CN111470677A - Method for producing ionic membrane caustic soda by using high-salt organic wastewater generated in epoxy chloropropane production process - Google Patents
Method for producing ionic membrane caustic soda by using high-salt organic wastewater generated in epoxy chloropropane production process Download PDFInfo
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Abstract
The application discloses a method for producing ionic membrane caustic soda by utilizing high-salt organic wastewater generated in an epoxy chloropropane production process, wherein the high-salt organic wastewater is prepared by preprocessing the high-salt organic wastewater, carrying out advanced oxidation and other steps to obtain clean saline with TOC (total organic carbon) less than or equal to 7 mg/L, mixing the clean saline with industrial salt in a salt dissolving barrel to obtain saturated crude saline, respectively conveying the saturated crude saline and a refining reactant to a reaction barrel for refining reaction, then conveying the clean saline to a clarifying barrel, adding a flocculating agent for clarification, carrying out rough filtration and fine filtration on the clarified saline, then conveying the clarified saline to an ion exchange resin tower for secondary refining to obtain refined saline meeting the operation requirement of an ionic membrane electrolytic tank, recycling the waste salt in the high-salt organic wastewater, and being simple and convenient in industrial process, simple in operation and easy to realize industrialization and capable of realizing the high-salt organic wastewater.
Description
Technical Field
The present invention belongs to the field of chemical engineering and technological technology. More particularly, the invention relates to a technical scheme for producing ionic membrane caustic soda by making high-salt organic wastewater have new changes in quality through means of chemical engineering and processes.
Background
In the industrial production processes of petrochemical industry, electric power, coal chemical industry and the like, a large amount of organic wastewater containing inorganic salt is generated. In the process of producing epichlorohydrin by a glycerol method, organic wastewater containing sodium chloride and high TOC is generated. The waste water has high salt content, and if the waste water is directly discharged, the waste water can damage the surrounding soil, increase the salt content of the water body and waste mineral resources. The treatment of high-salt wastewater is a worldwide problem, the amount of wastewater generated in China is more than 3 billion cubic meters every year, the byproduct high-salt dangerous waste is more than ten million tons, most of the waste is not reasonably treated, and huge pressure is brought to the ecological environment. Experts in the industry generally consider that the current high-salinity wastewater treatment lacks an economic and systematic treatment method, and byproducts generated by the treatment are difficult to identify, wherein the waste salt is often treated as dangerous waste, and the economic value is difficult to realize the maximization.
The basic idea of the prior conventional technology for treating high-salt-content wastewater is to separate salt and water with low investment and operation cost and recycle the salt and the water respectively. The application is more extensive mainly including thermal concentration technique and membrane separation technique.
Among the thermal concentration techniques, the main ones with lower processing costs are multi-effect evaporation and MVR techniques. The multi-effect evaporation is that several evaporators are connected in series to make the steam heat be used for several times, so that the utilization rate of heat energy can be raised. The multiple-effect evaporation has higher thermodynamic efficiency than the conventional evaporation, but occupies a large area. The thermodynamic efficiency of multi-effect evaporation is in direct proportion to the number of effects, and although the increase of the number of effects can improve the economy of a system and reduce the operation cost, the investment cost is increased.
The MVR technology utilizes a compressor to compress secondary steam generated in an evaporator, so that the pressure, the temperature and the enthalpy value of the secondary steam are increased, and then the secondary steam is used as heating steam, and has the advantages of small occupied area and low operation cost. Compared with multi-effect evaporation, the method can compress and recycle all secondary steam, and reduces the consumption of raw steam, thereby saving more energy. The Kingqiao Yihai (Lian Yun gang) chlor-alkali Limited company adopts MVR technology to concentrate the light salt brine, the thermodynamic efficiency of the MVR technology is equivalent to 20-30 effects of multi-effect evaporation, and the concentration cost of the light salt brine is greatly reduced. Compared with the multi-effect vacuum evaporation salt making process, the MVR salt making process introduced by the medium-salt gold altar salinization company Limited saves the energy consumption by more than 25 percent. In China, the MVR technology has an applied example in the salt manufacturing industry and has obvious energy-saving effect, but is still in the research and trial operation stage in the aspect of salt-containing wastewater treatment, mainly because the components of the high-salt-content wastewater are complex, the effect of the MVR is greatly influenced by the presence of organic pollutants in the wastewater, and the recovered industrial waste salt does not meet the GB/T5462-2015 standard of industrial salt and cannot be used for resource production of caustic soda and soda ash.
The membrane separation technology is driven by factors such as pressure difference, concentration difference, potential difference and the like, and is realized through size exclusion, charge repulsion and physicochemical action among solutes, a solvent and a membrane. Compared with thermal concentration, the membrane has simple structure, easy operation and low operation temperature, is a technology widely used in the market in recent years, but the membrane surface for separation is easy to pollute, the membrane separation performance is reduced, so a membrane surface cleaning method suitable for the process is required, and meanwhile, the stability, the drug resistance, the heat resistance and the solvent resistance of the membrane are limited, so the application field of the membrane separation technology is limited. Therefore, it is very important to research how to effectively treat the high-salinity wastewater and recycle the waste salt in the high-salinity wastewater.
In recent years, the industry has been dedicated to the production of raw materials for ionic membrane caustic soda from high-salt organic wastewater, and the raw materials for ionic membrane caustic soda are obtained by purifying chemical wastewater containing sodium chloride and organic pollutants.
GB/T5270-2018 physicochemical indexes of salt for ionic membrane caustic soda do not express the requirements on TOC in salt, but the TOC in the salt water is high and has great influence on the production of the ionic membrane caustic soda, organic matters in the salt water can cause the reduction of the filtering capacity of a Kjeldahl membrane filter, the swelling of ion exchange resin, the reduction of the current efficiency of an ionic membrane cell, the swelling of the ionic membrane, Haomingson, and the like in the 'influence of TOC on an ionic membrane electrolytic cell', and the tolerance limit of the membrane on the TOC mass fraction is 7 mg/L.
Patent CN107098360B method for producing raw material for ionic membrane caustic soda by using glyphosate waste salt water states that microfiltration membrane and nanofiltration membrane are adopted for filtration, and finally the filtration liquid is adsorbed by a chelating resin tower, thus obtaining the permeate liquid which is the raw material solution for ionic membrane caustic soda, but the patent can only treat waste salt water in the glyphosate process with TOC less than or equal to 20ppm, the TOC of waste water in the glyphosate production process reaches 40000 mg/L, the patent states that the prior glyphosate unit removes larger molecular organic matters in the glyphosate waste water by ECO catalytic oxidation, MVR and other processes and then extracts sodium chloride in the waste water to prepare refined salt, but the patent does not state the process method and the beneficial effects thereof.
Disclosure of Invention
The main purpose of the application is to provide a method for producing ionic membrane caustic soda by using high-salt organic wastewater generated in an epichlorohydrin production process, so that the quality of the high-salt organic wastewater is changed newly, and the technical scheme is used for producing the ionic membrane caustic soda.
In order to achieve the above object, the present application provides a method for producing ionic membrane caustic soda by using high-salt organic wastewater generated in an epichlorohydrin production process, comprising the following steps:
s1, carrying out pretreatment and advanced oxidation on the high-salinity organic wastewater to obtain clean saline water with TOC less than or equal to 7 mg/L;
s2, mixing the clean brine and industrial salt in a salt dissolving bucket to obtain saturated crude brine;
s3, respectively conveying the saturated crude brine and the refined reactant to a reaction barrel for refining reaction;
s4, conveying the solution after the refining reaction to a clarifying barrel, and adding a flocculating agent for clarification to obtain clarified brine;
s5, after coarse filtration and fine filtration, the clear brine enters an ion exchange resin tower for secondary refining to obtain refined brine meeting the operation requirement of the ion membrane electrolytic cell;
s6, preparing caustic soda by ion membrane from the obtained refined brine, wherein the obtained sodium hydroxide is a raw material in the epoxy chloropropane cyclization step and is also a raw material in epoxy resin production, and H is obtained by ion membrane electrolysis2And Cl2Obtaining HCl through reaction, and conveying the HCl to a device for producing epichlorohydrin by a glycerol method.
Preferably, in the step S1, the high-salt organic wastewater has a sodium chloride content of 5-20% by weight and a TOC of 1000-10000 mg/L value of 8-12.
Preferably, in step S1, the pretreatment is to remove water-insoluble substances in the high-salinity wastewater by microfiltration.
Preferably, in step S1, the advanced oxidation is one or more of Fenton oxidation, photocatalytic oxidation, ozone oxidation, and catalytic wet oxidation.
The advanced oxidation technology is also called deep oxidation technology, and is characterized by producing hydroxyl radical (OH) with strong oxidation capability, under the reaction conditions of high temperature and high pressure, electricity, sound, light irradiation, catalyst and the like, macromolecular refractory organics are oxidized into low-toxicity or non-toxic micromolecular substances, and further deeply oxidized into CO2And H2And O, mineralizing the organic matters in the wastewater. Depending on the manner of generating radicals and the reaction conditions, they can be classified into photochemical oxidation, catalytic wet oxidation, sonochemical oxidation, ozone oxidation, electrochemical oxidation, Fenton oxidation, and the like.
Preferably, the Fenton oxidation condition is that the reaction is carried out for 1-4 hours at 50-60 ℃ and normal pressure in the presence of a Fenton catalyst and a Fenton oxidant, the dosage of the Fenton catalyst is 5.0-8.0 per mill of the weight of the wastewater, and the dosage of the Fenton oxidant is 5.5-10 times of the TOC concentration in the high-salinity organic wastewater.
Preferably, the Fenton catalyst is ferrous chloride or ferric chloride, and the Fenton oxidant is H2O2。
Preferably, the photocatalytic oxidation is carried out under the condition that the reaction is carried out for 1-4 hours at the temperature of 50-60 ℃ and under the normal pressure by utilizing the synergistic effect of ultraviolet light and an oxidant, wherein the oxidant is H2O2The dosage of the organic wastewater is 4.5 to 6.5 times of the TOC concentration in the high-salt organic wastewater.
The photocatalytic oxidation technology utilizes photo-excitation oxidation to oxidize O2、H2O2The oxidizing agent is combined with the light radiation. The light used for photocatalytic oxidation is ultraviolet light, and in a Fenton system with the ultraviolet light, the ultraviolet light and iron ions have a synergistic effect to ensure that H is generated2O2The rate of generating hydroxyl free radicals by decomposition is greatly accelerated,promoting the oxidation removal of organic matters.
Preferably, the ozone oxidation condition is that ozone is introduced for reaction for 1-2 hours at the temperature of 40-60 ℃ and under normal pressure, and the using amount of the ozone is 3-5 times of the TOC concentration in the high-salinity organic wastewater.
The ozone oxidation utilizes ozone decomposition to generate OH free radicals, and the purpose of removing organic matters is achieved through oxidation reaction of OH and the organic matters.
Preferably, the catalytic wet oxidation is carried out for 2-6 h at the temperature of 220-280 ℃ and the pressure of 3.0-6.0 MPa, and the catalyst for catalytic wet oxidation is one or more of transition metal chlorides such as Fe, Cu, Ce, Mo, Mn, Ni, Co and the like.
The catalytic wet oxidation in the invention refers to the mineralization treatment of organic pollutants in wastewater under the conditions of high temperature, high pressure and catalyst existence.
Preferably, the catalytic wet oxidation is carried out in two oxidation towers which are connected in series, the oxidation towers are provided with two layers of flow passing plates, brine with TOC of about 100-500 mg/L is obtained in a first oxidation tower which is connected in series, the brine enters a second oxidation tower for deep oxidation, dilute brine with TOC of about 11 mg/L from an ion membrane electrolytic cell also enters the second oxidation tower which is connected in series, and clean brine with TOC less than or equal to 7 mg/L is obtained.
Preferably, in step S3, the refining reactants are sodium carbonate and sodium hydroxide, and the refining reactants are added to form water-insoluble precipitate of trace calcium and magnesium ions in the crude brine;
preferably, in step S4, the added flocculant is sodium polyacrylate, which is to aggregate the calcium and magnesium ion precipitates obtained in step S3 and suspended matters in the crude brine, and facilitate separation.
Preferably, in step S5, the content of calcium and magnesium ions in the primary refined brine obtained by rough filtration and fine filtration can reach 5 mg/L or less, but still cannot meet the requirement of entering an electrolytic cell, therefore, in step S5, the primary refined brine is secondarily refined by using ion exchange resin, and the content of calcium and magnesium ions in the secondary refined brine obtained is 20 μ g/L or less.
Preferably, in step S5, the ion exchange resin column is filled with chelating ion exchange resin or cation exchange resin, which is a commercially available product, such as D463 or D751 resin sold by great chemical company, east of shandong.
The beneficial effect of this application is: the invention provides a high-grade oxidation and membrane alkali-making process for high-salt organic wastewater generated in the production process of epoxy chloropropane, so that waste salt in the high-salt organic wastewater is recycled, the industrial process is simple and convenient, the operation is simple, the industrialization can be easily realized, and the zero emission of the high-salt organic wastewater can be realized.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this application, serve to provide a further understanding of the application and to enable other features, objects, and advantages of the application to be more apparent. The drawings and their description illustrate the embodiments of the invention and do not limit it. In the drawings:
FIG. 1 is a general flow chart of resource utilization of waste salt in high-salt organic wastewater;
figure 2-ionic membrane caustic soda flow diagram.
Detailed Description
In order to make the technical solutions better understood by those skilled in the art, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only partial embodiments of the present application, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.
It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It should be understood that the data so used may be interchanged under appropriate circumstances such that embodiments of the application described herein may be used. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
In this application, the terms "upper", "lower", "left", "right", "front", "rear", "top", "bottom", "inner", "outer", "middle", "vertical", "horizontal", "lateral", "longitudinal", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings. These terms are used primarily to better describe the present application and its embodiments, and are not used to limit the indicated devices, elements or components to a particular orientation or to be constructed and operated in a particular orientation.
Moreover, some of the above terms may be used to indicate other meanings besides the orientation or positional relationship, for example, the term "on" may also be used to indicate some kind of attachment or connection relationship in some cases. The specific meaning of these terms in this application will be understood by those of ordinary skill in the art as appropriate.
In addition, the term "plurality" shall mean two as well as more than two.
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present application will be described in detail below with reference to the embodiments with reference to the attached drawings.
Example 1:
the advanced oxidation adopts the combination of Fenton oxidation and ultraviolet light catalytic oxidation.
As shown in figure 1 and figure 2, 2000ml of epichlorohydrin wastewater is taken, wherein the sodium chloride content is 10 percent, the TOC content is 3700 mg/L, the pH is adjusted to 6, the wastewater is heated to 55 ℃, the temperature is kept constant, 12.8g of ferrous chloride is added, and then H is added in 3-4 times2O2In total 25 g/L, reacted for 1h, and thenFiltering to remove Fenton iron mud, conveying the filtered wastewater to an ultraviolet light catalytic reactor, and supplementing 5 g/L H with ultraviolet light with the wavelength of 254nm at 55 DEG C2O2The catalytic oxidation was carried out for 2h to obtain a clean brine with a TOC of 2.8 mg/L after oxidation.
The pretreatment is to remove water insoluble matters in the high-salinity wastewater through microfiltration. Mixing the clean brine and industrial salt in a salt dissolving bucket to obtain saturated crude brine; respectively conveying the saturated crude salt water and the refined reactant to a reaction barrel for refining reaction; the refining reactants are sodium carbonate and sodium hydroxide, and are added for leading trace calcium and magnesium ions in the crude brine to form water-insoluble precipitate; conveying the solution after the refining reaction to a clarifying barrel, and adding a flocculating agent for clarification to obtain clarified brine; the added flocculating agent is sodium polyacrylate, so that calcium and magnesium ion precipitates obtained in the step S3 and suspended matters in the crude brine are gathered, and separation is facilitated. After coarse filtration and fine filtration, the clarified brine enters an ion exchange resin tower for secondary refining to obtain refined brine meeting the operation requirement of an ion membrane electrolytic cell; subjecting the obtained refined brine to ion membrane to prepare caustic soda, wherein the obtained sodium hydroxide is a raw material in the step of epoxy chloropropane cyclization and is also a raw material in epoxy resin production, and H is obtained by ion membrane electrolysis2And Cl2Obtaining HCl through reaction, and conveying to the production of epichlorohydrin by a glycerol method.
The content of calcium and magnesium ions in the primary refined brine obtained by rough filtration and fine filtration can reach below 5 mg/L, but still can not meet the requirement of entering an electrolytic cell, therefore, in step S5, the primary refined brine is secondarily refined by using ion exchange resin, and the content of calcium and magnesium ions in the secondary refined brine obtained is below 20 mug/L.
The ion exchange resin column is packed with a chelate ion exchange resin or a cation exchange resin, and is a commercially available product such as D463 or D751 resins sold by Shandong Daihai chemical Co., Ltd.
Example 2:
the difference from example 1 is that: the advanced oxidation adopts the combination of Fenton oxidation and ozone oxidation.
Taking 2000ml of epichlorohydrin wastewater, wherein the sodium chloride content is 15%, the TOC content is 5600 mg/L, adjusting the pH value to 6, heating to 60 ℃, keeping the temperature constant, adding 15g of ferrous chloride, introducing ozone, and adding H for 3-4 times2O2The total amount of the reaction solution is 40 g/L, the reaction solution is reacted for 4 hours, and then the Fenton iron mud is filtered to remove, so that clean brine with the TOC of 3.6 mg/L after oxidation is obtained.
Example 3:
the difference from example 1 is that: the advanced oxidation adopts catalytic wet oxidation.
Taking 2000ml of epichlorohydrin wastewater, wherein the sodium chloride content is 20%, the TOC content is 9700 mg/L, removing insoluble substances in the wastewater through pretreatment, adding ferrous chloride accounting for 1% of the weight of the wastewater, adjusting the pH value to 5, conveying the wastewater into a primary catalytic wet oxidation reactor through a pump, oxidizing for 1h at the temperature of 220 ℃ and the pressure of 4.0MPa, conveying the wastewater into a secondary catalytic wet oxidation reactor through a pipeline, and oxidizing for 1h at the temperature of 240 ℃ and the pressure of 4.0MPa to obtain clean brine with the TOC of 2.25 mg/L after oxidation.
The catalyst for catalyzing wet oxidation is one or more of transition metal chlorides of Fe, Cu, Ce, Mo, Mn, Ni and Co.
The catalytic wet oxidation is carried out in two oxidation towers which are connected in series, wherein the oxidation towers are provided with two layers of flow passing plates, brine with TOC of 300 mg/L is obtained in a first oxidation tower which is connected in series, the brine enters a second oxidation tower for deep oxidation, dilute brine with TOC of 11 mg/L from an ion membrane electrolytic cell also enters the second oxidation tower which is connected in series, and clean brine with TOC less than or equal to 7 mg/L is obtained.
The high-salt organic wastewater generated in the production process of epoxy resin is wastewater with the sodium chloride content of 5-25 wt% and the pH 8-12 wastewater with the TOC content of 2000-20000 mg/L, and is subjected to catalytic oxidation to recover a catalyst to obtain refined brine with the TOC content of less than 10 mg/L, the TOC of the refined brine also has the original salt brought in, the light brine is accumulated and other factors, so when the TOC is less than or equal to 10 mg/L, the membrane in the membrane alkali-making process can still be greatly influenced to a certain extent, and further treatment is needed, so the TOC content can be further reduced by the method.
H obtained by the electrolysis of the ionic membrane2And Cl2The HCl obtained through the reaction is a raw material for producing epoxy chloropropane by a glycerol method, the obtained sodium hydroxide is a raw material in the step of cyclizing epoxy chloropropane and is also a raw material for producing epoxy resin, and the high-salt organic wastewater obtained in the production process of epoxy chloropropane and epoxy resin and the weak brine obtained by an ion membrane electrolytic cell can be continuously used for preparing caustic soda by an ion membrane after being treated by the steps, so that the high-salt organic wastewater is recycled.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (10)
1. A method for producing ionic membrane caustic soda by utilizing high-salt organic wastewater generated in the production process of epoxy chloropropane is characterized by comprising the following steps:
s1, carrying out pretreatment and advanced oxidation on the high-salinity organic wastewater to obtain clean saline water with TOC less than or equal to 7 mg/L;
s2, mixing the clean brine and industrial salt in a salt dissolving bucket to obtain saturated crude brine;
s3, respectively conveying the saturated crude brine and the refined reactant to a reaction barrel for refining reaction;
s4, conveying the solution after the refining reaction to a clarifying barrel, and adding a flocculating agent for clarification to obtain clarified brine;
s5, after coarse filtration and fine filtration, the clear brine enters an ion exchange resin tower for secondary refining to obtain refined brine meeting the operation requirement of the ion membrane electrolytic cell;
s6, preparing caustic soda by ion membrane from the obtained refined brine, wherein the obtained sodium hydroxide is a raw material in the epoxy chloropropane cyclization step and is also a raw material in epoxy resin production, and H is obtained by ion membrane electrolysis2And Cl2Obtaining HCl through reaction, and conveying to a method for producing glycerol from epoxy chlorideA propane plant.
2. The method for producing the ionic membrane caustic soda according to claim 1, wherein in step S1, the high-salt organic wastewater is generated from epichlorohydrin production process, and has a sodium chloride content of 5-20% by weight and a TOC of 1000-10000 mg/L value of 8-12.
3. The method for producing ionic membrane caustic soda according to claim 1, wherein the pretreatment is to remove water-insoluble substances in the high-salt wastewater by microfiltration in step S1.
4. The method for producing ionic membrane caustic soda according to claim 2, wherein in step S1, the advanced oxidation is one or more selected from the group consisting of Fenton oxidation, photocatalytic oxidation, ozone oxidation and catalytic wet oxidation.
5. The method for producing the ionic membrane caustic soda by using the high-salt organic wastewater generated in the epichlorohydrin production process according to claim 4, wherein the Fenton oxidation condition is that the reaction is carried out for 1-4 h at 50-60 ℃ and normal pressure in the presence of a Fenton catalyst and a Fenton oxidant, the dosage of the Fenton catalyst is 5.0-8.0 per mill of the weight of the wastewater, and the dosage of the Fenton oxidant is 5.5-10 times of the TOC concentration in the high-salt organic wastewater.
6. The method for producing the ionic membrane caustic soda according to claim 5, wherein the Fenton catalyst is ferrous chloride or ferric chloride, and the Fenton oxidant is H2O2。
7. The method for producing the ionic membrane caustic soda according to claim 4, wherein the photocatalytic oxidation is carried out at 50-60 ℃ and normal pressure for 1-4H by using the synergistic effect of ultraviolet light and oxidant, and the oxidant is H2O2The dosage of the organic wastewater is 4.5 to 6.5 times of the TOC concentration in the high-salt organic wastewater.
8. The method for producing the ionic membrane caustic soda according to claim 4, wherein the ozone oxidation is performed at 40-60 ℃ and normal pressure by introducing ozone for reaction for 1-2 h, and the amount of the ozone is 3-5 times of the TOC concentration in the high-salt organic wastewater.
9. The method for producing the ionic membrane caustic soda according to claim 4, wherein the conditions of the catalytic wet oxidation are that the reaction is carried out at 220-280 ℃ and 3.0-6.0 MPa for 2-6 h, and the catalyst of the catalytic wet oxidation is one or more of transition metal chlorides of Fe, Cu, Ce, Mo, Mn, Ni and Co.
10. The method for producing the ionic membrane caustic soda according to claim 4, wherein the catalytic wet oxidation is performed in two oxidation towers connected in series, the oxidation towers have two layers of flow plates, brine with TOC of 100-500 mg/L is obtained in the first oxidation tower connected in series, the brine enters the second oxidation tower for deep oxidation, and the dilute brine with TOC of 10-11 mg/L from the ionic membrane electrolyzer also enters the second oxidation tower connected in series, so that clean brine with TOC less than or equal to 7 mg/L is obtained.
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