreatment unit, and adding 10-20 mg/l of polymeric ferric sulfate and 1-5 mg/l of polyacrylamide to remove suspended impurities and/or macromolecular organic matters;
(2) first-order micron carrier fluidized bed: effluent of the pretreatment unit enters a first-stage micron carrier fluidized bed, meets the biochemical denitrification requirement under the action of a carbon source, and is fluidized by suspended fluidized micron carriers through an anoxic zone and an aerobic zone in the fluidized bed, and then flows into a sedimentation tank in the fluidized bed for mud-water separation; removing most COD, ammonia nitrogen and total nitrogen in the wastewater.
(3) An ozone catalytic oxidation unit: the effluent separated in the first-level micron carrier fluidized bed sedimentation tank is lifted to an ozone catalytic oxidation unit, and the COD concentration in the wastewater is reduced to below 500mg/L through direct oxidation and indirect oxidation under the action of an ozone catalyst;
(4) second-stage micron carrier fluidized bed: the effluent of the ozone catalytic oxidation unit enters a secondary micron carrier fluidized bed, the amount of supplemented carbon source meets the biochemical denitrification requirement of the secondary micron carrier fluidized bed, the wastewater is fluidized by suspended fluidized micron carriers through an anoxic zone and an aerobic zone in the fluidized bed, the treated wastewater is subjected to sludge-water separation by an MBR flat membrane in the aerobic zone, the COD, ammonia nitrogen and total nitrogen of the wastewater are further removed, the COD of the obtained effluent is less than or equal to 50mg/L, and the TN is less than or equal to 20mg/L to control the low COD of the effluent so as to ensure that a subsequent reverse osmosis system cannot be blocked by organic pollutants.
(5) Reverse osmosis separation: the MBR effluent of the second-stage micron carrier fluidized bed is lifted to a reverse osmosis unit, so that the concentration and separation of the high-salinity sewage and the strong brine are realized, and the produced fresh water can be discharged after reaching the standard.
Concentrated high-salt water generated by the reverse osmosis unit enters an MVR unit, and separated miscellaneous salt is transported out for disposal; the distilled water and the reverse osmosis fresh water are mixed and then discharged after reaching the standard.
In the reverse osmosis membrane separation step, a reverse osmosis membrane unit adopts a seawater desalination reverse osmosis membrane, the working pressure is 5.0-8.0 Mpa, and the desalination rate is more than or equal to 98%.
The ozone catalytic oxidation unit adopts a countercurrent fixed bed ozone catalytic oxidation tower, and an ozone generator generates ozone with the concentration of 80-200 g/Nm3The adding amount of ozone is 50-600 mg/L, a micro-nano aerator is adopted for ozone aeration, and the residence time of an empty tower is controlled to be 40-60 min
The invention has the advantages that:
1. the treatment system is organically connected with a pretreatment unit, a primary micron carrier fluidized bed, an ozone catalytic oxidation unit, a secondary micron carrier fluidized bed, a reverse osmosis membrane unit and an MVR unit, and MBR effluent of the secondary micron carrier fluidized bed is connected with the reverse osmosis membrane unit, so that the simple process and the low operation cost are ensured on the premise of realizing standard treatment of high-salt wastewater; an ozone catalytic oxidation unit is introduced into the middle stage of the two-stage biochemical unit, partial COD is removed through chemical oxidation, and the open loop and chain breaking are carried out on heterocyclic substances which are difficult to biochemically degrade, so that the efficiency of the second-stage biochemical unit is improved; and the concentrated water generated by the reverse osmosis membrane unit is processed by the MVR unit, so that the system can effectively desalt and simultaneously has no concentrated water; before the sewage enters the reverse osmosis system, the COD is controlled to be less than or equal to 50mg/l, so that membrane fouling and blocking are effectively prevented, the reverse osmosis membrane system is prevented from being cleaned frequently, and membrane elements are prevented from being replaced frequently; the concentrated water of the reverse osmosis system controls COD to be less than or equal to 300mg/l, so that organic matters of the MVR system are effectively prevented from being stuck on a wall and being burnt, frequent cleaning is avoided, and salt can be smoothly removed.
2. The invention combines the micron carrier fluidization process and the biological treatment process with the water purification process, the anaerobic tank and the anoxic aerobic tank are fluidized beds in the treatment process, and the micron carrier adding device adds micron carriers into each fluidized bed, and the composition and the properties of the micron carriers, so that firstly, the micron carriers are suspended in a mixed solution to be in a fluidization state by utilizing the biological fluidized bed technology, so that the carriers are fully mixed with a gas phase, a liquid phase and a gas-liquid phase, and the biological contact effect is fully exerted; secondly, the invention adopts the activated carbon and the ore powder as carriers, and the ratio, the specific surface area and the particle size of the activated carbon and the ore powder are controlled, so that the fluidized carriers preferentially adsorb bacteria secreting adhesive substances, the bacteria are attached and grown in the pores and on the surface of the micron carriers and are used as the core for forming granular sludge, the anaerobic granular sludge is accelerated to form, and polar functional groups on the surfaces of the carriers provide protection for the attached bacteria and the like, so that the bacteria are prevented from being damaged by high-concentration metal ions, and are gradually domesticated to adapt to high COD and high-salt wastewater, and the surfaces of the carriers can adsorb various pollutants which are difficult to degrade, thereby continuously providing nourishment for a microorganism source, improving the activity of microorganisms, and simultaneously improving the degradation capability.
3. The invention greatly improves the activated sludge concentration and the sludge retention time in the anaerobic fluidized bed and the anoxic aerobic fluidized bed. Specifically, the activated sludge in the first solid-liquid separation zone flows back to the anaerobic fluidized bed, the active concentration in the anaerobic carrier fluidized bed is improved, the anaerobic treatment time is prolonged, the sludge concentration in the anaerobic fluidized bed reaches 10000-50000mg/L, the sludge retention time reaches 40-100 days, a large amount of enriched anaerobic microorganisms generate sufficient denitrification reaction to decompose pollutants, the long-chain heterocyclic organic matters are subjected to ring opening and chain scission to become short-chain organic matters capable of being biochemically degraded, the biodegradability of sewage is improved, and the B/C ratio is greatly improved; the active sludge settled in the secondary sedimentation tank and the second solid-liquid separation zone flows back to the anoxic unit of the anoxic aerobic fluidized bed, the sludge concentration in the anoxic aerobic fluidized bed is improved, the sludge concentration in the aerobic fluidized bed reaches 5000 plus 10000mg/L, the sludge retention time is 10-50 days, and the ammonia nitrogen, COD and BOD are effectively removed.
In summary, the technical effects of the above distinguishing technical features of the present invention as an integral implementation are as follows: the removal rate of COD and total nitrogen of the industrial wastewater with high COD, high salt content and poor biodegradability is up to more than 97 percent.
Drawings
FIG. 1 is a flow chart of a method for advanced treatment of high-salinity wastewater provided by an embodiment of the invention.
Detailed Description
The technical solutions in the embodiments of the present invention are clearly and completely described below with reference to the specific contents of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present invention without making any creative effort, shall fall within the protection scope of the present invention. Details which are not described in detail in the embodiments of the invention belong to the prior art which is known to the person skilled in the art.
Aiming at the characteristics of poor biodegradability and extremely low B/C of high-COD and high-salt content industrial wastewater, the anaerobic and anoxic treatment units are enhanced in the treatment process, the anaerobic treatment time is prolonged, and the aerobic treatment time is shortened, because no oxygen is transferred in an anaerobic system, the MLVSS concentration can reach 5-10 times of the aerobic concentration by adopting microorganism immobilization technologies such as a micron carrier fluidized bed and the like; the activity of anaerobic organisms can be maintained for months or even years without serious decline; the characteristic that the anaerobic organism can greatly reduce the endogenous metabolic strength enables the anaerobic organism to survive in a hunger state, the ability of resisting hunger is much stronger than that of the anaerobic organism, the anaerobic microorganism is enriched in a large amount, the long-chain heterocyclic organic matter is likely to open and break the ring, the long-chain heterocyclic organic matter is changed into the short-chain organic matter which can be biochemically degraded, and the biodegradability of the wastewater is improved. The micron carrier fluidization process and the biological treatment process are combined together, so that the micron carrier fluidization process and the biological treatment process can play a role in a synergistic manner, and the biochemical treatment capacity is changed greatly; the input of the micron carrier increases about 1000 ten thousand meters in each cubic biochemical pool2The most fundamental point is that the retention time of the pollutants in the reaction tank is greatly prolonged, the upper limit is the solid retention time close to the system, but not the hydraulic retention time of the common activated sludge method, so that the pollutants which are originally difficult to biodegrade can be degraded. And the COD of the high-salinity wastewater before entering the reverse osmosis membrane can be less than or equal to 50mg/l, and the COD of the concentrated water is less than or equal to 300mg/l, so that the problem of membrane fouling is solved, and the adverse effect of high organic matter content in the concentrated water on salt crystallization is also solved.
Example 1
As shown in fig. 1, the treatment system comprises a pretreatment unit, a first-level micron carrier fluidized bed, an ozone catalytic oxidation unit, a second-level micron carrier fluidized bed, a reverse osmosis membrane unit and an MVR unit which are connected in sequence;
the pretreatment unit is provided with a high-salinity wastewater inlet and a high-salinity wastewater outlet respectively, and the water outlet is connected with the primary micron carrier fluidized bed, the ozone catalytic oxidation unit, the secondary micron carrier fluidized bed and the reverse osmosis membrane unit in series; the reverse osmosis membrane unit is respectively provided with a separated water outlet and a concentrated water outlet, and the separated water outlet is directly connected with a standard water outlet; the concentrated water outlet is connected with the MVR unit in series;
the front ends of the fluidized beds in the first-stage micron carrier fluidized bed and the second-stage micron carrier fluidized bed are anoxic zones, a submersible stirrer is arranged in the anoxic zones to enable micron carriers added in the anoxic zones to be capable of being suspended and fluidized, aerobic zones are arranged behind the anoxic zones, and microporous aerators are arranged in the aerobic zones to enable micron carriers added in the aerobic zones to be capable of being suspended and fluidized; a sedimentation tank is arranged behind the aerobic zone of the first-level micron carrier fluidized bed, and an MBR flat membrane used for mud-water separation is arranged in the aerobic zone of the second-level micron carrier fluidized bed.
Methanol and/or glucose are added into the first-stage micron carrier fluidized bed and the second-stage micron carrier fluidized bed; the adding amount of the carbon source is calculated according to the COD/TN being more than or equal to 5.
The reverse osmosis membrane unit adopts a seawater desalination membrane (the parameter desalination rate of the membrane is more than or equal to 98%).
The ozone catalytic oxidation unit adopts an ozone catalytic oxidation unit.
The micron carrier is one or more of powdered activated carbon, activated zeolite and activated diatomite; the particle size is 100-300 meshes, and the adding amount is 50-1000 mg/l according to different water quality.
The ozone catalytic oxidation unit is provided with an ozone generator and an ozone catalytic oxidation tower; the ozone catalytic oxidation tower is provided with an air inlet, an air outlet, a water inlet and a water outlet, and the water outlet of the ozone catalytic oxidation tower is connected to the secondary micron carrier fluidized bed through a pipeline; wherein, an ozone catalyst is added into the ozone catalytic oxidation tower.
The units can adopt units capable of realizing remote control, namely, remote control devices are arranged on the units, so that the automation degree of the whole method is improved, and the labor cost can be reduced.
Example 2
Adopt above-mentioned system, handle certain refuse factory leachate stoste, pH 6.8, COD content 3726mg/L, total nitrogen content 1023mg/L, TDS 16180mg/L, COD clearance is up to more than 98.4%, and the total nitrogen clearance of ammonia nitrogen is more than 97.9%.
(1) Pretreatment: high-salinity wastewater enters the pretreatment unit from a water inlet, 15mg/L of polyferric sulfate and 3mg/L of polyacrylamide are added into the pretreatment unit, the pH value of the wastewater is adjusted to 7-8, and suspended impurities and/or macromolecular organic matters are removed, so that the COD content of the effluent is 2198mg/L, the total nitrogen content is 750mg/L, and the TDS is 19828 mg/L;
(2) first-order micron carrier fluidized bed: the pretreated effluent enters a first-stage micron carrier fluidized bed, the front end of the fluidized bed is an anoxic zone, a submersible stirrer is arranged in the anoxic zone, powdered activated carbon serving as a micron carrier is put in the anoxic zone, the adding amount is 400mg/L, the micron carrier can be suspended and fluidized through the stirrer, meanwhile, methanol is added in the anoxic zone, the using amount of the methanol is 3.9ml/L, the methanol meets the requirements of biochemical denitrification, the treated micron carrier flows to an aerobic zone automatically after being treated in the anoxic zone, the micron carrier can be suspended and fluidized through a micropore aerator arranged in the aerobic zone for treatment, then, wastewater enters a settling zone, the carrier and activated sludge are separated from the wastewater, and the carrier and the activated sludge flow back to the anoxic zone through a submersible sewage pump. The COD content of the effluent is 412mg/L, and the total nitrogen content is 133 mg/L;
(3) an ozone catalytic oxidation unit: the effluent of the first-level micron carrier fluidized bed enters an ozone catalytic oxidation unit, a countercurrent fixed bed ozone catalytic oxidation tower is used for carrying out ozone oxidation, and an ozone generator generates ozone with the concentration of 80g/Nm3The ozone dosage is 535.5mg/L, the energy efficiency is 2.60kgO3Controlling the empty tower residence time to be 40min, further reducing organic matters, and enabling the effluent COD content to be 206mg/L, wherein a micro-nano aerator is adopted for ozone aeration;
(4) second-stage micron carrier fluidized bed: the water from the ozone oxidation unit flows to a second-stage micron carrier fluidized bed, the front end of the ozone oxidation unit is an anoxic zone, a submersible stirrer is arranged in the anoxic zone, powdered activated carbon is thrown into the anoxic zone to serve as a micron carrier, the adding amount is 50mg/L, the micron carrier can be suspended and fluidized through the stirrer, meanwhile, methanol is thrown into the anoxic zone, the using amount of the methanol is 0.8ml/L, the biochemical denitrification requirement is met, then the wastewater automatically flows to an aerobic zone, the micron carrier can be suspended and fluidized for treatment through a microporous aerator arranged in the aerobic zone, then the wastewater passes through the water outlet end of the aerobic zone, an MBR flat membrane is arranged as a carrier, activated sludge and sewage separation facilities are arranged, and the carrier and the activated sludge flow back to the anoxic zone through. The pH value of effluent is 7.25, the COD content is 45mg/L, and the total nitrogen content is 15 mg/L;
(5) reverse osmosis membrane separation: effluent of the MBR enters a reverse osmosis membrane unit, soluble humic acid organic matters and the like in water are concentrated under the action of pore size screening, charge effect and the like of the reverse osmosis membrane, COD (chemical oxygen demand) of the effluent is remarkably reduced, the operating pressure of the reverse osmosis membrane unit is 5.5MPa, the COD content of the effluent is 20mg/L, and the total nitrogen content is 10 mg/L; the COD content of the concentrated water is less than 300mg/L, the ammonia nitrogen content is less than 50mg/L, and the TDS is 97896 mg/L;
(6) MVR unit: concentrated water of the reverse osmosis membrane unit enters an MVR unit, the COD content of condensed water effluent is less than 50mg/L, and the ammonia nitrogen content is less than 20 mg/L; the content of organic substances for removing miscellaneous salts is less than 0.25 percent.
Therefore, the sewage treatment system adopting the micron carrier fluidized bed is widely suitable for high-salt, high-COD and difficult-biochemical industrial sewage, and has the advantages of strong applicability, good treatment effect, less occupied land, low cost, simple operation and maintenance, convenient operation and continuous treatment.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that can be easily conceived by those skilled in the art within the technical scope of the present invention are included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (10)
1. A high-salinity wastewater advanced treatment system is characterized in that the treatment system comprises a pretreatment unit, a first-stage micron carrier fluidized bed, an ozone catalytic oxidation unit, a second-stage micron carrier fluidized bed, a reverse osmosis membrane unit and an MVR unit which are sequentially connected; the pretreatment unit is provided with a high-salinity wastewater inlet and a high-salinity wastewater outlet respectively, and the water outlet is connected with the primary micron carrier fluidized bed, the ozone catalytic oxidation unit, the secondary micron carrier fluidized bed and the reverse osmosis membrane unit in series; the reverse osmosis membrane unit is respectively provided with a separated water outlet and a concentrated water outlet, and the separated water outlet is directly connected with a standard water outlet; the concentrated water outlet is connected with the MVR unit in series.
2. The advanced treatment system for high-salinity wastewater according to claim 1, characterized in that the primary micron carrier fluidized bed is provided with an anoxic zone, an aerobic zone and a primary sedimentation tank in sequence; the second-level micron carrier fluidized bed is sequentially provided with an anoxic zone and an aerobic zone, and an MBR flat membrane used for sludge-water separation is arranged in the aerobic zone.
3. The advanced high-salinity wastewater treatment system according to claim 2, characterized in that a device for suspending and fluidizing the added micron carriers is arranged in each of the primary micron carrier fluidized bed and the secondary micron carrier fluidized bed.
4. The high-salinity wastewater advanced treatment system according to claim 3, wherein the micron carrier is one or more of powdered activated carbon, activated zeolite and activated diatomite; the dosage is 50-1000 mg/l according to different water quality.
5. The high-salinity wastewater advanced treatment system according to claim 2, characterized in that the primary micron carrier fluidized bed and the secondary micron carrier fluidized bed are added with methanol and/or glucose; the adding amount of the carbon source is calculated according to the COD/TN being more than or equal to 5.
6. The high-salinity wastewater advanced treatment system according to claim 1, wherein the ozone catalytic oxidation unit is provided with an ozone generator and an ozone catalytic oxidation tower; the ozone catalytic oxidation tower is provided with an air inlet, an air outlet, a water inlet and a water outlet, and the water outlet of the ozone catalytic oxidation tower is connected to the secondary micron carrier fluidized bed through a pipeline; wherein, an ozone catalyst is added into the ozone catalytic oxidation tower.
7. A method for advanced treatment of high-salinity wastewater by using the system of claim 1,
(1) pretreatment: introducing high-salinity wastewater to be treated into a pretreatment unit, and adding 10-20 mg/l of polymeric ferric sulfate and 1-5 mg/l of polyacrylamide;
(2) first-order micron carrier fluidized bed: the effluent of the pretreatment unit enters a first-stage micron carrier fluidized bed, under the action of a carbon source, the wastewater passes through an anoxic zone and an aerobic zone in the fluidized bed and is fluidized by suspended fluidized micron carriers, and then the wastewater flows into a sedimentation tank in the fluidized bed for mud-water separation;
(3) an ozone catalytic oxidation unit: the effluent separated in the first-level micron carrier fluidized bed sedimentation tank is lifted to an ozone catalytic oxidation unit, and the concentration of COD in the wastewater is reduced through direct oxidation and indirect oxidation under the action of an ozone catalyst;
(4) second-stage micron carrier fluidized bed: the effluent of the ozone catalytic oxidation unit enters a secondary micron carrier fluidized bed, under the action of a carbon source, the wastewater passes through an anoxic zone and an aerobic zone in the fluidized bed and is subjected to fluidization treatment by suspended and fluidized micron carriers, and the treated wastewater is subjected to mud-water separation by an MBR flat membrane in the aerobic zone;
(5) reverse osmosis separation: and (3) lifting MBR effluent of the second-stage micron carrier fluidized bed to a reverse osmosis unit, concentrating soluble organic matters in water through the aperture screening and charge effect of the reverse osmosis membrane, and discharging the obtained effluent up to the standard.
8. The method for the advanced treatment of the high-salinity wastewater according to claim 7, characterized in that the concentrated water from the reverse osmosis unit enters an MVR unit, and the separated miscellaneous salts are transported to the outside for disposal; and mixing the water obtained by separation with the water discharged from the reverse osmosis unit and discharging the water after reaching the standard.
9. The method for the advanced treatment of the high-salinity wastewater according to claim 8, characterized in that in the reverse osmosis membrane separation step, a reverse osmosis membrane for seawater desalination is adopted as the reverse osmosis membrane unit, the working pressure is 5.0-8.0 MPa, and the desalination rate is more than or equal to 98%.
10. The method for advanced treatment of high-salinity wastewater according to claim 7, characterized in that the ozone catalytic oxidation unit adopts a countercurrent fixed bed ozone catalytic oxidation tower, and an ozone generator generates ozone with a concentration of 80-200 g/Nm3The adding amount of ozone is 50-600 mg/L, a micro-nano aerator is adopted for ozone aeration, and the residence time of an empty tower is controlled to be 40-60 min.
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