Evaporation concentration and crystallization device for cobalt sulfate-containing battery recovery leachate

Abstract

The utility model discloses an evaporation concentration and crystallization device for cobalt sulfate-containing battery recovery leachate, which is characterized in that an outlet of a cobalt sulfate feed liquid pipe is connected with a circulating pipe of a triple-effect falling film evaporation unit through a preheating unit, the triple-effect circulating pipe is connected with a circulating pipe of a first-effect evaporation system, the first-effect circulating pipe is connected with a circulating pipe of a second-effect evaporation system, and the second-effect circulating pipe is connected with a circulating pipe of a third-effect falling film evaporation unit. The double-effect circulating pipe is connected with a feed port of a DTB flash evaporation crystallizer through a double-effect discharge pump, a crystal slurry outlet of the DTB flash evaporation crystallizer is connected with an inlet of a flash evaporation thickening tank through a flash evaporation crystal slurry pump, a bottom outlet of the flash evaporation thickening tank is connected with an inlet of a centrifugal machine, and a solid phase outlet of the centrifugal machine is connected with a cobaltous sulfate discharge pipe; the first-effect secondary steam outlet is connected with a heat source inlet of the second-effect evaporation system, the second-effect secondary steam outlet and the third-effect secondary steam outlet are both connected with an inlet of the steam compressor, and a secondary steam pipe of the compressor is connected with heat source inlets of the first-effect evaporation system and the third-effect falling film evaporation unit. The device can reduce cost and energy consumption and improve economic benefits.

Description

Technical Field

[0001] The utility model relates to an evaporation concentration device, in particular to an evaporation concentration and crystallization device for recovering leaching liquid from a cobalt sulfate battery, belonging to the technical field of cobalt sulfate production equipment. Background Art

[0002] If large quantities of used batteries are not properly handled, the heavy metals they contain, such as lithium, nickel, cobalt, and manganese, will cause serious environmental pollution and represent a significant waste of resources. Therefore, the recycling and resource utilization of used batteries has become crucial. As a crucial component of the recycling process, the concentration and crystallization of cobalt sulfate solution significantly impacts the overall treatment process.

[0003] At present, the process of single-effect evaporation or multiple-effect evaporation is often used. For example, the Chinese utility model patent with the authorization announcement number CN209997230U discloses a cobalt sulfate evaporation crystallization device, comprising a preheater for preheating the material, a heater for heating the material, a separator for vapor-liquid separation of the material, and a crystal separation device for solid-liquid separation of the material. The preheater, the heater, the separator, and the crystal separation device are connected by a pipeline. The liquid inlet of the heater is connected to the liquid outlet of the separator. A compressor is connected between the gas outlet of the separator and the gas inlet of the heater. The gas outlet of the heater is connected to the preheater. This technical solution adopts single-effect evaporation crystallization, i.e., evaporation and concentration of the cobalt sulfate solution is carried out by a shell and tube heat exchanger. As the water content continues to decrease, the solution becomes supersaturated and cobalt sulfate crystals are precipitated. The defect of this technical solution is that the production process is relatively simple, the power source relies on a steam compressor to heat and pressurize the secondary steam, and the physical properties of the cobalt sulfate solution are not taken into account. The process of simply adopting evaporation crystallization is not fully suitable for the cobalt sulfate solution, and the crystallization efficiency is low. Utility Model Content

[0004] The purpose of this section is to summarize some aspects of the embodiments of the present invention and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the abstract and utility model title of this application, and such simplifications or omissions shall not be used to limit the scope of the present invention.

[0005] In view of the above problems and / or the problems existing in the prior art, the present utility model is proposed.

[0006] The purpose of the utility model is to overcome the problems existing in the prior art and provide an evaporation concentration and crystallization device for recovering leachate from batteries containing cobalt sulfate, which can achieve the requirements of efficient evaporation concentration and crystallization of cobalt sulfate while reducing costs and energy consumption, improving economic benefits, and realizing economic, environmental, and sustainable development.

[0007] In order to solve the above technical problems, the utility model provides an evaporation, concentration and crystallization device for recovering leachate from a cobalt sulfate-containing battery, comprising a cobalt sulfate feed liquid pipe, the outlet of the cobalt sulfate feed liquid pipe being connected to a circulation pipe of a triple-effect falling film evaporation unit via a preheating unit, the circulation pipe of the triple-effect falling film evaporation unit being connected to a circulation pipe of a first-effect evaporation system via a triple-effect transfer pipe, the circulation pipe of the first-effect evaporation system being connected to a circulation pipe of a second-effect evaporation system via a first-effect transfer pipe, the circulation pipe of the second-effect evaporation system being connected to an inlet of a second-effect discharge pump via a second-effect evaporation discharge pipe, the outlet of the second-effect discharge pump being connected to a feed port of a DTB flash crystallizer, the slurry outlet of the DTB flash crystallizer being connected to an inlet of a flash thickening tank via a flash slurry pump, the bottom outlet of the flash thickening tank being connected to an inlet of a centrifuge, and the solid phase outlet of the centrifuge being connected to a cobalt sulfate discharge pipe;

[0008] The secondary steam outlet of the first-effect evaporation system is connected to the heat source inlet of the second-effect evaporation system through a first-effect secondary steam pipe, the secondary steam outlet of the second-effect evaporation system is connected to a second-effect secondary steam pipe, the secondary steam outlet of the three-effect falling film evaporation unit is connected to a three-effect secondary steam pipe, the outlets of the second-effect secondary steam pipe and the three-effect secondary steam pipe are connected to the inlet of a steam compressor, and the outlet of the steam compressor is connected to the heat source inlets of the first-effect evaporation system and the three-effect falling film evaporation unit through a compressor secondary gas pipe.

[0009] As an improvement of the present invention, the preheating unit includes a condensate preheater and a non-condensable gas preheater, the outlet of the cobalt sulfate liquid pipe is connected to the cold side inlet of the condensate preheater, the cold side outlet of the condensate preheater is connected to the cold side inlet of the non-condensable gas preheater, and the cold side outlet of the non-condensable gas preheater is connected to the circulation pipe of the three-effect falling film evaporation unit.

[0010] As a further improvement of the present invention, the non-condensable gas outlets of the first-effect evaporation system, the second-effect evaporation system and the third-effect falling film evaporation unit are all connected to the non-condensable gas discharge pipe, the outlet of the non-condensable gas discharge pipe is connected to the hot side inlet of the non-condensable gas preheater, the hot side outlet of the non-condensable gas preheater is connected to the hot side inlet of the surface condenser, and the hot side outlet of the surface condenser is connected to the atmosphere through a vacuum pump.

[0011] As a further improvement of the present invention, the condensed water outlets of the first-effect evaporation system, the second-effect evaporation system and the third-effect falling film evaporation unit are respectively connected to the inlet of the condensed water tank, the outlet of the condensed water tank is connected to the hot side inlet of the condensed water preheater through a condensed water pump, and the hot side outlet of the condensed water preheater is connected to the condensed water discharge pipe.

[0012] As a further improvement of the present invention, the volute drain port of the steam compressor is connected to the inlet of the liquid accumulation tank, and the outlet of the liquid accumulation tank is connected to the condensed water tank through a liquid accumulation pump.

[0013] As a further improvement of the present utility model, the secondary steam outlet of the DTB flash crystallizer is connected to the inlet of the flash condenser, and the exhaust outlet of the flash condenser is connected to the atmosphere through a vacuum pump.

[0014] Compared with the prior art, the present utility model has achieved the following beneficial effects: 1. It solves the problems of low crystallization efficiency, high energy consumption and incomplete compliance with the characteristics of cobalt sulfate solution in the traditional treatment process, and improves the operation efficiency of the enterprise.

[0015] 2. The cobalt sulfate solution is first preheated in two stages to increase the solution temperature, which can reduce the heat load required for subsequent evaporation. The heat source for the first-stage preheating is the condensed water generated by the condensation of secondary steam in the system; the heat source for the second-stage preheating is the non-condensable gas in the system; while heating the material, the heat of the system is effectively recovered, and the waste heat of the system is utilized to the greatest extent, comprehensively improving the heat utilization rate and reducing the system energy consumption.

[0016] 3. By adopting the steam recompression technology, after the action of the steam compressor, the low-grade secondary steam evaporated by the system is compressed into high-grade steam with high temperature and high pressure, and then used as the heating steam of the evaporator, greatly reducing the steam consumption. Only about 0.1 ton of steam is needed to supplement the heat loss of the system for evaporating one ton of water. Compared with the traditional multi-effect evaporation using live steam, the steam energy consumption is reduced by about 80%, significantly reducing the production operation cost of the enterprise.

[0017] 4. The solubility of cobalt sulfate in water first increases and then decreases with the increase of temperature. In view of this important characteristic of the material, the present system adopts the cross-flow triple-effect evaporation process, and the discharge section is set in the second-effect evaporation of the system, and the second-effect evaporation temperature corresponds to the maximum solubility of cobalt sulfate, so as to ensure that the cobalt sulfate solution is transferred to the subsequent flash evaporation at the highest concentration, increasing the salt output of the flash evaporation system, making the evaporation process conform to the characteristics of cobalt sulfate solution, and improving the crystallization efficiency.

[0018] 5. By adopting the DTB flash crystallization system, the crystallization speed is fast and the quality is good, improving the production efficiency, solving the problem of slow intermittent cooling speed of the cooling kettle, and realizing continuous cooling and continuous feeding and discharging. At the same time, it avoids the problem of scaling on the wall of the cooling kettle and difficult cleaning, improves the continuous and stable operation cycle of the system, and reduces the operation and maintenance costs.

[0019] 6. Due to the above advantages, and adopting the route of combining MVR triple-effect evaporation concentration and flash crystallization, the advantages are obvious, the applicability is high, it realizes improving efficiency, energy saving and consumption reduction, and continuously operates stably and efficiently, meeting the production operation needs of major enterprises in the market, and achieving the goal of economic, environmental and sustainable development of the enterprise. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the following briefly introduces the drawings required for describing the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative work. The drawings are only provided for reference and explanation, and are not intended to limit the present invention. Among them:

[0021] Figure 1 This is a flow chart of the evaporation concentration and crystallization device for recovering leachate from cobalt sulfate batteries in the utility model;

[0022] Figure: 1. Condensate preheater; 2. Non-condensable gas preheater; 3. Three-effect falling film evaporator; 4. Three-effect falling film separator; 5. First-effect evaporator; 6. First-effect separator; 7. Second-effect evaporator; 8. Second-effect separator; 9. Surface condenser; 10. Condensate tank; 11. Steam compressor; 12. Liquid accumulation tank; 13. DTB flash crystallizer; 14. Flash thickening tank; 15. Centrifuge; 16. Flash condenser;

[0023] B1. Three-effect falling film circulation pump; B2. Single-effect circulation pump; B3. Second-effect circulation pump; B4. Second-effect discharge pump; B5. Condensate pump; B6. Vacuum pump 1; B7. Effluent pump; B8. Flash slurry pump; B9. Vacuum pump 2.

[0024] G1. Cobalt sulfate feed liquid pipe; G2. Three-effect transfer pipe; G3. First-effect transfer pipe; G4. Second-effect evaporation discharge pipe; G5. Condensate discharge pipe; G6. Non-condensable gas discharge pipe; G7. First-effect secondary steam pipe; G8. Second-effect secondary steam pipe; G9. Three-effect secondary steam pipe; G10. Compressor secondary gas pipe; G11. Flash condensate collection pipe; G12. Cobalt sulfate discharge pipe. DETAILED DESCRIPTION

[0025] In the following description of the present invention, the terms "upper", "lower", "front", "back", "left", "right", "inside", "outside", etc. indicate directions or positional relationships based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the present invention and simplifying the description, and do not mean that the device must have a specific direction.

[0026] In order to make the technical means, creative features, objectives and effects of the present invention easier to understand, the present invention is further described below with reference to specific figures. Obviously, the embodiments described are only a part of the present invention, not all of the embodiments.

[0027] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the technical field to which this utility model belongs. The terms used herein in the specification of this utility model are for the purpose of describing specific embodiments only and are not intended to limit this utility model.

[0028] As Figure 1 shown, the evaporation concentration and crystallization device for the cobalt sulfate battery recycling leaching solution of this utility model includes a cobalt sulfate feed liquid pipe G1, a first-effect evaporation system, a second-effect evaporation system, a triple-effect falling-film evaporation unit, and a DTB flash crystallizer 13. The first-effect evaporation system includes a first-effect evaporator 5, a first-effect separator 6, and a first-effect circulation pump B2. The second-effect evaporation system includes a second-effect evaporator 7, a second-effect separator 8, and a second-effect circulation pump B3. The triple-effect falling-film evaporation unit includes a triple-effect falling-film evaporator 3, a triple-effect falling-film separator 4, and a triple-effect falling-film circulation pump B1.

[0029] The outlet of the cobalt sulfate feed liquid pipe G1 is connected to the cold-side inlet of the condensate preheater 1. The cold-side outlet of the condensate preheater 1 is connected to the cold-side inlet of the non-condensable gas preheater 2. The cold-side outlet of the non-condensable gas preheater 2 is connected to the triple-effect circulation pipe at the outlet of the triple-effect falling-film circulation pump B1. The outlet of the triple-effect circulation pipe is connected to the top inlet of the triple-effect falling-film evaporator 3. The lower side wall of the triple-effect falling-film evaporator 3 is connected to the triple-effect falling-film separator 4 through a connecting pipe. The bottom outlet of the triple-effect falling-film evaporator 3 is connected to the inlet of the triple-effect falling-film circulation pump B1.

[0030] The triple-effect circulation pipe is also connected to the bottom outlet of the first-effect separator 6 through a triple-effect transfer pipe G2. The bottom outlet pipe of the first-effect separator 6 is connected to the inlet of the first-effect circulation pump B2. The outlet of the first-effect circulation pump B2 is connected to the lower end inlet of the first-effect evaporator 5. The upper end outlet of the first-effect evaporator 5 is connected to the side wall inlet of the first-effect separator 6.

[0031] The bottom outlet pipe of the first-effect separator 6 is also connected to the lower inlet of the second-effect evaporator 7 through a first-effect transfer pipe G3. The upper end outlet of the second-effect evaporator 7 is connected to the side wall inlet of the second-effect separator 8. The bottom outlet of the second-effect separator 8 is connected to the inlet of the second-effect circulation pump B3. The outlet of the second-effect circulation pump B3 is connected to the lower inlet of the second-effect evaporator 7.

[0032] The inlet of the second-effect circulation pump B3 is also connected to the inlet of the second-effect discharge pump B4 through a second-effect evaporation discharge pipe G4. The outlet of the second-effect discharge pump B4 is connected to the feed inlet of the DTB flash crystallizer 13. The crystal slurry outlet of the DTB flash crystallizer 13 is connected to the inlet of the flash crystal slurry pump B8. The outlet of the flash crystal slurry pump B8 is connected to the inlet of the flash thickener 14. The bottom outlet of the flash thickener 14 is connected to the inlet of the centrifuge 15. The solid phase outlet of the centrifuge 15 is connected to the cobalt sulfate discharge pipe G12.

[0033] The secondary steam outlet at the top of the first-effect separator 6 is connected to the upper shell inlet of the second-effect evaporator 7 through the first-effect secondary steam pipe G7, and the lower shell outlet of the second-effect evaporator 7 is connected to the condensed water tank 10 through the second-effect condensed water pipe.

[0034] The secondary steam outlet at the top of the second-effect separator 8 is connected to the second-effect secondary steam pipe G8, and the secondary steam outlet at the top of the third-effect falling film separator 4 is connected to the third-effect secondary steam pipe G9. The outlets of the second-effect secondary steam pipe G8 and the third-effect secondary steam pipe G9 are both connected to the inlet of the steam compressor 11. The outlet of the steam compressor 11 is connected to the compressor secondary gas pipe G10. The outlet of the compressor secondary gas pipe G10 is respectively connected to the upper shell inlet of the first-effect evaporator 5 and the upper shell inlet of the third-effect falling film evaporator 3.

[0035] The lower shell-side outlet of the first-effect evaporator 5 is connected to the condensate tank 10 via a first-effect condensate pipe. The lower shell-side outlet of the third-effect falling-film evaporator 3 is also connected to the condensate tank 10 via a third-effect condensate pipe. The volute drain port of the steam compressor 11 is connected to the inlet of the liquid accumulation tank 12. The outlet of the liquid accumulation tank 12 is connected to the condensate tank 10 via a liquid accumulation pump. The outlet of the condensate tank 10 is connected to the hot-side inlet of the condensate preheater 1 via a condensate pump. The hot-side outlet of the condensate preheater 1 is connected to the condensate discharge pipe G5.

[0036] The non-condensable gas outlets of the first-effect evaporator 5, the second-effect evaporator 7 and the third-effect falling film evaporator 3 are all connected to the non-condensable gas discharge pipe G6, the outlet of the non-condensable gas discharge pipe G6 is connected to the hot side inlet of the non-condensable gas preheater 2, the hot side outlet of the non-condensable gas preheater 2 is connected to the hot side inlet of the surface condenser 9, and the hot side outlet of the surface condenser 9 is vented to the atmosphere through a vacuum pump.

[0037] The secondary steam outlet of the DTB flash crystallizer 13 is connected to the air inlet of the flash condenser 16, the exhaust port of the flash condenser 16 is connected to the atmosphere through a vacuum pump, and the shell-side condensate outlet of the flash condenser 16 is connected to the flash condensate collection pipe G11.

[0038] The cobalt sulfate solution, delivered to the system via cobalt sulfate feed pipe G1, is at approximately 45°C. It undergoes a primary preheating to approximately 63°C on the cold side of condensate preheater 1. The heat source is the evaporated condensate pumped from condensate tank 10 via condensate pump B5. After heat exchange, the condensate is discharged through condensate drain pipe G5 and can be used in other production processes. This primary preheating of the cobalt sulfate solution then proceeds to the cold side of non-condensable gas preheater 2 for a secondary preheating to approximately 65°C. The heat source is the non-condensable gas within the system, which is drawn from non-condensable gas drain pipe G6. After heat exchange, the non-condensable gas enters surface condenser 9 for cooling before being discharged via vacuum pump B6.

[0039] The cobalt sulfate solution at about 65°C after two-stage preheating enters the triple-effect falling-film evaporator 3 for evaporation. The heat source medium is the secondary steam evaporated from the second effect. The condensed water after heat exchange flows into the condensate tank 10 by gravity. After triple-effect evaporation, the temperature of the cobalt sulfate solution rises to about 57°C and is pumped into the triple-effect falling-film evaporator 3 by the triple-effect falling-film circulation pump B1 for circulation, and part of it enters the first-effect evaporation system through the triple-effect transfer pipe G2.

[0040] After evaporation in the first-effect evaporator 5, the temperature of the cobalt sulfate solution rises to about 85°C and is sent into the first-effect separator 6 by the first-effect circulation pump B2 for circulation, and part of it is pumped into the second-effect evaporation system through the first-effect transfer pipe G3.

[0041] After evaporation in the second-effect evaporator 7, the temperature of the cobalt sulfate solution rises to about 72°C and is sent into the second-effect separator 8 by the second-effect circulation pump B3 for circulation. Part of the second-effect circulating liquid is pumped into the DTB flash crystallization tank 13 through the second-effect evaporation discharge pipe G4 and the second-effect discharge pump B4 for crystallization and crystal cultivation. The flash crystallization temperature is about 30°C. After crystal precipitation, it is pumped into the flash thickening tank 14 by the flash crystal slurry pump B8 for thickening, and finally enters the centrifuge 15 to centrifugally produce cobalt sulfate products.

[0042] The triple-effect secondary gas discharged from the top of the triple-effect falling-film separator 4 and the second-effect secondary gas discharged from the top of the second-effect separator 8 jointly enter the steam compressor 11 for compression. After being heated and pressurized under the action of the steam compressor 11, it becomes high-quality secondary steam and enters the shell sides of the triple-effect falling-film evaporator 3 and the first-effect evaporator 5 through the compressor secondary gas pipe G10 as a heat source to provide heat for the evaporation of the cobalt sulfate solution. The condensed water discharged from the volute of the steam compressor 11 enters the liquid accumulation tank 12 for collection and is sent into the condensate tank 10 by the liquid accumulation pump B7.

[0043] The secondary steam evaporated from the first effect is discharged from the top of the first-effect separator 6 and enters the shell side of the second-effect evaporator 7 under the action of the pressure difference to continue evaporating the solution.

[0044] The secondary steam discharged from the top of the DTB flash crystallization tank 13 enters the flash condenser 16 for condensation under the action of the vacuum pump two B9. The condensed water is discharged externally through the flash condensed water collection pipe G11, and the remaining non-condensable gas is discharged externally through the vacuum pump two B9.

[0045] The above are only the preferred and feasible embodiments of the present utility model, which illustrate and describe the basic principles, main features and advantages of the present utility model. However, the patent protection scope of the present utility model is not limited thereby. Those skilled in the art should understand that the present utility model is not restricted by the above embodiments. Except for the above embodiments, without departing from the spirit and scope of the present utility model, the present utility model may have other implementation manners. The present utility model will also have various changes and improvements. Any technical solutions formed by equivalent substitution or equivalent transformation shall fall within the protection scope required by the present utility model. The protection scope required by the present utility model is defined by the appended claims and their equivalents. The technical features not described in the present utility model can be realized by or adopt the prior art, and will not be elaborated herein.

Claims

1. An evaporation concentration and crystallization device for a cobalt sulfate battery recycling leaching solution, including a cobalt sulfate feed liquid pipe, characterized in that: The outlet of the cobalt sulfate liquid pipe is connected to the circulation pipe of the triple-effect falling film evaporation unit via a preheating unit, the circulation pipe of the triple-effect falling film evaporation unit is connected to the circulation pipe of the first-effect evaporation system via a triple-effect transfer pipe, the circulation pipe of the first-effect evaporation system is connected to the circulation pipe of the second-effect evaporation system via the first-effect transfer pipe, the circulation pipe of the second-effect evaporation system is connected to the inlet of the second-effect discharge pump via the second-effect evaporation discharge pipe, the outlet of the second-effect discharge pump is connected to the feed port of the DTB flash crystallizer, the slurry outlet of the DTB flash crystallizer is connected to the inlet of the flash thickening tank via the flash slurry pump, the bottom outlet of the flash thickening tank is connected to the inlet of the centrifuge, and the solid phase outlet of the centrifuge is connected to the cobalt sulfate discharge pipe; The secondary steam outlet of the first-effect evaporation system is connected to the heat source inlet of the second-effect evaporation system through a first-effect secondary steam pipe, the secondary steam outlet of the second-effect evaporation system is connected to the second-effect secondary steam pipe, the secondary steam outlet of the three-effect falling film evaporation unit is connected to the three-effect secondary steam pipe, the outlets of the second-effect secondary steam pipe and the three-effect secondary steam pipe are connected to the inlet of the steam compressor, and the outlet of the steam compressor is connected to the heat source inlets of the first-effect evaporation system and the three-effect falling film evaporation unit through the compressor secondary steam pipe.

2. The evaporation concentration and crystallization device for the cobalt sulfate-containing battery recycling leaching solution according to claim 1, wherein: The preheating unit includes a condensate preheater and a non-condensable gas preheater. The outlet of the cobalt sulfate liquid pipe is connected to the cold side inlet of the condensate preheater, the cold side outlet of the condensate preheater is connected to the cold side inlet of the non-condensable gas preheater, and the cold side outlet of the non-condensable gas preheater is connected to the circulation pipe of the three-effect falling film evaporation unit.

3. The evaporation concentration and crystallization device for the cobalt sulfate-containing battery recycling leaching solution according to claim 2, characterized in that: The non-condensable gas outlets of the first-effect evaporation system, the second-effect evaporation system and the third-effect falling film evaporation unit are all connected to the non-condensable gas discharge pipe, the outlet of the non-condensable gas discharge pipe is connected to the hot side inlet of the non-condensable gas preheater, the hot side outlet of the non-condensable gas preheater is connected to the hot side inlet of the surface condenser, and the hot side outlet of the surface condenser is connected to the atmosphere through a vacuum pump.

4. The evaporation concentration and crystallization device for the cobalt sulfate-containing battery recycling leaching solution according to claim 2, characterized in that: The condensed water outlets of the first-effect evaporation system, the second-effect evaporation system and the third-effect falling film evaporation unit are respectively connected to the inlet of the condensed water tank, the outlet of the condensed water tank is connected to the hot side inlet of the condensed water preheater through a condensed water pump, and the hot side outlet of the condensed water preheater is connected to the condensed water discharge pipe.

5. The evaporation concentration and crystallization device for the leaching solution of cobalt sulfate-containing battery recycling according to claim 4, characterized in that: The volute drain port of the steam compressor is connected to the inlet of the liquid accumulation tank, and the outlet of the liquid accumulation tank is connected to the condensed water tank through a liquid accumulation pump.

6. The evaporation concentration and crystallization device for the leaching solution of cobalt sulfate-containing battery recycling according to any one of claims 1 to 5, characterized in that: The secondary steam outlet of the DTB flash crystallizer is connected to the air inlet of the flash condenser, and the exhaust port of the flash condenser is connected to the atmosphere through a vacuum pump.

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