Energy-saving evaporative crystallization device with cobalt chloride

Abstract

The utility model relates to evaporative crystallization equipment related technical field, especially energy -conserving evaporative crystallization equipment of cobalt chloride, including the raw liquid jar, the right -hand pipeline connection of raw liquid jar has raw liquid pump, the upper end pipeline connection of raw liquid pump has distilled water preheater, the lower end pipeline connection of distilled water preheater has distilled water pump, the upper end pipeline connection of distilled water preheater has incondensable gas preheater, the upper end pipeline connection of incondensable gas preheater has falling film heat exchanger, the right -hand pipeline connection of falling film heat exchanger has falling film separator, this device can evaporative crystallization preparation cobalt chloride hexahydrate by cobalt chloride solution directly, equipment simple structure, small footprint, reduced equipment investment cost, and realized cobalt chloride hexahydrate from cobalt chloride raw liquid's processing to get cobalt chloride hexahydrate product's automatic production process, production efficiency is high, no destruction to the environment, is a kind of energy -conserving, degree of automation high equipment.

Description

Technical Field

[0001] This utility model relates to the technical field of evaporation crystallization equipment, and in particular to an energy-saving evaporation crystallization equipment for cobalt chloride. Background Technology

[0002] Cobalt chloride, a commonly used cobalt salt compound, is widely used in industrial manufacturing, scientific research, and agricultural production due to its unique physicochemical properties. These fields have stringent requirements for product quality and performance, and high-purity cobalt salts are key to meeting these requirements. Currently, the raw materials for cobalt chloride production mainly come from natural ore refining, cobalt smelting by-product recovery and recycling. Most production processes require steps such as evaporation concentration, cooling crystallization, and centrifugal separation to obtain cobalt chloride salts. Multi-effect evaporation concentration and freeze crystallization methods for producing cobalt chloride have become more widely used in enterprises in recent years. Due to the strong corrosiveness and high boiling point of cobalt chloride, multi-effect evaporation generally only uses two-effect evaporation.

[0003] Traditional cobalt energy-saving evaporation crystallization equipment has a complex structure, large footprint, high investment, low automation, low production efficiency, high energy consumption, complex process, and high production cost.

[0004] To address the aforementioned issues, a search revealed a patent with publication number CN120169003A disclosing an integrated MVR evaporation crystallization device. The patent proposes "applying torque to the heat exchange tubes through the gravity of the liquid medium, causing the tubes to rotate and thus disturbing the steam within the evaporation shell. This ensures uniform temperature throughout the evaporation shell, resulting in a uniform evaporation rate of the liquid medium within each heat exchange tube, making the degree of evaporation in each tube more consistent (preventing excessive evaporation and scaling in individual tubes). This guarantees the concentration of the concentrated liquid accumulated at the bottom of the evaporation shell, facilitating uniform crystal precipitation during subsequent crystallization." However, this patent relies on traditional steam heating and does not mention a waste heat recovery system, making it impossible to recycle secondary steam and resulting in low energy efficiency.

[0005] In light of this, in-depth research into the aforementioned issues led to the creation of this case. Utility Model Content

[0006] The purpose of this utility model is to provide an energy-saving cobalt chloride evaporation crystallization device to solve the problems mentioned in the background art, such as the complex structure, large footprint, high investment, low degree of automation, low production efficiency, high energy consumption, complex process, and high production cost of traditional cobalt energy-saving evaporation crystallization devices.

[0007] To achieve the above objectives, this utility model provides the following technical solution: an energy-saving cobalt chloride evaporation crystallization device, comprising a raw liquid tank, a raw liquid pump connected to the right end of the raw liquid tank, a distillation water preheater connected to the upper end of the raw liquid pump, a distillation water pump connected to the lower end of the distillation water preheater, a non-condensable gas preheater connected to the upper end of the distillation water preheater, a falling film heat exchanger connected to the upper end of the non-condensable gas preheater, a falling film separator connected to the right end of the falling film heat exchanger, a falling film transfer pump connected to the lower end of the falling film heat exchanger, a forced circulation heat exchanger connected to the upper end of the falling film transfer pump, a forced circulation pump connected to the lower end of the forced circulation heat exchanger, and an Oslo crystallizer connected to the upper end of the forced circulation pump. The forced circulation pump has a mother liquor pump connected to its right end, which in turn has a mother liquor tank connected to its right end. The Oslo crystallizer has a discharge pump connected to its right end. The mother liquor tank has a horizontal concentrator and filter centrifuge connected to its upper end, which has a hydrocyclone connected to its upper end. The non-condensable gas preheater has a non-condensable gas condenser connected to its lower end. The Oslo crystallizer has a steam compressor connected to its upper end. The Oslo crystallizer has a fine crystal removal pump connected to its right end, which has a fine crystal removal tank connected to its right end. The fine crystal removal tank has an impurity filter press connected to its upper end, which has a filter press feed pump connected to its upper end. The steam compressor has a liquid storage pipeline connected to its right end.

[0008] Preferably, the right end of the distilled water pump is connected to a distilled water tank, and the upper end of the falling film heat exchanger is connected to a falling film circulation pump.

[0009] Preferably, the upper end pipe of the non-condensable gas condenser is connected to a vacuum pump.

[0010] Preferably, the steam compressor is connected to the forced circulation heat exchanger pipeline.

[0011] Preferably, the left end of the liquid storage pipeline is connected to a gas three-way control valve, and the lower end of the liquid storage pipeline is connected to a liquid three-way control valve.

[0012] Preferably, the liquid storage pipeline is connected to the drainage tank pipeline.

[0013] The energy-saving evaporation crystallization process for cobalt chloride comprises the following steps: S1. Preheating of raw solution: The cobalt chloride solution is transported to the raw solution tank and then pumped into the raw solution preheating unit through the raw solution pump. It exchanges heat with distilled water and non-condensable gas in sequence to raise the temperature to the evaporation temperature. S2, Evaporation and Concentration Unit: The preheated cobalt chloride solution enters the falling film heat exchanger for evaporation and concentration. By evaporating the water, a nearly saturated cobalt chloride solution is obtained. S3, Evaporation and Crystallization Unit: The nearly saturated cobalt chloride solution obtained by evaporation and concentration through the falling film heat exchanger enters the forced circulation heat exchanger for heating and pressurization, and then flash-concentrates and crystallizes in the Oslo crystallizer. By evaporating water, cobalt chloride hexahydrate crystals are continuously saturated and precipitated. S4. Vacuum drainage: The secondary steam flashed out in the falling film separator enters the Oslo crystallizer and mixes with the secondary steam flashed out in the Oslo crystallizer. After being heated and pressurized by the compressor, it enters the falling film heat exchanger and the forced circulation heat exchanger as a heat source. The system has a low evaporation temperature. The vacuum drainage tank is designed to be connected to the liquid storage pipeline through a pipeline. The liquid storage pipeline is connected to the compressor inlet and outlet pipelines and the compressor volute through a pipeline. The compressor volute condensate is directly discharged through the automatic control system. S5. Filtration and separation: The solution containing cobalt chloride hexahydrate crystals produced by evaporation and crystallization is sent to the hydrocyclone in the filtration and separation unit, and then enters the horizontal concentration and filtration centrifuge for centrifugal separation to obtain saturated concentrate and cobalt chloride hexahydrate crystals. The saturated concentrate is then sent to the evaporation and concentration system for further evaporation, concentration and crystallization. S6. Fine crystal removal: Fine crystals generated in the Oslo crystallizer accumulate in the upper part of the liquid phase section. This part of the solution containing fine crystals is transported to the fine crystal removal tank by the fine crystal removal pump. By mixing and heating the high-temperature concentrate with the fine crystal solution, the unsaturated high-temperature concentrate dissolves the fine crystals. The dissolved solution is transported to the impurity filter press by the filter press feed pump to further remove impurities in the system. The filtered clear liquid enters the mother liquor tank and returns to the system for continued evaporation and crystallization.

[0014] Preferably, in step S1, the stock solution is preheated to an evaporation temperature of 40°C. Only distilled water and non-condensable gases are used to exchange heat with the stock solution to recover residual heat. No additional steam heat source is required for preheating the stock solution.

[0015] Preferably, the secondary steam obtained in step S2 has a temperature of 40°C and a pressure of 7.4 kPa. After step S2, the secondary steam is further heated and pressurized to 55°C and 15.7 kPa.

[0016] Preferably, the vacuum drainage pressure in step S3 is 7.4 kPa, which is close to vacuum. By automatically controlling the three-way valves of the gas and liquid phases, stable drainage is ensured under near-vacuum conditions.

[0017] Compared with existing technologies, the beneficial effects of this utility model are as follows: This cobalt chloride energy-saving evaporation crystallization equipment includes a preheating unit, an evaporation concentration unit, an evaporation crystallization unit, a vacuum drainage unit, a filtration and separation unit, and a fine crystal removal unit connected in sequence. It also includes a control unit for controlling these units. This device can directly prepare cobalt chloride hexahydrate from cobalt chloride solution through evaporation and crystallization. The equipment has a simple structure, small footprint, and reduced investment costs. It also achieves an automated production process from processing cobalt chloride stock solution to obtaining cobalt chloride hexahydrate product. It boasts high production efficiency, no environmental impact, and is a low-energy-consumption, highly automated device. Cobalt chloride is preheated, evaporated, concentrated, and directly crystallized to obtain the product, which is then filtered and separated. The product quality is high, steam consumption is low, the process is simple, energy consumption is low, and production costs are low. Furthermore, compared with conventional processes, the use of MVR low-temperature evaporation technology reduces energy consumption, making it an energy-saving and environmentally friendly production process. Attached Figure Description

[0018] Figure 1 This is a schematic diagram of the overall appearance and structure of this utility model.

[0019] In the diagram: 1. Raw material tank; 2. Raw material pump; 3. Distilled water preheater; 4. Distilled water pump; 5. Non-condensable gas preheater; 6. Distilled water tank; 7. Falling film circulation pump; 8. Falling film heat exchanger; 9. Falling film separator; 10. Falling film transfer pump; 11. Forced circulation heat exchanger; 12. Forced circulation pump; 13. Oslo crystallizer; 14. Mother liquor pump; 15. Mother liquor tank; 16. Discharge pump; 17. Horizontal concentration and filtration centrifuge; 18. Hydrocyclone; 19. Vacuum pump; 20. Non-condensable gas condenser; 21. Drain tank; 22. Steam compressor; 23. Fine crystal removal pump; 24. Fine crystal removal tank; 25. Impurity filter press; 26. Filter press feed pump; 27. Gas three-way control valve; 28. Accumulated liquid storage pipeline; 29. ​​Liquid three-way control valve. Detailed Implementation

[0020] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0021] Please see Figure 1This utility model provides a technical solution: a cobalt chloride energy-saving evaporation crystallization device, including a raw liquid tank 1, a raw liquid pump 2 connected to the right end of the raw liquid tank 1, a distillation water preheater 3 connected to the upper end of the raw liquid pump 2, a distillation water pump 4 connected to the lower end of the distillation water preheater 3, a non-condensable gas preheater 5 connected to the upper end of the distillation water preheater 3, a falling film heat exchanger 8 connected to the upper end of the non-condensable gas preheater 5, a falling film separator 9 connected to the right end of the falling film heat exchanger 8, a falling film transfer pump 10 connected to the lower end of the falling film transfer pump 8, a forced circulation heat exchanger 11 connected to the upper end of the falling film transfer pump 10, a forced circulation pump 12 connected to the lower end of the forced circulation heat exchanger 11, an Oslo crystallizer 13 connected to the upper end of the forced circulation pump 12, and a forced circulation pump 12 connected to the right end of the forced circulation pump 12. The system is connected to a mother liquor pump 14, with a mother liquor tank 15 connected to the right end of the mother liquor pump 14. A discharge pump 16 is connected to the right end of the Oslo crystallizer 13. A horizontal concentrator / filter centrifuge 17 is connected to the upper end of the mother liquor tank 15. A hydrocyclone 18 is connected to the upper end of the horizontal concentrator / filter centrifuge 17. A non-condensable gas condenser 20 is connected to the lower end of the non-condensable gas preheater 5. A steam compressor 22 is connected to the upper end of the Oslo crystallizer 13. A fine crystal removal pump 23 is connected to the right end of the Oslo crystallizer 13. A fine crystal removal tank 24 is connected to the right end of the fine crystal removal tank 23. An impurity filter press 25 is connected to the upper end of the impurity filter press 25. A filter press feed pump 26 is connected to the upper end of the impurity filter press 25. A liquid storage pipeline 28 is connected to the right end of the steam compressor 22.

[0022] Furthermore, the right end of the distilled water pump 4 is connected to a distilled water tank 6, and the upper end of the falling film heat exchanger 8 is connected to a falling film circulation pump 7. Through the setting of the falling film heat exchanger 8, the preheated cobalt chloride solution can be efficiently evaporated and concentrated, and water can be quickly removed to obtain a near-saturated solution.

[0023] Furthermore, the upper end of the non-condensable gas condenser 20 is connected to a vacuum pump 19. Through the setting of the non-condensable gas condenser 20, the non-condensable gas discharged from the non-condensable gas preheater 5 can be condensed. In conjunction with the vacuum pump 19, the system vacuum environment is maintained to avoid the accumulation of non-condensable gas and hinder heat transfer.

[0024] Furthermore, the steam compressor 22 is connected to the forced circulation heat exchanger 11 via pipeline. Through the setting of the steam compressor 22, the secondary steam generated by the falling film separator 9 and the Oslo crystallizer 13 can be heated and pressurized and then circulated as the heat source for the falling film heat exchanger 8 and the forced circulation heat exchanger 11, thereby realizing the recovery of secondary steam energy.

[0025] Furthermore, the left end of the liquid storage pipeline 28 is connected to a gas three-way control valve 27, and the lower end of the liquid storage pipeline 28 is connected to a liquid three-way control valve 29. By setting the liquid three-way control valve 29, the liquid passage between the liquid storage pipeline 28, the drain tank 21, and the atmosphere can be adjusted in conjunction with the gas three-way control valve 27.

[0026] Furthermore, the liquid storage pipeline 28 is connected to the drain tank 21. Through the installation of the drain tank 21, it can cooperate with the liquid storage pipeline 28 and the automatic control valve group to receive the condensate in the compressor system and discharge it stably under vacuum.

[0027] The energy-saving evaporation crystallization process for cobalt chloride comprises the following steps: S1. Preheating of raw solution: The cobalt chloride solution is transported to the raw solution tank 1 and then pumped into the raw solution preheating unit through the raw solution pump 2. It exchanges heat with distilled water and non-condensable gas in sequence to raise the temperature to the evaporation temperature. S2, Evaporation and Concentration Unit: The preheated cobalt chloride solution enters the falling film heat exchanger 8 for evaporation and concentration. By evaporating the water, a nearly saturated cobalt chloride solution is obtained. S3, Evaporation and Crystallization Unit: The nearly saturated cobalt chloride solution obtained by evaporation and concentration in the falling film heat exchanger 8 enters the forced circulation heat exchanger 11 for heating and pressurization, and then flash-concentrates and crystallizes in the Oslo crystallizer 13. By evaporating water, cobalt chloride hexahydrate crystals are continuously saturated and precipitated. S4. Vacuum drainage: The secondary steam flashed out in the falling film separator 9 enters the Oslo crystallizer 13 and mixes with the secondary steam flashed out in the Oslo crystallizer 13. After being heated and pressurized by the compressor, it enters the falling film heat exchanger 8 and the forced circulation heat exchanger 11 as a heat source. The system has a low evaporation temperature. The vacuum drainage tank 21 is designed to be connected to the liquid storage pipeline 28 through a pipeline. The liquid storage pipeline 28 is connected to the compressor inlet and outlet pipelines and the compressor volute through a pipeline. The compressor volute condensate is directly discharged through the automatic control system. S5. Filtration and separation: The solution containing cobalt chloride hexahydrate crystals produced by evaporation and crystallization is sent to the hydrocyclone in the filtration and separation unit, and then enters the horizontal concentration and filtration centrifuge 17 for centrifugal separation to obtain saturated concentrate and cobalt chloride hexahydrate crystals. The saturated concentrate is then sent to the evaporation and concentration system for further evaporation, concentration and crystallization. S6. Fine crystal removal: The fine crystals generated in the Oslo crystallizer 13 are enriched in the upper part of the liquid phase section. This part of the solution containing fine crystals is transported to the fine crystal removal tank by the fine crystal removal pump 23. By mixing the high-temperature concentrate with the fine crystal solution and heating it, the unsaturated high-temperature concentrate dissolves the fine crystals. The dissolved solution is transported to the impurity filter press 25 by the filter press feed pump 26 to further remove impurities in the system. The filtered clear liquid enters the mother liquor tank 15 and returns to the system to continue evaporation and crystallization.

[0028] Furthermore, in step S1, the raw liquid is preheated to an evaporation temperature of 40°C. Only distilled water and non-condensable gas are used to exchange heat with the raw liquid to recover residual heat. No additional steam heat source is needed for preheating the raw liquid. By setting step S1, energy is efficiently recovered and the feed to the subsequent evaporation and concentration unit is provided with the required temperature, thus reducing system energy consumption.

[0029] Furthermore, the secondary steam obtained in step S2 has a temperature of 40°C and a pressure of 7.4 kPa. After step S2, the secondary steam is further heated and pressurized to 55°C and 15.7 kPa. Through the setting of step S2, the preheated cobalt chloride solution can be heated and evaporated with the secondary steam in the falling film heat exchanger 8. After gas-liquid separation is completed by the falling film separator 9, a nearly saturated concentrate is obtained.

[0030] Furthermore, the vacuum drainage pressure in step S3 is 7.4 kPa, which is close to vacuum. By automatically controlling the three-way valves of the gas and liquid phases, stable drainage is ensured under near-vacuum conditions. Through the setting of step S3, the nearly saturated cobalt chloride solution can be heated and pressurized by the forced circulation heat exchanger 11 and then flash-concentrated and crystallized in the Oslo crystallizer 13.

[0031] Working principle: Cobalt chloride stock solution is stored in stock solution tank 1 and transported to the preheating unit by stock solution pump 2. It first enters the distilled water preheater 3, where it exchanges heat with the 60°C secondary condensate from the forced circulation heat exchanger 11. The residual heat of the condensate is used to initially raise the temperature of the stock solution. Then it enters the non-condensable gas preheater 5, where it exchanges heat with the secondary steam entrained in the system's non-condensable gas, further raising the temperature to the evaporation temperature of 45°C. The entire preheating process relies only on the system's residual heat and does not require additional steam, achieving efficient energy recovery. The preheated 45°C solution enters the lower tube box of the falling film heat exchanger 8 and is transported to the upper distributor by the falling film circulation pump 7. It is evenly distributed into the heat exchange tubes and exchanges heat with the secondary steam in the shell side for evaporation, producing secondary steam and concentrate. The gas-liquid mixture is first initially separated in the lower tube box of the falling film heat exchanger 8 and then completely separated in the falling film separator 9. The concentrate is returned to the heat exchanger for circulation and concentration until the density reaches 1.4 g / cm³. Then it is sent to the crystallization unit by the falling film transfer pump 10. In the unit, the separated secondary steam enters the Oslo crystallizer 13 for further purification to avoid entrained droplets affecting subsequent processes. The concentrated liquid first enters the mother liquor tank 15, where it is mixed with the solution containing fine crystals to dissolve the fine crystals. Then, it is sent by the mother liquor pump 14 to the inlet of the forced circulation pump 12. Driven by the forced circulation pump 12, the solution enters the forced circulation heat exchanger 11 for heating and pressurization, and then enters the Oslo crystallizer 13 for flash concentration. Water is evaporated, making the solution supersaturated, and cobalt chloride hexahydrate crystals continuously precipitate. Particle classification is achieved in the crystal fluidized bed of the crystallizer to ensure uniform product particle size. At the same time, the secondary steam generated by the Oslo crystallizer 13 and the falling film separator 9 is mixed and then enters the steam compressor 22 for heating and pressurization to 60°C and 19.9 kPa. It is circulated as a heat source to the falling film heat exchanger 8 and the forced circulation heat exchanger 11 to achieve secondary steam energy recovery and significantly reduce energy consumption. The system is maintained at 99°C by the vacuum pump 19 and the non-condensable gas condenser 20.A 6 kPa vacuum environment ensures low-temperature evaporation. Condensate in the steam compressor 22 and pipelines is collected via condensate storage pipeline 28. Under the automatic control of the gas three-way control valve 27 and the liquid three-way control valve 29, the drain tank 21 is first connected to the condensate pipeline. The condensate is then discharged into the drain tank using the vacuum pressure difference. After the condensate is emptied, the valves are switched to connect the drain tank to the atmosphere, allowing for spontaneous discharge of the condensate and preventing disruption of the system's vacuum stability during the drainage process. The slurry containing large crystal particles at the bottom of the Oslo crystallizer 13 is transported by the discharge pump 16 to the hydrocyclone 18 for thickening, and then enters the horizontal concentration and filtration centrifuge 17. Under centrifugal force... In the Oslo crystallizer 13, solid crystals are deposited on the drum wall and pushed to the slag discharge port by the conveying screw. The saturated liquid mother liquor overflows into the mother liquor tank 15 and is then returned to the forced circulation system via the mother liquor pump 14 to continue participating in evaporation and crystallization, achieving closed-loop material utilization. Fine crystals enriched in the upper part of the liquid phase are sent to the fine crystal elimination tank 24 by the fine crystal elimination pump 23, where they are mixed with the high-temperature concentrate and heated to dissolve the fine crystals. The dissolved solution is then sent to the impurity filter press 25 by the filter feed pump 26. The filter cloth intercepts impurities, forming a filter cake which is discharged. The purified clear liquid returns to the mother liquor tank 15, thus eliminating fine crystals to ensure product particle size and removing system impurities to improve purity.

[0032] Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the present invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A cobalt chloride energy-saving evaporation crystallization device, comprising a raw liquid tank (1), characterized in that: The raw liquid tank (1) is connected to a raw liquid pump (2) via a pipe at its right end. The raw liquid pump (2) is connected to a distilled water preheater (3) via a pipe at its upper end. The distilled water preheater (3) is connected to a distilled water pump (4) via a pipe at its lower end. The distilled water preheater (3) is connected to a non-condensable gas preheater (5) via a pipe at its upper end. The non-condensable gas preheater (5) is connected to a falling film heat exchanger (8) via a pipe at its right end. The falling film heat exchanger (8) is connected to a falling film separator via a pipe at its right end. 9), the lower end of the falling film heat exchanger (8) is connected to a falling film transfer pump (10), the upper end of the falling film transfer pump (10) is connected to a forced circulation heat exchanger (11), the lower end of the forced circulation heat exchanger (11) is connected to a forced circulation pump (12), the upper end of the forced circulation pump (12) is connected to an Oslo crystallizer (13), the right end of the forced circulation pump (12) is connected to a mother liquor pump (14), the mother liquor pump (14) is connected to a mother liquor pump (15) 4) The right end of the pipeline is connected to the mother liquor tank (15), the right end of the Oslo crystallizer (13) is connected to the discharge pump (16), the upper end of the mother liquor tank (15) is connected to the horizontal concentrator and filter centrifuge (17), the upper end of the horizontal concentrator and filter centrifuge (17) is connected to the hydrocyclone (18), the lower end of the non-condensable gas preheater (5) is connected to the non-condensable gas condenser (20), and the upper end of the Oslo crystallizer (13) is connected to the mother liquor tank (15). There is a steam compressor (22), the right end of the Oslo crystallizer (13) is connected to a fine crystal removal pump (23), the right end of the fine crystal removal pump (23) is connected to a fine crystal removal tank (24), the upper end of the fine crystal removal tank (24) is connected to an impurity filter press (25), the upper end of the impurity filter press (25) is connected to a filter press feed pump (26), and the right end of the steam compressor (22) is connected to a liquid storage pipeline (28).

2. The cobalt chloride energy-saving evaporation crystallization equipment according to claim 1, characterized in that: The right end of the distilled water pump (4) is connected to a distilled water tank (6), and the upper end of the falling film heat exchanger (8) is connected to a falling film circulation pump (7).

3. The cobalt chloride energy-saving evaporation crystallization equipment according to claim 1, characterized in that: The upper end of the non-condensable gas condenser (20) is connected to a vacuum pump (19).

4. The cobalt chloride energy-saving evaporation crystallization equipment according to claim 1, characterized in that: The steam compressor (22) is connected to the forced circulation heat exchanger (11) via pipeline.

5. The cobalt chloride energy-saving evaporation crystallization equipment according to claim 1, characterized in that: The left end of the liquid storage pipeline (28) is connected to a gas three-way control valve (27), and the lower end of the liquid storage pipeline (28) is connected to a liquid three-way control valve (29).

6. The cobalt chloride energy-saving evaporation crystallization equipment according to claim 1, characterized in that: The liquid storage pipeline (28) is connected to the drainage tank (21).

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