High-salt organic waste liquid treatment zero discharge system based on supercritical water catalytic oxidation

Abstract

The invention provides a high-salt organic waste liquid treatment zero-discharge system based on supercritical water catalytic oxidation, which comprises a storage unit, a mixing unit, a heating unit, a reaction unit, a salt crystallization unit and an electric power unit, the mixing unit pressurizes a mixed reaction medium to a target pressure and then conveys the mixed reaction medium into the heating unit; the heating unit is used for heating the mixed reaction medium to a target temperature so that the mixed reaction medium is converted into a supercritical water state; the heating unit is used for conveying the mixed reaction medium in the supercritical water state into the reaction unit, and the reaction unit is used for carrying out gas-liquid separation on the mixed reaction medium in the supercritical water state, so that the mixed reaction medium is divided into a steam medium and a saline medium; the salt crystallization unit can cool the salt water medium and then solidify and crystallize the salt water medium; the electric power unit is used for generating electricity by using the steam medium and storing electric energy of the steam medium so as to supply the electric energy to each electric device in the waste liquid treatment system; the technical problem that an existing waste liquid treatment system cannot recycle high-temperature waste heat of supercritical water is solved.

Description

Technical Field

[0001] The present application relates to the technical field of new energy and environmental protection, and in particular to a zero-emission system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation. Background Art

[0002] Experimental and production processes generate large quantities of toxic, hazardous, and difficult-to-degrade organic wastewater containing high levels of salt, nitrogen, sulfur, phosphorus, and oil. If discharged without proper treatment, these organic wastewaters can cause severe pollution to water, soil, and ecosystems, and even threaten human health. Therefore, the efficient and safe treatment of these challenging organic wastewaters has become a critical component in ensuring ecological and environmental safety and achieving sustainable development strategies. Strengthening the research, development, and application of wastewater treatment technologies is not only an urgent need for environmental governance but also a crucial technical support for promoting green manufacturing and building an ecological civilization.

[0003] In recent years, supercritical water oxidation (SCWO) technology, as a cutting-edge and highly efficient method for treating organic wastewater, has garnered widespread attention and application in engineering practice. This technology heats and pressurizes organic wastewater to a supercritical state (i.e., temperatures exceeding 374.3°C and pressures exceeding 22.1 MPa), significantly altering the water's physical and chemical properties, such as reduced polarity, increased diffusion coefficient, decreased dielectric constant, and reduced density. This significantly enhances its solubility for organic matter and the efficiency of the oxidation reaction. In this state, the introduction of liquid oxygen or air oxygen into the system completely oxidizes organic pollutants in the wastewater within tens of seconds into harmless gases such as carbon dioxide, high-temperature oxidized water vapor, and nitrogen. Dissolved inorganic components such as metal ions, chlorine, sulfur, and phosphorus rapidly crystallize out, forming stable solid crystalline salts that facilitate subsequent recovery and resource utilization. Compared to traditional treatment processes, SCWO offers significant advantages, including fast reaction speed, thorough treatment, no pretreatment requirements, and low byproduct count. It is considered an ideal solution for treating high-salinity, difficult-to-degrade, and high-concentration organic wastewater.

[0004] Although supercritical water oxidation technology has shown good treatment effects and broad application prospects in the treatment of organic waste liquid, the current actual treatment system still has obvious problems in efficient energy recovery and resource utilization. In particular, in the process of heating the organic waste liquid to the supercritical water state, the organic matter will quickly crack and gasify to produce a large amount of high-temperature waste heat. However, the existing system structure does not effectively recycle and reuse this part of the thermal energy, resulting in high overall energy consumption. For example, after the completion of the organic matter oxidation reaction, cracking and gasification, the high-temperature and high-pressure fluid still contains a large amount of recoverable thermal energy, but due to the lack of supporting thermal energy recovery and energy storage devices or high-temperature oxidation water energy cascade utilization system design, this part of the heat is often directly cooled and discharged, resulting in serious energy waste. Therefore, it is urgent to develop a new supercritical water oxidation treatment system with an efficient thermal energy recovery mechanism to improve the energy utilization efficiency of organic waste liquid and reduce the operating cost of organic waste liquid disposal. Summary of the Invention

[0005] In the embodiments of the present application, a zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation is provided to solve the technical problem that existing waste liquid treatment systems based on supercritical water oxidation technology cannot effectively recycle the high-temperature waste heat of supercritical water. The technical solution is as follows:

[0006] In an embodiment of the present application, a zero-emission system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation is provided, comprising: a storage unit for temporarily storing a waste liquid medium; a mixing unit connected to the storage unit for mixing a catalyst solvent and an oxygen medium with the waste liquid medium extracted from the storage unit to form a mixed reaction medium; a heating unit connected to the storage unit via the mixing unit, the mixing unit pressurizing the mixed reaction medium to a target pressure and then transporting it to the heating unit, the heating unit heating the mixed reaction medium to a target temperature so that the mixed reaction medium is converted into a supercritical water state; a reaction unit connected to the heating unit for heating the reaction medium. The element transports the mixed reaction medium in the supercritical water state to the reaction unit, and the reaction unit is used to perform gas-liquid separation on the mixed reaction medium in the supercritical water state, so as to separate the mixed reaction medium in the supercritical water state into a steam medium and a concentrated brine medium; the salt separation and crystallization unit is connected to the reaction unit and is used to receive the concentrated brine medium, and the salt separation and crystallization unit can cool the concentrated brine medium to solidify and crystallize the concentrated brine medium; and the power unit is connected to the reaction unit and is used to receive the steam medium, and the power unit can use the steam medium to generate electricity and store its electrical energy to supply electrical energy to various electrical equipment in the waste liquid treatment system.

[0007] In one embodiment, the heating unit includes: a first heat exchange mechanism, connected to the power unit, for receiving the steam medium that has completed power generation, and the heat exchange structure uses the residual temperature of the steam medium to perform a first heating of the mixed reaction medium obtained in the mixing unit; an electromagnetic heating mechanism, connected to the first heat exchange mechanism and the power unit, the electromagnetic heating mechanism can obtain electrical energy from the power unit and convert it into thermal energy, and is used to reheat the mixed reaction medium that has completed the first heating in the first heat exchange mechanism until the mixed reaction medium is converted into a supercritical water state.

[0008] In one embodiment, the storage unit includes: a first storage container for storing a waste liquid medium of a thin viscosity; a second storage container for storing a waste liquid medium of a target viscosity; a first waste liquid pressure pump connected to the first storage container and configured to pump the waste liquid medium of a thin viscosity out of the first storage container, the first waste liquid pressure pump being electrically connected to a power unit so as to obtain electrical energy from the power unit; an evaporation and concentration mechanism connected between the first waste liquid pressure pump and the second storage container and configured to adjust the waste liquid medium of a thin viscosity pumped out of the first storage container to a target viscosity and discharge the waste liquid medium of the target viscosity into the second storage container;

[0009] The first heat exchange mechanism is connected to the evaporation and concentration mechanism to supply the steam medium that has completed the first heating of the mixed reaction medium to the evaporation and concentration mechanism for continued use.

[0010] In one embodiment, it also includes: a condensation water storage unit, which is connected to the evaporation and concentration mechanism and is used to receive the steam medium discharged by the evaporation and concentration mechanism. The condensation water storage unit can condense the steam medium into a reusable clean water medium and store the clean water medium to supply the clean water medium to various water-using equipment in the waste liquid treatment system.

[0011] In one embodiment, the condensation water storage unit includes: a third storage container for storing clean water medium, the third storage container is connected to the salt separation crystallization unit so that the clean water medium can be transported to the salt separation crystallization unit, so that the concentrated salt water medium is solidified and crystallized after cooling by the clean water medium; a second heat exchange mechanism, connected between the evaporation concentration mechanism and the second storage container, the second heat exchange mechanism is used to condense the steam medium obtained in the evaporation concentration mechanism into clean water medium; a cooling mechanism, connected to the second heat exchange mechanism, for supplying refrigerant medium to the second heat exchange mechanism; the cooling mechanism is also connected to the third storage container so that it can obtain clean water medium from the third storage container, thereby converting the clean water medium into refrigerant medium through the cooling mechanism.

[0012] In one embodiment, the system further includes an oxygen supply unit connected to the mixing unit and configured to supply oxygen medium to the mixing unit.

[0013] In one embodiment, the oxygen supply unit includes: a fourth storage container for storing oxygen medium in a gaseous state; a gas oxygen pressure pump connected between the fourth storage container and the mixing unit, the gas oxygen pressure pump being electrically connected to the power unit so as to be able to obtain electrical energy from the power unit;

[0014] The gas-oxygen pressure pump is used to pump the oxygen medium in the fourth storage container into the mixing unit, so that the waste liquid medium in the mixing unit is mixed with the oxygen medium in a gaseous state.

[0015] In one embodiment, the oxygen supply unit includes: a fourth storage container for storing oxygen medium in a liquid state; a liquid oxygen pressure pump connected between the fourth storage container and the mixing unit through the salt separation and crystallization unit, and the liquid oxygen pressure pump is electrically connected to the power unit so as to obtain electrical energy from the power unit;

[0016] Among them, the liquid oxygen pressure pump can pump the oxygen medium in the fourth storage container into the salt separation crystallization unit, so that the oxygen medium and the concentrated brine medium exchange heat. The concentrated brine medium solidifies and crystallizes after being cooled by the oxygen medium, and the oxygen medium is converted into a gaseous state with the help of the heat of the concentrated brine medium and then input into the mixing unit to mix the waste liquid medium in the mixing unit with the oxygen medium in a gaseous state.

[0017] In one embodiment, the mixing unit includes: a second waste liquid pressure pump, connected to the second storage container in the storage unit, for extracting the waste liquid medium from the second storage container, and the waste liquid medium is pressurized to a target pressure by the second waste liquid pressure pump, the second waste liquid pressure pump is electrically connected to the power unit so as to be able to obtain electrical energy from the power unit; a jet mixer, connected between the second waste liquid pressure pump and the first heat exchange mechanism in the heating unit, the jet mixer is also connected to the oxygen supply unit, the jet mixer can receive the waste liquid medium at the target pressure in the second waste liquid pressure pump and the oxygen medium in the oxygen supply unit, the waste liquid medium and the oxygen medium are mixed through the jet mixer to form a mixed reaction medium.

[0018] In one embodiment, the mixing unit further comprises: a preheating feeding mechanism connected to the second waste liquid pressure pump, the preheating feeding mechanism being capable of delivering an organic solvent that promotes the reaction of the waste liquid medium into the second waste liquid pressure pump;

[0019] The preheating and feeding mechanism includes: a fifth storage container for storing clean water medium, the fifth storage container is connected to the second waste liquid pressure pump so that the fifth storage container can transport clean water medium to the second waste liquid pressure pump, and the fifth storage container is also connected to the jet mixer through a micro-nano cavitation bubble generator to transport bubble medium for auxiliary cleaning to the jet mixer, and the condensation water storage unit is connected to the fifth storage container so that the condensation water storage unit can supply clean water medium to the fifth storage container; a sixth storage container for storing organic solvent, the sixth storage container is connected to the second waste liquid pressure pump so that the organic solvent can be transported to the second waste liquid pressure pump; a seventh storage container for storing catalyst solvent, the seventh storage container is connected to the second waste liquid pressure pump so that the catalyst solvent can be transported to the second waste liquid pressure pump.

[0020] Compared with the existing technology, the zero-emission system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation proposed in the above technical solution introduces a power unit on the basis of the organic waste liquid treatment system based on supercritical water oxidation, and realizes efficient linkage with the reaction unit. The high-temperature and high-pressure steam discharged after gas-liquid separation is used to drive the power unit to generate electricity, thereby realizing energy cascade energy utilization and resource recovery in the process of organic waste liquid treatment, significantly improving the energy utilization efficiency and operation economy of the system. This design breaks through the limitations of traditional organic waste liquid treatment systems that only focus on the removal of pollutants to meet environmental standards while ignoring energy recovery and utilization. Through the recycling and reuse of high-temperature and high-pressure steam, the efficient conversion of waste heat into electrical energy is realized, avoiding the energy waste problem caused by traditional cooling emissions, and greatly improving the energy utilization rate of the entire system. By integrating storage, mixing, heating, reaction, salt separation and crystallization, and power generation, a comprehensive organic waste liquid treatment system integrating organic pollutant degradation, gasification and energy recovery has been constructed. This system can not only decompose high-concentration, difficult-to-degrade high-salt organic pollutants, but also simultaneously realize the salt separation and crystallization recovery of metal salts and the power generation utilization of steam thermal energy. It is particularly suitable for high-organic pollution industries such as military industry, chemical industry, and laboratory, and will help promote the development of the environmental protection industry towards a green circular economy.

[0021] In summary, the present application provides a zero-emission system for the treatment of high-salt organic waste liquid by supercritical water catalytic oxidation with a reasonable structure, complete functions, energy saving and environmental protection. It successfully solves the technical bottleneck of the existing system that cannot effectively recover the waste heat of high-temperature steam, significantly improves the energy utilization efficiency and environmental friendliness in the organic waste liquid treatment process, has broad application prospects and promotion value, and is of great significance for promoting technological progress and industrial upgrading in my country's high-end environmental protection equipment manufacturing industry.

[0022] The above summary is for illustrative purposes only and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments and features described above, further aspects, embodiments and features of the present application will be readily apparent by reference to the accompanying drawings and the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] In the accompanying drawings, unless otherwise specified, the same reference numerals throughout the multiple drawings represent the same or similar components or elements. These drawings are not necessarily drawn to scale. It should be understood that these drawings only depict some embodiments disclosed in this application and should not be construed as limiting the scope of this application.

[0024] Figure 1 This is a structural distribution diagram of a zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation in an embodiment of the present application;

[0025] Figure 2 This is an enlarged diagram of the structure of the reaction unit and the salt separation crystallization unit in the application example.

[0026] Reference numerals:

[0027] 101. First storage container; 102. Second storage container; 103. First waste liquid pressure pump; 104. Evaporation and concentration mechanism; 105. Second waste liquid pressure pump; 106. Jet mixer; 107. Fourth storage container; 108. Gas oxygen pressure pump; 109. Liquid oxygen pressure pump; 110. First heat exchange mechanism; 111. Electromagnetic heating mechanism; 112. Reaction unit; 113. Salt separation and crystallization unit; 114. Power unit; 115. Third storage container; 116. Second heat exchange mechanism; 117. Cooling mechanism; 118. Fifth storage container; 119. Micro-nano cavitation bubble generator; 120. Sixth storage container; 121. Seventh storage container.

[0028] 112a, reaction tube body; 112b, filler tube body; 112c, silicon carbide-supported rare earth catalyst filler; 112d, material inlet; 112e, material outlet; 112f, steam outlet; 112g, ceramic microporous filter plate; 112h, first area; 112i, second area; 113a, cooling crystallization equipment; 113b, salt grinding and crushing equipment. DETAILED DESCRIPTION

[0029] Hereinafter, only certain exemplary embodiments are briefly described. As will be appreciated by those skilled in the art, the described embodiments may be modified in various ways without departing from the spirit or scope of the present application. Therefore, the drawings and description are to be regarded as illustrative in nature and not restrictive.

[0030] Reference Figure 1 As shown, in the embodiment of the present application, a zero-emission system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation is proposed. The waste liquid treatment system may include: a storage unit for temporarily storing waste liquid medium; a mixing unit, connected to the storage unit, for mixing the catalyst solvent and the oxygen medium in the waste liquid medium extracted from the storage unit to form a mixed reaction medium; a heating unit, connected to the storage unit through the mixing unit, the mixing unit pressurizes the mixed reaction to the target pressure and then transports it to the heating unit, the heating unit heats the mixed reaction medium to the target temperature, so that the mixed reaction medium is converted into a supercritical water state; a reaction unit 112, connected to the heating unit, the heating unit will be in supercritical water The mixed reaction medium in the supercritical water state is transported to the reaction unit 112, and the reaction unit 112 is used to perform gas-liquid separation on the mixed reaction medium in the supercritical water state, so as to separate the mixed reaction medium in the supercritical water state into a steam medium and a concentrated brine medium; a salt separation crystallization unit 113 is connected to the reaction unit 112, and is used to receive the concentrated brine medium, and the salt separation crystallization unit 113 can cool the concentrated brine medium so that the concentrated brine medium is solidified into salt separation crystals; and a power unit 114 is connected to the reaction unit 112, and is used to receive the steam medium, and the power unit 114 can use the remaining steam medium to generate electricity and store its electrical energy to supply electrical energy to various electrical equipment in the waste liquid treatment system.

[0031] Specifically, in the technical solution adopted in the present application, the storage unit may include several containers with built-in holding chambers, and the waste liquid medium to be processed can be temporarily placed in the container for standby; the mixing unit measures and extracts the waste liquid medium in the storage unit to pressurize the waste liquid medium to a target pressure and mix it with the catalyst solvent and the oxygen medium. Pressurizing the waste liquid medium to the target pressure is to prepare for converting the waste liquid medium into a supercritical water state. One of the conditions for forming a supercritical water state is to adjust the pressure of the medium to an initial input reaction pressure of 25 MPA. Therefore, the target pressure of the pressurized mixed medium is 25 MPA, and the catalyst solvent and the oxygen medium are mixed in the waste liquid medium and then input, which can enable the waste liquid medium to undergo catalytic and oxidative reactions to form a mixed reaction medium. The mixing unit transports the mixed reaction medium at the target pressure to the heating unit, and the heating unit heats the mixed reaction medium to a target temperature. In this embodiment, the target initial input reaction temperature is 380°C to 500°C. The conditions for making the mixed reaction medium reach the supercritical water state are that the pressure is 25 MPA and the temperature is 380°C to 500°C. 0℃, wherein the initial input reaction temperature of the mixed reaction medium can preferably be controlled to be higher than 380℃; then, the mixed reaction medium that has completed heating is transported to the reaction unit 112, so that the mixed reaction medium in the supercritical water state is subjected to gas-liquid separation in the reaction unit 112, thereby forming a steam medium in a gaseous state and a concentrated brine medium in a liquid state, and the concentrated brine medium is discharged into the salt separation crystallization unit 113 for cooling and crystallization. It should be explained that after the concentrated brine medium is cooled to different temperatures for crystallization, different sodium salts can be formed, such as sodium sulfate, sodium chloride, etc., so that the required cooling temperature can be adjusted according to actual needs to allow the concentrated brine medium to cool and crystallize; and the steam medium is transported to the power unit 114 through the reaction unit 112. The power unit 114 uses the steam medium as the basic energy source, and drives the turbine turbine to rotate by the kinetic energy of the steam medium, and the turbine turbine then drives the generator to rotate, thereby converting mechanical energy into electrical energy. The power unit 114 uses the steam medium as the power source for generating electricity, which is a prior art. Its structure is not the core improvement to be protected by this application, so it will not be described in detail. This part introduces existing steam power generation equipment, which can generate electricity using the steam medium discharged from the reaction unit 112.

[0032] Reference Figure 2As shown, in one embodiment, the reaction unit 112 can be an existing core-tube reactor, which includes: a reaction tube body 112a and a filler tube body 112b sleeved on the reaction tube body 112a. A spiral scraper mechanism is configured in the reaction tube body 112a, and a silicon carbide-supported rare earth catalyst filler 112c located between the outer wall of the reaction tube body 112a and the inner wall of the filler tube body 112b can be configured in the filler tube body 112b to promote a catalytic oxidation reaction of the mixed reaction medium, so that the mixed reaction medium with a target pressure and a target temperature is transported from the heating unit to the reaction tube body 112a. In the reaction tube body 112a, the mixed reaction medium can be driven by the spiral scraper mechanism from the direction of the material inlet 112d to the direction of the material outlet 112e. When the mixed reaction medium is located at the material outlet 112e, the concentrated brine medium continues to fall due to its own weight, and because the density of the steam medium is smaller than that of the concentrated brine medium, the steam gaseous medium rises to a higher place due to its own light weight, and then returns and rises into the filling tube body 112b, and finally the steam medium is discharged through the steam outlet 112f on the filling tube body 112b, thereby realizing the gas-liquid separation of the mixed reaction medium in the supercritical water state. The mixed reaction medium in the supercritical water state, under the action of the high-temperature and high-pressure oxygen medium and the catalyst medium in the reaction tube body 112a, catalytically activates the molecular water in the mixed reaction medium and first converts it into hydroxyl radicals and hydrogen peroxide. The hydroxyl radicals and hydrogen peroxide then oxidize and decompose all the homogeneously dissolved organic matter, ammonia nitrogen and nitrate nitrogen in the mixed reaction medium into single atomic states (active oxygen-rich atoms, active hydrogen atoms, active nitrogen atoms, active carbon atoms, etc.); and in the supercritical water state region near the material outlet 112e, the homogeneously dissolved organic matter, ammonia nitrogen and nitrate nitrogen single atomic states in the mixed reaction medium are all constrained and catalytically polymerized into high-temperature and high-pressure water vapor, carbon dioxide, nitrogen, residual oxygen and metal crystalline salts, and precipitate and deposit on the ceramic microporous filter plate 112g of the material outlet 112e. The bottom of the reaction unit 112 near the material outlet 112e can be divided into a first area 112h and a second area 112i by a ceramic microporous filter plate 112g. Since the mixed reaction medium in the first area 112h is in a supercritical water state, the temperature of the first area 112h is between 400 and 580°C, and the mixed reaction medium in the second area 112i is in a subcritical water state, so the temperature of the second area 112i is between 150 and 350°C. Therefore, the mixed reaction medium in the second area 112i will dissolve into a concentrated brine medium so as to be discharged from the reaction unit through the material outlet 112e, so as to solve the problem that the existing core shell and tube reactor often has crystallized salt solidification during operation, and seriously blocks the pipes or valves, so as to solve the problem that the core shell and tube reactor cannot operate continuously.

[0033] In one embodiment, the purpose of forming the second region 112i in the reaction unit is to dissolve the solid crystalline salt precipitated from the first region 112h into a concentrated brine medium through ultrasonic spray cooling, and to filter and separate organic matter, ammonia nitrogen, and solid impurities through the ceramic microporous filter plate 112g and then flow into the salt separation crystallization unit 113, so as to obtain the required sodium chloride, sodium sulfate, potassium chloride and other national standard pure salt crystal products through the intelligent gradient control cooling temperature of the salt separation crystallization unit 113. The use of this structure can effectively prevent the solid crystalline salt from clogging the material outlet 112e of the core sleeve reactor, and enable the filler tube 112b to continuously work and output high-temperature and high-pressure gas, and cooperate with the reaction tube 112a to obtain sodium chloride, sodium sulfate, potassium chloride and other national standard pure salt crystal products. The salt separation crystallization unit 113 can guide the concentrated brine medium discharged from the material outlet 112e according to the temperature difference technology of various single salt crystallization points and the seed spraying technology, and separate the monomer pure crystalline salt by temperature control and cooling, and carry out classified resource recycling.

[0034] It should be noted that, since the core shell and tube reactor can separate the mixed reaction medium in the supercritical water state into gas and liquid, the separated gas medium is a steam medium, which is used as the thermal energy of the power unit 114 for power generation and energy storage, so as to be used by the electrical equipment in the waste liquid treatment system, and the separated liquid medium is a concentrated brine medium, which can be gasified and cooled by the salt separation crystallization unit 113, so that the concentrated brine medium is crystallized to obtain the required sodium salt, so that the organic waste liquid can be treated to achieve the purpose of reduction, harmlessness, resource utilization, and ecological recycling, so that the disposal of organic waste liquid and waste, which was originally handled by the national governments at all levels, can be reduced to a certain level. The mandatory compliance behaviors stipulated in government policy documents and national and local environmental protection laws are converted into voluntary compliance by enterprises to utilize the large amount of steam energy generated after the harmless disposal and resource utilization of organic waste liquid and waste, supply electricity for their own supercritical water oxidation equipment and convert excess electricity into energy storage and recycling, and use excess thermal energy to generate steam power and sell electricity on the grid for profit and income. The resource-based energy recycling and profit-generating effect of waste disposal technology has mobilized the awareness, initiative and enthusiasm of enterprises and institutions in the field of new energy technology equipment investment and promotion, so as to promote the practical application and large-scale market promotion of this technology in a wider range of new energy and environmental protection technology intelligent equipment.

[0035] Reference Figure 2As shown, in one embodiment, the salt separation crystallization unit 113 may include: a cooling crystallization device 113a and a salt grinding and crushing device 113b, the cooling crystallization device 113a is connected to the material outlet 112e on the reaction unit 112, and is used to receive the concentrated brine medium obtained by gas-liquid separation in the reaction unit 112, and the concentrated brine medium forms sodium salt after cooling and crystallization in the cooling crystallization device 113a, and the sodium salt is transported to the salt grinding and crushing device 113b to be ground and crushed into powdery fine crystal particles for easy packaging and transportation. In this embodiment, the existing cooling crystallization device 113a and the salt grinding and crushing device 113b can be used, and their specific structures do not need to be improved in this application. Therefore, in this application, the salt separation crystallization unit 113 is no longer described. It can complete the cooling crystallization of the concentrated brine medium and use the grinding and crushing method to decompose the crystallized sodium salt into powdery fine crystal particles that are convenient for packaging and transportation.

[0036] Further, refer to Figure 1 As shown, in some embodiments, the heating unit includes: a first heat exchange mechanism 110, which is connected to the power unit 114 and is used to receive the steam medium that has completed power generation, and the heat exchange structure uses the residual temperature of the steam medium to perform a first heating of the mixed reaction medium obtained in the mixing unit; an electromagnetic heating mechanism 111, which is connected to the first heat exchange mechanism 110 and the power unit 114, and the electromagnetic heating mechanism 111 can obtain electrical energy from the power unit 114 and convert it into thermal energy, and is used to reheat the mixed reaction medium that has completed the first heating in the first heat exchange mechanism 110 until the mixed reaction medium is converted into a supercritical water state.

[0037] Specifically, in the technical solution adopted in this application, the heating unit can use a multiple heating method to gradually increase the temperature gradient of the mixed reaction medium. Therefore, the heating unit in this embodiment includes: a first heat exchange mechanism 110 and an electromagnetic heating mechanism 111. The first heat exchange mechanism 110 is configured as an evaporator, which can use the heat of steam to preliminarily heat the mixed reaction medium. The mixed reaction medium that reaches a certain heating temperature is then heated to the target temperature by the electromagnetic heating mechanism 111, thereby providing a certain buffer during the heating process of the mixed reaction medium, effectively avoiding adverse reactions caused by the linear increase in the temperature gradient of the mixed reaction medium during the heating process. In this embodiment, preliminary heating by the first heat exchange mechanism 110 can also reduce the difficulty of subsequent heating to the target temperature, reducing the operating pressure of the electromagnetic heating mechanism 111, and the heat consumed by the first heat exchange mechanism 110 can be obtained from the steam medium discharged from the power unit 114. Specifically, the first heat exchange mechanism 110 can be connected to the power unit 114, so that the steam medium that completes the power generation work in the power unit 114 is discharged into the first heat exchange mechanism 110 to transfer the heat on the steam medium to the first heat exchange mechanism 110. Therefore, the purpose of the first heating of the mixed reaction medium in the first heat exchange mechanism 110 is achieved; and the electromagnetic heating mechanism 111 converts electrical energy into thermal energy to achieve the heating of the mixed reaction medium with a certain amount of heat to the target temperature. In this embodiment, the electromagnetic heating mechanism 111 can obtain electrical energy from the power unit 114 or from an external power supply. In this embodiment, the thermal energy of the steam medium and the electrical energy generated by the power unit 114 can form an energy cycle, thereby promoting the continuous operation of the waste liquid treatment system.

[0038] Further, refer to Figure 1 As shown, in some embodiments, the storage unit includes: a first storage container 101 for storing waste liquid medium; a second storage container 102 for storing waste liquid medium of target viscosity; a first waste liquid pressure pump 103 connected to the first storage container 101 and used to pump the waste liquid medium out of the first storage container 101, the first waste liquid pressure pump 103 being electrically connected to a power unit 114 so as to obtain electrical energy from the power unit 114; an evaporation and concentration mechanism 104 connected between the first waste liquid pressure pump 103 and the second storage container 102 and used to adjust the waste liquid medium pumped from the first storage container 101 to a target viscosity and discharge the waste liquid medium of target viscosity into the second storage container 102;

[0039] The first heat exchange mechanism 110 is connected to the evaporation and concentration mechanism 104 to supply the steam medium that has completed the first heating of the mixed reaction medium to the evaporation and concentration mechanism 104 for continued use.

[0040] Specifically, in the technical solution adopted in the present application, since the core-tube reactor requires the waste liquid medium to reach a target concentration during the gas-liquid separation of the mixed reaction medium, the storage unit in this embodiment may include: a first storage container 101 and a second storage container 102. Thus, during use, the waste liquid medium that has not reached the target consistency can be temporarily stored in the first storage container 101, while the waste liquid medium that has reached the target consistency can be stored in the second storage container 102. After the waste liquid treatment system is operated, the waste liquid in the first storage container 101 is concentrated and purified to reach the target consistency and then discharged into the second storage container 102 for standby use. Specifically, a first storage container 101 is connected to an evaporation and concentration mechanism 104 via a first waste liquid pressure pump 103. The waste liquid medium in the first storage container 101 is pumped out by the first waste liquid pressure pump 103 and then discharged into the evaporation and concentration mechanism 104. The evaporation and concentration mechanism 104 evaporates the water in the waste liquid medium by heating, thereby concentrating the waste liquid medium. When the waste liquid medium reaches a target consistency, it is discharged into the second storage container 102. In this embodiment, the consistency of the waste liquid medium is determined by the chemical oxygen demand (COD) and total dissolved solids (TDS) of the waste liquid medium. When the COD of the waste liquid medium reaches 20,000 to 500,000 (mg / L) and the TDS of the waste liquid medium reaches 100,000 to 450,000 (mg / L), it indicates that the waste liquid medium has reached the target consistency.

[0041] In one embodiment, in order to enable the waste liquid medium to reach a target consistency through the evaporation and concentration mechanism 104, multiple evaporators can be arranged in the evaporation and concentration mechanism 104 so that the waste liquid medium can be heated multiple times in the process of passing through the evaporation and concentration mechanism 104, thereby continuously stripping off excess water from the waste liquid medium through the evaporation principle until the waste liquid medium reaches the target consistency.

[0042] Further, refer to Figure 1 As shown, in some embodiments, it also includes: a condensation water storage unit, which is connected to the evaporation concentration mechanism 104 and is used to receive the steam medium discharged by the evaporation concentration mechanism 104. The condensation water storage unit can condense the steam medium into a reusable clean water medium, and store the clean water medium to supply the clean water medium to various water-using equipment in the waste liquid treatment system.

[0043] Specifically, in the technical solution adopted by the present application, in order to further recover the high-temperature, high-pressure steam medium for use in the waste liquid treatment system, a condensation water storage unit connected to the evaporation and concentration mechanism 104 may also be included, so that the steam medium that completes heat exchange in the evaporation and concentration mechanism 104 and the steam medium converted into the waste liquid medium can be discharged into the condensation water storage unit. The condensation water storage unit condenses the steam medium obtained in the evaporation and concentration mechanism 104 into a clean water medium, and stores the clean water medium for standby use, thereby providing the clean water medium to the water-using equipment of the waste liquid treatment system.

[0044] Further, refer to Figure 1 As shown, in some embodiments, the condensation water storage unit includes: a third storage container 115, which is used to store clean water medium. The third storage container 115 is connected to the salt separation crystallization unit 113 so that the clean water medium can be transported to the salt separation crystallization unit 113, so that the concentrated salt water medium is solidified and crystallized after cooling by the clean water medium; a second heat exchange mechanism 116, which is connected between the evaporation concentration mechanism 104 and the second storage container 102, and the second heat exchange mechanism 116 is used to condense the steam medium obtained in the evaporation concentration mechanism 104 into clean water medium; a cooling mechanism 117, which is connected to the second heat exchange mechanism 116 and is used to supply refrigerant medium to the second heat exchange mechanism 116; the cooling mechanism 117 is also connected to the third storage container 115 so that it can obtain clean water medium from the third storage container 115, so that the clean water medium is converted into refrigerant medium through the cooling mechanism 117.

[0045] Specifically, in the technical solution adopted in the present application, in order to realize that the condensation water storage unit can convert the steam medium into a clean water medium. Specifically, the condensation water storage unit may include: a second heat exchange mechanism 116 connected to the evaporation and concentration mechanism 104, a cooling mechanism 117 connected to the second heat exchange mechanism 116, and a third storage container 115 connected to the water outlet of the second heat exchange mechanism 116. The second heat exchange mechanism 116 is used to convert the steam medium into a clean water medium and can be set as a condenser. It should be explained that the steam medium evaporated by heating in the waste liquid medium is the water in the waste liquid medium, and the pollutants in the waste liquid medium cannot be converted into a gaseous state by heating. Therefore, the steam medium is converted from a gaseous state to a liquid to form a clean water medium. At present, the purity of the clean water medium can only meet the requirements of cleaning functional equipment in the waste liquid treatment system or be used as a cooling medium. The cooling mechanism 117 is used to supply refrigerant to the second heat exchange mechanism 116, so that the second heat exchange mechanism 116 has the function of condensing steam medium. The cooling mechanism 117 discharges the refrigerant into the second heat exchange mechanism 116, so that the steam medium contacts the refrigerant for heat exchange, thereby converting the steam medium into liquid to form a clean water medium. The third storage container 115 is equipped with a storage chamber for storing clean water medium to store the clean water medium for standby use. It should be noted that the cooling mechanism 117 can be connected to the third storage container 115, so that the cooling mechanism 117 can obtain clean water medium from the third storage container 115, and then cool the clean water medium to form a refrigerant medium after heat exchange and discharge it into the second heat exchange mechanism 116. It can be understood that the water-using equipment mentioned in the above embodiment includes the cooling mechanism 117.

[0046] Further, refer to Figure 1 As shown, in some embodiments, it further includes: an oxygen supply unit connected to the mixing unit, for supplying oxygen medium to the mixing unit.

[0047] Further, refer to Figure 1 As shown, in some embodiments, the oxygen supply unit includes: a fourth storage container 107 for storing oxygen medium in a gaseous state; an oxygen pressure pump 108 connected between the fourth storage container 107 and the mixing unit, and the oxygen pressure pump 108 is electrically connected to the power unit 114 so as to obtain electrical energy from the power unit 114;

[0048] The gas-oxygen pressure pump 108 is used to pump the oxygen medium in the fourth storage container 107 into the mixing unit, so that the waste liquid medium in the mixing unit is mixed with the oxygen medium in a gaseous state.

[0049] Specifically, in the technical solution adopted in the present application, when the chemical oxygen demand of the waste liquid medium in the second storage container 102 is lower than 50,000 (mg / L), the oxygen medium in a gaseous state can be stored in the fourth storage container 107, and the oxygen medium can be pumped into the mixing unit through the gas-oxygen pressure pump 108, so that the oxygen medium can be added to the waste liquid medium with an oxygen demand lower than 50,000 (mg / L) in the mixing unit, thereby accelerating the oxidation reaction of the waste liquid medium.

[0050] Further, refer to Figure 1 As shown, in some embodiments, the oxygen supply unit includes: a fourth storage container 107 for storing oxygen medium in a liquid state; a liquid oxygen pressure pump 109 connected between the fourth storage container 107 and the mixing unit through a salt separation and crystallization unit 113, and the liquid oxygen pressure pump 109 is electrically connected to a power unit 114 so as to obtain electrical energy from the power unit 114;

[0051] Among them, the liquid oxygen pressure pump 109 can pump the oxygen medium in the fourth storage container 107 into the salt separation crystallization unit 113 for vaporization, so that the oxygen medium and the concentrated brine medium are heat exchanged, and the concentrated brine medium is solidified and crystallized after being cooled by the oxygen medium, and the oxygen medium is converted into a gaseous state with the help of the heat of the concentrated brine medium and then input into the mixing unit, so that the waste liquid medium in the mixing unit is mixed with the oxygen medium in a gaseous state.

[0052] Specifically, in the technical solution adopted by the present application, when the chemical oxygen demand of the waste liquid medium in the second storage container 102 is higher than 50,000 (mg / L), an oxygen medium in a liquid state can be stored in the fourth storage container 107. Since the liquid oxygen medium is compressed from a low-temperature oxygen medium in a gaseous state, the oxygen content of the liquid oxygen medium far exceeds the oxygen concentration of the gaseous oxygen medium. The oxygen medium is gasified into oxygen and then input into the mixing unit, and mixed with the waste liquid medium with a chemical oxygen demand of more than 20,000 (mg / L) in the mixing unit to accelerate its oxidation reaction by adapting to the chemical oxygen demand of the waste liquid medium. In one embodiment, the liquid oxygen medium can release its pressure through a capillary line, thereby being discharged into the mixing unit in the form of gas. In a preferred embodiment of the present application, the oxygen supply unit may further include: a liquid oxygen pressure pump 109 connected to the salt separation crystallization unit 113, and the heat exchange tube in the salt separation crystallization unit 113 can be connected to the mixing unit. During use, the oxygen medium in the fourth storage container 107 is extracted by the liquid oxygen pressure pump 109 and input into the salt separation crystallization unit 113 for vaporization. It should be noted that when the oxygen medium is converted from liquid to gaseous, an endothermic effect will be generated, so that the temperature of the oxygen medium will drop sharply, so that the oxygen medium and the concentrated brine medium in the salt separation crystallization unit 113 can exchange heat, so that the temperature of the oxygen medium is increased and finally input into the mixing unit, and the concentrated brine medium is cooled and crystallized into the required pure crystalline salt. After adopting the preferred embodiment of the present application, the temperature of the liquid oxygen medium itself can be fully utilized to cool the concentrated brine medium in the salt separation crystallization unit 113. Conversely, the temperature of the concentrated brine medium can convert the oxygen medium from liquid to gaseous, so as to facilitate the input into the mixing unit to promote the oxidation reaction of the waste liquid medium to be uniform in temperature.

[0053] Further, refer to Figure 1 As shown, in some embodiments, the mixing unit includes: a second waste liquid pressure pump 105, connected to the second storage container 102 in the storage unit, for extracting the waste liquid medium from the second storage container 102, and the waste liquid medium is pressurized to a target pressure by the second waste liquid pressure pump 105, and the second waste liquid pressure pump 105 is electrically connected to the power unit 114 so as to be able to obtain electrical energy from the power unit 114; a jet mixer 106, connected between the second waste liquid pressure pump 105 and the first heat exchange mechanism 110 in the heating unit, the jet mixer 106 is also connected to the oxygen supply unit, the jet mixer 106 can receive the waste liquid medium at the target pressure in the second waste liquid pressure pump 105 and the oxygen medium in the oxygen supply unit, and the waste liquid medium and the oxygen medium are mixed through the jet mixer 106 to form a mixed reaction medium.

[0054] Specifically, in the technical solution adopted in the present application, the mixing unit may include a second waste liquid pressure pump 105 and a jet mixer 106. The second waste liquid pressure pump 105 is connected to the second storage container 102 and is used to extract the waste liquid medium from the second storage container 102 and discharge it into the jet mixer 106. In this embodiment, during the process of extracting the waste liquid medium from the second storage container 102, the second waste liquid pressure pump 105 can adjust the pressure of the waste liquid medium to a target pressure before discharging it into the jet mixer 106, so that the mixed reaction medium obtained by mixing in the jet mixer 106 can meet the pressure condition for converting to a supercritical water state, that is, the above-mentioned pressure of 25 MPA. The jet mixer 106 is connected to the supply unit and the first heat exchange mechanism 110 to mix the oxygen medium and the catalyst solvent in the waste liquid medium of the jet mixer 106. Referring to the above embodiment, the jet mixer 106 can be connected to the fourth storage container 107 through the gas oxygen pressure pump 108, or can be connected to the fourth storage container 107 through the salt separation crystallization unit 113 and the liquid oxygen pressure pump 109. It can be selected according to the chemical oxygen demand of the waste liquid medium in actual application, so as to realize the discharge of the oxygen medium stored in the fourth storage container 107 into the jet mixer 106, which can promote the oxidation reaction of the waste liquid medium.

[0055] Further, refer to Figure 1 As shown, in some embodiments, the mixing unit further includes: a preheating feeding mechanism connected to the second waste liquid pressure pump 105, the preheating feeding mechanism can deliver a solvent that promotes the reaction of the waste liquid medium to the second waste liquid pressure pump 105;

[0056] The preheating feeding mechanism includes: a fifth storage container 118, which is used to store clean water medium. The fifth storage container 118 is connected to the second waste liquid pressure pump 105 so that the fifth storage container 118 can transport clean water medium to the second waste liquid pressure pump 105, and the fifth storage container 118 is also connected to the jet mixer 106 through the micro-nano cavitation bubble generator 119 to transport bubble medium for auxiliary cleaning to the jet mixer 106. The condensation water storage unit is connected to the fifth storage container 118 so that the condensation water storage unit can supply clean water medium to the fifth storage container 118; a sixth storage container 120, which is used to store organic solvent. The sixth storage container 120 is connected to the second waste liquid pressure pump 105 so that the organic solvent can be transported to the second waste liquid pressure pump 105; a seventh storage container 121, which is used to store catalyst solvent. The seventh storage container 121 is connected to the second waste liquid pressure pump 105 so that the catalyst solvent can be transported to the second waste liquid pressure pump 105.

[0057] Specifically, in the technical solution adopted in the present application, the fifth storage container 118 is equipped with a storage chamber for storing clean water medium, which can be connected to the third storage container 115 to obtain clean water medium in the third storage container 115. The fifth storage container 118 is connected to the second waste liquid pressure pump 105 so as to be able to transport clean water medium to the second waste liquid pressure pump 105, and the fifth storage container 118 is also connected to the jet mixer 106 through the micro-nano cavitation bubble generator 119 to convert the clean water medium into bubble medium through the micro-nano cavitation bubble generator 119 to increase the effect of cleaning the waste liquid treatment system. When in use, the waste liquid treatment system needs to be preheated when it is started for the first time, so that the clean water medium is transported to the second waste liquid pressure pump 105 through the fifth storage container 118, and the second waste liquid pressure pump 105 pressurizes the clean water medium and discharges it into the jet mixer 106; at the same time, the micro-nano cavitation bubble generator 119 extracts the clean water medium from the fifth storage and converts it into a bubble medium, and finally transports the bubble medium to the jet mixer 106, and the jet mixer 106 discharges the clean water medium and the bubble medium into the heating unit for heating. Specifically, the battery heating mechanism heats the clean water medium and the bubble medium and discharges them into the reaction unit 112, and detects the pressure and temperature at the steam outlet 112f of the reaction unit 112. When the pressure and temperature are close to the target pressure and target temperature for forming supercritical water, the second waste liquid pressure pump 105 is started to extract the waste liquid medium from the second storage container 102. Using the clean water medium for preheating the waste liquid treatment system in this embodiment not only improves the quality of waste liquid treatment, but also enhances the cleanliness of the waste liquid treatment system by adding the bubble medium before treatment. It should be noted that after the waste liquid treatment system stops treating waste liquid, clean water medium can be drawn from the fifth storage container 118 to clean the waste liquid treatment system.

[0058] In some embodiments, the preheating and replenishing unit includes a sixth storage container 120 and a seventh storage container 121. The sixth storage container 120 is used to store an organic solvent and is connected to the second waste liquid pressure pump 105 so as to be able to deliver the organic solvent to the second waste liquid pressure pump 105. During use, if the waste liquid medium in the second storage container 102, after evaporation and concentration, still fails to reach a chemical oxygen demand of 20,000 (mg / L), then when the second waste liquid pressure pump 105 extracts the waste liquid medium from the second storage container 102, the organic solvent is delivered to the waste liquid medium in the second waste liquid pressure pump 105 through the sixth storage container 120, so that the waste liquid medium reaches a chemical oxygen demand of 20,000 (mg / L) or above, thereby meeting the basic requirements for starting the waste liquid treatment system, maintaining stable operation balance of the reaction system, and maintaining thermal self-sustaining energy. In this embodiment, the organic solvent can be methanol, waste oil, or biodiesel. The seventh storage container 121 is used to store the catalyst solvent and is also connected to the second waste liquid pressure pump 105 so as to be able to deliver the catalyst solvent to the second waste liquid pressure pump 105. During use, if the oxygen supply unit is insufficient due to excessively high chemical oxygen demand of the waste liquid medium, the catalyst solvent can be delivered to the waste liquid medium in the second waste liquid pressure pump 105 through the seventh storage container 121, thereby improving the oxidation effect of the waste liquid medium. In this embodiment, the catalyst solvent can be sodium hydroxide.

[0059] Reference Figure 1 As shown, the working principle of the zero-emission system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation proposed in this application is as follows:

[0060] When started for the first time, the entire system is preheated and cleaned by using the preheating replenishment unit and the oxygen supply unit. The clean water medium and the organic solvent are discharged into the second waste liquid pressure pump 105 through the preheating replenishment unit. The second waste liquid pressure pump 105 pressurizes the clean water medium and the organic solvent and discharges them into the jet mixer 106. At the same time, the micro-nano cavitation bubble generator 119 extracts the clean water medium from the fifth storage container 118, converts the clean water medium into a bubble medium, and then discharges it into the jet mixer 106. The oxygen supply unit discharges the oxygen medium into the jet mixer 106. Subsequently, the jet mixer 106 mixes the clean water medium, the bubble medium, and the oxygen medium with a certain pressure and then transports them to the heating unit. The element is heated, and after being heated to the target temperature, a supercritical water state is formed and enters the reaction unit 112. The mixed reaction medium containing the organic solvent, the clean water medium and the oxygen cut-off stays for about 1 minute under the action of the active oxygen in the reaction unit 112, and a catalytic combustion homogeneous oxidation reaction occurs with water as a homogeneous compatibilizer. Specifically, the active oxygen first reacts with the water molecules of the mixture in a homogeneous phase, thereby generating a large amount of high-concentration hydroxyl free radicals and hydrogen peroxide. Then, the hydroxyl free radicals and hydrogen peroxide in the reaction unit 112 react with the organic matter or the reducible inorganic matter in a strong chain oxidation reaction. When there is sufficient or excessive oxygen, the carbon-containing organic compounds, phosphorus-containing organic compounds, sulfur-containing organic compounds, The macromolecules of harmful and toxic organic waste liquids such as chlorofluorohalogenated hydrocarbons, heterocyclic hydrocarbons, cycloalkanes, aliphatic hydrocarbons, alkenes, alkynes, alcohols, benzene rings, ketones, paint solvents, epoxy resins, phenolic resins, organic carboxylic acids, amino acids, aromatic hydrocarbons, proteins and peptides, nitrobenzene, phosphamides, pesticides, dyes, fiber organic matter, organic nitrogen, ammonia nitrogen, nitrite-nitrite nitrogen compounds, etc. are rapidly ring-opened and chain-broken. They are first oxidized and cracked into small organic molecules, such as formic acid, methanol, methane and other single-carbon low-molecules, and finally oxidized and cracked into single atomic states; all organic nitrogen is first oxidized and cracked into ammonia nitrogen and nitrate nitrogen, and finally oxidized and cracked into single nitrogen atomic states; light and heat are generated in the system during the oxidative cracking reaction. , releasing a large amount of heat; organic matter, ammonia nitrogen and nitrate nitrogen are under the action of high-temperature and high-pressure active oxygen and the nanocatalyst attached to the catalytic membrane group. After controlling the reaction time, temperature and pressure parameters, each single atom can produce a constrained polymerization reaction under the action of the catalyst. Single atomic carbon preferentially electro-adsorbs two active oxygens to become carbon dioxide, and single nitrogen atoms preferentially electro-adsorb active nitrogen to become nitrogen. Ultimately, organic matter, ammonia nitrogen and nitrate nitrogen are rapidly gasified into high-temperature and high-pressure carbon dioxide, nitrogen, high-temperature water vapor, oxygen, etc. in the reaction unit; while the solubility product of inorganic metal cations and anions after electro-adsorption is very small, and they do not dissolve in the reaction unit and become solid crystalline salts that precipitate and precipitate at the material outlet 112e at the bottom of the reaction unit;High-temperature and high-pressure carbon dioxide, nitrogen, high-temperature oxidized water vapor, residual oxygen and other gaseous substances are separated into gas, liquid and solid under the action of gravity. High-temperature oxidized water vapor, carbon dioxide CO2 gas, nitrogen and residual oxygen gas float upward and are finally discharged from the steam outlet 112f of the reaction unit 112. The pressure and temperature of the steam medium are detected at the steam outlet 112f. When the pressure reaches 25MPA and the temperature is close to 380-400℃, it means that the waste liquid treatment system is preheated.

[0061] The steam medium discharged from the reaction unit 112 enters the power unit 114, where it generates electricity by converting thermal energy into energy and kinetic energy into electrical energy. The generated electrical energy is then stored for use by electrical equipment in the waste liquid treatment system. The steam medium discharged from the power unit 114 is transported to the first heat exchange mechanism 110 in the heating unit, so that the first heat exchange mechanism 110 has a heating function. The first heat exchange mechanism 110 is connected to the evaporation and concentration mechanism 104, so that the steam medium that has completed heat exchange in the first heat exchange mechanism 110 is discharged into the evaporation and concentration mechanism 104 for heating and concentrating the waste liquid medium. Finally, the evaporation and concentration mechanism 104 is connected to the cold water storage unit, and the steam medium that has completed heat exchange in the evaporation and concentration mechanism 104 and the steam medium that has converted excess water in the waste liquid medium are both transported to the cold water storage unit for condensation and conversion, thereby converting the steam medium into a clean water medium through the cold water storage unit and storing it for standby use for water-using equipment in the waste liquid treatment system, such as the fifth storage container 118.

[0062] After the waste liquid treatment system is preheated, the first waste liquid pressure pump 103 and the second waste liquid pressure pump 105 can be started. The first waste liquid pressure pump 103 transports the waste liquid in the first storage container 101 to the evaporation and concentration mechanism 104. The waste liquid medium after the evaporation and concentration mechanism 104 adjusts the viscosity is discharged into the second storage container 102; and the second waste liquid pressure pump 105 pressurizes the waste liquid medium in the second storage container 102 and transports it to the jet mixer 106. When the chemical oxygen demand of the waste liquid medium is lower than 20,000 (mg / L), the organic solvent is transported to the second waste liquid pressure pump 105 through the sixth storage container 120 in the preheating replenishment unit to increase the chemical oxygen demand concentration of the waste liquid medium to 20,000 (mg / L) or above. When the chemical oxygen demand concentration of the waste liquid medium is too high (i.e., the chemical oxygen demand concentration exceeds 50,000-1,000,000 mg / L or above), the supply When the oxygen supply of the oxygen unit is insufficient, the catalyst solvent is transported to the second waste liquid pressure pump 105 through the seventh storage container 121 in the preheating replenishment unit to enhance the oxidation reaction of the waste liquid medium through the catalyst solvent. After being fully mixed in the jet mixer 106, a mixed reaction medium is formed. The jet mixer 106 transports the mixed reaction medium to the heating unit for heating so that the mixed reaction medium reaches 380-400°C. Since the mixed reaction medium reaches the target pressure and target temperature, it is converted into a supercritical water state and discharged into the reaction unit 112. The mixed reaction medium in the supercritical water state is fully oxidized in the reaction unit 112 and then separated into gas and liquid to form a concentrated brine medium and a steam medium. The concentrated brine medium is transported to the salt separation crystallization unit 113 for cooling to form sodium salt for recycling, while the steam medium is transported to the power unit 114 as heat energy for power generation. Please refer to the above steps for details.

[0063] In the description of this specification, the reference terms "one embodiment," "some embodiments," "example," "specific example," or "some examples" mean that the specific features, structures, materials, or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. Moreover, the specific features, structures, materials, or characteristics described may be combined in any appropriate manner in any one or more embodiments or examples. In addition, those skilled in the art may combine and combine different embodiments or examples described in this specification, as well as features of different embodiments or examples, unless they are mutually inconsistent.

[0064] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features being referred to. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. Throughout the description of this application, "plurality" means two or more, unless otherwise specifically defined.

[0065] Any process or method description in a flow chart or otherwise described herein can be understood to represent a module, segment or portion of code comprising one or more executable instructions for implementing the steps of a specific logical function or process. The scope of the preferred embodiments of the present application includes additional implementations in which the functions may be performed in a different order than shown or discussed, including in a substantially simultaneous manner or in a reverse order depending on the functions involved.

[0066] The logic and / or steps represented in the flowchart or otherwise described herein may be considered, for example, as an ordered list of executable instructions for implementing logical functions, and may be embodied in any computer-readable medium for use by, or in conjunction with, an instruction execution system, apparatus, or device (such as a computer-based system, a system including a processor, or other system that can fetch and execute instructions from an instruction execution system, apparatus, or device).

[0067] It should be understood that various parts of the present application can be implemented using hardware, software, firmware, or a combination thereof. In the above embodiments, multiple steps or methods can be implemented using software or firmware stored in a memory and executed by a suitable instruction execution system. All or part of the steps of the above embodiment method can be completed by instructing the relevant hardware through a program, which can be stored in a computer-readable storage medium. When the program is executed, it includes one or a combination of the steps of the method embodiment.

[0068] In addition, the functional units in the various embodiments of the present application may be integrated into a single processing module, or each unit may exist physically separately, or two or more units may be integrated into a single module. The aforementioned integrated modules may be implemented in the form of hardware or in the form of software functional modules. If the aforementioned integrated modules are implemented in the form of software functional modules and sold or used as independent products, they may also be stored in a computer-readable storage medium. The storage medium may be a read-only memory, a magnetic disk, or an optical disk, etc.

[0069] The above description is merely a specific embodiment of the present application, but the scope of protection of the present application is not limited thereto. Any person skilled in the art can easily conceive of various modifications or substitutions within the technical scope disclosed in this application, and such modifications or substitutions should be included within the scope of protection of the present application. Therefore, the scope of protection of the present application should be based on the scope of protection of the claims.

Claims

1. A zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation, characterized in that: include: a storage unit for temporarily storing waste liquid media; a mixing unit connected to the storage unit and configured to mix a catalyst solvent and an oxygen medium with the waste liquid medium extracted from the storage unit to form a mixed reaction medium; a heating unit connected to the storage unit via the mixing unit, wherein the mixing unit pressurizes the mixed reaction medium to a target pressure and then transfers the pressurized mixed reaction medium to the heating unit, and the heating unit heats the mixed reaction medium to a target temperature so as to convert the mixed reaction medium into a supercritical water state; a reaction unit connected to the heating unit, wherein the heating unit transports the mixed reaction medium in the supercritical water state to the reaction unit, and the reaction unit is used to perform gas-liquid separation on the mixed reaction medium in the supercritical water state, so as to separate the mixed reaction medium in the supercritical water state into a steam medium and a concentrated brine medium; A salt separation crystallization unit is connected to the reaction unit and is used to receive the concentrated brine medium. The salt separation crystallization unit can cool the concentrated brine medium to solidify and crystallize the concentrated brine medium. as well as, The power unit is connected to the reaction unit and is used to receive the steam medium. The power unit can use the steam medium to generate electricity and store the converted electrical energy to supply electrical energy to various electrical devices in the waste liquid treatment system.

2. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 1 is characterized in that: The heating unit comprises: a first heat exchange mechanism connected to the power unit, configured to receive the steam medium that has completed power generation, and wherein the heat exchange mechanism heats the mixed reaction medium obtained in the mixing unit for the first time by using the residual temperature of the steam medium; An electromagnetic heating mechanism is connected to the first heat exchange mechanism and the power unit. The electromagnetic heating mechanism can obtain electrical energy from the power unit and convert it into thermal energy, so as to reheat the mixed reaction medium that has been heated for the first time in the first heat exchange mechanism until the mixed reaction medium is converted into a supercritical water state.

3. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 2 is characterized in that: The storage unit includes: a first storage container for storing the waste liquid medium of thin consistency; a second storage container for storing the waste liquid medium of target consistency; a first waste liquid pressure pump connected to the first storage container and configured to pump the thin-viscosity waste liquid medium out of the first storage container, the first waste liquid pressure pump being electrically connected to the power unit so as to obtain electrical energy from the power unit; an evaporation and concentration mechanism connected between the first waste liquid pressure pump and the second storage container, configured to adjust the waste liquid medium of thin consistency extracted from the first storage container to a target consistency, and discharge the waste liquid medium of target consistency into the second storage container; The first heat exchange mechanism is connected to the evaporation and concentration mechanism to supply the steam medium that has completed the first heating of the mixed reaction medium to the evaporation and concentration mechanism for continued use.

4. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 3 is characterized in that: Also includes: A condensation water storage unit is connected to the evaporation and concentration mechanism and is used to receive the steam medium discharged by the evaporation and concentration mechanism. The condensation water storage unit can condense the steam medium into a reusable clean water medium and store the clean water medium to supply the clean water medium to various water-using equipment in the waste liquid treatment system.

5. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 4 is characterized in that: The condensation water storage unit comprises: a third storage container for storing a clean water medium, the third storage container being connected to the salt separation crystallization unit so as to be able to transport the clean water medium to the salt separation crystallization unit, so that the concentrated brine medium solidifies and crystallizes after being cooled by the clean water medium; a second heat exchange mechanism connected between the evaporation and concentration mechanism and the second storage container, the second heat exchange mechanism being used to condense the steam medium obtained in the evaporation and concentration mechanism into the clean water medium; a cooling mechanism connected to the second heat exchange mechanism and configured to supply a refrigerant medium to the second heat exchange mechanism; The cooling mechanism is further connected to the third storage container so as to obtain the clean water medium from the third storage container, thereby converting the clean water medium into the refrigerant medium through the cooling mechanism.

6. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 4 is characterized in that: Also includes: The oxygen supply unit is connected to the mixing unit and is used to supply the oxygen medium to the mixing unit.

7. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 6 is characterized in that: The oxygen supply unit comprises: a fourth storage container, for storing the oxygen medium in a gaseous state; an oxygen pressure pump connected between the fourth storage container and the mixing unit, the oxygen pressure pump being electrically connected to the power unit so as to obtain electrical energy from the power unit; The gas-oxygen pressure pump is used to pump the oxygen medium in the fourth storage container into the mixing unit, so that the waste liquid medium in the mixing unit is mixed with the oxygen medium in a gaseous state.

8. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 6 is characterized in that: The oxygen supply unit comprises: a fourth storage container, for storing the oxygen medium in a liquid state; a liquid oxygen pressure pump connected between the fourth storage container and the mixing unit through the salt separation and crystallization unit, the liquid oxygen pressure pump being electrically connected to the power unit so as to be able to obtain electrical energy from the power unit; In which, the liquid oxygen pressure pump can pump the oxygen medium in the fourth storage container into the salt separation crystallization unit, so that the oxygen medium and the concentrated brine medium exchange heat, and the concentrated brine medium solidifies and crystallizes after being cooled by the oxygen medium, and the oxygen medium is converted into a gaseous state with the help of the heat of the concentrated brine medium and then discharged into the mixing unit, so that the waste liquid medium in the mixing unit is mixed with the oxygen medium in a gaseous state.

9. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 6 is characterized in that: The mixing unit comprises: a second waste liquid pressure pump connected to a second storage container in the storage unit, configured to pump the waste liquid medium out of the second storage container, wherein the waste liquid medium is pressurized to a target pressure by the second waste liquid pressure pump, and the second waste liquid pressure pump is electrically connected to the power unit so as to obtain electrical energy from the power unit; a jet mixer connected between the second waste liquid pressure pump and the first heat exchange mechanism in the heating unit, the jet mixer also being connected to the oxygen supply unit; the jet mixer being capable of receiving the waste liquid medium at the target pressure in the second waste liquid pressure pump and the oxygen medium in the oxygen supply unit; the waste liquid medium and the oxygen medium are mixed through the jet mixer to form the mixed reaction medium.

10. The zero-discharge system for treating high-salt organic waste liquid based on supercritical water catalytic oxidation according to claim 9 is characterized in that: The mixing unit further comprises: a preheating and feeding mechanism connected to the second waste liquid pressure pump, the preheating and feeding mechanism being capable of feeding an organic solvent into the second waste liquid pressure pump to promote the reaction of the waste liquid medium; The preheating feeding mechanism comprises: a fifth storage container for storing the clean water medium, the fifth storage container being connected to the second waste liquid pressure pump so that the fifth storage container can deliver the clean water medium to the second waste liquid pressure pump, and the fifth storage container being further connected to the jet mixer via a micro-nano cavitation bubble generator so as to deliver a bubble medium for auxiliary cleaning to the jet mixer, and the condensation water storage unit being connected to the fifth storage container so that the condensation water storage unit can supply the clean water medium to the fifth storage container; a sixth storage container, for storing an organic solvent, wherein the sixth storage container is connected to the second waste liquid pressure pump so as to be able to transport the organic solvent to the second waste liquid pressure pump; A seventh storage container is used to store the catalyst solvent. The seventh storage container is connected to the second waste liquid pressure pump so as to be able to transport the catalyst solvent to the second waste liquid pressure pump.

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