Device for recycling lithium hydroxide from waste lithium ion battery black powder

Abstract

The utility model discloses a device for recovering lithium hydroxide from waste lithium ion battery black powder, which is characterized in that an outlet of a feed pump is connected with a TVR (Thermal Vapor Recompression) crystallization separator through a cold side of a preheater, and a bottom outlet of the TVR crystallization separator circulates through a TVR evaporation feed liquid circulating pipe, a TVR evaporation forced circulating pump and a TVR heater tube pass; the TVR evaporation transfer pipe is connected with a flash evaporation feed liquid circulating pipe, an outlet of the flash evaporation feed liquid circulating pipe is connected with an inlet of a cooling discharge pump, and an outlet of the cooling discharge pump is connected with a feed port of a cooling crystallization separator; the outlet of the cooling discharge pump is also connected with a thickener, an overflow port of the thickener is connected with a mother liquor tank, a bottom outlet of the thickener is connected with an inlet of a centrifugal machine, a mother liquor outlet of the centrifugal machine is also connected with the mother liquor tank, and an outlet of the mother liquor tank is connected with reflux inlets of the cooling crystallization separator and the TVR crystallization separator; and a solid phase outlet of the centrifugal machine is connected with an inlet of the disc dryer through the spiral conveyor. The device can reduce environmental pollution, reduce energy consumption and improve the resource utilization rate.

Description

Technical Field

[0001] The utility model relates to a waste lithium battery processing device, in particular to a device for recovering lithium hydroxide from black powder of waste lithium ion batteries, belonging to the technical field of waste lithium battery recovery and utilization. Background Art

[0002] In recent years, with the rapid development of the new energy vehicle industry, a large number of waste batteries have been generated. The batteries contain a large amount of rare precious metals such as lithium, nickel, and cobalt. If they are discarded or incinerated at will, they will cause serious pollution and waste. It is very important to recycle and reuse the valuable materials and resources in waste lithium batteries.

[0003] Evaporators play an important role in lithium battery recycling, which can realize solvent recovery and concentration operations, reduce resource waste and environmental pollution. As the importance of lithium battery recycling continues to increase, the scale of traditional single-effect lithium hydroxide devices is generally small, and the product price is relatively high. Most of them use two-effect or three-effect evaporators to achieve solution evaporation, concentration and crystallization, which consumes a lot of energy, has low resource utilization, occupies a large area, and has strong correlations between the effects and interferes with each other.

[0004] With the rapid development of lithium battery vehicles in recent years, the demand for lithium raw materials has increased, and the expansion speed of new equipment has been relatively fast, resulting in a sharp drop in product prices. If two-effect evaporation is still used, the energy consumption will be too large, the production cost will be too high, and the product price will not be competitive in the market, and it will soon be eliminated by the market. Therefore, in order to gain an invincible position in the market, it is necessary to save energy and reduce consumption and reduce product costs. Utility Model Content

[0005] The purpose of this section is to summarize some aspects of the embodiments of the utility model and briefly introduce some preferred embodiments. Some simplifications or omissions may be made in this section and the abstract of the specification of this application and the name of the utility model, and such simplifications or omissions cannot be used to limit the scope of the utility model.

[0006] In view of the above problems and / or the problems existing in the prior art, the present utility model is proposed.

[0007] The purpose of the utility model is to overcome the problems existing in the prior art and provide a device for recovering lithium hydroxide from black powder of waste lithium-ion batteries, which can reduce environmental pollution, reduce energy consumption and improve resource utilization.

[0008] In order to solve the above technical problems, the utility model provides a device for recovering lithium hydroxide from waste lithium-ion battery black powder, comprising a feed pump, the outlet of the feed pump is connected to the cold side inlet of the preheater, the cold side outlet of the preheater is connected to the feed inlet of the TVR crystal separator, the bottom outlet of the TVR crystal separator is connected to the bottom tube side inlet of the TVR heater through the TVR evaporation liquid circulation pipe and the TVR evaporation forced circulation pump, and the top tube side outlet of the TVR heater is connected to the circulating liquid inlet of the TVR crystal separator;

[0009] The outlet of the TVR evaporation forced circulation pump is also connected to the inlet of the transfer pump, the outlet of the transfer pump is connected to the feed liquid reflux port and the transfer pipe of the TVR crystallizer, the outlet of the transfer pipe is connected to the flash evaporation feed liquid circulation pipe, the outlet of the flash evaporation feed liquid circulation pipe is connected to the inlet of the cooling discharge pump, and the outlet of the cooling discharge pump is connected to the feed port of the cooling crystallizer;

[0010] The outlet of the cooling discharge pump is also connected to the inlet of the thickener, the overflow port of the thickener is connected to the mother liquid tank, the bottom outlet of the thickener is connected to the inlet of the centrifuge, the mother liquid outlet of the centrifuge is also connected to the mother liquid tank, and the bottom outlet of the mother liquid tank is connected to the cooling crystallization separator and the reflux port of the TVR crystallization separator through the mother liquid pump;

[0011] The solid phase outlet of the centrifuge is connected to the inlet of the screw conveyor, and the outlet of the screw conveyor is connected to the inlet of the disc dryer.

[0012] As an improvement of the utility model, the top secondary gas outlet of the TVR crystal separator is connected to the hot side inlet of the surface condenser and the suction port of the steam jet pump, the hot side outlet of the surface condenser is connected to the inlet of the surface cooler condensate tank, and the top outlet of the surface cooler condensate tank is connected to the inlet of the TVR evaporative vacuum pump;

[0013] The power steam port of the steam jet pump is connected to the raw steam pipe, the mixed steam outlet of the steam jet pump is connected to the shell side inlet of the TVR heater, and the shell side outlet of the TVR heater is connected to the steam-out water bucket; the bottom outlet of the condensate tank of the surface cooler is also connected to the steam-out water bucket, the outlet of the steam-out water bucket is connected to the hot side inlet of the preheater through the steam-out water pump, and the hot side outlet of the preheater is connected to the evaporated water output pipe.

[0014] As a further improvement of the utility model, the top secondary gas outlet of the cooling crystallization separator is connected to the hot side inlet of the cooling condenser, the hot side outlet of the cooling condenser is connected to the inlet of the cooling condenser condensate tank, the exhaust port of the cooling condenser condensate tank is connected to the cooling evaporation vacuum pump; the bottom drain port of the cooling condenser condensate tank is connected to the reflux port of the cooling crystallization separator.

[0015] Compared with the prior art, the utility model has achieved the following beneficial effects: 1. The horizontal double-flow process is adopted to realize the simultaneous heat exchange of two fluids, effectively utilize the heat exchange temperature difference, reduce heat loss, and improve the heat exchange efficiency; at the same time, the horizontal evaporator has a compact structure, a small footprint, and makes full use of the space; the operation and maintenance of the horizontal evaporator are relatively simple, and it is easy to clean and repair;

[0016] 2. The device uses steam ejector equipment to recycle the heat energy generated during the evaporation process, reducing energy consumption and achieving sustainable use of energy;

[0017] 3. The device adopts a combination of TVR evaporation and flash cooling crystallization technology to achieve low-cost recovery of lithium hydroxide. While using flash cooling crystallization separation, it reduces environmental pollution, improves resource utilization, achieves energy conservation and circular economy, and effectively improves system operation stability and reliability, with great economic and environmental benefits;

[0018] 4. The flash evaporation produces condensed water during the flash cooling process in the device, which indirectly reduces the evaporation of the entire system and reduces energy consumption. The separation of flash steam and materials increases the solid content of flash circulating materials, and the thickening tank is used to further increase the solid content of the centrifuge feed;

[0019] 5. The device uses a fully automatic scraper unloading centrifuge, which can quickly collect solid particles and effectively separate liquid samples with smaller particles. It has a high degree of automation: it can realize fully automatic operation of feeding, primary filtration, fine filtration, unloading, etc., effectively reducing the labor intensity of manual operation and reducing labor costs for enterprises.

[0020] 6. The device uses a disc dryer, which uses indirect heat transfer to transfer heat energy to the material, reducing a large amount of heat transfer losses and effectively reducing the energy consumption of the equipment. The advanced control system and automation technology are used to comprehensively monitor and adjust the operation of the equipment, so as to achieve the best drying effect and minimize energy consumption; during the drying process, the material will not directly contact the gas or combustion materials, which can effectively reduce the emission of harmful gases, dust and other pollutants, and avoid the potential harm to the environment caused by harmful gases such as carbon dioxide generated by combustion; during the operation, advanced dust removal equipment and purification systems are also used to capture and treat the generated waste gas and dust, protect the environment, and ensure the cleanliness and comfort of the production environment. It is a new environmentally friendly drying equipment. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] In order to more clearly illustrate the technical solutions of the embodiments of the present utility model, the following will briefly introduce the drawings required for the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative labor. The drawings are only provided for reference and explanation, not for limiting the present utility model. Among them:

[0022] Figure 1 This is a flow chart of a device for recovering lithium hydroxide from black powder of waste lithium-ion batteries according to the utility model;

[0023] In the figure: 1. Preheater; 2. Evaporation bucket; 3. TVR heater; 4. TVR crystallizer; 4a. TVR crystallizer feed port; 5. Steam jet pump; 6. Surface condenser; 7. Surface cooler condensate tank; 8. Cooling crystallizer; 8a. Cooling crystallizer feed port; 9. Cooling condenser; 10. Cooling condenser condensate tank; 11. Thickener; 12. Centrifuge; 13. Mother liquor tank; 14. Screw conveyor; 15. Disc dryer; 16. Scrubber;

[0024] G1. Liquid feed pipe; G2. TVR evaporation liquid circulation pipe; G3. TVR heater outlet pipe; G4. TVR evaporation secondary gas pipe; G5. Steam ejector suction pipe; G6. Raw steam pipe; G7. TVR heater secondary gas pipe; G8. Primary discharge pipe; G9. Liquid reflux pipe; G10. Transfer pipe; G11. Flash evaporation liquid circulation pipe; G12. Flash evaporation secondary gas pipe; G13. Secondary discharge pipe; G14. Accident discharge pipe; G15. Centrifuge feed pipe; G16. Evaporated water output pipe; G17. Mother liquor return to flash evaporation system pipe; G18. Mother liquor return to TVR system pipe; G19. Centrifugal mother liquor pipe; G20. Thickener overflow pipe; G21. Centrifuge salt outlet pipe; G22. Disc dryer feed pipe; G23. Tail gas pipe; G24. TVR cooler circulating water pipe; G25. Cooling cooler circulating water pipe;

[0025] B1. Incoming material pump; B2. Evaporation water pump; B3. TVR evaporation forced circulation pump; B4. Transfer material pump; B5. Cooling discharge pump; B6. Mother liquor pump; B7. TVR evaporation vacuum pump; B8. Cooling evaporation vacuum pump. DETAILED DESCRIPTION

[0026] In the following description of the utility model, 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 utility model and simplifying the description, and do not mean that the device must have a specific direction.

[0027] 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 described embodiments are only part of the embodiments of the present invention, not all of them.

[0028] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as those commonly understood by those skilled in the art of the present invention. The terms used in the specification of the present invention are only for the purpose of describing specific embodiments and are not intended to limit the present invention.

[0029] like Figure 1 As shown, the utility model comprises a device for recovering lithium hydroxide from black powder of waste lithium-ion batteries, comprising a feed pump B1 connected to a feed liquid feed pipe G1, the outlet of the feed pump B1 is connected to a cold side inlet of a preheater 1, the cold side outlet of the preheater 1 is connected to a TVR crystal separator feed port 4a of a TVR crystal separator 4, the bottom outlet of the TVR crystal separator 4 is connected to a TVR evaporation feed liquid circulation pipe G2, the outlet of the TVR evaporation feed liquid circulation pipe G2 is connected to an inlet of a TVR evaporation forced circulation pump B3, the outlet of the TVR evaporation forced circulation pump B3 is connected to a bottom tube side inlet of a TVR heater 3, and the top tube side outlet of the TVR heater 3 is connected to a circulating liquid inlet of the TVR crystal separator 4 through a TVR heater outlet pipe G3.

[0030] The outlet of the TVR evaporation forced circulation pump B3 is also connected to the inlet of the transfer pump B4 through the primary discharge pipe G8, the outlet of the transfer pump B4 is connected to the feed liquid reflux pipe G9 and the transfer pipe G10, the outlet of the feed liquid reflux pipe G9 is connected to the feed liquid reflux port of the TVR crystallizer separator 4, and the outlet of the transfer pipe G10 is connected to the flash evaporation feed liquid circulation pipe G11.

[0031] The outlet of the evaporated secondary gas at the top of the TVR crystallizer separator 4 is connected to the hot side inlet of the surface condenser 6 through the TVR evaporated secondary gas pipe G4, the hot side outlet of the surface condenser 6 is connected to the inlet of the surface cooler condensate tank 7, the top outlet of the surface cooler condensate tank 7 is connected to the inlet of the TVR evaporative vacuum pump B7, the outlet pipe of the TVR evaporative vacuum pump B7 is connected to the external pipe, and the cold side of the surface condenser 6 is connected to the circulating water pipe G24.

[0032] At the same time, the top of the TVR crystal separator 4 is connected to the suction port of the steam jet pump 5 through the steam jet suction pipe G5, the outlet of the raw steam pipe G6 is connected to the power steam port of the steam jet pump 5, the mixed steam outlet of the steam jet pump 5 is connected to the shell side inlet of the TVR heater 3 through the TVR heater secondary gas pipe G7, the shell side outlet of the TVR heater 3 is connected to the inlet of the steam bucket 2; the bottom outlet of the surface cooler condensate tank 7 is also connected to the inlet of the steam bucket 2. The outlet of the steam bucket 2 is connected to the inlet of the steam pump B2, the outlet of the steam pump B2 is connected to the hot side inlet of the preheater 1, and the hot side outlet of the preheater 1 is connected to the evaporated water output pipe G16.

[0033] Waste lithium batteries are pretreated to obtain lithium-containing black powder. The black powder is leached with a wet leaching process in a sulfuric acid system with a reducing agent to extract nickel, cobalt, manganese and lithium. The leaching solution is subjected to impurity removal, extraction, stripping and other processes to obtain nickel sulfate, manganese sulfate and cobalt sulfate solutions respectively. Finally, the extract is evaporated and concentrated, and sodium hydroxide solution is added to obtain crude lithium hydroxide. After dissolution and a precipitant is added, the fine lithium hydroxide solution is obtained by filtration.

[0034] The feed liquid from the feed liquid feed pipe G1 is a fine lithium hydroxide solution with a temperature of 60°C, a concentration of 75-85%, and a sodium sulfate content of ≤1% obtained after front-end treatment. It is sent to the cold side of the preheater 1 by the feed pump B1, and after heat exchange with the distilled water at a temperature of 90°C, the feed liquid temperature rises to 70°C and enters the TVR crystal separator 4. After mixing with the circulating feed liquid, it is sent to the tube side of the TVR heater 3 for heating by the TVR evaporation forced circulation pump B3, and flows through each heat exchange tube of the TVR heater 3 at a certain flow rate, and exchanges heat with the 90°C heating steam on the shell side of the heater. The temperature of the heated feed liquid is about 82°C, and the first-level evaporation concentration is completed in the TVR crystal separator 4. The first-level concentrated liquid with a concentration of about 90% is pumped into the flash evaporation feed liquid circulation pipe G11 by the transfer pump B4 and enters the flash evaporation system for flash evaporation.

[0035] With fresh steam as the heat source, secondary steam is injected with raw steam to generate negative pressure at the injection port, and energy is transferred with fresh steam through the mixing section. After being pressurized by the steam jet pump 5, it enters the shell inlet of the TVR heater 3, and becomes condensed water after heat exchange and enters the steam output bucket 2.

[0036] The upper end of the flash evaporation liquid circulation pipe G11 is connected to the bottom outlet of the cooling crystallization separator 8, and the outlet of the flash evaporation liquid circulation pipe G11 is connected to the inlet of the cooling discharge pump B5, and the outlet of the cooling discharge pump B5 is connected to the cooling crystallizer feed port 8a of the cooling crystallization separator 8. The outlet of the cooling discharge pump B5 is also connected to an accident discharge pipeline G14 for discharge in an emergency.

[0037] The outlet of the secondary steam at the top of the cooling crystallization separator 8 is connected to the hot side inlet of the cooling condenser 9 through the secondary steam pipe G12, the hot side outlet of the cooling condenser 9 is connected to the inlet of the cooling condenser condensate tank 10, the exhaust port of the cooling condenser condensate tank 10 is connected to the inlet of the cooling evaporation vacuum pump B8, the outlet of the cooling evaporation vacuum pump B8 is emptied, and the cold side of the cooling condenser 9 is connected to the cooling surface cooler circulating water pipeline G25. The bottom drain port of the cooling condenser condensate tank 10 is connected to the reflux port of the cooling crystallization separator 8. The negative pressure condition in the whole system is maintained by the cooling condenser 9 + cooling evaporation vacuum pump B8, the vacuum pump continuously extracts the non-condensable gas in the system, establishes a vacuum environment, and prevents the heat transfer condition from deteriorating and the pressure from rising; the cooling condenser 9 condenses and cools the non-condensable gas and the small amount of steam extracted by the vacuum pump, effectively reducing the workload of the vacuum pump, and the two together ensure the normal operation of various parameters of the evaporation system.

[0038] The outlet pipe of the cooling discharge pump B5 is also connected to the inlet of the thickener 11 through the secondary discharge pipe G13. The primary concentrated liquid enters the cooling crystallization separator 8 for flash evaporation and cooling. After flash evaporation, it is discharged to the thickener 11 at 40°C for crystal growth. The overflow port of the thickener 11 is connected to the inlet of the mother liquid tank 13 through the thickener overflow pipe G20. The bottom outlet of the thickener 11 is connected to the inlet of the centrifuge 12 through the centrifuge feed pipe G15. The mother liquid outlet of the centrifuge 12 is connected to the mother liquid tank 13 through the centrifuge mother liquid pipe G19. The bottom outlet of the mother liquid tank 13 is connected to the inlet of the mother liquid pump B6. The outlet of the mother liquid pump B6 is connected to the reflux port of the cooling crystallization separator 8 through the mother liquid return flash evaporation system pipe G17, and is also connected to the reflux port of the TVR crystallization separator 4 through the mother liquid return TVR system pipe G18.

[0039] The solid phase outlet of the centrifuge 12 is connected to the lower inlet of the screw conveyor 14 through the centrifuge salt outlet pipe G21, the upper outlet of the screw conveyor 14 is connected to the inlet of the disc dryer 15 through the disc dryer feed pipe G22, and the exhaust port of the disc dryer 15 is connected to the inlet of the washing tower 16 through the tail gas pipe G23.

[0040] TVR uses fresh steam as heat source, and uses the method of live steam to induce secondary steam to create vacuum, so that the system evaporates at low temperature. TVR, flashed non-condensable gas and secondary steam enter the surface condenser 6 for condensation. The negative pressure of the system is maintained by the vacuum pump to continuously discharge the non-condensable gas in the system and discharge it through the vacuum pump.

[0041] The high-temperature condensed water generated by the evaporator and the surface cooler enters the distillation water bucket 2, and the high-temperature condensed water is discharged from the system after being preheated by the preheater 1 to preheat the raw materials.

[0042] The secondary gas temperature of TVR evaporation is 90℃ and the pressure is -0.03Mpa. Part of it is used as the heat source for heating TVR heater 3 through the secondary gas pipe, and part of it enters the steam ejector 5 as the suction gas. After being mixed with the 0.6Mpa raw steam, the 0.2Mpa steam enters the shell of TVR heater 3 as the heat source for TVR evaporation, saving about 18% of steam consumption.

[0043] After flash evaporation, the liquid changes from saturation to supersaturation. Supersaturation is the driving force of crystal growth. The supersaturation of the liquid in the cooling crystallization separator 8 is used for crystal growth. After the solid-liquid ratio of the liquid slurry after flash evaporation concentration reaches the requirement, it is pumped into the liquid thickening tank 11 by the cooling discharge pump B5. After thickening and concentration, the upper clear liquid of the liquid thickening tank 11 overflows to the liquid mother liquid tank 13. After the lower crystal slurry of the liquid thickening tank 11 reaches the centrifugal solid-liquid ratio, it enters the centrifuge 12 for solid-liquid separation to obtain wet material monohydrate lithium hydroxide solid. The wet material is continuously added to the first drying plate on the top of the disc dryer 15 by the screw conveyor 14. The rake arm with rake leaves rotates to make the rake leaves stir the material continuously. The large and small drying plates are arranged alternately up and down, so that the material can continuously flow through the entire dryer, and the dry material is discharged from the bottom layer for direct packaging. The mother liquor after solid-liquid separation enters the liquid mother liquid tank 13 and is pumped back to the TVR evaporation or flash evaporation by the mother liquid pump B6. The tail gas is discharged from the dehumidification port on the top cover of the disc dryer 15 and enters the spray absorption tower 16. The micro powder material is collected by the water film, and the clean tail gas is discharged to the outside by the induced draft fan.

[0044] The above description is only the preferred feasible embodiment of the utility model, which shows and describes the basic principle, main features and advantages of the utility model, but does not limit the scope of patent protection of the utility model. The technicians in this industry should understand that the utility model is not limited by the above embodiments. In addition to the above embodiments, the utility model can also have other implementation modes without departing from the spirit and scope of the utility model. The utility model will also have various changes and improvements. All technical solutions formed by equivalent replacement or equivalent transformation fall within the scope of protection required by the utility model. The scope of protection required by the utility model is defined by the attached claims and their equivalents. The technical features not described in the utility model can be achieved by or using existing technologies, which will not be repeated here.

Claims

1. A device for recovering lithium hydroxide from black powder of waste lithium-ion batteries, comprising a feed pump, characterized in that: The outlet of the feed pump is connected to the cold side inlet of the preheater, the cold side outlet of the preheater is connected to the feed port of the TVR crystal separator, the bottom outlet of the TVR crystal separator is connected to the bottom tube side inlet of the TVR heater through the TVR evaporation liquid circulation pipe and the TVR evaporation forced circulation pump, and the top tube side outlet of the TVR heater is connected to the circulating liquid inlet of the TVR crystal separator; The outlet of the TVR evaporation forced circulation pump is also connected to the inlet of the transfer pump, the outlet of the transfer pump is connected to the feed liquid reflux port and the transfer pipe of the TVR crystallizer, the outlet of the transfer pipe is connected to the flash evaporation feed liquid circulation pipe, the outlet of the flash evaporation feed liquid circulation pipe is connected to the inlet of the cooling discharge pump, and the outlet of the cooling discharge pump is connected to the feed port of the cooling crystallizer; The outlet of the cooling discharge pump is also connected to the inlet of the thickener, the overflow port of the thickener is connected to the mother liquid tank, the bottom outlet of the thickener is connected to the inlet of the centrifuge, the mother liquid outlet of the centrifuge is also connected to the mother liquid tank, and the bottom outlet of the mother liquid tank is connected to the cooling crystallization separator and the reflux port of the TVR crystallization separator through the mother liquid pump; The solid phase outlet of the centrifuge is connected to the inlet of the screw conveyor, and the outlet of the screw conveyor is connected to the inlet of the disc dryer.

2. The device for recovering lithium hydroxide from waste lithium ion battery black powder according to claim 1, characterized in that: The top secondary gas outlet of the TVR crystal separator is connected to the hot side inlet of the surface condenser and the suction port of the steam jet pump, the hot side outlet of the surface condenser is connected to the inlet of the surface cooler condensate tank, and the top outlet of the surface cooler condensate tank is connected to the inlet of the TVR evaporative vacuum pump; The power steam port of the steam jet pump is connected to the raw steam pipe, the mixed steam outlet of the steam jet pump is connected to the shell side inlet of the TVR heater, and the shell side outlet of the TVR heater is connected to the steam-out water bucket; the bottom outlet of the condensate tank of the surface cooler is also connected to the steam-out water bucket, the outlet of the steam-out water bucket is connected to the hot side inlet of the preheater through the steam-out water pump, and the hot side outlet of the preheater is connected to the evaporated water output pipe.

3. The device for recovering lithium hydroxide from waste lithium ion battery black powder according to claim 1 or 2, characterized in that: The top secondary gas outlet of the cooling crystallization separator is connected to the hot side inlet of the cooling condenser, the hot side outlet of the cooling condenser is connected to the inlet of the cooling condenser condensate tank, and the exhaust port of the cooling condenser condensate tank is connected to the cooling evaporation vacuum pump; The bottom drain port of the cooling condenser condensate tank is connected to the reflux port of the cooling crystallization separator.

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