CN112811442A - Process and system for refining salt by using high-salinity wastewater - Google Patents
Process and system for refining salt by using high-salinity wastewater Download PDFInfo
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- CN112811442A CN112811442A CN202011519484.2A CN202011519484A CN112811442A CN 112811442 A CN112811442 A CN 112811442A CN 202011519484 A CN202011519484 A CN 202011519484A CN 112811442 A CN112811442 A CN 112811442A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 34
- 150000003839 salts Chemical class 0.000 title claims abstract description 34
- 238000007670 refining Methods 0.000 title claims abstract description 18
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 51
- 238000001728 nano-filtration Methods 0.000 claims abstract description 27
- 239000011780 sodium chloride Substances 0.000 claims abstract description 26
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 26
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 25
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 25
- 238000002425 crystallisation Methods 0.000 claims abstract description 24
- 230000008025 crystallization Effects 0.000 claims abstract description 24
- 239000012528 membrane Substances 0.000 claims abstract description 18
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 11
- 150000002500 ions Chemical class 0.000 claims abstract description 10
- 238000004094 preconcentration Methods 0.000 claims abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000005516 engineering process Methods 0.000 claims abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- 238000001179 sorption measurement Methods 0.000 claims description 8
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 5
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000292 calcium oxide Substances 0.000 claims description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 5
- 239000011734 sodium Substances 0.000 claims description 5
- 229910052708 sodium Inorganic materials 0.000 claims description 5
- 238000006065 biodegradation reaction Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 4
- 238000000262 chemical ionisation mass spectrometry Methods 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 239000004902 Softening Agent Substances 0.000 claims description 2
- 239000008395 clarifying agent Substances 0.000 claims description 2
- 238000005352 clarification Methods 0.000 abstract description 13
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000005262 decarbonization Methods 0.000 abstract description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 5
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000000909 electrodialysis Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002957 persistent organic pollutant Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- -1 suspended matters Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
- C01D3/06—Preparation by working up brines; seawater or spent lyes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- 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
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/041—Treatment of water, waste water, or sewage by heating by distillation or evaporation by means of vapour compression
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- 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
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- 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
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/02—Softening water by precipitation of the hardness
- C02F5/06—Softening water by precipitation of the hardness using calcium compounds
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to the technical field of wastewater treatment, and particularly relates to a process and a system for refining salt by using high-salinity wastewater. The process comprises the following steps: the method comprises the steps of pretreating high-salinity wastewater, pre-concentrating the pretreated wastewater by an MVR mechanical vapor recompression technology, concentrating the wastewater by an ED ion membrane after pre-concentration, separating sodium chloride and sodium sulfate by a two-stage nanofiltration system, and respectively preparing the sodium chloride and the sodium sulfate by cooling crystallization. The system comprises a softening clarification tank, an ozone biochar filter tank, a decarbonization tower, an MVR evaporator, an ED concentration device and two-stage nanofiltration equipment which are sequentially connected, wherein the two-stage nanofiltration equipment is connected with a sodium chloride crystallizer and a sodium sulfate crystallizer. On the basis of reducing production energy consumption, the method greatly improves the recovery rate and purity of the product salt, and realizes resource utilization of high-salinity wastewater.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a process and a system for refining salt by using high-salinity wastewater.
Background
The high-salt wastewater refers to wastewater with the total salt mass fraction of more than 1%, mainly comes from industrial production processes of papermaking, printing and dyeing, chemical industry, petroleum and natural gas collection and processing and the like, is wide in production path, and the water quantity is increased year by year. The organic matters in the high-salt wastewater have great differences in the types and chemical properties of the organic matters according to different production processes, but most of the salt substances are Cl-、SO4 2-、Na+、Ca2+And the like, the removal of organic pollutants in the high-salt wastewater is of great importance to reduce the influence of the organic pollutants on the environment.
The technologies commonly used for treating high-salinity wastewater at present are incineration, electrodialysis, membrane separation, biological treatment and evaporative concentration-cooling crystallization. The burning method has high energy consumption, limited treatment effect and high operation cost; the electrodialysis method and the membrane separation method have complex processes and expensive equipment, scale formation is easy to occur, the water production efficiency of the membrane and evaporation is reduced if the equipment is expensive, the membrane, a pipeline or a device is blocked if the equipment is heavy, and the maintenance cost is high; the biological treatment method is easy to damage because of the large culture period of the biological strains, and also causes higher maintenance cost; the traditional evaporation concentration-cooling crystallization treatment method has the advantages of low product purity, relatively low yield and long required time.
Disclosure of Invention
Aiming at the problems of high energy consumption, easy scaling and relatively low salt yield and purity in the existing high-salt wastewater treatment technology, the invention provides a process for refining salt by using high-salt wastewater, and the recovery rate and purity of product salt are greatly improved on the basis of reducing production energy consumption.
The invention provides a process for refining salt by using high-salinity wastewater, which comprises the following steps: the method comprises the steps of pretreating high-salinity wastewater, pre-concentrating the pretreated wastewater by an MVR mechanical vapor recompression technology, concentrating the wastewater by an ED ion membrane after pre-concentration, separating sodium chloride and sodium sulfate by a two-stage nanofiltration system, and respectively preparing the sodium chloride and the sodium sulfate by cooling crystallization.
Further, the pretreatment step is as follows: sequentially carrying out softening clarification, ozone catalytic oxidation, biodegradation and adsorption, activated carbon adsorption and decarburization treatment on the high-salinity wastewater to remove impurities such as suspended matters, colloids and Mg in the wastewater2+And Ca2+Plasma reduces the hardness and the alkalinity of waste water, improves the biodegradability of waste water, prevents scaling during subsequent concentration, and satisfies the requirement of intaking of subsequent concentration.
Further, the softening and clarifying agents used include: calcium oxide and sodium metaaluminate in a weight ratio of 1: 1. Mg in wastewater2+、Ca2+Can be reacted with Cl-Producing a chemical reaction to produce Ca4Al2Cl2(OH)12Is a layered precipitate which can be removed by filtration, and Mg is present in a weight ratio of calcium oxide to sodium metaaluminate of 1:12+And Ca2+The removal rate of (2) is highest.
Furthermore, the pH value of softening and clarifying is 8-9.5, the temperature of softening and clarifying is 20-40 ℃, and the time of softening and clarifying is 0.5-1.5 h. Under certain alkaline condition, Mg in the wastewater can be led to2+、Ca2+With Cl-The chemical reaction is carried out more fully, and the limited temperature and time are the optimal temperature and time for leading the reaction to be more fully on the basis of the lowest energy consumption.
Further, the temperature of the pre-concentration is 500-550 ℃, and the pressure is 9.5-10.5 MPa.
Furthermore, the nanofiltration membrane adopted by the double-stage nanofiltration system is a monovalent ion selective membrane ACS-CIMS.
Further, the crystallization temperature of the sodium chloride is 10-18 ℃, and the crystallization time is 1.2-2.0 h; the crystallization temperature of the sodium sulfate is 14-22 ℃, and the crystallization time is 1.5-2.2 h.
The system used in the process for refining salt by using high-salinity wastewater comprises a softening and clarifying tank, an ozone biochar filter, a decarbonizing tower, an MVR evaporator, an ED concentration device and two-stage nanofiltration equipment which are sequentially connected, wherein the two-stage nanofiltration equipment is connected with a sodium chloride crystallizer and a sodium sulfate crystallizer.
The invention has the beneficial effects that:
according to the process for refining salt by using high-salinity wastewater, the MVR mechanical vapor recompression technology is adopted to prevent blockage caused by scaling in the concentration process, secondary vapor can be used for heating, external energy consumption is reduced, and concentration by combining an ED ion membrane enables the concentration process to be more accurate and sufficient on the basis of lowest energy consumption; the double-stage nanofiltration system is adopted to ensure that the purity of the separated salt is higher, and the pressure drop between two stages causes the booster pump between the two stages to basically not work, so the specific energy consumption of the separated salt is the lowest, and the double-stage nanofiltration system is more energy-saving than the single-stage nanofiltration system. According to the invention, through setting reasonable pretreatment, concentration, salt separation and crystallization steps and selecting optimal process parameters, the recovery rate and purity of the product salt are greatly improved on the basis of reducing production energy consumption, the purity can reach the standard of industrial salt, and the resource utilization of high-salinity wastewater is realized.
Drawings
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present invention, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a schematic diagram of a system for refining salt using high-salinity wastewater according to an embodiment of the present invention.
In the figure, 1-softening clarification tank, 2-ozone biochar filter tank, 3-decarbonization tower, 4-MVR evaporator, 5-ED concentration device, 6-double stage nanofiltration equipment, 7-sodium chloride crystallizer and 8-sodium sulfate crystallizer.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the drawings in the embodiment of the present invention, and it is obvious that the described embodiment is only a part of the embodiment 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 given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The embodiment of the invention provides a process for refining salt by using high-salinity wastewater, and as shown in figure 1, the system adopted by the process comprises a softening and clarifying tank 1, an ozone biochar filter 2, a decarbonizing tower 3, an MVR evaporator 4, an ED concentration device 5 and a two-stage nanofiltration equipment 6 which are sequentially connected, wherein the two-stage nanofiltration equipment 6 is connected with a sodium chloride crystallizer 7 and a sodium sulfate crystallizer 8.
The process specifically comprises the following steps:
(1) pretreatment: the high-salinity wastewater firstly enters a softening clarification tank 1 for softening clarification, the pH value of the softening clarification is controlled to be 8, softening clarification reagents are calcium oxide and sodium metaaluminate in a weight ratio of 1:1, the wastewater after softening clarification enters an ozone biochar filter tank 2 for catalytic oxidation, biodegradation and adsorption and activated carbon adsorption of ozone, and then enters a decarbonization tower 3 for decarbonization treatment.
(2) Concentration: the pretreated wastewater firstly enters an MVR evaporator 4 for preconcentration, the preconcentration temperature is 500 ℃, the pressure is 9.5MPa, and the wastewater enters an ED concentration device 5 for ED ion membrane concentration after the preconcentration is finished.
(3) Salt separation: after concentration, the mixture enters a double-stage nanofiltration device 6 to separate sodium chloride from sodium sulfate, and a nanofiltration membrane adopted by a double-stage nanofiltration system is a monovalent ion selective membrane ACS-CIMS.
(4) And (3) crystallization: after salt separation is finished, sodium chloride and sodium sulfate are respectively prepared through a sodium chloride crystallizer 7 and a sodium sulfate crystallizer 8, the crystallization temperature of the sodium chloride crystallizer 7 is 10 ℃, the crystallization time is 2.0 hours, the crystallization temperature of the sodium sulfate crystallizer 8 is 14 ℃, and the crystallization time is 2.2 hours.
The recovery rate of the sodium chloride and the sodium sulfate prepared by the embodiment is more than 80%, and the purity of the sodium chloride and the purity of the sodium sulfate can reach more than 99%, so that the national standard of industrial salt is met.
Example 2
The embodiment of the invention provides a process for refining salt by using high-salinity wastewater, and as shown in figure 1, the system adopted by the process comprises a softening and clarifying tank 1, an ozone biochar filter 2, a decarbonizing tower 3, an MVR evaporator 4, an ED concentration device 5 and a two-stage nanofiltration equipment 6 which are sequentially connected, wherein the two-stage nanofiltration equipment 6 is connected with a sodium chloride crystallizer 7 and a sodium sulfate crystallizer 8.
The process specifically comprises the following steps:
(1) pretreatment: the high-salinity wastewater firstly enters a softening clarification tank 1 for softening clarification, the pH value of the softening clarification is controlled at 9.5, softening clarification reagents are calcium oxide and sodium metaaluminate in a weight ratio of 1:1, the wastewater after softening clarification enters an ozone biochar filter tank 2 for catalytic oxidation, biodegradation and adsorption and activated carbon adsorption of ozone, and then enters a decarbonization tower 3 for decarbonization treatment.
(2) Concentration: the pretreated wastewater firstly enters an MVR evaporator 4 for preconcentration at the temperature of 550 ℃ and under the pressure of 10.5MPa, and then enters an ED concentration device 5 for ED ion membrane concentration after the preconcentration is finished.
(3) Salt separation: after concentration, the mixture enters a double-stage nanofiltration device 6 to separate sodium chloride from sodium sulfate, and a nanofiltration membrane adopted by a double-stage nanofiltration system is a monovalent ion selective membrane ACS-CIMS.
(4) And (3) crystallization: after salt separation is finished, sodium chloride and sodium sulfate are respectively prepared through a sodium chloride crystallizer 7 and a sodium sulfate crystallizer 8, the crystallization temperature of the sodium chloride crystallizer 7 is 18 ℃, the crystallization time is 1.2 hours, the crystallization temperature of the sodium sulfate crystallizer 8 is 22 ℃, and the crystallization time is 1.5 hours.
The recovery rate of the sodium chloride and the sodium sulfate prepared by the embodiment is more than 80%, and the purity of the sodium chloride and the purity of the sodium sulfate can reach more than 99%, so that the national standard of industrial salt is met.
Although the present invention has been described in detail by referring to the drawings in connection with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (8)
1. A process for refining salt by using high-salinity wastewater is characterized by comprising the following steps: the method comprises the steps of pretreating high-salinity wastewater, pre-concentrating the pretreated wastewater by an MVR mechanical vapor recompression technology, concentrating the wastewater by an ED ion membrane after pre-concentration, separating sodium chloride and sodium sulfate by a two-stage nanofiltration system, and respectively preparing the sodium chloride and the sodium sulfate by cooling crystallization.
2. The process for refining salt by using high-salinity wastewater as claimed in claim 1, wherein the pretreatment step comprises: softening and clarifying the high-salinity wastewater, performing ozone catalytic oxidation, performing biodegradation and adsorption, performing activated carbon adsorption and decarbonizing treatment in sequence.
3. The process for refining salt by using high-salinity wastewater as claimed in claim 2, wherein the softening and clarifying agents used comprise: calcium oxide and sodium metaaluminate in a weight ratio of 1: 1.
4. The process for refining salt by using high-salinity wastewater as claimed in claim 3, wherein the pH value of softening and clarifying is 8-9.5, the temperature of softening and clarifying is 20-40 ℃, and the time of softening and clarifying is 0.5-1.5 h.
5. The process for refining salt by using high-salinity wastewater as claimed in claim 1, wherein the temperature of the pre-concentration is 500-550 ℃, and the pressure is 9.5-10.5 MPa.
6. The process for refining the salt by using the high-salinity wastewater as claimed in claim 1, wherein the nanofiltration membrane adopted by the double-stage nanofiltration system is a monovalent ion selective membrane ACS-CIMS.
7. The process for refining salt by using high-salinity wastewater as claimed in claim 1, wherein the crystallization temperature of the sodium chloride is 10-18 ℃, and the crystallization time is 1.2-2.0 h; the crystallization temperature of the sodium sulfate is 14-22 ℃, and the crystallization time is 1.5-2.2 h.
8. The system of any one of claims 1 to 7, comprising a softening and clarifying tank, an ozone biochar filter, a decarbonizing tower, an MVR evaporator, an ED concentration device and a two-stage nanofiltration device which are connected in sequence, wherein the two-stage nanofiltration device is connected with a sodium chloride crystallizer and a sodium sulfate crystallizer.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113582371A (en) * | 2021-06-09 | 2021-11-02 | 北京清新环境技术股份有限公司 | Membrane concentration treatment method for high-salinity wastewater |
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