Method for comprehensive recycling of steam condensate water in lithium ion battery factory

Abstract

The application discloses a kind of lithium ion battery factory steam condensate comprehensive recycling methods, comprising ① collection pressure steam condensate ② recovery condensate flash steam top heat energy, it is used for air conditioning heating water heating, while flash steam is condensed after in steam-water heat exchanger and flows to condensate collecting tank ③ make condensate collecting tank in steam condensate sequentially through organic rankine cycle generator set, first plate heat exchanger, second plate heat exchanger and third plate heat exchanger heat cascade utilization ④ low-temperature steam condensate is directly or through steam condensate cooling tower cooling and enters low-temperature condensate tank, for in-plant refrigeration machine, air compressor and other process equipment low-temperature soft water supply.The application makes full use of the low-grade heat energy and condensate itself contained in steam condensate, reduces the comprehensive energy consumption of lithium ion battery factory.

Description

Technical Field

[0001] This invention relates to the field of steam condensate recovery and utilization technology, and in particular to a comprehensive method for the recovery and utilization of steam condensate from a lithium-ion battery factory. Background Technology

[0002] In recent years, with the widespread adoption and promotion of new energy vehicles, electrochemical energy storage, and mobile phones, the lithium battery industry has experienced rapid development. Lithium battery plants consume a significant amount of steam. Taking a 15GWh battery project in Suzhou as an example, steam consumption accounts for 50.2% of the plant's total energy consumption, amounting to 4.01 million tons per year. Steam is mainly used in two ways: firstly, in the coating and drying process of lithium-ion battery production; and secondly, to maintain the constant temperature and humidity environment required for plant production, for the regeneration and heating of dehumidifiers and air conditioners.

[0003] To optimize the business environment and attract industrial investment, local governments typically construct municipal steam pipeline networks to facilitate enterprise access, effectively reducing the initial investment and daily operating costs for lithium battery companies. However, due to various reasons, municipal steam systems generally do not recycle and reuse steam condensate. Steam condensate has two important values: firstly, its high temperature and rich low-grade heat energy; secondly, it is deionized water, pure and resistant to scaling, although the production cost of such deionized water in factories is relatively high.

[0004] Currently, most lithium-ion battery factories have not established effective recycling mechanisms for steam condensate, or have failed to fully explore its potential value, often discharging it directly. During the discharge process, low-temperature tap water must be added to cool the water to below 40°C, further resulting in a double waste of energy and water resources. Summary of the Invention

[0005] To address the aforementioned problems, this invention provides a method for the comprehensive recovery and utilization of steam condensate from lithium-ion battery factories. This method fully utilizes the low-grade heat energy contained in the steam condensate and also allows for the reuse of the condensate itself. Specifically, the following technical solution can be adopted:

[0006] The method for comprehensive recovery and utilization of steam condensate from lithium-ion battery factories according to the present invention is implemented through a steam condensate recovery and utilization system, including:

[0007] First, pressurized steam condensate from each workshop is collected using condensate manifolds;

[0008] Second, the flash steam heat energy at the top of the condensate manifold is recovered through the steam-water heat exchanger and used for heating the air conditioning heating water. At the same time, the flash steam is condensed in the steam-water heat exchanger and flows back to the condensate manifold.

[0009] Third, the steam condensate in the condensate manifold passes through the organic Rankine cycle generator set, the first plate heat exchanger, the second plate heat exchanger and the third plate heat exchanger in sequence to utilize the heat in a cascade manner. During this process, the steam condensate releases heat and its temperature decreases. Part of the heat is converted into electricity to supply the factory with electricity, and part of the heat is used to heat the air conditioning water, the domestic hot water, and the tap water in the ultrapure water preparation system.

[0010] Fourth, the low-temperature steam condensate from the third plate heat exchanger enters the low-temperature condensate tank directly, or it enters the low-temperature condensate tank after being cooled by the steam condensate cooling tower. The qualified low-temperature steam condensate in the low-temperature condensate tank is used for the low-temperature soft water supply of the plant's refrigeration units, air compressors and other process equipment.

[0011] The steam condensate recovery and utilization system used in this invention includes a condensate manifold, which is connected to the pressurized condensate drainage pipe of the workshop. A flash steam pipe is installed at the top of the condensate manifold, and the flash steam pipe is connected to a steam-water heat exchanger, which is installed on the air conditioning / heating return water pipe. The drain outlet of the condensate manifold is connected to a high-temperature condensate tank via a pipe. The outlet of the high-temperature condensate tank is connected to a primary hot water pipe, which is connected to an organic Rankine cycle generator set. The organic Rankine cycle generator set is connected to a first plate heat exchanger via a secondary hot water pipe. The first plate heat exchanger is connected to a second plate heat exchanger via a tertiary hot water pipe. The second plate heat exchanger is connected to a third plate heat exchanger via a quaternary hot water pipe. The third plate heat exchanger is cooled by steam condensate via a quinary hot water pipe. The steam condensate cooling tower is connected to a low-temperature condensate tank via six stages of hot water pipes. A low-temperature soft water supply pipe is installed at the outlet of the low-temperature condensate tank. A first bypass pipe is installed between the first and third stages of hot water pipes. A second bypass pipe is installed between the first and fourth stages of hot water pipes. A third bypass pipe is installed between the second and fifth stages of hot water pipes. A fourth bypass pipe is installed between the sixth and fifth stages of hot water pipes. A condensate recovery pump is installed on the pipe between the condensate manifold and the high-temperature condensate tank. A condensate utilization pump is installed at the outlet of the high-temperature condensate tank. Valves are installed on the first, second, third, fourth, fifth, and sixth stages of hot water pipes, as well as the first, second, third, and fourth bypass pipes.

[0012] As can be seen, this invention first centrally collects pressurized condensate from each workshop into a normal-pressure condensate manifold. Due to a sudden pressure drop generating flash steam, a steam-water heat exchanger is installed to recover its heat before the flash steam is released into the atmosphere. This heat is then used to heat the workshop's air conditioning water. The flash steam then returns to the condensate manifold as condensate. The low-grade heat energy contained in the condensate in the manifold is first converted into electrical energy by an organic Rankine cycle generator set to supply the factory's electricity. Then, it undergoes heat exchange through multiple plate heat exchangers, used for heating the workshop's air conditioning water, domestic hot water, and tap water in the ultrapure water preparation system, thereby maximizing the utilization of the condensate's heat energy. Finally, the condensate is cooled to a suitable temperature for use as low-temperature soft water replenishment for the factory's chillers, air compressors, and other process equipment. In this process, the low-grade heat energy contained in the steam condensate and the condensate itself are fully utilized, reducing the overall energy consumption of the lithium-ion battery factory.

[0013] Preferably, the pressurized condensate drainage pipeline in the workshop includes a 0.8 MPa coating drying steam condensate drainage pipeline and other steam condensate drainage pipelines at 0.5 MPa. Lithium-ion battery factories typically include both types of pressurized condensate. Without heat recovery, the "white vapor" generated by flash evaporation after entering the condensate manifold not only easily causes water vapor corrosion to surrounding equipment but also wastes a large amount of latent heat of vapor.

[0014] The amount of flash steam generated by condensate can be calculated based on the pressure of the condensate and the pressure of the condensate recovery device, using the law of conservation of energy. Taking a conventional dehumidifier with a saturated steam pressure of 0.5 MPa and a condensate manifold pressure slightly higher than atmospheric pressure (0.05 MPa) as an example, and assuming a condensate flow rate of 1 t / h, the amount of flash steam that can be generated is:

[0015] m2=m1(h1-h2) / (h2'-h2)=1* (670.67-467.17) / (2226.2-467.17)=11.57%, that is, the flash steam production at this pressure is 11.57% of the condensate production.

[0016] Therefore, the total flash steam generated by 1t / h of steam condensate is 1*11.57%=0.1157t / h.

[0017] Where m1 is the condensate flow rate (t / h), m2 is the flash vapor generated per unit of condensate (kg / kg), h1 is the enthalpy of condensate at 0.5 MPa (670.67 KJ / kg), h2 is the enthalpy of saturated water at 0.05 MPa (467.17 KJ / kg), and h2' is the latent heat of vaporization of water at 0.5 MPa (2226.2 KJ / kg).

[0018] Taking a yearly base of 330 days and a day of 22 hours as an example, the total annual working hours are 7260 hours. Assuming a steam price of 300 yuan / ton, and considering thermal efficiency and load factor, with a comprehensive efficiency of 70%, the energy cost savings from this portion of flash steam is:

[0019] 7260 * 0.1157 * 300 * 70% = 176,300 yuan / year.

[0020] Preferably, the organic Rankine cycle generator set is connected to the tap water system. The heated tap water is connected to the cold water inlet of the third plate heat exchanger through a pipeline, and the cold water outlet of the third plate heat exchanger is connected to the ultrapure water preparation system through a pipeline. After the high-temperature condensate is collected in the water tank, its heat energy is first used to drive the organic Rankine cycle generator set to generate electricity. The tap water that is about to enter the ultrapure water system is used as a cold source, and the high-temperature condensate can be cooled from 95°C to 70°C. The specific volume of water is 4.18 kJ / kg·K. Assuming a power generation efficiency of 10%, and taking a condensate flow rate of 1 t / h, an annual working day base of 330 days, 22 hours per day, and a total annual working hour of 7260 hours as an example, the theoretical annual power generation is 7260*1000*(95-70)*4.18*10% / 3600=21,000 kWh. The tap water used to prepare ultrapure water is heated through the third plate heat exchanger, and the condensate is cooled from 50°C to 33°C. Taking a condensate flow rate of 1t / h, an annual base of 330 days, 22 hours per day, and a total annual working hours of 7260h as an example, with a heat exchange efficiency of 95%, the annual recoverable heat is 7260*1000*(50-33)*4.18*0.95=490.1MJ.

[0021] Preferably, the cold water inlet of the first plate heat exchanger is connected to the air conditioning heating return water pipe from the outlet of the steam-water heat exchanger, and the cold water outlet of the first plate heat exchanger is connected to the air conditioning heating supply water pipe. Under normal circumstances, the condensate water passing through the first plate heat exchanger can be cooled from 70℃ to 62℃. Taking a condensate flow rate of 1t / h, a yearly base of 330 days, 22 hours per day, and a total annual working hours of 7260 hours as an example, with a heat exchange efficiency of 95%, the annual recoverable heat is 7260*1000*(70-62)*4.18*0.95=230.6MJ.

[0022] Preferably, the cold water inlet of the second plate heat exchanger is connected to the domestic hot water return pipe, and the cold water outlet of the second plate heat exchanger is connected to the domestic hot water supply pipe. Under normal circumstances, the condensate water passing through the second plate heat exchanger can be cooled from 62℃ to 50℃. Taking a condensate flow rate of 1t / h, a yearly base of 330 days, 22 hours per day, and a total annual working hours of 7260 hours as an example, with a heat exchange efficiency of 95%, the annual recoverable heat is 7260*1000*(62-50)*4.18*0.95=345.9MJ.

[0023] This invention provides a comprehensive method for the recovery and utilization of steam condensate in lithium-ion battery factories. Based on a detailed investigation of the heat usage of equipment within the factory and combined with existing steam condensate process parameters, a comprehensive steam condensate recovery and utilization system is designed, integrating flash steam heat recovery, thermal power generation, air conditioning and heating, domestic hot water supply, ultrapure water heating from tap water, and low-temperature process soft water replenishment. It cleverly incorporates a steam-water heat exchanger to use flash steam heat for heating the workshop's air conditioning water. Simultaneously, according to the heat requirements of the target equipment, a series-connected plate heat exchanger is used to utilize the latent heat energy of the steam condensate in a tiered manner, maximizing the release of the latent heat carried by the steam condensate. Finally, the low-temperature steam condensate is used for soft water replenishment for various process equipment. This invention fully utilizes the low-grade heat energy contained in the steam condensate and the condensate itself, reducing the overall energy consumption of lithium-ion battery factories and achieving good economic benefits. Attached Figure Description

[0024] Figure 1 This is a schematic diagram of the steam condensate recovery and utilization system described in this invention. Detailed Implementation

[0025] The embodiments of the present invention will be described in detail below with reference to the accompanying drawings. These embodiments are implemented based on the technical solution of the present invention, and detailed implementation methods and specific working processes are given. However, the scope of protection of the present invention is not limited to the following embodiments.

[0026] Example 1:

[0027] The method for comprehensive recovery and utilization of steam condensate from lithium-ion battery factories described in this invention, through methods such as... Figure 1 The steam condensate recovery and utilization system shown includes a condensate manifold 1 connected to the pressurized condensate drain pipe in the workshop. The pressurized condensate drain pipe typically includes a 0.8 MPa coating drying steam condensate drain pipe 201 and other 0.5 MPa steam condensate drain pipes 202.

[0028] A flash steam pipe 101 is installed on the top of the condensate manifold 1. The flash steam pipe 101 is connected to the steam-water heat exchanger 3, which is installed on the air conditioning heating return water pipe 401. The drain outlet of the condensate manifold 1 is connected to the high-temperature condensate tank 5 through a pipe. A condensate recovery pump 102 is installed on the aforementioned connecting pipe. The outlet of the high-temperature condensate tank 5 is connected to the primary hot water pipe 501. A condensate utilization pump 502 is installed on the primary hot water pipe 501. The primary hot water pipe 501 is connected to the hot water inlet of the organic Rankine cycle generator set 6. The potential energy of the condensate in the primary hot water pipe 501 is used to drive the organic Rankine cycle generator set 6 to generate electricity. The hot water outlet of the organic Rankine cycle generator set 6 is connected to the secondary hot water pipe 601, which is connected to the hot water inlet of the first plate heat exchanger 7. The hot water outlet of the first plate heat exchanger 7 is connected to the hot water inlet of the second plate heat exchanger 8 via the tertiary hot water pipe 701. The hot water outlet of the second plate heat exchanger 8 is equipped with a quaternary hot water pipe 801, which is connected to the hot water inlet of the third plate heat exchanger 9. The hot water outlet of the third plate heat exchanger 9 is equipped with a quinary hot water pipe 901, which is connected to the inlet of the steam condensate cooling tower 10. The outlet of the steam condensate cooling tower 10 is connected to the inlet of the low-temperature condensate tank 11 via a sixth hot water pipe 1001. The outlet of the low-temperature condensate tank 11 is equipped with a low-temperature soft water makeup pipe 1101.

[0029] The chilled water inlet of the aforementioned organic Rankine cycle generator set 6 is connected to the municipal water supply system, and the chilled water outlet is connected to the chilled water inlet of the third plate heat exchanger 9 via a pipe, used to send heated municipal water into the third plate heat exchanger 9. The chilled water outlet of the third plate heat exchanger 9 is connected to the ultrapure water preparation system via a pipe. The chilled water inlet of the first plate heat exchanger 7 is connected to the air conditioning and heating return water pipe 401 from the outlet of the steam-water heat exchanger 3, and the chilled water outlet of the first plate heat exchanger 7 is connected to the air conditioning and heating supply water pipe 402. The chilled water inlet of the second plate heat exchanger 8 is connected to the domestic hot water return water pipe, and the chilled water outlet of the second plate heat exchanger is connected to the domestic hot water supply water pipe.

[0030] In addition, a first bypass pipe 1201 is installed between the primary hot water pipe 501 and the tertiary hot water pipe 701; a second bypass pipe 1202 is installed between the first bypass pipe 1201 and the quaternary hot water pipe 801; a third bypass pipe 1203 is installed between the second bypass pipe 1202 and the quinary hot water pipe 901; and a fourth bypass pipe 1204 is installed between the sixth hot water pipe 1001 and the quinary hot water pipe 901. Valves are installed on all of the aforementioned primary hot water pipes 501, 601, 701, 801, 901, 1001, 1201, 1202, 1203, and 1204.

[0031] Example 2:

[0032] The method for comprehensive recovery and utilization of steam condensate from lithium-ion battery factories according to the present invention includes:

[0033] First, a condensate collection tank 1 is used to collect pressurized steam condensate from each workshop, including 0.8 MPa coating drying steam condensate and 0.5 MPa other steam condensate;

[0034] Secondly, the temperature of the steam condensate in the aforementioned condensate manifold 1 is typically around 95°C, and the pressure inside the manifold is 0.05 MPa. Because the pressure decreases after the steam condensate enters the condensate manifold 1, flash steam is generated. The flash steam pipe 101 is connected to the steam-water heat exchanger 3, and the steam-water heat exchanger 3 is connected to the air conditioning / heating return water pipe 401. Therefore, through heat exchange, the air conditioning / heating water temperature can be raised from 50°C to approximately 55°C, while the flash steam is condensed and returned to the condensate manifold 1.

[0035] Third, under the action of the condensate recovery pump 102 and the condensate utilization pump 502, the steam condensate in the condensate manifold 1 first enters the high-temperature condensate tank 5, and then passes through the organic Rankine cycle generator set 6, the first plate heat exchanger 7, the second plate heat exchanger 8 and the third plate heat exchanger 9 in sequence for the cascade utilization of heat. During this process, the steam condensate releases heat and the temperature decreases. Part of the heat is converted into electrical energy to supply the factory's electricity, and part of the heat is used to heat the air conditioning water, the domestic hot water, and the tap water in the ultrapure water preparation system in the factory.

[0036] Specifically, the condensate at 95°C in the primary hot water pipe 501 is cooled to 70°C after passing through the organic Rankine cycle generator set 6 and enters the first plate heat exchanger 7. The released condensate potential energy drives the organic Rankine cycle generator set 6 to generate electricity. At the same time, the tap water connected to the condensate potential energy organic Rankine cycle generator set 6 is heated from 10°C to 12-15°C, and then heated to 25°C after passing through the third plate heat exchanger 9.

[0037] The cold water inlet of the first plate heat exchanger 7 is connected to the air conditioning heating return water pipe 401 from the outlet of the steam-water heat exchanger 3, and the cold water outlet of the first plate heat exchanger 7 is connected to the air conditioning heating supply water pipe 402. The condensate water at 70°C in the secondary hot water pipe 601 is cooled to 62°C after heat exchange, while the air conditioning heating water is heated from 50°C to 60°C.

[0038] The cold water inlet of the second plate heat exchanger 8 is connected to the domestic hot water return pipe, and the cold water outlet of the second plate heat exchanger is connected to the domestic hot water supply pipe. After heat exchange, the condensate in the tertiary hot water pipe 701 at 70°C is cooled to 50°C, while the domestic hot water is heated from 20°C to 45°C.

[0039] The cold water inlet of the third plate heat exchanger 9 is connected to the tap water pipe from the outlet of the organic Rankine cycle generator set 6, while the cold water outlet is connected to the ultrapure water preparation system. After heat exchange, the condensate in the fourth-stage hot water pipe 801 at 50°C is cooled to 33°C, while the tap water is heated from 12-15°C to 25°C.

[0040] Fourth, the low-temperature steam condensate from the third plate heat exchanger 9 enters the low-temperature condensate tank 11 directly through the fourth bypass pipe 1204. The qualified low-temperature steam condensate (≤33℃) in the low-temperature condensate tank 11 is used for the low-temperature soft water supply of the plant's refrigeration units, air compressors and other process equipment.

[0041] When the present invention operates under the above-mentioned process parameters, with an annual base of 330 days, 22 hours per day, and a total annual working hours of 7260 hours, and a flash vapor recovery rate of 1 t / h, the energy cost savings are RMB 176,300 per year. The theoretical annual power generation generated by the recovered heat is 21,000 kWh. At the same time, it can provide 230.6 MJ of recovered heat to the plant's air conditioning and heating system, 345.9 MJ of recovered heat to the plant's domestic hot water supply system, and 490.1 MJ of recovered heat to the plant's ultrapure water preparation system, significantly reducing the overall production cost of the lithium-ion battery factory.

[0042] Example 3:

[0043] The method for comprehensive recovery and utilization of steam condensate from lithium-ion battery factories according to the present invention includes:

[0044] First, a condensate collection tank 1 is used to collect pressurized steam condensate from each workshop, including 0.8 MPa coating drying steam condensate and 0.5 MPa other steam condensate;

[0045] Secondly, the temperature of the steam condensate in the aforementioned condensate manifold 1 is typically around 95°C, and the pressure inside the manifold is 0.05 MPa. Because the pressure decreases after the steam condensate enters the condensate manifold 1, flash steam is generated. The flash steam pipe 101 is connected to the steam-water heat exchanger 3, and the steam-water heat exchanger 3 is connected to the air conditioning / heating return water pipe 401. Therefore, through heat exchange, the air conditioning / heating water temperature can be raised from 50°C to approximately 55°C, while the flash steam is condensed and returned to the condensate manifold 1.

[0046] Third, as the operating conditions of the organic Rankine cycle generator set 6, the operating conditions of the ultrapure water production system, the demand for air conditioning and heating, and the demand for domestic hot water change (referring to a decrease in heat demand), the opening and closing status of the corresponding valves can be adjusted according to the actual situation so that the steam condensate does not pass through the organic Rankine cycle generator set 6, the first plate heat exchanger 7, the second plate heat exchanger 8 and / or the third plate heat exchanger 9 for heat exchange and cooling, but directly reaches the fifth-stage hot water pipe 901 through the first bypass pipe 1201, the second bypass pipe 1202 and / or the third bypass pipe 1203.

[0047] Fourth, since the temperature of the steam condensate in the fifth-stage hot water pipe 901 is relatively high at this time, it is necessary to close the fourth bypass pipe 1204 so that the steam condensate can be cooled by passing through the steam condensate cooling tower 10. When the steam condensate is cooled to below 33°C, it is collected in the low-temperature condensate tank 11 through the sixth-stage hot water pipe 1001 and then used for low-temperature soft water replenishment for the refrigeration unit, air compressor and other process equipment.

[0048] It should be noted that in the description of this invention, terms such as "front," "rear," "left," "right," "vertical," "horizontal," "inner," and "outer" indicating orientation or positional relationships are based on the orientation or positional relationships shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

Claims

1. A method for comprehensive recycling of steam condensate from a lithium-ion battery factory, implemented through a steam condensate recycling system, characterized in that... include: First, pressurized steam condensate from each workshop is collected using condensate manifolds; Second, the flash steam heat energy at the top of the condensate manifold is recovered through the steam-water heat exchanger and used for heating the air conditioning heating water. At the same time, the flash steam is condensed in the steam-water heat exchanger and flows back to the condensate manifold. Third, the steam condensate in the condensate manifold passes through the organic Rankine cycle generator set, the first plate heat exchanger, the second plate heat exchanger and the third plate heat exchanger in sequence to utilize the heat in a cascade manner. During this process, the steam condensate releases heat and its temperature decreases. Part of the heat is converted into electricity to supply the factory with electricity, and part of the heat is used to heat the air conditioning water, the domestic hot water, and the tap water in the ultrapure water preparation system. Fourth, the low-temperature steam condensate from the third plate heat exchanger enters the low-temperature condensate tank directly, or enters the low-temperature condensate tank after being cooled by the steam condensate cooling tower. The qualified low-temperature steam condensate in the low-temperature condensate tank is used for the low-temperature soft water supply of the plant's refrigeration units, air compressors and other process equipment. The steam condensate recovery and utilization system includes a condensate manifold, which is connected to the pressurized condensate drainage pipe in the workshop. A flash steam pipe is installed at the top of the condensate manifold, and this flash steam pipe is connected to a steam-water heat exchanger, which is installed on the air conditioning / heating return water pipe. The drain outlet of the condensate manifold is connected to a high-temperature condensate tank via a pipe. The outlet of the high-temperature condensate tank is connected to a primary hot water pipe, which is connected to an organic Rankine cycle generator set. The organic Rankine cycle generator set is connected to a first plate heat exchanger via a secondary hot water pipe. The first plate heat exchanger is connected to a second plate heat exchanger via a tertiary hot water pipe. The second plate heat exchanger is connected to a third plate heat exchanger via a quaternary hot water pipe. The third plate heat exchanger is connected to a steam condensate cooling tower via a quinary hot water pipe. The steam condensate cooling tower is connected to a low-temperature condensate tank via a six-stage hot water pipe. A low-temperature soft water supply pipe is installed at the outlet of the low-temperature condensate tank. A first bypass pipe is installed between the first-stage and third-stage hot water pipes. A second bypass pipe is installed between the first-stage and fourth-stage hot water pipes. A third bypass pipe is installed between the second-stage and fifth-stage hot water pipes. A fourth bypass pipe is installed between the sixth-stage and fifth-stage hot water pipes. A condensate recovery pump is installed on the pipe between the condensate manifold and the high-temperature condensate tank. A condensate utilization pump is installed at the outlet of the high-temperature condensate tank. Valves are installed on the first-stage, second-stage, third-stage, fourth-stage, fifth-stage, sixth-stage hot water pipes, the first bypass pipe, the second bypass pipe, the third bypass pipe, and the fourth bypass pipe.

2. The method for comprehensive recovery and utilization of steam condensate from a lithium-ion battery factory according to claim 1, characterized in that: The pressurized condensate drainage pipeline in the workshop includes a 0.8 MPa coating drying steam condensate drainage pipeline and other 0.5 MPa steam condensate drainage pipelines.

3. The method for comprehensive recovery and utilization of steam condensate from a lithium-ion battery factory according to claim 1, characterized in that: The organic Rankine cycle generator set is connected to the tap water system. The heated tap water is connected to the cold water inlet of the third plate heat exchanger through a pipeline. The cold water outlet of the third plate heat exchanger is connected to the ultrapure water preparation system through a pipeline.

4. The method for comprehensive recovery and utilization of steam condensate from a lithium-ion battery factory according to claim 1, characterized in that: The cold water inlet of the first plate heat exchanger is connected to the air conditioning and heating return water pipe from the outlet of the steam-water heat exchanger, and the cold water outlet of the first plate heat exchanger is connected to the air conditioning and heating supply water pipe.

5. The method for comprehensive recovery and utilization of steam condensate from a lithium-ion battery factory according to claim 1, characterized in that: The cold water inlet of the second plate heat exchanger is connected to the domestic hot water return pipe, and the cold water outlet of the second plate heat exchanger is connected to the domestic hot water supply pipe.

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