Evaporative crystallization device and high-temperature oxidation device combined process system

Abstract

The embodiment of the utility model provides a process system combining an evaporative crystallization device and a high-temperature oxidation device. The process system comprises a first-stage evaporative concentration device, the high-temperature oxidation device and a second-stage evaporative crystallization device, the first-stage evaporation and concentration device is provided with a strong brine inlet and an evaporation and concentration liquid outlet; the high-temperature oxidation device is provided with an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; the evaporation and concentration liquid inlet is connected with the evaporation and concentration liquid outlet; the second-stage evaporative crystallization device is provided with a high-temperature oxidation liquid inlet, a crystallized salt discharge port and a second reuse water discharge port; and the high-temperature oxidation liquid inlet is connected with the high-temperature oxidation liquid outlet. Therefore, in the evaporative crystallization process, organic matters in the strong brine are decomposed through the high-temperature oxidation device, so that COD (Chemical Oxygen Demand) and TOC (Total Organic Carbon) are effectively reduced, the influence on the operation stability and treatment efficiency of equipment is avoided, the chromaticity of crystallized salt is reduced, and the purity of the crystallized salt is improved.

Description

Technical Field

[0001] This application relates to the field of wastewater treatment technology, and in particular to a process system that combines an evaporation crystallization device with a high-temperature oxidation device. Background Technology

[0002] Zero discharge of industrial wastewater has become an important approach to achieving sustainable economic and social development in recent years, playing a crucial role, especially in resolving the conflict between water environmental protection and industrial development. With the acceleration of industrialization, water scarcity and water pollution have become increasingly prominent. The promotion and application of zero discharge technology for industrial wastewater can not only effectively reduce water consumption but also minimize the negative environmental impact of industrial production, providing strong support for achieving green development and ecological civilization.

[0003] Generally, industrial wastewater treatment technologies can include evaporation crystallization, which separates water from wastewater by evaporation while simultaneously crystallizing dissolved salts into solids, thereby achieving water reuse and effective separation of product salts. This process not only recovers a large amount of clean water resources for industrial production or ecological replenishment but also utilizes the salts in wastewater as resources, reducing solid waste emissions and yielding significant economic and environmental benefits.

[0004] However, in existing evaporation crystallization technologies, concentrated brine often contains a high concentration of organic matter. This organic matter easily forms foam or adheres to the equipment surface during evaporation, leading to increased mist entrainment and even causing operational instability such as tank tipping. Secondly, the concentrated brine often has a high color, possibly originating from contaminants such as dyes and organic solvents. These substances not only affect the operating efficiency of the evaporation crystallization system but also negatively impact the quality of the product salt, causing problems such as decreased product salt purity and abnormal color. Furthermore, it can easily lead to difficulties in mother liquor evaporation and a high rate of impurities. Utility Model Content

[0005] This application provides a process system that combines an evaporation crystallization device with a high-temperature oxidation device to solve the problems of high organic matter concentration and poor operational stability of existing evaporation crystallization technologies.

[0006] This application discloses a process system that combines an evaporation crystallization device with a high-temperature oxidation device. The process system includes a first-stage evaporation concentration device, a high-temperature oxidation device, and a second-stage evaporation crystallization device.

[0007] The first-stage evaporation and concentration device is equipped with a concentrated brine inlet and an evaporation and concentration liquid outlet;

[0008] The high-temperature oxidation device is provided with an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; wherein, the evaporation and concentration liquid inlet is connected to the evaporation and concentration liquid outlet;

[0009] The second-stage evaporation crystallization device is equipped with a high-temperature oxidizing liquid inlet, a crystallizing salt outlet, and a second recycled water outlet; wherein the high-temperature oxidizing liquid inlet is connected to the high-temperature oxidizing liquid outlet.

[0010] Optionally, the process system further includes a high-temperature oxidation raw material tank;

[0011] The high-temperature oxidation raw material tank is connected to both the evaporation and concentration liquid outlet and the evaporation and concentration liquid inlet.

[0012] Optionally, the process system further includes a first cooling heat exchanger;

[0013] The first cooling heat exchanger is connected to both the evaporation and concentration liquid outlet and the high-temperature oxidation raw material tank.

[0014] Optionally, the process system further includes a high-pressure pump;

[0015] The high-pressure pump is connected to both the high-temperature oxidation raw material tank and the evaporation and concentration liquid inlet.

[0016] Optionally, the process system further includes a steam mixing heater;

[0017] The steam mixing heater is connected to both the high-pressure pump and the evaporation and concentration liquid inlet.

[0018] Optionally, the process system further includes an oxidation product water tank;

[0019] The oxidation product tank is connected to both the high-temperature oxidation liquid outlet and the high-temperature oxidation liquid inlet.

[0020] Optionally, the process system further includes a second cooling heat exchanger;

[0021] The second cooling heat exchanger is connected to both the high-temperature oxidizing liquid outlet and the oxidizing water tank.

[0022] Optionally, the process system further includes a booster pump;

[0023] The booster pump is used to connect the high-temperature oxidizing liquid outlet and the high-temperature oxidizing liquid inlet.

[0024] Optionally, the first-stage evaporation and concentration unit is provided with a first recycled water outlet; the process system also includes a recycled water tank;

[0025] The first recycled water outlet and the second recycled water outlet are respectively connected to the recycled water pool.

[0026] Optionally, the process system further includes an evaporation feed tank connected to the concentrated brine inlet.

[0027] The embodiments of this application have the following advantages:

[0028] The process system provided in this embodiment includes a first-stage evaporation and concentration device, a high-temperature oxidation device, and a second-stage evaporation and crystallization device. The first-stage evaporation and concentration device has a concentrated brine inlet and an evaporation and concentration liquid outlet. The high-temperature oxidation device has an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; wherein the evaporation and concentration liquid inlet is connected to the evaporation and concentration liquid outlet. The second-stage evaporation and crystallization device has a high-temperature oxidation liquid inlet, a crystallized salt outlet, and a second recycled water outlet; wherein the high-temperature oxidation liquid inlet is connected to the high-temperature oxidation liquid outlet. Therefore, by adding a high-temperature oxidation device to the evaporation and crystallization process, the organic matter in the concentrated brine is decomposed, effectively reducing COD (Chemical Oxygen Demand) and TOC (Total Organic Carbon). This avoids problems such as foaming, scaling, and mist entrainment in the subsequent second-stage evaporation and concentration process, which seriously affect the operational stability and processing efficiency of the equipment. Simultaneously, it can reduce the color of the crystallized salt and improve its purity. Attached Figure Description

[0029] Figure 1 This is a schematic diagram of a process system combining an evaporation crystallization device and a high-temperature oxidation device, as provided in the embodiments of this application.

[0030] The system includes a first-stage evaporation and concentration unit 1, a high-temperature oxidation unit 2, a second-stage evaporation and crystallization unit 3, a recycled water tank 4, and an evaporation raw material tank 5. Detailed Implementation

[0031] To make the above-mentioned objectives, features and advantages of this application more apparent and understandable, the application will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0032] This application discloses a process system that combines an evaporation crystallization device with a high-temperature oxidation device. The process system includes a first-stage evaporation concentration device 1, a high-temperature oxidation device 2, and a second-stage evaporation crystallization device 3.

[0033] The first-stage evaporation and concentration device 1 is equipped with a concentrated brine inlet and an evaporation and concentration liquid outlet;

[0034] The high-temperature oxidation device 2 is provided with an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; wherein, the evaporation and concentration liquid inlet is connected to the evaporation and concentration liquid outlet;

[0035] The second-stage evaporation crystallization device 3 is provided with a high-temperature oxidizing liquid inlet, a crystallizing salt outlet, and a second recycled water outlet; wherein the high-temperature oxidizing liquid inlet is connected to the high-temperature oxidizing liquid outlet.

[0036] In this embodiment, the process system can be further supplemented with a high-temperature oxidation device 2 based on the first-stage evaporation and concentration device 1 and the second-stage evaporation and crystallization device 3. The high-temperature oxidation device 2 can be used to oxidize concentrated brine at high temperatures to remove organic matter, thereby effectively reducing the COD (chemical oxygen demand) and TOC (total organic carbon) levels of the discharged water.

[0037] Specifically, the first-stage evaporation and concentration unit 1 is equipped with a concentrated brine inlet and an evaporation and concentration liquid outlet. The concentrated brine inlet is used to receive concentrated brine with a TDS (Total Dissolved Solids) of 50,000 mg / L to 80,000 mg / L, indicating a high overall salt content and classifying it as a high-concentration brine. Simultaneously, the concentrated brine has a pH range of 8 to 9.5, is weakly alkaline, operates at a temperature of 25℃ to 45℃, and has a COD (Chemical Oxygen Demand) of 500 mg / L to 2000 mg / L, containing a certain amount of organic pollutants.

[0038] Subsequently, the first-stage evaporation and concentration unit 1 can concentrate the brine. In the first-stage evaporation and concentration section, the brine is heated and evaporated, the water content gradually decreases, the salt concentration further increases, and it is discharged through the evaporation and concentration liquid outlet. The evaporation and concentration liquid discharged from the outlet has a TDS index of 120,000 mg / L to 160,000 mg / L, a temperature of 60℃ to 80℃, and a COD index of 1,000 mg / L to 4,000 mg / L.

[0039] The concentrated brine is concentrated by the first-stage evaporation and concentration unit 1. In the subsequent high-temperature oxidation process, the high-temperature oxidation unit 2 can take advantage of the temperature of the material discharged from the first-stage evaporation and concentration section. Instead of starting the temperature rise from room temperature, it can directly use the waste heat of the concentrated liquid for heating, which greatly reduces the heating energy consumption of the high-temperature oxidation unit 2 and lowers the overall operating cost of the system.

[0040] Meanwhile, placing the high-temperature oxidation unit 2 after the first-stage evaporation and concentration section effectively reduces the volume of water it can process. Since the first-stage evaporation and concentration section has already performed preliminary evaporation and concentration of the concentrate, the volume of liquid entering the high-temperature oxidation unit 2 is significantly reduced, thereby lowering the equipment size and initial investment cost of the high-temperature oxidation unit 2. Simultaneously, the reduced water volume also lowers the operating load of the high-temperature oxidation unit 2, further reducing the system's operating costs.

[0041] The high-temperature oxidation device 2 may be provided with an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; wherein, the evaporation and concentration liquid inlet is connected to the evaporation and concentration liquid outlet.

[0042] The evaporation concentrate inlet can be used to receive the evaporation concentrate discharged from the evaporation concentrate outlet. In the high-temperature oxidation unit 2, organic matter can be efficiently oxidized and decomposed by an oxidant (such as oxygen or hydrogen peroxide), achieving a COD removal rate of 30%–70%. This process not only effectively reduces the organic matter content in the concentrate but also significantly improves the operating conditions for subsequent evaporation and crystallization, avoiding problems such as foaming, scaling, and mist entrainment during subsequent evaporation processes.

[0043] After the high-temperature oxidation device 2 completes the processing of the evaporated and concentrated liquid, a high-temperature oxidized liquid is obtained and discharged from the high-temperature oxidized liquid outlet.

[0044] The second-stage evaporation crystallization device 3 is equipped with a high-temperature oxidizing liquid inlet, a crystallizing salt outlet, and a second recycled water outlet; wherein the high-temperature oxidizing liquid inlet is connected to the high-temperature oxidizing liquid outlet.

[0045] Specifically, the second-stage evaporation crystallization unit 3 can receive the high-temperature oxidizing liquid discharged from the high-temperature oxidizing unit 2 through the high-temperature oxidizing liquid inlet. The discharge from the high-temperature oxidizing unit 2 can be well connected to the second-stage evaporation crystallization section, and the temperature of the high-temperature oxidizing liquid can meet the requirements of the second-stage evaporation crystallization unit 3, without the need for further heating of the high-temperature oxidizing liquid.

[0046] The high-temperature oxidizing liquid can then be further evaporated and concentrated. During the evaporation and crystallization process, the water is evaporated and separated, while the salt crystallizes into solid crystalline salt.

[0047] Crystallized salt can be taken out from the crystallized salt discharge port, dried, and then transported and sold as a by-product of resource utilization.

[0048] The condensate can be discharged from the second recycled water outlet and reused to supplement the water demand of the system.

[0049] Some of the mother liquor contains high levels of impurities and salts, making it unsuitable for direct reuse. Therefore, it is discharged into the mixed salt treatment system for further processing to ensure the overall operational efficiency of the system and meet environmental protection requirements.

[0050] The process system provided in this application includes a first-stage evaporation and concentration device 1, a high-temperature oxidation device 2, and a second-stage evaporation and crystallization device 3. The first-stage evaporation and concentration device 1 has a concentrated brine inlet and an evaporation and concentration liquid outlet. The high-temperature oxidation device 2 has an evaporation and concentration liquid inlet and a high-temperature oxidation liquid outlet; wherein the evaporation and concentration liquid inlet is connected to the evaporation and concentration liquid outlet. The second-stage evaporation and crystallization device 3 has a high-temperature oxidation liquid inlet, a crystallized salt outlet, and a second recycled water outlet; wherein the high-temperature oxidation liquid inlet is connected to the high-temperature oxidation liquid outlet. Therefore, by adding the high-temperature oxidation device 2 to the evaporation and crystallization process, the organic matter in the concentrated brine is decomposed, effectively reducing COD (chemical oxygen demand) and TOC (total organic carbon). This avoids problems such as foaming, scaling, and mist entrainment in the subsequent second-stage evaporation and concentration process, which seriously affect the operational stability and processing efficiency of the equipment. Simultaneously, it can reduce the color of the crystallized salt and improve its purity.

[0051] In one embodiment of this application, the process system further includes a high-temperature oxidation raw material tank;

[0052] The high-temperature oxidation raw material tank is connected to both the evaporation and concentration liquid outlet and the evaporation and concentration liquid inlet.

[0053] Specifically, the process system also includes a high-temperature oxidation feed tank. This tank can be connected to both the evaporated and concentrated liquid outlet and the evaporated and concentrated liquid inlet. Thus, after the evaporated and concentrated liquid is discharged from the evaporated and concentrated liquid outlet of the first-stage evaporation and concentration unit 1, it can be temporarily stored in the high-temperature oxidation feed tank for later use.

[0054] In one embodiment of this application, the process system further includes a first cooling heat exchanger;

[0055] The first cooling heat exchanger is connected to both the evaporation and concentration liquid outlet and the high-temperature oxidation raw material tank.

[0056] Specifically, the process system may also include a first cooling heat exchanger, which can be connected to the outlet of the evaporated and concentrated liquid, so as to cool the evaporated and concentrated liquid discharged from the first-stage evaporation and concentration unit 1. After the evaporated and concentrated liquid is cooled to a suitable temperature, it is then fed into a high-temperature oxidation raw material tank for storage and later use.

[0057] In one embodiment of this application, the process system further includes a high-pressure pump;

[0058] The high-pressure pump is connected to both the high-temperature oxidation raw material tank and the evaporation and concentration liquid inlet.

[0059] Specifically, the process system may further include a high-pressure pump, which can be connected to both the high-temperature oxidation raw material tank and the evaporation and concentration liquid inlet simultaneously. The high-pressure pump obtains the evaporation and concentration liquid from the high-temperature oxidation raw material tank and pressurizes it to meet the feeding requirements of the high-temperature oxidation unit 2. Subsequently, the high-pressure pump delivers the pressurized evaporation and concentration liquid to the evaporation and concentration liquid inlet of the high-temperature oxidation unit 2, thereby providing raw materials for the high-temperature oxidation unit 2.

[0060] In one embodiment of this application, the process system further includes a steam mixing heater;

[0061] The steam mixing heater is connected to both the high-pressure pump and the evaporation and concentration liquid inlet.

[0062] Specifically, the process system may further include a steam mixing heater, which can be connected to both the high-pressure pump and the inlet of the evaporated and concentrated liquid. Thus, after pressurizing the evaporated and concentrated liquid, it can be further heated to 120°C–160°C using steam mixing to meet the requirements of the high-temperature oxidation unit 2 for the oxidation reaction.

[0063] In one embodiment of this application, the process system further includes an oxidation product water tank;

[0064] The oxidation product tank is connected to both the high-temperature oxidation liquid outlet and the high-temperature oxidation liquid inlet.

[0065] In a specific implementation, the process system may also include an oxidation product water tank, which can be connected to both the high-temperature oxidation liquid outlet and the high-temperature oxidation liquid inlet, so that the high-temperature oxidation liquid discharged from the high-temperature oxidation device 2 can be temporarily stored in the oxidation product water tank for later use.

[0066] In one embodiment of this application, the process system further includes a second cooling heat exchanger;

[0067] The second cooling heat exchanger is connected to both the high-temperature oxidizing liquid outlet and the oxidizing water tank.

[0068] In a specific implementation, the process system may further include a second cooling heat exchanger. The second cooling heat exchanger can be connected simultaneously to both the high-temperature oxidation liquid outlet and the oxidation product water tank. The second cooling heat exchanger can be used to cool the high-temperature oxidation liquid discharged from the high-temperature oxidation liquid outlet of the high-temperature oxidation device 2 to a suitable temperature before storing it in the oxidation product water tank for later use.

[0069] In one embodiment of this application, the process system further includes a booster pump;

[0070] The booster pump is used to connect the high-temperature oxidizing liquid outlet and the high-temperature oxidizing liquid inlet.

[0071] In a specific implementation, the process system may further include a booster pump, which connects the high-temperature oxidizing liquid outlet and the high-temperature oxidizing liquid inlet. The booster pump can be used to raise the position of the high-temperature oxidizing liquid and transport it to the higher-positioned high-temperature oxidizing liquid inlet to meet the needs of the second-stage crystallization and concentration unit.

[0072] In one embodiment of this application, the first-stage evaporation and concentration device 1 is provided with a first recycled water outlet; the process system further includes a recycled water tank 4;

[0073] The first recycled water outlet and the second recycled water outlet are respectively connected to the recycled water tank 4.

[0074] Specifically, the first-stage evaporation and concentration unit 1 is equipped with a first recycled water outlet, thereby allowing the first-stage evaporation and concentration unit 1 to discharge the condensate generated during the evaporation and concentration process. Furthermore, the condensate discharged from the first recycled water outlet and the condensate discharged from the second recycled water outlet can be transported together to the recycled water tank 4 for recycling.

[0075] In one embodiment of this application, the process system further includes an evaporation raw material tank 5, which is connected to the concentrated brine inlet.

[0076] Specifically, the process system also includes an evaporation feed tank 5, which can store concentrated brine obtained after treatment by the reverse osmosis unit, and is used to provide the process system with the concentrated brine that needs to be treated.

[0077] As a specific example of this application, the evaporation feed tank 5 can store concentrated brine obtained from reverse osmosis, with a flow rate of 50 m³ / h. 3 / h, pH 8.5, TDS 64000mg / L, total hardness <20mg / L, COD 1200mg / L, temperature 35℃, color 100 times.

[0078] The concentrated brine can be sequentially fed into the first-stage evaporation and concentration section, the high-temperature oxidation section, and the second-stage evaporation and crystallization section through the process system provided in the embodiments of this application.

[0079] Specifically, concentrated brine can be passed through the following devices in sequence: raw material tank → heating heat exchanger → first-stage evaporation and concentration device 1 → cooling heat exchanger → high-temperature oxidation raw material tank → high-pressure pump → steam mixing heater → high-temperature oxidation device 2 → cooling heat exchanger → oxidation product water tank → lift pump → second-stage evaporation and crystallization device 3, thereby obtaining crystalline salt.

[0080] The evaporated and concentrated liquid discharged from the first-stage evaporation and concentration unit 1 has a material parameter of a flow rate of 20 m³ / s. 3 / h, TDS index 160000mg / L, COD index 3000mg / L, temperature 60℃, color 400 times.

[0081] The reaction temperature of the high-temperature oxidation device 2 can be 120℃~160℃. The high-temperature oxidation liquid obtained after treatment and cooling by the high-temperature oxidation device 2 has the following material parameters: flow rate 20m³ / h. 3 / h, TDS 160000mg / L, COD 1050mg / L, temperature 60℃, color 50 times.

[0082] After processing by the second-stage evaporation and crystallization unit 3, the resource utilization of crystalline salt product can reach 2560 kg / h. The crystalline salt product is white granules, and the impurity salt is 640 kg / h, with an impurity salt rate of 20%. The cleaning cycle of the second-stage evaporation and concentration is 60 days.

[0083] If a high-temperature oxidation section is not included, and crystalline salt products are obtained only through a first-stage evaporation and concentration section and a second-stage evaporation and crystallization section, then the feed parameters for the second-stage evaporation and crystallization unit 3 can be the feed parameters for the second-stage evaporation section: 20m 3 / h, TDS 160000mg / L, COD 3000mg / L, color 400 times, after the second stage of evaporation and concentration treatment, the product salt for resource utilization is 2080kg / h, the product salt is yellowish granules, the impurity salt is 1120kg / h, the impurity salt rate is 35%, and the cleaning cycle of the second stage of evaporation and concentration is 15 days.

[0084] As can be seen, by setting up a high-temperature oxidation device in the embodiments of this application, the high-temperature oxidation device can be used in conjunction with the evaporation and crystallization device. This not only effectively solves the problems of high organic content, high color, and poor product salt quality in the evaporation concentrate, but also significantly reduces the system's energy consumption and operating costs by optimizing the process flow design.

[0085] By organically combining multi-stage evaporation concentration, high-temperature oxidation, and evaporation crystallization processes, the system achieves highly efficient treatment of concentrated brine from reverse osmosis units. The system not only effectively removes organic pollutants and reduces COD levels, but also enables water reuse and resource utilization of product salts. Furthermore, the miscellaneous salt treatment system solves the problem of mother liquor discharge, providing reliable technical support for zero-discharge of industrial wastewater.

[0086] It should be noted that, in this document, relational terms such as "first" and "second" are used merely to distinguish one entity or operation from another, and do not necessarily require or imply any such actual relationship or order between these entities or operations. Furthermore, the terms "comprising," "including," or any other variations thereof are intended to cover non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements includes not only those elements but also other elements not expressly listed, or elements inherent to such a process, method, article, or apparatus. Without further limitations, an element defined by the phrase "comprising one..." does not exclude the presence of other identical elements in the process, method, article, or apparatus that includes said element.

[0087] The various embodiments in this specification are described in a related manner. Similar or identical parts between embodiments can be referred to mutually. Each embodiment focuses on describing the differences from other embodiments. In particular, the system embodiments are basically similar to the method embodiments, so the description is relatively simple; relevant parts can be referred to the descriptions of the method embodiments.

[0088] The above description is merely a preferred embodiment of this application and is not intended to limit the scope of protection of this application. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this application are included within the scope of protection of this application.

Claims

1. A process system for the evaporation crystallization of a material in combination with a high temperature oxidation system, characterized in that, The process system comprises a first-stage evaporation concentration device, a high-temperature oxidation device, and a second-stage evaporation crystallization device; The first-stage evaporation concentration device is provided with a concentrated brine inlet and an evaporation concentrated liquid outlet; The high-temperature oxidation device is provided with an evaporation concentrated liquid inlet and a high-temperature oxidation liquid outlet; the evaporation concentrated liquid inlet is connected with the evaporation concentrated liquid outlet; The second-stage evaporation crystallization device is provided with a high-temperature oxidation liquid inlet, a crystallized salt outlet, and a second recycled water outlet; the high-temperature oxidation liquid inlet is connected with the high-temperature oxidation liquid outlet.

2. The process system of claim 1, wherein, The process system further comprises a high-temperature oxidation raw material barrel; The high-temperature oxidation raw material barrel is connected with the evaporation concentrated liquid outlet and the evaporation concentrated liquid inlet.

3. The process system of claim 2, wherein, The process system further comprises a first cooling heat exchanger; The first cooling heat exchanger is connected with the evaporation concentrated liquid outlet and the high-temperature oxidation raw material barrel.

4. The process system of claim 2, wherein, The process system further comprises a high-pressure pump; The high-pressure pump is connected with the high-temperature oxidation raw material barrel and the evaporation concentrated liquid inlet.

5. The process system of claim 4, wherein, The process system further comprises a steam mixed heater; The steam mixed heater is connected with the high-pressure pump and the evaporation concentrated liquid inlet.

6. The process system of claim 1, wherein, The process system further comprises an oxidation product water barrel; The oxidation product water barrel is connected with the high-temperature oxidation liquid outlet and the high-temperature oxidation liquid inlet.

7. The process system of claim 6, wherein, The process system further comprises a second cooling heat exchanger; The second cooling heat exchanger is connected with the high-temperature oxidation liquid outlet and the oxidation product water barrel.

8. The process system of claim 6, wherein, The process system further comprises a lifting pump; The lifting pump is connected with the high-temperature oxidation liquid outlet and the high-temperature oxidation liquid inlet.

9. The process system of claim 1, wherein, The first-stage evaporation concentration device is provided with a first recycled water outlet; the process system further comprises a recycled water pool; The first recycled water outlet and the second recycled water outlet are connected with the recycled water pool.

10. The process system of claim 1, wherein, The process system further comprises an evaporation raw material pool, which is connected with the concentrated brine inlet.

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