CN113979576A - Resource treatment method and system for high-salinity mixed salt concentrated water - Google Patents
Resource treatment method and system for high-salinity mixed salt concentrated water Download PDFInfo
- Publication number
- CN113979576A CN113979576A CN202111624174.1A CN202111624174A CN113979576A CN 113979576 A CN113979576 A CN 113979576A CN 202111624174 A CN202111624174 A CN 202111624174A CN 113979576 A CN113979576 A CN 113979576A
- Authority
- CN
- China
- Prior art keywords
- electrodialyzer
- salt
- selective
- bipolar membrane
- flotation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
- C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
Abstract
The invention relates to a resource treatment method of high-salinity mixed salt concentrated water, which comprises the following steps: s1, carrying out electric flocculation flotation treatment on the high salinity miscellaneous salt concentrated water to remove impurities such as silicon-containing compounds, hardness and the like in the miscellaneous salt concentrated water; s2, removing insoluble impurities, and then separating divalent salt by using a selective electrodialyzer to obtain monovalent salt solution in a strong salt chamber and divalent salt solution in a weak salt chamber; and S3, respectively injecting the monovalent salt solution and the divalent salt solution into the salt solution chambers of the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer to carry out bipolar membrane electrodialysis treatment, and respectively obtaining high-purity acid and alkali in the acid solution chamber and the alkali solution chamber of the respective bipolar membrane electrodialyzer, wherein the high-purity acid and alkali can be output as products or used for cleaning an electroflocculation flotation device/an ultrafiltration device. The method effectively solves the problem of discharge pollution of high-salinity mixed salt concentrated water, realizes the recycling treatment of the mixed salt acid-base production, and has the characteristics of high impurity removal and quality separation efficiency, short period, simple flow, low operation cost and green and environment-friendly treatment process.
Description
Technical Field
The invention relates to the technical field of wastewater recycling treatment, in particular to a method and a system for recycling high-salinity mixed salt concentrated water.
Background
A large amount of miscellaneous salt waste water is generated in the industrial production process, and the waste water is comprehensively treated, discharged or recycled according to the environmental protection requirement at present. However, the high salinity miscellaneous salt concentrated water generated after wastewater treatment is difficult to further treat, and if the high salinity miscellaneous salt concentrated water is directly discharged without treatment, the high salinity miscellaneous salt concentrated water not only causes great harm to the natural environment, but also wastes salt resources in waste liquid. The high-salinity mixed salt concentrated water generally contains chloride ions, sulfate ions, calcium and magnesium ions, silicate and the like. Therefore, the high-salinity mixed salt concentrated water treatment technology with high efficiency and energy conservation is developed, the discharge of mixed salt wastewater is reduced, the utilization rate of salt in the mixed salt concentrated water is improved, and the method has important significance for industrial clean production and green low-carbon high-quality development.
At present, most of the high-salinity mixed salt water and the concentrated mixed salt water involved in the industrial wastewater treatment process are treated as waste salt by evaporation, and part of the high-salinity mixed salt water and the concentrated mixed salt water are chemically added and then subjected to resource treatment. The method for removing impurities by adding drugs has the disadvantages of large drug consumption, complex and tedious treatment process, high drug adding amount control difficulty, large influence of residual drugs on subsequent treatment, low equipment treatment efficiency, secondary pollution of water caused by the drugs, and great difficulty in further separation under the condition of high mineralization degree, so that the whole process flow is very long and tedious. In recent years, researches on impurity removal of miscellaneous salt concentrated water and resource treatment of miscellaneous salt solution after impurity removal are more and more, but the removal efficiency of impurities such as hardness and silicon-containing compounds in high-concentration salt solution is low, the medicament consumption is large, the quality separation effect of miscellaneous salts is poor, and the utilization rate of separated salts is low. Therefore, the prior art resource treatment process for the high-salinity mixed salt concentrated water also has the problems of low impurity removal efficiency, poor mixed salt separation effect, high mixed salt treatment cost, high utilization rate of salt resources in the concentrated brine and the like.
Disclosure of Invention
Technical problem to be solved
In view of the defects and shortcomings of the prior art, the invention provides a resource treatment method and system for high-salinity mixed salt concentrated water, which are used for solving the problem of discharge pollution of the mixed salt concentrated water and realizing resource application such as acid and alkali preparation by using mixed salt.
(II) technical scheme
In order to achieve the purpose, the invention adopts the main technical scheme that:
in a first aspect, the invention provides a resource treatment method for high-salinity mixed salt concentrated water, which comprises the following steps:
s1, carrying out electric flocculation flotation treatment on the high salinity miscellaneous salt concentrated water, and removing silicon-containing compounds and hardness-generating impurities in the miscellaneous salt concentrated water to obtain electric flocculation flotation produced water;
s2, removing insoluble impurities in the produced water of the electric flocculation flotation, then separating divalent salt by using a selective electrodialyzer, obtaining divalent salt solution in a weak solution chamber of the selective electrodialyzer, and obtaining monovalent salt solution in a thick solution chamber of the selective electrodialyzer;
and S3, respectively injecting the monovalent salt solution and the divalent salt solution into the salt solution chamber of the first bipolar membrane electrodialyzer and the salt solution chamber of the second bipolar membrane electrodialyzer to carry out bipolar membrane electrodialysis treatment, and respectively obtaining high-purity acid and high-purity alkali in the acid solution chamber and the alkali solution chamber of the bipolar membrane electrodialyzer.
It should be noted that, the concentrate chamber and the dilute chamber are relative terms, one of them is the concentrate chamber, and the other is the dilute chamber, and the concentration and the dilution are not used to limit the concentration of the solution contained therein.
Preferably, in S1, an integrated electrocoagulation-flotation device is used in the electrocoagulation-flotation process, wherein the electrodes are concentric cylindrical electrodes, and the flotation tower is connected with a micro-bubble distributor. The selection of the electric flocculation flotation device can improve the efficiency of electric flocculation reaction and flocculation flotation and realize the purpose of reaction-air flotation synchronization.
Preferably, in S2, the method for removing the insoluble impurities is: the water produced by the electroflocculation flotation is subjected to ultrafiltration treatment, and then the ultrafiltration filtrate is subjected to selective electrodialyzer separation of S2. Preferably, the ultrafiltration is polyvinylidene fluoride ultrafiltration membrane with filtration pore diameter of 10-100 nm.
After the water produced by the electro-flocculation flotation is treated by ultrafiltration, insoluble impurities (including flocculate and the like) contained in the water are intercepted and removed so as to reduce the running pollution and blockage risk of a selective electrodialyzer and ensure the purity of acid and alkali prepared subsequently.
Preferably, in S2, the selective electrodialyzer employs a monovalent ion selective ion exchange membraneThe selective transmittance is 97-99%, and the membrane resistance is 1.5-5.5 Ω · cm2The current density is 100-350A/m2。
The monovalent ion selective ion exchange membrane meeting the parameter requirements can be selected to effectively separate monovalent salt and divalent salt in the mixed salt solution (to obtain purified salt solution); if the selective permeability is too low, the purification quality (purity) of the salt solution can not be ensured, and the operation energy consumption can be increased due to too high membrane resistance; if the selective transmittance is too high or the membrane resistance is too low, the overall investment cost may be increased; if the current density is too low, the separation effect of the mixed salt is poor and the treatment efficiency is low, while if the current density is too high, the selective ion exchange membrane is likely to be damaged.
Preferably, in S3, the selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 97.5 to 99.5%, and the membrane resistance is 10 to 20. omega. cm2The current density is 200-600A/m2。
The bipolar membrane meeting the parameter requirements can be used for efficiently preparing high-purity acid and alkali at low cost, and if the selective transmittance is too low, the treatment efficiency and the acid and alkali purity can be reduced, and the running cost can be increased due to too high membrane resistance; the too large membrane selective permeability or the too small membrane resistance may cause the equipment investment to be increased and the economic benefit to be obviously reduced; too low a current density may result in low acid and base production efficiency or failure to achieve high quality acid and base, while too high a current density may damage the ion exchange membrane or deteriorate the operational stability.
Preferably, in S3, the high-purity acid and alkali obtained from the electrodialysis treatment of the first and second bipolar membranes can be output as products or used for cleaning an electroflocculation flotation device/ultrafiltration device.
In a second aspect, the invention provides a resource treatment system for high salinity mixed salt concentrated water, which comprises: an electrocoagulation flotation device, an ultrafiltration device, a selective electrodialyzer and a first bipolar membrane electrodialyzer and a second bipolar membrane electrodialyzer;
wherein the water production side of the electroflocculation flotation device is connected with the ultrafiltration device, and the filtrate side of the ultrafiltration device is connected with the selective electrodialyzer; the selective electrodialyzer comprises a selective electrodialyzer concentrate chamber and a selective electrodialyzer diluate chamber which are respectively connected with the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer; the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer respectively comprise a salt liquid chamber, an acid liquid chamber and an alkali liquid chamber of the bipolar membrane electrodialyzer; the salt liquid chamber of the first bipolar membrane electrodialyzer is connected with a concentrated liquid chamber of the selective electrodialyzer, the salt liquid chamber of the second bipolar membrane electrodialyzer is connected with a diluted liquid chamber of the selective electrodialyzer, the acid liquid chamber of the first bipolar membrane electrodialyzer outputs high-purity acid, and the alkali liquid chamber outputs high-purity alkali; the second bipolar membrane electrodialyzer acid liquid chamber outputs high-purity acid, and the alkali liquid chamber outputs high-purity alkali.
According to the preferred embodiment of the present invention, the connection is achieved by using pipes or a combination of pumps and pipes.
According to the preferred embodiment of the invention, the electric flocculation flotation device is an electric flocculation flotation integrated device, wherein the electrode adopts a concentric cylindrical electrode, and the flotation tower is connected with a micro-bubble distributor; the ultrafiltration device adopts a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 10-100 nm; the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane, the selective transmittance is 97-99%, and the membrane resistance is 1.5-5.5 omega-cm2The current density is 100-350A/m2(ii) a The selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 97.5-99.5%, and the membrane resistance is 10-20 omega cm2The current density is 200-600A/m2。
(III) advantageous effects
The invention has the beneficial effects that:
according to the invention, the high-salinity mixed salt concentrated water is subjected to impurity removal, salt separation and acid and alkali preparation treatment through electric flocculation flotation, ultrafiltration, selective electrodialysis and bipolar membrane electrodialysis, so that the problems of high impurity removal agent consumption, low impurity removal rate, poor mixed salt concentrated water separation effect, low salt resource utilization rate and the like in the prior art are solved. The method not only achieves the purpose of removing impurity and separating salt from miscellaneous salt, but also can recycle acid and alkali prepared from the purified salt solution, reduce the discharge of waste salt and realize the green treatment and resource application of miscellaneous salt. The resource treatment system for the high-salinity mixed salt concentrated water has the advantages of high treatment efficiency, good quality of prepared acid and alkali, short and simple process flow, high efficiency, short period and low operation cost.
The high-salinity mixed salt concentrated water can be treated by the method to obtain high-purity acid and alkali which can be recycled or used for cleaning an electric flocculation flotation device/ultrafiltration device, and the acid and alkali purity is over 96 percent; the high-efficiency impurity and salt removing and separating and green harmless acid and alkali preparation process greatly reduces the discharge of high-salinity wastewater, obviously improves the utilization rate of salt resources and realizes the resource utilization of high-salinity mixed salt concentrated water. In addition, the whole process of the invention does not relate to the adding use of acid-base reagents/impurity removal reagents and the discharge of salt-containing wastewater, and the process has high environmental protection.
Drawings
FIG. 1 is a schematic flow chart of a resource treatment method of high-salinity mixed salt concentrated water according to an example of the invention.
Detailed Description
For the purpose of better explaining the present invention and to facilitate understanding, the present invention will be described in detail by way of specific embodiments with reference to the accompanying drawings.
The scheme of the invention mainly comprises the steps of removing impurities such as silicon compounds, hardness and the like (such as calcium salt, magnesium salt and the like) contained in high-salinity mixed salt concentrated water by an electrocoagulation floatation method, carrying out ultrafiltration treatment on the obtained electrocoagulation floatation produced water, separating divalent salt from ultrafiltration filtrate by using a selective electrodialyzer, and respectively treating monovalent salt and divalent salt by bipolar membrane electrodialysis to obtain high-purity alkali and acid, thereby effectively improving the impurity removal and separation efficiency and acid-alkali purity of the mixed salt concentrated water.
In order to better understand the above technical solutions, exemplary embodiments of the present invention will be described in more detail below with reference to the accompanying drawings.
As shown in fig. 1, a schematic flow chart of a resource treatment method for high salinity mixed salt concentrated water according to an example of the present invention is shown, and the flow chart specifically includes the following steps:
the method comprises the steps of firstly, carrying out electrocoagulation-flotation treatment on high-salinity mixed salt concentrated water by using an electrocoagulation-flotation integrated device, wherein the electrode is a concentric cylindrical electrode, and a flotation tower is connected with a microbubble distributor so as to remove impurities such as silicon-containing compounds, hardness and the like in the mixed salt concentrated water. And (3) performing ultrafiltration treatment on the produced water by the electrocoagulation-flotation through a polyvinylidene fluoride ultrafiltration membrane with the aperture of 10-100nm to remove insoluble impurities so as to reduce the risk of pollution and blockage in the operation of a selective electrodialyzer and ensure the purity of the acid and the alkali prepared subsequently. Separating divalent salt from the ultrafiltered filtrate with selective electric dialyzer, and transferring monovalent ions (such as sodium ions and chloride ions) from the dilute solution chamber of the selective electric dialyzer to the concentrated solution chamber of the selective electric dialyzer to obtain monovalent salt solution and divalent salt solution. Therefore, the separation of monovalent salt and divalent salt in high-concentration salt solution is realized through the selective electrodialysis treatment. And respectively injecting the separated monovalent salt solution and divalent salt solution into a salt solution chamber of a first bipolar membrane electrodialyzer and a salt solution chamber of a second bipolar membrane electrodialyzer to perform bipolar membrane electrodialysis treatment, correspondingly, respectively obtaining high-purity acid and alkali in an acid solution chamber and an alkali solution chamber of the respective bipolar membrane electrodialyzer, and respectively performing first bipolar membrane electrodialysis treatment on the monovalent salt solution to obtain acid I (acid solution chamber) and alkali I (alkali solution chamber) and performing second bipolar membrane electrodialysis treatment on the divalent salt solution to obtain acid II (acid solution chamber) and alkali II (alkali solution chamber).
Wherein the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane, the selective transmittance is 97-99%, and the membrane resistance is 1.5-5.5 Ω & cm2The current density is 100-350A/m2。
Wherein the bipolar membrane selective permeability of the bipolar membrane electrodialyzer is 97.5-99.5%, and the membrane resistance is 10-20 Ω -cm2The current density is 200-600A/m2。
In the invention, the purities of acid and alkali produced in the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer can reach more than 96 percent; besides, the desalted fresh water is output from the brine chamber of the first and second bipolar membrane electrodialysers.
The features and effects of the present invention will be described below with reference to specific application examples.
Example 1
In this example, the highly mineralized brine concentrated solution contains 72800mg/L of chloride ions, 29300mg/L of sulfate ions, 235mg/L of hardness and 67mg/L of silicon compounds. Wherein, the electrode of the electric flocculation flotation adopts a concentric cylindrical electrode, and the flotation tower is connected with a microbubble distributor; the ultrafiltration is a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 20 nm; the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane with a selective permeability of 98% and a membrane resistance of 2 Ω · cm2The current density is 350A/m2(ii) a The selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 98.5%, and the membrane resistance is 12 Ω · cm2The current density is 450A/m2。
The acid I (hydrochloric acid) obtained by the above treatment has a concentration of 8.4%, a purity of 96.9%, the alkali I (NaOH) has a concentration of 9.8%, a purity of 97.8%, the acid II (sulfuric acid) has a concentration of 3.1%, a purity of 98.7%, the alkali II (NaOH) has a concentration of 3.5%, and a purity of 98.3%.
Example 2
In this example, the highly mineralized brine concentrated solution contains 23600mg/L of chloride ions, 51500mg/L of sulfate ions, 159mg/L of hardness and 83mg/L of silicon compounds. Wherein, the electrode of the electric flocculation flotation adopts a concentric cylindrical electrode, and the flotation tower is connected with a microbubble distributor; the ultrafiltration is performed by a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 100 nm; the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane, the selective permeability of which is 97%, and the membrane resistance of which is 5.5 omega cm2Current density of 200A/m2(ii) a The selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 98.5%, and the membrane resistance is 20 Ω · cm2The current density is 300A/m2. The concentration of the acid I (hydrochloric acid) is 2.6%, the purity is 97.2%, the concentration of the alkali I (NaOH) is 3.2%, the purity is 98%, the concentration of the acid II (sulfuric acid) is 5.6%, the purity is 97.8%, the concentration of the alkali II (NaOH) is 6.3%, and the purity is 98.4%.
Example 3
In this example, the highly mineralized brine concentrated solution contains 50400mg/L of chloride ions, 42300mg/L of sulfate ions, 357mg/L of hardness and 59mg/L of silicon compounds.Wherein, the electrode of the electric flocculation flotation adopts a concentric cylindrical electrode, and the flotation tower is connected with a microbubble distributor; the ultrafiltration is performed by a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 50 nm; the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane, the selective permeability of which is 98.5%, and the membrane resistance of which is 3.5 omega cm2The current density is 300A/m2(ii) a The selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 98%, and the membrane resistance is 17 Ω · cm2The current density is 600A/m2. The acid I (hydrochloric acid) with the concentration of 5.7 percent and the purity of 96.5 percent, the alkali I (NaOH) with the concentration of 6.8 percent and the purity of 97.4 percent, the acid II (sulfuric acid) with the concentration of 5.2 percent and the purity of 99 percent, the alkali II (NaOH) with the concentration of 5.7 percent and the purity of 98.7 percent are obtained by the treatment.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A resource treatment method for high-salinity mixed salt concentrated water is characterized by comprising the following steps:
s1, carrying out electric flocculation flotation treatment on the high salinity miscellaneous salt concentrated water, and removing silicon-containing compounds and hardness-generating impurities in the miscellaneous salt concentrated water to obtain electric flocculation flotation produced water;
s2, removing insoluble impurities in the produced water of the electric flocculation flotation, then separating divalent salt by using a selective electrodialyzer, obtaining divalent salt solution in a weak solution chamber of the selective electrodialyzer, and obtaining monovalent salt solution in a thick solution chamber of the selective electrodialyzer;
and S3, respectively injecting the monovalent salt solution and the divalent salt solution into the salt solution chamber of the first bipolar membrane electrodialyzer and the salt solution chamber of the second bipolar membrane electrodialyzer to carry out bipolar membrane electrodialysis treatment, and respectively obtaining high-purity acid and high-purity alkali in the acid solution chamber and the alkali solution chamber of the bipolar membrane electrodialyzer.
2. The method as claimed in claim 1, wherein in step S1, the electroflocculation flotation process is performed by using an electroflocculation flotation integrated device, wherein the electrodes are concentric cylindrical electrodes, and the flotation tower is connected with a micro bubble distributor.
3. The method for recycling concentrated water containing high salinity and miscellaneous salts according to claim 1, wherein in S2, the method for removing the insoluble impurities comprises: the water produced by the electroflocculation flotation is subjected to ultrafiltration treatment, and then the ultrafiltration filtrate is subjected to selective electrodialyzer separation of S2.
4. The resource treatment method of the high-salinity mixed salt concentrated water according to claim 3, characterized in that the ultrafiltration is a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 10-100 nm.
5. The method according to claim 1, wherein in S2, the selective electrodialyzer employs a monovalent ion selective ion exchange membrane, the permselectivity is 97-99%, and the membrane resistance is 1.5-5.5 Ω -cm2The current density is 100-350A/m2。
6. The method according to claim 1, wherein in S3, the permselectivity of the bipolar membrane in the first and second bipolar membrane electrodialysers is 97.5-99.5%, and the membrane resistance is 10-20 Ω -cm2The current density is 200-600A/m2。
7. The method as claimed in claim 1, wherein in S3, the high-purity acid and alkali obtained from the electrodialysis treatment of the first and second bipolar membranes are used as product for output or reused for cleaning the electroflocculation flotation/ultrafiltration device.
8. A high-salinity mixed salt concentrated water resource treatment system is characterized by comprising: an electrocoagulation flotation device, an ultrafiltration device, a selective electrodialyzer and a first bipolar membrane electrodialyzer and a second bipolar membrane electrodialyzer;
wherein the water production side of the electroflocculation flotation device is connected with the ultrafiltration device, and the filtrate side of the ultrafiltration device is connected with the selective electrodialyzer; the selective electrodialyzer comprises a selective electrodialyzer concentrate chamber and a selective electrodialyzer diluate chamber which are respectively connected with the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer; the first bipolar membrane electrodialyzer and the second bipolar membrane electrodialyzer both comprise a bipolar membrane electrodialyzer salt liquid chamber, an acid liquid chamber and a base liquid chamber; the salt liquid chamber of the first bipolar membrane electrodialyzer is connected with a concentrated liquid chamber of the selective electrodialyzer, the salt liquid chamber of the second bipolar membrane electrodialyzer is connected with a diluted liquid chamber of the selective electrodialyzer, the acid liquid chamber of the first bipolar membrane electrodialyzer outputs high-purity acid, and the alkali liquid chamber outputs high-purity alkali; the second bipolar membrane electrodialyzer acid liquid chamber outputs high-purity acid, and the alkali liquid chamber outputs high-purity alkali.
9. The system for recycling concentrated water containing high salinity and miscellaneous salts according to claim 8, wherein the connection is realized by a pipeline or a combination of a pump and a pipeline.
10. The resource treatment system for the highly mineralized mixed salt concentrated water according to claim 8,
the electric flocculation flotation treatment adopts an electric flocculation flotation integrated device, wherein the electrode adopts a concentric cylindrical electrode, and a flotation tower is connected with a microbubble distributor;
the ultrafiltration is a polyvinylidene fluoride ultrafiltration membrane with the filtration pore diameter of 10-100 nm; the selective electrodialyzer adopts a monovalent ion selective ion exchange membrane, the selective transmittance is 97-99%, and the membrane resistance is 1.5-5.5 omega-cm2Current densityThe degree is 100-350A/m2；
The selective permeability of the bipolar membrane in the first and second bipolar membrane electrodialysers is 97.5-99.5%, and the membrane resistance is 10-20 omega cm2The current density is 200-600A/m2。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111624174.1A CN113979576A (en) | 2021-12-28 | 2021-12-28 | Resource treatment method and system for high-salinity mixed salt concentrated water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111624174.1A CN113979576A (en) | 2021-12-28 | 2021-12-28 | Resource treatment method and system for high-salinity mixed salt concentrated water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113979576A true CN113979576A (en) | 2022-01-28 |
Family
ID=79734679
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111624174.1A Pending CN113979576A (en) | 2021-12-28 | 2021-12-28 | Resource treatment method and system for high-salinity mixed salt concentrated water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113979576A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20160257577A1 (en) * | 2015-03-02 | 2016-09-08 | Harper Biotech Llc D/B/A Simbuka Energy, Llc | Method for treating dense deepwater from lake kivu |
| CN205710215U (en) * | 2016-04-06 | 2016-11-23 | 北京高能时代环境技术股份有限公司 | A kind of strong brine step processing equipment for recycling |
| CN106587446A (en) * | 2016-11-27 | 2017-04-26 | 杭州水处理技术研究开发中心有限公司 | Method for removing chloride from power plant desulfurized wastewater |
| CN111362480A (en) * | 2020-04-03 | 2020-07-03 | 中煤能源研究院有限责任公司 | Method for treating reverse osmosis strong brine |
| CN112624448A (en) * | 2020-12-30 | 2021-04-09 | 杭州蓝然技术股份有限公司 | Method for treating wastewater generated in white carbon black production process by precipitation process |
| CN112960815A (en) * | 2021-02-23 | 2021-06-15 | 中国石油大学(北京) | Recycling treatment method and device for fracturing flowback fluid |
-
2021
- 2021-12-28 CN CN202111624174.1A patent/CN113979576A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20160257577A1 (en) * | 2015-03-02 | 2016-09-08 | Harper Biotech Llc D/B/A Simbuka Energy, Llc | Method for treating dense deepwater from lake kivu |
| CN205710215U (en) * | 2016-04-06 | 2016-11-23 | 北京高能时代环境技术股份有限公司 | A kind of strong brine step processing equipment for recycling |
| CN106587446A (en) * | 2016-11-27 | 2017-04-26 | 杭州水处理技术研究开发中心有限公司 | Method for removing chloride from power plant desulfurized wastewater |
| CN111362480A (en) * | 2020-04-03 | 2020-07-03 | 中煤能源研究院有限责任公司 | Method for treating reverse osmosis strong brine |
| CN112624448A (en) * | 2020-12-30 | 2021-04-09 | 杭州蓝然技术股份有限公司 | Method for treating wastewater generated in white carbon black production process by precipitation process |
| CN112960815A (en) * | 2021-02-23 | 2021-06-15 | 中国石油大学(北京) | Recycling treatment method and device for fracturing flowback fluid |
Non-Patent Citations (3)
| Title |
|---|
| 方映春: "高浓高盐化工废水的资源化综合处理工艺", 《化工设计通讯》 * |
| 曾萍等: "《辽河流域制药废水处理与资源化技术》", 30 November 2019, 中国环境出版集团 * |
| 韩庆生等: "《污水净化电化学技术》", 31 December 1988, 武汉大学出版社 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107640860A (en) | A kind of saliferous industrial wastewater desalination reuse technology of calcic magnesium ion, sulfate ion | |
| WO2021223369A1 (en) | Chemical-free electric method combined treatment process system and method for circulating water of thermal power plant | |
| US20180327287A1 (en) | System for regenerating sodium hydroxide and sulfuric acid from waste water stream containing sodium and sulfate ions | |
| WO2022143014A1 (en) | Resourceful treatment system and method for sodium nitrate wastewater | |
| JP4478996B2 (en) | Treatment method of polarizing plate manufacturing waste liquid | |
| WO2011044782A1 (en) | Super advanced sewage treatment method and device | |
| CN112794292B (en) | Method and system for purifying and recycling waste sulfuric acid | |
| CN111675394A (en) | High-salt industrial wastewater resource recovery treatment system and method | |
| CN109437455A (en) | The processing equipment and method of secondary clarifier effluent Treated sewage reusing | |
| WO2019033936A1 (en) | Device for use in water treatment and material separation and separation method therefor | |
| CN209890428U (en) | Harmless treatment system for printing and dyeing high-concentration wastewater | |
| CN113979576A (en) | Resource treatment method and system for high-salinity mixed salt concentrated water | |
| JP2000317457A (en) | Production of pure water | |
| CN111252968A (en) | Method for concentrating copper sulfate by using membrane technology | |
| CN217119879U (en) | Electrodialysis desalination system of purification glufosinate-ammonium | |
| CN115448525A (en) | High-salinity mine water recycling treatment process | |
| CN215102340U (en) | Low-cost resourceful treatment system of coal industry high salt waste water | |
| CN108101273A (en) | A kind of leather industry comprehensive wastewater recycling treatment process system | |
| CN212999369U (en) | Beta-alanine electrodialysis desalination system | |
| CN214528496U (en) | High COD waste water zero release's of high salt processing apparatus | |
| CN210122533U (en) | Processing system who contains salt waste water | |
| CN114133087A (en) | Resourceful treatment process for high-salinity wastewater | |
| CN206970371U (en) | A kind of casing processes sewage-treatment plant | |
| CN109896685B (en) | Printing and dyeing high-concentration wastewater harmless treatment system and method | |
| Zeng et al. | Study on Treatment of Preserved Wastewater by Combined Ultrafiltration-Nanofiltration |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20220128 |
|
| RJ01 | Rejection of invention patent application after publication |