CN221836869U - A treatment system for purifying highly concentrated brine by coupling hot and cold methods - Google Patents

Abstract

The utility model discloses a treatment system for purifying high-concentration brine by coupling a cold method and a hot method, which comprises a pretreatment unit, a mixed salt evaporation crystallization unit and a freezing crystallization unit; the water outlet of the V-shaped filter chamber of the pretreatment unit is communicated with the inlet of a mixed salt evaporation crystallizer of the mixed salt evaporation crystallization unit through a pipeline, and the crystallization salt outlet of a mixed salt centrifuge of the mixed salt evaporation crystallization unit is communicated with the inlet of a mixed salt dissolution tank of the freezing crystallization unit. The advantages are that: according to the utility model, after simple pretreatment, salt separation is directly carried out by adopting a mode of combining evaporation and freezing, and the pollutant which has great influence on evaporation crystallization, namely sodium nitrate and organic matters, are centrifuged by a mixed salt centrifuge and are discharged from an evaporation mother liquor as dangerous waste mixed salt, so that the high requirement on wastewater pretreatment during the traditional nanofiltration membrane salt separation is avoided, and a great amount of organic matters and pollutants are enriched on the nanofiltration concentrate side after membrane separation is also avoided.

Description

A treatment system for purifying highly concentrated brine by coupling hot and cold methods

Technical field:

The utility model relates to a high-concentration brine processing system, in particular to a processing system for purifying high-concentration brine by coupling a cold and hot method.

Background technology:

Evaporation ponds, also known as drying ponds, use natural effects (sunlight, wind, etc.) to evaporate the high-concentration salt water remaining after the factory's wastewater treatment, and ultimately achieve zero wastewater discharge in areas such as the west that lack polluted water bodies. An ideal evaporation pond is one where industrial wastewater undergoes biochemical treatment, "recycled water" is returned to the industrial system for use, and then the brine is concentrated to form a high-concentration salt water containing extremely trace organic matter, which is discharged into the evaporation pond for drying and evaporation. However, in actual use, many industrial and mining enterprises discharge not treated high-concentration salt water into evaporation ponds, but untreated industrial wastewater and a large amount of accidental sewage, resulting in poor water quality and complex composition of evaporation pond wastewater. It is mainly manifested in high salt content, high concentration of organic matter, high concentration of hardness and alkalinity and other easy-to-scale and volatile substances, and high concentration of nitrates and other substances. In addition, due to factors such as weather and water quality, natural evaporation is limited, resulting in no economically feasible treatment technology for evaporation pond wastewater.

Since the salt content of wastewater is as high as 70000mg/L~250000mg/L and has great volatility, the current process mainly evaporates the wastewater from the evaporation pond directly to obtain impure salts and condensed water to achieve zero discharge of wastewater. However, this process produces a large amount of solid impurity salts, and due to the complex composition of the water quality in the evaporation pond, the evaporation is not complete, and a large amount of evaporation residual liquid remains. At present, the solid impurity salts and evaporation residual liquid produced by evaporation are managed and disposed of as hazardous waste. At the same time, due to the high concentration of organic matter in the wastewater, the evaporated condensed water often cannot be used as recycled water, resulting in a waste of water resources.

The existing technologies all use nanofiltration membranes to perform preliminary separation of sodium chloride and sodium sulfate. Since the retention rate of chloride ions by nanofiltration membranes is 5%-10% and the retention rate of sulfate ions is 98%, the water production side after nanofiltration salt separation is almost entirely sodium chloride, and the concentrated water side of nanofiltration contains both sodium chloride and sodium sulfate. Then, evaporation and crystallization are used on the water production side of nanofiltration, and evaporation or freezing crystallization is used on the concentrated water side of nanofiltration to achieve a good salt separation effect.

Utility model content:

In order to solve the above problems, the purpose of the utility model is to provide a processing system for purifying highly concentrated brine by coupling cold and hot methods.

The utility model is implemented by the following technical solutions:

A treatment system for purifying highly concentrated brine by coupling cold and hot methods, comprising a pretreatment unit, a mixed salt evaporation crystallization unit and a freezing crystallization unit;

The water outlet of the V-shaped filter tank of the pretreatment unit is connected to the inlet of the mixed salt evaporation crystallizer of the mixed salt evaporation crystallization unit through a pipeline, and the crystallized salt outlet of the mixed salt centrifuge of the mixed salt evaporation crystallization unit is connected to the inlet of the mixed salt dissolution tank of the freezing crystallization unit.

Furthermore, the pretreatment unit includes a regulating tank, a high-density sedimentation tank, a V-type filter tank and a reagent storage tank;

The water outlet of the regulating tank is connected to the water inlet of the high-density sedimentation tank through a pipeline, and the supernatant outlet of the high-density sedimentation tank is connected to the water inlet of the V-type filter through a pipeline; the drug outlet of the drug storage tank is connected to the water inlet of the high-density sedimentation tank through a pipeline.

Furthermore, the pretreatment unit also includes a sludge storage tank and a plate and frame filter press, the sludge outlet of the high-density sedimentation tank is connected to the inlet of the sludge storage tank, the outlet of the sludge storage tank is connected to the inlet of the plate and frame filter press, and the filtrate outlet of the plate and frame filter press is connected to the inlet of the regulating tank through a pipeline.

Further, the mixed salt evaporation crystallization unit includes a mixed salt evaporation crystallizer, a mixed salt centrifuge, a mixed salt mother liquor tank, a mixed salt evaporation crystallizer, a mixed salt centrifuge and a wet mixed salt storage tank;

The slurry outlet of the mixed salt evaporation crystallizer is connected to the inlet of the mixed salt centrifuge through a pipeline, the mother liquor outlet of the mixed salt centrifuge is connected to the inlet of the mixed salt mother liquor tank through a pipeline, the outlet of the mixed salt mother liquor tank is connected to the inlet of the mixed salt evaporation crystallizer through a pipeline, the slurry outlet of the mixed salt evaporation crystallizer is connected to the inlet of the mixed salt centrifuge through a pipeline, the mother liquor outlet of the mixed salt centrifuge is connected to the inlet of the wet mixed salt storage tank through a pipeline, and the outlet of the wet mixed salt storage tank is connected to the inlet of the mixed salt mother liquor tank through a pipeline.

Furthermore, the outlet of the mixed salt mother liquor tank is also connected to the inlet of the mixed salt evaporation crystallizer through a pipeline.

Further, the freezing crystallization unit includes a mixed salt dissolution tank, a freezing crystallizer, a freezing crystal growing tank, a sodium chloride evaporation crystallizer, a sodium chloride centrifuge, a refrigerated centrifuge, a mirabilite dissolution tank, a sodium sulfate evaporation crystallizer, a sodium sulfate centrifuge and a water source;

The liquid outlet of the mixed salt dissolution tank is connected to the inlet of the freezing crystallizer through a pipeline, the slurry outlet of the freezing crystallizer is connected to the inlet of the freezing crystal growing tank through a pipeline, the supernatant outlet of the freezing crystal growing tank is connected to the inlet of the sodium chloride evaporation crystallizer through a pipeline, and the slurry outlet of the sodium chloride evaporation crystallizer is connected to the inlet of the sodium chloride centrifuge through a pipeline;

The crystal slurry outlet of the frozen crystal growing tank is connected to the inlet of the refrigerated centrifuge through a pipeline, the crystal salt outlet of the refrigerated centrifuge is connected to the inlet of the mirabilite dissolving tank, the outlet of the mirabilite dissolving tank is connected to the inlet of the sodium sulfate evaporation crystallizer through a pipeline, and the crystal slurry outlet of the sodium sulfate evaporation crystallizer is connected to the inlet of the sodium sulfate centrifuge through a pipeline;

The outlet of the water source is divided into two routes, one route is connected to the inlet of the mixed salt dissolution tank through a pipeline, and the other route is connected to the inlet of the mirabilite dissolution tank through a pipeline.

Furthermore, the centrifugal mother liquor outlet of the sodium sulfate centrifuge is connected to the inlet of the sodium sulfate evaporation crystallizer through a pipeline.

Furthermore, the centrifuged mother liquor outlet of the sodium chloride centrifuge is connected to the inlet of the sodium chloride evaporation crystallizer through a pipeline.

Furthermore, the centrifuge outlet of the refrigerated centrifuge is connected to the inlet of the frozen crystal growing tank through a pipeline.

Furthermore, the evaporation residual liquid outlet of the sodium chloride evaporation crystallizer of the freezing crystallization unit is connected to the inlet of the regulating tank of the pretreatment unit through a pipeline.

Advantages of the utility model:

After simple pretreatment, the utility model directly uses a combination of evaporation and freezing to separate salts, and utilizes the process of evaporation and salt mixing to separate pollutants that have a greater impact on evaporation crystallization, namely sodium nitrate and organic matter, which are discharged from the evaporation mother liquor as hazardous waste salts after centrifugation in a salt centrifuge. This not only avoids the high requirements for wastewater pretreatment during traditional nanofiltration membrane salt separation, but also avoids the accumulation of a large amount of organic matter and pollutants on the nanofiltration concentrated water side after membrane separation, which leads to great difficulty in subsequent treatment, low purity of crystallized salt, and avoidance of membrane fouling. It also avoids the high energy consumption and catalyst fouling problems of using advanced oxidation methods to remove organic matter under high salt content conditions.

In the utility model, a variety of centrifugal mother liquor reflux pipelines are designed to fully crystallize the inorganic salt, maximize the resource utilization rate of the crystallized salt, and the overall resource recovery rate of the inorganic salt can reach more than 90%, while improving the purity of the crystallized salt.

Description of the drawings:

In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

FIG1 is a schematic diagram of system connection of this embodiment.

In the figure: pretreatment unit 1, regulating tank 11, high-density sedimentation tank 12, V-type filter tank 13, reagent storage tank 14, sludge storage tank 15, plate and frame filter press 16, mixed salt evaporation crystallization unit 2, mixed salt evaporation crystallizer 21, mixed salt centrifuge 22, mixed salt mother liquor tank 23, miscellaneous salt evaporation crystallizer 24, miscellaneous salt centrifuge 25, wet miscellaneous salt storage tank 26, frozen crystallization unit 3, mixed salt dissolution tank 31, frozen crystallizer 32, frozen crystal growing tank 33, sodium chloride evaporation crystallizer 34, sodium chloride centrifuge 35, frozen centrifuge 36, Glauber's salt dissolution tank 37, sodium sulfate evaporation crystallizer 38, sodium sulfate centrifuge 39, water source 310.

Specific implementation method:

The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

Embodiment 1:

As shown in FIG1 , a treatment system for purifying highly concentrated brine by coupling cold and hot methods comprises a pretreatment unit 1, a mixed salt evaporation crystallization unit 2, and a freezing crystallization unit 3;

The pretreatment unit 1 includes a regulating tank 11, a high-density sedimentation tank 12, a V-type filter tank 13 and a reagent storage tank 14; the pretreatment unit 1 also includes a sludge storage tank 15 and a plate and frame filter press 16; the mixed salt evaporation crystallization unit 2 includes a mixed salt evaporation crystallizer 21, a mixed salt centrifuge 22, a mixed salt mother liquor tank 23, a mixed salt evaporation crystallizer 24, a mixed salt centrifuge 25 and a wet mixed salt storage tank 26; the mixed salt evaporation crystallizer 21 adopts a double-effect countercurrent contact forced heat exchange evaporator; the frozen crystallization unit 3 includes a mixed salt dissolution tank 31, a frozen crystallizer 32, a frozen crystal tank 33, a sodium chloride evaporation crystallizer 34, a sodium chloride centrifuge 35, a frozen centrifuge 36, a mirabilite dissolution tank 37, a sodium sulfate evaporation crystallizer 38, a sodium sulfate centrifuge 39 and a water source 310.

Specifically: the water outlet of the regulating tank 11 is connected to the water inlet of the high-density sedimentation tank 12 through a pipeline, and the supernatant outlet of the high-density sedimentation tank 12 is connected to the water inlet of the V-type filter 13 through a pipeline; the drug outlet of the reagent storage tank 14 is connected to the water inlet of the high-density sedimentation tank 12 through a pipeline. The mud outlet of the high-density sedimentation tank 12 is connected to the inlet of the sludge storage tank 15, and the outlet of the sludge storage tank 15 is connected to the inlet of the plate-frame filter press 16. The filtrate outlet of the plate-frame filter press 16 is connected to the inlet of the regulating tank 11 through a pipeline, and the dehydrated sludge with a water content of 70% produced by the plate-frame filter press 16 is transported out for treatment. The water outlet of the V-type filter 13 is connected to the inlet of the mixed salt evaporation crystallizer 21 through a pipeline, the slurry outlet of the mixed salt evaporation crystallizer 21 is connected to the inlet of the mixed salt centrifuge 22 through a pipeline, the mother liquor outlet of the mixed salt centrifuge 22 is connected to the inlet of the mixed salt mother liquor tank 23 through a pipeline, the outlet of the mixed salt mother liquor tank 23 is connected to the inlet of the mixed salt evaporation crystallizer 24 through a pipeline, the slurry outlet of the mixed salt evaporation crystallizer 24 is connected to the inlet of the mixed salt centrifuge 25 through a pipeline, and the hazardous waste mixed salt discharged from the crystallized salt outlet of the mixed salt centrifuge 25 is centrally processed; the mother liquor outlet of the mixed salt centrifuge 25 is connected to the inlet of the wet mixed salt storage tank 26 through a pipeline, and the outlet of the wet mixed salt storage tank 26 is connected to the inlet of the mixed salt mother liquor tank 23 through a pipeline. The outlet of the mixed salt mother liquor tank 23 is also connected to the inlet of the mixed salt evaporation crystallizer 21 through a pipeline.

The crystallized salt outlet of the mixed salt centrifuge 22 is connected to the inlet of the mixed salt dissolving tank 31. The liquid outlet of the mixed salt dissolving tank 31 is connected to the inlet of the freezing crystallizer 32 through a pipeline, the crystal slurry outlet of the freezing crystallizer 32 is connected to the inlet of the freezing crystal tank 33 through a pipeline, the supernatant outlet of the freezing crystal tank 33 is connected to the inlet of the sodium chloride evaporation crystallizer 34 through a pipeline, the crystal slurry outlet of the sodium chloride evaporation crystallizer 34 is connected to the inlet of the sodium chloride centrifuge 35 through a pipeline, and the sodium chloride discharged from the crystallized salt outlet of the sodium chloride centrifuge 35 is dried to obtain industrial sodium chloride; the centrifuged mother liquor outlet of the sodium chloride centrifuge 35 is connected to the inlet of the sodium chloride evaporation crystallizer 34 through a pipeline. The evaporation residual liquid outlet of the sodium chloride evaporation crystallizer 34 is connected to the inlet of the regulating tank 11 through a pipeline.

The crystal slurry outlet of the frozen crystal growing tank 33 is connected to the inlet of the refrigerated centrifuge 36 through a pipeline, and the centrifuge outlet of the refrigerated centrifuge 36 is connected to the inlet of the frozen crystal growing tank 33 through a pipeline. The crystal salt outlet of the refrigerated centrifuge 36 is connected to the inlet of the mirabilite dissolving tank 37, and the outlet of the mirabilite dissolving tank 37 is connected to the inlet of the sodium sulfate evaporation crystallizer 38 through a pipeline, and the crystal slurry outlet of the sodium sulfate evaporation crystallizer 38 is connected to the inlet of the sodium sulfate centrifuge 39 through a pipeline. The sodium sulfate discharged from the crystal salt outlet of the sodium sulfate centrifuge 39 is dried to obtain industrial sodium sulfate; the centrifuge mother liquor outlet of the sodium sulfate centrifuge 39 is connected to the inlet of the sodium sulfate evaporation crystallizer 38 through a pipeline.

The outlet of the water source 310 is divided into two paths, one of which is connected to the inlet of the mixed salt dissolution tank 31 through a pipeline, and the other is connected to the inlet of the mirabilite dissolution tank 37 through a pipeline.

Working principle:

In this embodiment, a high-density sedimentation tank 12 is provided to firstly react the highly concentrated brine to remove the scaling substances and suspended solids contained therein, and then the calcium, magnesium, silicon, fluorine, carbonate, bicarbonate and other substances in the wastewater are precipitated and removed by chemical dosing. By providing a mixed salt evaporation crystallizer 21, more than 90% of the inorganic salts in the wastewater are precipitated in the form of mixed salts; at this time, the main components of the mixed salts are inorganic salts, including sodium chloride and sodium sulfate. The pollutants that have a greater impact on evaporation and crystallization, sodium nitrate and organic matter, are discharged from the evaporation mother liquor as hazardous waste salts after centrifugation in the mixed salt centrifuge 25, thereby realizing the preliminary separation of inorganic salts in the evaporation pond wastewater. The mixed salt separated by the mixed salt centrifuge 22 enters the mixed salt dissolution tank 31 and is dissolved by adding water to form a saturated mixed salt solution of sodium chloride and sodium sulfate with a salt content mass ratio of 20%, and then passes through the freezing crystallizer 32. The operating temperature of the freezing crystallizer 32 is set to -5°C. According to the ternary phase diagram, sodium sulfate precipitates in the form of decahydrated sodium sulfate crystals at -2°C to -5°C. When the material is transferred to the freezing crystal tank 33, more than 95% of the sodium sulfate precipitates in the form of decahydrated sodium sulfate crystals, and the impurities in the sodium chloride and salt solution remain in the frozen supernatant, thereby achieving the separation of sodium chloride and sodium sulfate.

The frozen supernatant is passed through a sodium chloride evaporation crystallizer 34 and a sodium chloride centrifuge 35 to obtain sodium chloride. The separated sodium sulfate decahydrate enters a sodium sulfate dissolving tank 37 and is dissolved in water to obtain a sodium sulfate solution, which is then passed through a sodium sulfate evaporation crystallizer 38 and a sodium sulfate centrifuge 39 to obtain sodium sulfate.

When the mixed salt of sodium chloride and sodium sulfate is frozen and crystallized, the freezing efficiency can be improved in the presence of high-concentration sodium chloride, which is more conducive to the precipitation of sodium sulfate in the form of mirabilite, ensuring that the sodium sulfate can reach more than 95% after freezing and crystallization and crystal cultivation. The supernatant contains almost only sodium chloride, and the solid contains almost only sodium sulfate. Compared with the traditional nanofiltration salt separation, it not only reduces the use of membranes, but also improves the separation efficiency of sodium chloride and sodium sulfate, achieving multiple goals at one stroke. This embodiment makes full use of the process principle and operation characteristics of frozen crystallization, and makes full use of the greater tolerance of the frozen crystallizer 32 to the feed system, and directly enters the frozen crystallizer 32 after the mixed salt is dissolved by the mixed salt evaporation crystallizer 21. This embodiment can separate salt after simple softening and hardness removal. Compared with the traditional membrane concentration technology that requires a large amount of pretreatment, this embodiment simplifies the process flow, saves investment, and also reduces the equipment failure rate such as membrane fouling.

The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. A treatment system for purifying high-concentration brine by coupling a cold method and a hot method is characterized by comprising a pretreatment unit, a mixed salt evaporation crystallization unit and a freezing crystallization unit;

The water outlet of the V-shaped filter tank of the pretreatment unit is communicated with the inlet of the mixed salt evaporation crystallizer of the mixed salt evaporation crystallization unit through a pipeline, and the crystallization salt outlet of the mixed salt centrifuge of the mixed salt evaporation crystallization unit is communicated with the inlet of the mixed salt dissolution tank of the freezing crystallization unit.

2. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 1, wherein the pretreatment unit comprises an adjusting tank, a high-concentration sedimentation tank, a V-shaped filter tank and a medicament storage tank;

the water outlet of the regulating tank is communicated with the water inlet of the high-density sedimentation tank through a pipeline, and the supernatant outlet of the high-density sedimentation tank is communicated with the water inlet of the V-shaped filter tank through a pipeline; and a medicine outlet of the medicine storage tank is communicated with a water inlet of the high-density sedimentation tank through a pipeline.

3. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 2, wherein the pretreatment unit further comprises a sludge storage tank and a plate-and-frame filter press, a sludge outlet of the high-density sedimentation tank is communicated with an inlet of the sludge storage tank, an outlet of the sludge storage tank is communicated with an inlet of the plate-and-frame filter press, and a filtrate outlet of the plate-and-frame filter press is communicated with an inlet of the regulating tank through a pipeline.

4. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 1, wherein the mixed salt evaporation crystallization unit comprises a mixed salt evaporation crystallizer, a mixed salt centrifuge, a mixed salt mother liquor tank, a mixed salt evaporation crystallizer, a mixed salt centrifuge and a wet mixed salt storage tank;

The crystal slurry outlet of the mixed salt evaporation crystallizer is communicated with the inlet of the mixed salt centrifuge through a pipeline, the mother liquor outlet of the mixed salt centrifuge is communicated with the inlet of the mixed salt mother liquor tank through a pipeline, the outlet of the mixed salt mother liquor tank is communicated with the inlet of the mixed salt evaporation crystallizer through a pipeline, the crystal slurry outlet of the mixed salt evaporation crystallizer is communicated with the inlet of the mixed salt centrifuge through a pipeline, the mother liquor outlet of the mixed salt centrifuge is communicated with the inlet of the wet mixed salt storage tank through a pipeline, and the outlet of the wet mixed salt storage tank is communicated with the inlet of the mixed salt mother liquor tank through a pipeline.

5. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 4, wherein the outlet of the mixed salt mother liquor tank is also communicated with the inlet of the mixed salt evaporation crystallizer through a pipeline.

6. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 1, wherein the freezing and crystallizing unit comprises a mixed salt dissolving tank, a freezing crystallizer, a freezing crystal growing tank, a sodium chloride evaporating crystallizer, a sodium chloride centrifuge, a freezing centrifuge, a mirabilite dissolving tank, a sodium sulfate evaporating crystallizer, a sodium sulfate centrifuge and a water source;

The liquid outlet of the salt mixing dissolving tank is communicated with the inlet of the freezing crystallizer through a pipeline, the crystal slurry outlet of the freezing crystallizer is communicated with the inlet of the freezing crystal growing tank through a pipeline, the supernatant outlet of the freezing crystal growing tank is communicated with the inlet of the sodium chloride evaporating crystallizer through a pipeline, and the crystal slurry outlet of the sodium chloride evaporating crystallizer is communicated with the inlet of the sodium chloride centrifuge through a pipeline;

The crystal slurry outlet of the frozen crystal growing tank is communicated with the inlet of the freezing centrifuge through a pipeline, the crystal salt outlet of the freezing centrifuge is communicated with the inlet of the mirabilite dissolving tank, the outlet of the mirabilite dissolving tank is communicated with the inlet of the sodium sulfate evaporation crystallizer through a pipeline, and the crystal slurry outlet of the sodium sulfate evaporation crystallizer is communicated with the inlet of the sodium sulfate centrifuge through a pipeline;

the outlet of the water source is divided into two paths, one path is communicated with the inlet of the salt mixing dissolving tank through a pipeline, and the other path is communicated with the inlet of the mirabilite dissolving tank through a pipeline.

7. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 6, wherein a centrifugal mother liquor outlet of the sodium sulfate centrifuge is communicated with an inlet of the sodium sulfate evaporation crystallizer through a pipeline.

8. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 6, wherein a centrifugal mother liquor outlet of the sodium chloride centrifuge is communicated with an inlet of the sodium chloride evaporation crystallizer through a pipeline.

9. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 6, wherein a centrifugate outlet of the refrigerated centrifuge is communicated with an inlet of the refrigerated crystal growing tank through a pipeline.

10. The treatment system for purifying high-concentration brine by coupling cold and hot method according to claim 1, wherein an evaporation raffinate outlet of a sodium chloride evaporation crystallizer of the freezing crystallization unit is communicated with an inlet of an adjusting tank of the pretreatment unit through a pipeline.