Organic waste liquid treatment system

Abstract

The invention relates to the technical field of waste liquid treatment, and provides an organic waste liquid treatment system, which comprises an oxidation salt elimination device, a pressure reduction energy storage unit, a three-phase separator, an evaporation precipitator and a crystallizer, the depressurization energy storage unit is connected with a reactant outlet of the oxidation salt elimination device through a pipeline, and the depressurization energy storage unit is electrically connected with the feeding unit; the depressurization energy storage unit is connected to the inlet end of the three-phase separator through a pipeline, a liquid phase outlet of the three-phase separator is connected with the evaporation precipitator through a pipeline, and a gas phase outlet of the three-phase separator is connected with the evaporation precipitator and the crystallizer through pipelines. A liquid outlet of the evaporation precipitator is connected with the crystallizer through a pipeline, and a liquid outlet of the crystallizer is connected with the feeding unit through a pipeline. The method realizes inorganic treatment of organic matters in the wastewater and wastewater resource recycling, and meanwhile, salt is subjected to crystallization recycling, so that the environmental protection property of waste liquid discharge is improved.

Description

Technical Field

[0001] The invention relates to the technical field of waste liquid treatment, and in particular to a treatment system for organic waste liquid. Background Art

[0002] The chemical, pharmaceutical, petrochemical and other industries produce a large amount of high-salt organic waste liquid or organic waste liquid containing a high proportion of heteroatoms every year. The treatment of these waste liquids is a major problem in the environmental protection industry and is often treated as hazardous waste. Incineration technology is mostly used in existing technologies, but the salt in the high-salt waste liquid during the incineration process seriously corrodes the equipment and seriously reduces the life of the equipment. Supercritical water oxidation technology can effectively treat organic matter in waste liquid, but because most salts have extremely low solubility in supercritical water, equipment corrosion and salt precipitation blockage problems occur frequently, and continuous and stable operation cannot be achieved.

[0003] At present, a large amount of cooling water is usually introduced into the reactor outlet to cool the supercritical water to the subcritical temperature and redissolve the salt. This is effective in avoiding salt precipitation blockage, but it can only achieve the purpose of inorganicization of organic waste liquid. Moreover, the large amount of cooling water added will increase the amount of salt water produced, resulting in waste liquid discharge causing pollution to the environment. Summary of the invention

[0004] The problem solved by the invention is how to improve the environmental protection of waste liquid discharge.

[0005] In order to solve the above problems, the present invention provides a system for treating organic waste liquid.

[0006] In a first aspect, the present invention provides a system for treating organic waste liquid, comprising an oxidation and salt removal device, a feeding unit, a pressure reduction energy storage unit, a three-phase separator, an evaporation precipitator and a crystallizer;

[0007] The feed unit is connected to the reactant inlet of the oxidation and salt removal device through a pipeline, the inlet end of the step-down energy storage unit is connected to the reactant outlet of the oxidation and salt removal device through a pipeline, and the step-down energy storage unit is also electrically connected to the feed unit, and the step-down energy storage unit is used to convert the heat energy of the waste liquid discharged from the reactant outlet of the oxidation and salt removal device into electrical energy for storage, and provide electrical energy for the feed unit;

[0008] The outlet end of the step-down energy storage unit is connected to the inlet end of the three-phase separator through a pipeline, the liquid phase outlet of the three-phase separator is connected to the evaporative precipitator through a pipeline, the gas phase outlet of the three-phase separator is connected to the evaporative precipitator and the crystallizer through pipelines, respectively, the evaporative precipitator is used to perform salt precipitation on the waste liquid discharged from the liquid phase outlet of the three-phase separator according to the steam discharged from the gas phase outlet of the three-phase separator, the liquid outlet of the evaporative precipitator is connected to the crystallizer through a pipeline, and is used to discharge the supernatant generated after the salt precipitation into the crystallizer, and the crystallizer is used to perform salt crystallization on the supernatant discharged from the liquid outlet of the evaporative precipitator according to the steam discharged from the gas phase outlet of the three-phase separator;

[0009] The liquid outlet of the crystallizer is connected to the feed unit through a pipeline, so as to provide condensed water to the feed unit.

[0010] Optionally, the oxidation and salt removal device includes a reactor and a particle separator, the reactor is used to perform a supercritical water oxidation reaction, salt precipitation particles are arranged in the reactor, the salt precipitation particles are used to precipitate inorganic salts in the waste liquid after the oxidation reaction, the inlet of the particle separator is connected to the particle outlet of the reactor, the particle separator is provided with a particle outlet and a drain outlet, and the particle separator is used to separate salt water and the salt precipitation particles;

[0011] The reactor is provided with a reactant inlet and a reactant outlet. The reactant inlet is connected to the feed unit through a pipeline, and the reactant outlet is connected to the inlet end of the step-down energy storage unit through a pipeline.

[0012] Optionally, two oxidation and salt removal devices are provided, one of which is a main device and the other is a backup device;

[0013] The organic waste liquid treatment system also includes a three-way feed valve, a first three-way valve, a second three-way valve, a feed pipeline, a main discharge pipeline and a spare discharge pipeline, the feed pipeline is connected between the feed unit, the feed port of the main device and the feed port of the spare device, the three-way feed valve is arranged on the feed pipeline, the main discharge pipeline is connected between the reactant outlet of the main device, the inlet end of the step-down energy storage unit and the discharge port of the spare device, the first three-way valve is arranged on the main discharge pipeline, the spare discharge pipeline is connected between the reactant outlet of the standby device, the inlet end of the step-down energy storage unit and the feed port of the main device, and the second three-way valve is arranged on the spare discharge pipeline.

[0014] Optionally, the organic waste liquid treatment system also includes a particle conveyor and a particle valve, one end of the particle conveyor is connected to the particle outlet through a pipeline, and the other end of the particle conveyor is connected to the reactant outlet of the reactor through a pipeline, and the particle valve is arranged between the particle conveyor and the reactant outlet of the reactor, and the particle conveyor is used to convey the salt-precipitated particles discharged from the particle outlet to the reactor.

[0015] Optionally, the organic waste liquid treatment system also includes a drain valve, a brine tank and a salt separation unit, wherein both ends of the drain valve are respectively connected to the drain outlet and the inlet of the brine tank through pipelines, the outlet of the brine tank is connected to the salt separation unit through a pipeline, the salt separation unit is used to separate the brine discharged from the outlet, the salt separation unit is connected to the crystallizer through a pipeline, and the crystallizer is used to crystallize the salt separated brine.

[0016] Optionally, the organic waste liquid treatment system further comprises a condensate tank, the inlet of the condensate tank is connected to the liquid outlet of the crystallizer and the liquid outlet of the evaporation-precipitation device via a pipeline, and the outlet of the condensate tank is connected to the feed unit via a pipeline.

[0017] Optionally, the feed unit includes an oxidant pump, a gas heater, a start-up fuel pump, a waste liquid inlet valve and a mixed feed pump, one end of the oxidant pump is connected to the reactant inlet of the oxidation and salt removal device through a pipeline, and the other end is connected to the oxidant material source through a pipeline, and the gas heater is arranged between the oxidant pump and the oxidation and salt removal device;

[0018] The inlet of the starting fuel pump is connected to the starting fuel source through a pipeline, the inlet of the waste liquid inlet valve is connected to the waste liquid source, one end of the mixed feed pump is connected to the outlet of the starting fuel pump and the outlet of the waste liquid inlet valve through a pipeline, and the other end is connected to the reactant inlet of the oxidation and salt removal device through a pipeline.

[0019] Optionally, the evaporator-precipitator includes a low-temperature evaporation unit and a precipitation separation unit, the inlet of the low-temperature evaporation unit is respectively connected to the liquid phase outlet of the three-phase separator and the gas phase outlet of the three-phase separator, the low-temperature evaporation unit is used to evaporate and concentrate the waste liquid discharged from the liquid phase outlet of the three-phase separator according to the steam discharged from the gas phase outlet of the three-phase separator, the outlet of the low-temperature evaporation unit is connected to the inlet of the precipitation separation unit, the outlet of the precipitation separation unit is connected to the condensed water tank, and the precipitation separation unit is used to precipitate and separate the waste liquid after evaporation and concentration.

[0020] Optionally, the organic waste liquid treatment system also includes a pH detector, a cooling water pump and an alkali liquid pump, the pH detector is arranged between the pressure-reducing energy storage unit and the three-phase separator, the alkali liquid pump is connected to the cooling water pump and the alkali liquid source through a pipeline, the pH detector is electrically connected to the alkali liquid pump, and the outlet of the cooling water pump is connected to the cooling water inlet of the oxidation and salt removal device through a pipeline.

[0021] Optionally, the oxidation and salt removal device further comprises a differential pressure gauge and a temperature gauge, wherein the differential pressure gauge is connected between the reactant inlet of the oxidation and salt removal device and the reactant outlet of the oxidation and salt removal device, and the temperature gauge is arranged at the reactant inlet of the oxidation and salt removal device.

[0022] The beneficial effect of the treatment system of organic waste liquid of the present invention is that a feed unit is connected to the reactant inlet of the oxidation and desalination device through a pipeline to provide waste liquid and reaction materials for the supercritical water oxidation reaction of the oxidation and desalination device. The oxidation and desalination device performs a primary oxidation reaction and desalination on the waste liquid, and performs a primary treatment on the waste liquid. A step-down energy storage unit is provided to be connected to the reactant outlet of the oxidation and salt removal device through a pipeline, and the step-down energy storage unit is electrically connected to the feeding unit. The step-down energy storage unit reduces the pressure and temperature of the high-temperature and high-pressure waste liquid discharged from the oxidation and salt removal device, and converts the high pressure and high temperature into electrical energy for storage, so as to drive the feeding unit to operate, and recover and resource the high-temperature and high-pressure energy. The step-down energy storage unit is connected to the inlet end of the three-phase separator through a pipeline, the liquid phase outlet of the three-phase separator is connected to the evaporative precipitator through a pipeline, and the gas phase outlet of the three-phase separator is connected to the evaporative precipitator and the crystallizer through pipelines respectively. The evaporative precipitator uses the steam discharged from the gas phase outlet of the three-phase separator to precipitate salt in the waste liquid discharged from the liquid phase outlet of the three-phase separator, and the liquid outlet of the evaporative precipitator is connected to the crystallizer through a pipeline. The supernatant generated by the salt precipitation in the evaporative precipitator is discharged into the crystallizer, and the crystallizer uses the steam discharged from the gas phase outlet of the three-phase separator to further crystallize the salt in the supernatant, and further removes salt from the waste liquid after the supercritical oxidation reaction. The liquid outlet of the crystallizer is connected to the feed unit through a pipeline, and the gathered and generated condensed water is introduced into the feed unit to provide raw materials for the supercritical water oxidation reaction, achieving zero wastewater discharge and resource recycling. At the same time, the salt is crystallized and resourced to improve the environmental friendliness of waste liquid discharge. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a schematic structural diagram of an organic waste liquid treatment system according to an embodiment of the present invention.

[0024] Description of reference numerals:

[0025] 1-oxidation and salt removal device; 101-main device; 102-backup device;

[0026] 1.2-reactor; 1.21-salt precipitating particles;

[0027] 1.3- Particle separator;

[0028] 1.4-Differential pressure gauge;

[0029] 2- step-down energy storage unit; 3- three-phase separator;

[0030] 4-evaporation precipitator; 4.1-low temperature evaporation unit; 4.2-precipitation separation unit;

[0031] 5-crystallizer; 6-three-way feed valve; 7-first three-way valve; 8-second three-way valve; 9-particle conveyor; 10-particle valve; 11-drain valve; 12-brine tank; 13-salt separation unit; 14-condensate tank; 15-PH detector; 16-cooling water pump; 17-alkali liquid pump;

[0032] 18-feeding unit; 18.1-oxidant pump; 18.2-gas heater; 18.3-starting fuel pump; 18.4-waste liquid inlet valve; 18.5-mixed feed pump. DETAILED DESCRIPTION

[0033] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the specific embodiments of the present invention are described in detail below in conjunction with the accompanying drawings. Although certain embodiments of the present invention are shown in the accompanying drawings, it should be understood that the present invention can be implemented in various forms and should not be interpreted as being limited to the embodiments described herein. On the contrary, these embodiments are provided to provide a more thorough and complete understanding of the present invention. It should be understood that the drawings and embodiments of the present invention are only for exemplary purposes and are not intended to limit the scope of protection of the present invention.

[0034] The term "including" and its variations used in this document are open inclusions, that is, "including but not limited to"; the term "based on" means "based at least in part on"; the term "one embodiment" means "at least one embodiment"; the term "another embodiment" means "at least one other embodiment"; the term "some embodiments" means "at least some embodiments"; the term "optionally" means "optional embodiments". The relevant definitions of other terms will be given in the following description. It should be noted that the concepts of "first", "second", etc. mentioned in the present invention are only used to distinguish different devices, modules or units, and are not used to limit the order or interdependence of the functions performed by these devices, modules or units.

[0035] It should be noted that the modifications of "one" and "plurality" mentioned in the present invention are illustrative rather than restrictive, and those skilled in the art should understand that, unless otherwise clearly indicated in the context, it should be understood as "one or more".

[0036] In the related art, salts are divided into first-class salts and second-class salts according to their solubility in supercritical water. The first-class salts have higher solubility in supercritical water and can precipitate in supercritical water, such as K 3 PO 4 , KNO 3 This type of salt accounts for a very small proportion, while the second type of salt, which accounts for the majority, has extremely low solubility in supercritical reactions, such as KCl, Na 2 SO 4 Such salts are very likely to precipitate and adhere to the inner wall of the reactor during the subsequent discharge of waste liquid, causing corrosion and scaling, which can easily cause damage or blockage of the export pipeline, etc., and the discharge of higher concentrations of brine will damage the environment.

[0037] like Figure 1 As shown, in view of the problems existing in the above-mentioned related technologies, this embodiment provides a treatment system for organic waste liquid, including an oxidation and salt removal device 1, a feeding unit 18, a pressure reduction energy storage unit 2, a three-phase separator 3, an evaporation precipitator 4 and a crystallizer 5;

[0038] The feeding unit 18 is connected to the reactant inlet of the oxidation and salt removal device 1 through a pipeline, and the inlet end of the step-down energy storage unit 2 is connected to the reactant outlet of the oxidation and salt removal device 1 through a pipeline. The step-down energy storage unit 2 is also electrically connected to the feeding unit 18. The step-down energy storage unit 2 is used to convert the thermal energy of the waste liquid discharged from the reactant outlet of the oxidation and salt removal device 1 into electrical energy for storage, and to provide electrical energy for the feeding unit 18.

[0039] Specifically, the oxidation and salt removal device 1 is an integrated device for supercritical water oxidation reaction and salt removal. In the oxidation and salt removal device 1, the waste liquid is subjected to supercritical water oxidation reaction, and the precipitated second type of salt is filtered and discharged to achieve primary salt removal. In a preferred embodiment, the oxidation and salt removal device 1 may include a supercritical water oxidation reaction unit and a salt removal unit. The supercritical water oxidation reaction unit performs a supercritical water oxidation reaction on the waste liquid, and discharges the precipitated first type of salt or brine into the salt removal unit, and filters or precipitates the second type of salt to achieve the discharge of the second type of salt.

[0040] The feed unit 18 is connected to the reactant inlet of the oxidation and desalination device 1 through a pipeline to provide the oxidation and desalination device 1 with waste liquid and related materials for supercritical oxidation reaction, such as water, oxygen, precious metal catalyst, low-ignition-point organic matter, etc. In a preferred embodiment, the feed unit 18 may include an oxygen injector for injecting oxygen into the oxidation and desalination device 1, and may include a catalyst injector for injecting a catalyst into the oxidation and desalination device 1.

[0041] The supercritical oxidation reaction will produce high temperature and high pressure, and its temperature usually reaches 600-700°C, and the pressure reaches more than 23MPa. After the waste liquid undergoes supercritical oxidation reaction in the oxidation and salt removal device 1, the insoluble second type of salt has been removed, and the waste at the reactant outlet is still in a supercritical state, that is, when discharged from the reactant outlet of the oxidation and salt removal device 1, the waste liquid still maintains a high temperature and a high pressure, for example, it can still maintain a supercritical water oxidation reaction of 600°C-700°C. If it is discharged directly, the high temperature and high pressure of the waste liquid may cause damage to subsequent devices or pipelines and leakage of waste liquid. A step-down energy storage unit 2 is set to be connected to the reactant outlet of the oxidation and salt removal device 1. When the waste liquid after the supercritical oxidation reaction flows through the step-down energy storage unit 2, the step-down energy storage unit 2 will reduce the pressure and temperature of the waste liquid, and convert the high temperature and high pressure into electrical energy for storage, so as to provide electrical energy for devices that need electrical energy in the system, such as the waste liquid pump in the feed unit 18, or to provide electrical energy for other fields such as factories. Preferably, the step-down energy storage unit 2 may be a steam turbine generator, a supercritical steam power generation system, or the like.

[0042] The outlet end of the step-down energy storage unit 2 is connected to the inlet end of the three-phase separator 3 through a pipeline, the liquid phase outlet of the three-phase separator 3 is connected to the evaporative precipitator 4 through a pipeline, and the gas phase outlet of the three-phase separator 3 is connected to the evaporative precipitator 4 and the crystallizer 5 through pipelines, respectively. The evaporative precipitator 4 is used to perform salt precipitation on the waste liquid discharged from the liquid phase outlet of the three-phase separator 3 according to the steam discharged from the gas phase outlet of the three-phase separator 3, and the liquid outlet of the evaporative precipitator is connected to the crystallizer through a pipeline, and is used to discharge the supernatant and condensed water generated after the salt precipitation into the crystallizer, and the crystallizer is used to perform salt crystallization on the supernatant discharged from the liquid outlet of the evaporative precipitator according to the steam discharged from the gas phase outlet of the three-phase separator.

[0043] The liquid outlet of the crystallizer is connected to the feed unit through a pipeline, so as to provide condensed water to the feed unit.

[0044] Specifically, a three-phase separator 3 is provided to be connected to the outlet end of the step-down energy storage unit 2 to perform three-phase separation on the waste liquid after the temperature and pressure reduction treatment. The solid outlet of the three-phase separator 3 can be connected to a salt collection box to collect the solid salt in the waste liquid. It should be noted that since the oxidation and salt removal device 1 has already performed the initial salt removal on the waste liquid, the solid content of the waste liquid flowing into the three-phase separator 3 is very small, mainly a trace amount of metal oxides and particulate products. Therefore, a salt collection box is provided at its solid outlet to collect the solid salt, and it can be cleaned regularly; the liquid phase outlet of the three-phase separator 3 is connected to the evaporative precipitator 4, which evaporates and precipitates the salt in the waste liquid after the supercritical oxidation reaction, for example, by adding a corresponding precipitant (the type of precipitant is determined according to the type of salt) to evaporate and precipitate the precipitable and separable salt therein. The by-product salt 1 is obtained by precipitating the waste liquid. A salt collecting box can be set at the bottom of the evaporation precipitator 4 to collect the salt, or the evaporation precipitator 4 can be cleaned regularly. When the evaporation precipitator 4 evaporates and precipitates the waste liquid, a large amount of supernatant or distilled water will be produced. The liquid outlet of the evaporation precipitator 4 is connected to the crystallizer 5. The distilled water and supernatant produced by the evaporation precipitator 4 flow into the crystallizer 5 for collection. The supernatant is further crystallized to produce by-product salt 3. The gas phase outlet of the three-phase separator 3 is connected to the evaporation precipitator 4 and the crystallizer 5 respectively. The gas phase product includes a large amount of high-temperature water vapor and residual air. The high-temperature steam enters the evaporation precipitator 4 and the crystallizer 5 as a steam heat source for the evaporation precipitation of the salt and the crystallization of the salt. The crystallizer 5 is connected to the feed unit 18. The crystallizer 5 passes the collected distilled water and the distilled water produced by the crystallizer 5 itself through the salt crystallization into the feed unit 18 to provide a water source for the supercritical water oxidation reaction of the oxidation and salt removal device 1.

[0045] In this embodiment, a feed unit 18 is provided to be connected to the reactant inlet of the oxidation and salt removal device 1 through a pipeline, so as to provide waste liquid and reactant materials for the supercritical water oxidation reaction of the oxidation and salt removal device 1. A step-down energy storage unit 2 is provided to be connected to the reactant outlet of the oxidation and salt removal device 1 through a pipeline, and the step-down energy storage unit 2 is electrically connected to the feed unit 18. The step-down energy storage unit 2 reduces the pressure and temperature of the high-temperature and high-pressure waste liquid discharged from the oxidation and salt removal device 1, and converts the high pressure and high temperature into electrical energy for storage, so as to drive the feed unit 18 (such as an oxygen pump, a heating pump, etc.) to operate, and recover and resource the high-temperature and high-pressure energy. The step-down energy storage unit 2 is connected to the inlet end of the three-phase separator 3 through a pipeline, and the liquid phase outlet of the three-phase separator 3 is connected to the evaporation precipitator 4 through a pipeline. The three-phase The gas phase outlet of the separator 3 is connected to the evaporation precipitator 4 and the crystallizer 5 through pipelines. The evaporation precipitator 4 uses the steam discharged from the gas phase outlet of the three-phase separator 3 to precipitate salt in the waste liquid discharged from the liquid phase outlet of the three-phase separator 3. The liquid outlet of the evaporation precipitator 4 is connected to the crystallizer 5 through a pipeline. The supernatant and condensed water produced by the salt precipitation in the evaporation precipitator 4 are discharged into the crystallizer 5. The crystallizer 5 uses the steam discharged from the gas phase outlet of the three-phase separator 3 to further crystallize the salt in the supernatant, and further discharge the salt from the waste liquid after the supercritical oxidation reaction. The liquid outlet of the crystallizer 5 is connected to the feed unit 18 through a pipeline, and the produced water is converted into condensed water. The condensed water generated is collected and passed into the feed unit 18 to provide raw materials for the supercritical water oxidation reaction, realize zero wastewater discharge and resource reuse, and at the same time, the salt is crystallized and resourced to improve the environmental protection of waste liquid discharge.

[0046] Alternatively, if Figure 1 As shown, the oxidation and salt removal device 1 includes a reactor 1.2 and a particle separator 1.3. The reactor 1.2 is used for supercritical water oxidation reaction. Salt precipitation particles 1.21 are arranged in the reactor 1.2. The salt precipitation particles 1.21 are used to precipitate inorganic salts in the waste liquid after the oxidation reaction. The inlet of the particle separator 1.3 is connected to the particle outlet of the reactor 1.2. The particle separator 1.3 is provided with a particle outlet and a drain outlet. The particle separator 1.3 is used to separate brine and the salt precipitation particles 1.21.

[0047] The reactor 1.2 is provided with a reactant inlet and a reactant outlet. The reactant inlet is connected to the feed unit 18 through a pipeline, and the reactant outlet is connected to the inlet end of the step-down energy storage unit 2 through a pipeline.

[0048] Specifically, the oxidation and salt removal device 1 includes a reactor 1.2 and a particle separator 1.3. Salt precipitation particles 1.21 are arranged in the reactor 1.2. When the feeding unit 18 passes the waste liquid into the reactor 1.2 from the reactant inlet, after the waste liquid undergoes a supercritical water oxidation reaction, the salt precipitation particles 1.21 at the bottom layer precipitate the second type of salt that is insoluble in supercritical water and enrich it on the surface of the salt precipitation particles 1.21. After the supercritical water oxidation reaction is completed, the salt precipitation particles 1.21 enriched with the second type of salt are discharged into the particle separator 1.3, or cooling water is passed into the reactor 1.2 to clean the microsphere particles, so that the enriched second type of salt is dissolved in water to form brine, and then discharged into the particle separator 1.3 together with the salt precipitation particles 1.2 for further cleaning and separation. A particle outlet and a drain outlet are provided on the particle separator 1.3. The particle separator 1.3 is used to separate brine and the salt-precipitating particles 1.21. For example, a sieve plate can be set in the middle position of the particle separator 1.3. The diameter of the sieve holes of the sieve plate is smaller than the diameter of the salt-precipitating particles 1.21. Since the precipitated solid inorganic salt has a small volume, the solid inorganic salt or brine can directly fall into the bottom of the particle separator 1.3 through the sieve holes and be discharged through the drain outlet. The salt-precipitating particles 1.21 are filtered onto the sieve plate and discharged through the particle outlet.

[0049] In addition, a compressed air port can be provided at the top of the particle separator 1.3, and the microsphere separation salt dissolving device can be sprayed into the particle separator 1.3 to disturb the microsphere particles, prevent the particles from sticking together, and make the catalyst microsphere particles with smaller particles fall into the lower layer through the sieve plate to achieve the separation of the microsphere particles. An exhaust port can also be provided at the top of the particle separator 1.3, and a pressure relief valve can be connected. When the salt precipitation particles 1.21 are discharged into the particle separator 1.3, the pressure relief valve needs to be opened to release the pressure. When the pressure of the reactor 1.2 is released to 5-10MPa, it is in a safe state.

[0050] In addition, catalyst particles may be arranged in the reactor 1.2 to further completely oxidize the residual small organic molecules that are difficult to degrade in the waste liquid, and the waste liquid may also be discharged into the particle separator 1.3 for further cleaning and separation so as to be recycled and reused.

[0051] The reactor 1.2 and the particle separator 1.3 can be connected via a particle discharge device, for example, the particle discharge device has a switchable orifice plate at the upper end and a multifunctional valve group with adjustable switch and opening at the lower end, and the two can be controlled separately.

[0052] Alternatively, if Figure 1 As shown, two oxidation and salt removal devices 1 are provided, one of the oxidation and salt removal devices 1 is a main device 101 , and the other oxidation and salt removal device 1 is a backup device 102 .

[0053] The organic waste liquid treatment system also includes a three-way feed valve 6, a first three-way valve 7, a second three-way valve 8, a feed pipeline, a main discharge pipeline and a spare discharge pipeline. The feed pipeline is connected between the feed unit 18, the feed port of the main device 101 and the discharge port of the spare device 102. The three-way feed valve 6 is arranged on the feed pipeline, the main discharge pipeline is connected between the reactant outlet of the main device 101, the inlet end of the step-down energy storage unit 2 and the feed port of the spare device 102, the first three-way valve 7 is arranged on the main discharge pipeline, the spare discharge pipeline is connected between the reactant outlet of the spare device 102, the inlet end of the step-down energy storage unit 2 and the feed port of the main device 101, and the second three-way valve 8 is arranged on the spare discharge pipeline.

[0054] Specifically, long-term operation of an oxidation and desalination device 1 may cause malfunction or accumulation of impurities, requiring shutdown for repair or cleaning, which affects the waste liquid treatment efficiency. Therefore, a main device 101 and a backup device 102 are set. When the main device 101 runs for a long time, the supercritical water oxidation reaction and desalination can be gradually switched to the backup equipment for operation online without shutdown. While ensuring the waste liquid treatment efficiency, the main device 101 can be repaired or cleaned.

[0055] The method of switching from the main device 101 to the backup device 102 includes:

[0056] When the main device 101 is running, the three-way feed valve 6 on the feed pipeline faces the reactant inlet direction of the main device 101 and the feed unit 18, the first three-way valve 7 on the main discharge pipeline faces the pressure-reducing energy storage unit 2 and the reactant outlet direction of the main device 101, and the second three-way valve 8 on the standby discharge pipeline faces the reactant outlet direction of the standby device 102 and the reactant inlet direction of the main device 101. The feed unit 18 injects waste liquid into the main device 101 through the three-way feed valve 6 to perform a supercritical water oxidation reaction. The waste liquid after the reaction is discharged from the reactant outlet, flows through the first three-way valve 7, and then flows into the pressure-reducing energy storage unit;

[0057] When switching from the main device 101 to the backup device 102, the second discharge valve 8 on the backup discharge pipeline is switched from the feed port direction of the main device 101 to the direction of the step-down energy storage unit 2, and the first discharge valve 7 on the feed pipeline is gradually switched from the feed port direction of the main device 101 to the reactant inlet direction of the backup device 102. The backup device is preheated using the high-temperature and high-pressure waste liquid discharged from the main device 101, so that the switching process between the main device 101 and the backup device 102 eliminates the need for pressurization and preheating time and energy costs, and the switching is smooth, ensuring continuous and stable operation of the system. When the preheating is completed, for example, when the temperature in the backup device reaches 380°C and meets the conditions for the supercritical water oxidation reaction, the three-way feed valve 6 is switched from the reactant inlet direction of the main device 101 to the reactant inlet direction of the backup device 102, and the waste liquid is injected into the backup device 102 to carry out the supercritical water oxidation reaction;

[0058] The operation of the main device 101 is stopped, and the main device 101 is repaired or cleaned.

[0059] On the contrary, the method for switching from the backup device 102 to the main device 101 is not described here.

[0060] Optionally, the organic waste liquid treatment system also includes a particle conveyor 9 and a particle valve 10, one end of the particle conveyor 9 is connected to the particle outlet through a pipeline, and the other end of the particle conveyor 9 is connected to the reactant outlet of the reactor 1.2 through a pipeline, and the particle valve 10 is arranged between the particle conveyor 9 and the reactant outlet of the reactor 1.2, and the particle conveyor 9 is used to convey the salt precipitation particles 1.21 discharged from the particle outlet to the reactor 1.2.

[0061] Specifically, the particle valve 10 is connected to the particle outlet of the particle separator 1.3, and the valve port size can be adjusted to facilitate particle feeding or feeding suspension. One end of the particle conveyor 9 is connected to the particle valve 10, and the other end 8 is connected to the reactant outlet of the oxidation and salt removal device 1. When the main device 101 is cleaned, the salt-precipitated particles 1.21 cleaned in the particle separator 1.3 pass through the particle valve 10 and are then conveyed by the particle conveyor 9 to the reactor 1.2 of the main device 101, so that when the main device 101 is operated again, the waste liquid is salted, and the salt-precipitated particles 1.21 are cleaned and reused.

[0062] Additionally, a particle three-way valve may be provided between the particle conveyor 9, the reactant outlet of the main device 101 and the reactant outlet of the backup device 102 to adjust the injection direction of the salt precipitation particles 1.21.

[0063] Optionally, the organic waste liquid treatment system also includes a drain valve 11, a brine tank 12 and a salt separation unit 13, the two ends of the drain valve 11 are respectively connected to the drain port and the inlet of the brine tank 12 through pipelines, the outlet of the brine tank 12 is connected to the salt separation unit 13 through a pipeline, the salt separation unit 13 is used to separate the brine discharged from the discharge port, the salt separation unit 13 is connected to the crystallizer 5 through a pipeline, and the crystallizer 5 is used to crystallize the salt separated brine.

[0064] Specifically, the brine containing the second type of salt discharged from the particle separator 1.3 is discharged through the drain port set at the bottom of the particle separator 1.3, flows through the drain valve 11 and enters the brine tank 12 for temporary storage, and the brine in the brine tank 12 flows into the salt separation unit 13, and the salt separation unit 13 uses a membrane method, a thermal method or a precipitation method to separate the salt, and obtains the by-product salt 2, which is discharged and collected through the discharge port set at the bottom of the salt separation unit 13, or cleaned regularly. The separated salt solution enters the crystallizer 5, and the steam discharged from the gas phase outlet of the three-phase separator 4 is used as a heat source to crystallize the salt solution again to obtain the by-product salt 4, etc. The by-product salt produced can be recycled after washing, drying and other steps.

[0065] Optionally, the organic waste liquid treatment system also includes a condensate tank 14, the inlet of the condensate tank 14 is connected to the liquid outlet of the crystallizer 5 and the liquid outlet of the evaporative precipitator 4 through a pipeline, and the condensate generated by the crystallizer 5 and the evaporative precipitator 4 can be temporarily stored in the condensate tank 14, and the outlet of the condensate tank 14 is connected to the feeding unit 18 through a pipeline to provide raw materials for the oxidation and salt removal device 1.

[0066] Optionally, the feeding unit 18 includes an oxidant pump 18.1, a gas heater 18.2, a starting fuel pump 18.3, a waste liquid inlet valve 18.4 and a mixed feed pump 18.5, one end of the oxidant pump 18.1 is connected to the reactant inlet of the oxidation and salt removal device 1 through a pipeline, and the other end is connected to the oxidant material source through a pipeline, and the gas heater 18.2 is arranged between the oxidant pump 18.1 and the oxidation and salt removal device 1.

[0067] The inlet of the starting fuel pump 18.3 is connected to the starting fuel source through a pipeline, the inlet of the waste liquid inlet valve 18.4 is connected to the waste liquid source, one end of the mixed feed pump 18.5 is connected to the inlet of the starting fuel pump 18.3 and the inlet of the waste liquid inlet valve 18.4 through a pipeline, and the other end is connected to the reactant inlet of the oxidation and salt removal device 1 through a pipeline.

[0068] Specifically, the supercritical water oxidation reaction requires a certain temperature and reaction medium, and the reaction medium includes water, oxidant, start-up fuel, etc. The oxidant is pressurized by the oxidant pump 18.1 and enters the gas heater 18.2 for preheating, and enters the reactor 1.2. When the air in the reactor 1.2 is preheated to above 400°C, the start-up fuel is mixed with a small amount of low-pressure cooling water (or condensed water) and waste liquid by the start-up fuel pump 18.3 using the mixed feed pump 18.5 and then enters the reactor 1.2 to perform the supercritical water oxidation reaction.

[0069] Optionally, the evaporation precipitator 4 includes a low-temperature evaporation unit 4.1 and a precipitation separation unit 4.2, the inlet of the low-temperature evaporation unit 4.1 is connected to the liquid phase outlet of the three-phase separator 3 and the gas phase outlet of the three-phase separator 3 respectively, the low-temperature evaporation unit 4.1 is used to evaporate and concentrate the waste liquid discharged from the liquid phase outlet of the three-phase separator 3 according to the steam discharged from the gas phase outlet of the three-phase separator 3, and an exhaust port is provided on the low-temperature evaporation unit 4.1 so as to discharge without a condenser. The outlet of the low-temperature evaporation unit 4.1 is connected to the inlet of the precipitation separation unit 4.2, the outlet of the precipitation separation unit 4.2 is connected to the condensed water tank 14, and the precipitation separation unit 4.2 is used to precipitate and separate the waste liquid after evaporation and concentration to produce by-product salt 1.

[0070] Specifically, if the liquid product does not contain the first type of salt, it can be directly reused after meeting the standards. If the liquid product still contains a small amount of the first type of salt, it enters the low-temperature evaporation unit 4.1 and is concentrated using the hot steam from the three-phase separator 3. The generated distilled water is reused in the plant, and the concentrated water (concentration factor is greater than 10) enters the precipitation separation unit 4.2, where the corresponding precipitant (the precipitant is determined according to the salt type) is added to recover the salt resources that can be precipitated and separated to form by-product salt 1.

[0071] Optionally, the organic waste liquid treatment system also includes a pH detector 15, a cooling water pump 16 and an alkali liquid pump 17, the pH detector 15 is arranged between the pressure-reducing energy storage unit 2 and the three-phase separator 3, the alkali liquid pump 17 is connected to the cooling water pump 16 and the alkali liquid source through a pipeline, the pH detector 15 is electrically connected to the alkali liquid pump 17, and the outlet of the cooling water pump 16 is connected to the cooling water inlet of the oxidation and salt removal device 1 through a pipeline.

[0072] Specifically, when treating the waste liquid, some alkali solution is usually added to neutralize it so as to perform salt precipitation treatment on the waste liquid. Therefore, an alkali solution pump 17 is provided to control the amount of alkali solution injected into the reactor 1.2. At the same time, when the reactor 1.2 is undergoing supercritical water oxidation reaction, the temperature inside the reactor 1.2 will rise. Therefore, a cooling water inlet is introduced into the reactor 1.2, and a cooling water pump 16 is provided to control the speed or amount of cooling water entering the reactor 1.2. The cooling water pump 16 is connected to the alkali solution pump 17, and the alkali solution and cooling water are neutralized and then injected into the reactor 1.2. The alkali solution component is potassium hydroxide or sodium hydroxide or other components, which are selected according to the salt cations and separation requirements in the actual waste liquid.

[0073] The pH detector 15 is disposed between the step-down energy storage unit 2 and the three-phase separator 3 , and can monitor the pH value of the waste liquid at any time when the waste liquid is treated, and control the alkali liquid injection amount of the alkali liquid pump 17 according to the pH value.

[0074] Optionally, the oxidation and salt removal device 1 also includes a differential pressure gauge 1.4 and a thermometer, wherein the differential pressure gauge 1.4 is connected between the reactant inlet of the oxidation and salt removal device 1 and the reactant outlet of the oxidation and salt removal device 1, and the thermometer is arranged at the reactant inlet and outlet of the oxidation and salt removal device 1 to detect the temperature and pressure difference in the reactor 1.2 at any time, and to switch the backup device 102 in time to avoid damage to the oxidation and salt removal device 1 due to excessive operation time.

[0075] In addition, if Figure 1 As shown, the reactor 1.2 of this embodiment is divided into zones by water-permeable pipes to obtain supercritical water oxidation reaction zone A, salt precipitation zone B and catalytic zone C. The salt precipitation particles 1.21 are arranged in zone B to precipitate salt on the waste liquid after the supercritical water oxidation reaction. The waste liquid after salt precipitation undergoes a catalytic reaction again in zone C and flows out of the reactor 1.2 from the reactant outlet, wherein a baffle is provided in zone C to prevent solid salt from flowing out of the reactor 1.2, and its cooling water can enter zones A and C through water-permeable pipes and form a water film on the tube wall, thereby preventing salt from adhering to the tube wall and corroding the tube wall while cooling the interior of the reactor 1.2.

[0076] It should be noted that the three-way valve with a closed position used in the system can also be replaced by two cut-off valves on the two outlet branches. The branch switching can be achieved by opening and closing the two valves, and the incoming flow can be blocked by closing the two valves at the same time.

[0077] This embodiment uses organic phosphorus waste liquid containing potassium chloride and potassium sulfate to illustrate the operation method of the treatment system of organic waste liquid:

[0078] Startup phase:

[0079] The oxidation reaction is carried out in the main device 101. The oxidant is pressurized by the oxidant pump 18.1 and enters the gas heater 18.2 for preheating, and then is injected into the reactor 1.2 of the main device 102. A small amount of cooling water is injected into the reactor through the cooling water pump 16. After the air in the reactor is preheated to above 400°C, the start-up fuel is mixed with a small amount of low-pressure cooling water or condensed water through the start-up fuel pump 18.3 and injected into the reactor 1.2 through the mixed feed pump 18.5. Supercritical water oxidation reaction occurs rapidly in the A zone of the reactor 1.2, so that the temperature of the reactor is rapidly increased. A small amount of cooling water penetrates into the A zone through the inner permeable pipe of the reactor 1.2, and most of the cooling water penetrates into the C zone through the outer permeable pipe, reducing the temperature and corrosion of the permeable pipe wall, and at the same time reducing the reaction temperature of the C zone. The pH detector automatically controls the alkali liquid pump 17 to add alkali liquid potassium hydroxide, and the waste liquid meets potassium hydroxide to produce the first type of salt potassium phosphate, and the cooling water pump 16 injects cooling water into the reactor 1.2. Gradually increase the amount of cooling water and start-up fuel, and reach the supercritical water oxidation condition in the reactor 1.2. Subsequently, the waste liquid feed amount is continuously increased by adjusting the waste liquid inlet valve 18.4, and the start-up fuel amount is gradually adjusted to reduce the start-up fuel amount by starting the fuel pump 18.3 until it is completely replaced by waste liquid, and enters the stable operation stage of waste liquid treatment. During the waste liquid treatment operation stage, the temperature in zone A reaches 600-700°C, and the pressure reaches above 23MPa. An efficient supercritical water oxidation reaction occurs, oxidizing the organic matter in the waste liquid into water, carbon dioxide and inorganic salts. After the material completes the reaction in zone A, it enters zone B. First, the second type of salt insoluble in supercritical water is precipitated and enriched on the surface of the salt precipitation particles 1.21 through the salt precipitation particles 1.21 at the bottom of zone B, and then the catalyst particles on the top layer of zone B are used to further thoroughly oxidize the residual difficult-to-degrade organic small molecules in the waste liquid. After the waste liquid enters zone C, the temperature is lowered to a certain extent due to the presence of cooling water, but the supercritical water oxidation reaction at 400°C to 450°C can still be maintained. After the residual salt is further intercepted by the baffle, the product fluid flows out of the reactor 1.2 and flows into the pressure-reducing energy storage unit 2 through the first three-way valve 7, converting the high pressure of the fluid into electrical energy for storage and reuse within the plant. The product fluid after pressure reduction enters the gas three-phase separator 3 for separation. The solid phase product is mainly a trace amount of metal oxides and particulate products, which are discharged regularly after deposition. The gas phase product still contains a large amount of high-temperature water vapor and residual air, which serves as a steam heat source for subsequent low-temperature evaporation and crystallization. If the liquid phase product does not contain the first type of salt, it can be directly reused after meeting the standards. If the liquid phase product still contains a small amount of the first type of salt, it enters the low-temperature evaporation unit 4.1 and is concentrated using the hot steam from the three-phase separator 3. The distilled water produced is reused in the plant. The concentrated concentrated water (concentration multiple greater than 10) enters the precipitation separation unit 4.2, where calcium chloride is added to recover the by-product calcium phosphate that can be precipitated and separated. The supernatant potassium chloride solution is transferred to the crystallizer 5 to produce by-product potassium sulfate salt.

[0080] Switching stage of oxidation salt precipitation device 1:

[0081] As salts accumulate in area B of the reactor 1.2, the pressure difference of the fluid passing through area B gradually increases. When the value of the pressure difference table 1.4 rises to the set value 1, the device switching begins. The second discharge valve 8 on the standby discharge pipeline is switched from the feed port direction of the main device 101 to the direction of the step-down energy storage unit 2, and the first discharge valve 7 on the feed pipeline is gradually switched from the feed port direction of the main device 101 to the reactant inlet direction of the standby device 102. The standby device is preheated using the high-temperature and high-pressure waste liquid discharged from the main device 101. The cooling water pump 16 connected to the standby device 102 passes a small amount of cooling water into the standby device 102. After the preheating is completed, for example, when the temperature in the standby device reaches 380°C and the conditions for the supercritical water oxidation reaction are met, the three-way feed valve 6 is switched from the reactant inlet direction of the main device 101 to the reactant inlet direction of the standby device 102, and waste liquid is injected into the standby device 102. A small amount of waste liquid enters the A zone of the reactor 1.2 of the standby device 102 after mixing with the oxidant and the outflow product of the main device 101, and a supercritical water oxidation reaction occurs after mixing, releasing heat, so that the standby device The temperature of zone A of device 102 rises, and the oxidant and waste liquid injected into the standby device 102 by the three-way feed valve 6 are gradually increased. During this period, the cooling water pump 16 connected to the main device 101 and the standby device 102 is automatically controlled to increase or decrease the amount of cooling water introduced by the cooling water pump 16 according to the reaction temperature of zone C, until all the waste liquid is cut into the standby device 102, the first discharge valve 7, the alkali liquid pump 17 connected to the main device 101 and the cooling water pump 16 connected to the main device 101 are closed, and the pH detector 15 is switched to automatically control the amount of alkali liquid added by the alkali liquid pump connected to the standby device 102. Then the standby device 102 is operated as the main reactor.

[0082] Salt removal stage:

[0083] When the backup device 102 completes the switch, the pressure relief valve connected to the main device 101 is opened, and the multifunctional valve group in the particle discharge device is gradually opened to gradually release the pressure on the reactor 1.2 of the main device 101, and the pressure relief gas is discharged through the pressure relief valve. After the pressure relief is completed, the multifunctional valve group is closed, and the cooling water pump 16 connected to the main device 101 is started to pass a certain amount of cooling water to clean and soak the water permeable pipe of the reactor 1.2 and the residual salt in the inner cavity of the reactor 1.2 and the salt precipitation particles 1.21. After the salt is dissolved, the multifunctional valve group is opened, and the concentrated brine flows into the particle separator 1.3 and is injected into the brine tank 12 through the drain valve 11. . The salt discharge and cleaning of the main device 101 are completed. Subsequently, the main device 101 and the backup device 102 are automatically switched online at any time to ensure the continuous and stable operation of the system.

[0084] The second type of high-concentration brine entering the brine tank 12 is temporarily stored, and then flows into the salt separation unit for nanofiltration salt separation, and potassium sulfate solution and potassium chloride solution are separated and enter the crystallizer 5. The steam of the three-phase separator 3 and the electric energy of the step-down energy storage unit are used as heat sources. The potassium chloride solution is directly mixed with the supernatant discharged from the precipitation separation unit 4.2 for crystallization to obtain by-product potassium chloride salt. The potassium sulfate solution is crystallized to obtain by-product potassium sulfate salt. The produced potassium chloride salt and potassium sulfate salt are washed, dried and other links to realize resource utilization.

[0085] It should be noted that after the same oxidation salt precipitation device has been used, discharged and cleaned for 3 to 5 times, the particles need to be thoroughly cleaned to prevent particle adhesion. The thorough particle cleaning process is carried out after the reactor is switched. The pressure relief valve is opened, and the multifunctional valve group in the particle discharge device is gradually opened to preliminarily relieve the pressure of the reactor 1.2 of the oxidation salt precipitation device 1. When the pressure of the reactor 1.2 is 5 to 10 MPa, the multifunctional valve and orifice plate are fully opened, and the salt precipitation particles 1.21 are discharged into the microsphere separator 1.3 with the help of the residual pressure of the reactor 1.2. A certain amount of cooling water is introduced by the cooling water pump 16 to clean the residual salt in the water permeable pipe of the reactor 1.2 and the residual salt in the inner cavity of the reactor 1.2 and the salt precipitation particles 1.21, and then flow into the microsphere separator 1.3 to clean and dissolve the salt on the salt precipitation particles 1.21. The formed highly concentrated brine is discharged from the brine outlet through the drain valve 11 into the brine tank 12. Close the pressure relief valve, open the compressed air shut-off valve, and spray into the microsphere separator 1.3 intermittently multiple times to disturb the salt precipitating particles 1.21 to achieve separation of the salt precipitating particles. Repeat the cleaning process and the purge process 2 to 3 times to complete the particle regeneration and separation. The cleaned and separated salt precipitating particles 1.21 are transported back to the main device 101 by the particle conveyor 9 via the particle valve 10, where the particle conveyor 9 is shared by the two devices.

[0086] Although the present invention is disclosed as above, the protection scope of the present invention is not limited thereto. Those skilled in the art may make various changes and modifications without departing from the spirit and scope of the present invention, and these changes and modifications will fall within the protection scope of the present invention.

Claims

1. A system for treating organic waste liquid, characterized in that: It comprises an oxidation and salt removal device (1), a feed unit (18), a pressure-reducing energy storage unit (2), a three-phase separator (3), an evaporation precipitator (4) and a crystallizer (5); The feed unit (18) is connected to the reactant inlet of the oxidation and salt removal device (1) via a pipeline, the inlet end of the pressure-reducing energy storage unit (2) is connected to the reactant outlet of the oxidation and salt removal device (1) via a pipeline, the pressure-reducing energy storage unit (2) is also electrically connected to the feed unit (18), and the pressure-reducing energy storage unit (2) is used to convert the heat energy of the waste liquid discharged from the reactant outlet of the oxidation and salt removal device (1) into electrical energy for storage, and to provide electrical energy for the feed unit (18); The outlet end of the step-down energy storage unit (2) is connected to the inlet end of the three-phase separator (3) through a pipeline, the liquid phase outlet of the three-phase separator (3) is connected to the evaporative precipitator (4) through a pipeline, the gas phase outlet of the three-phase separator (3) is connected to the evaporative precipitator (4) and the crystallizer (5) through pipelines respectively, the evaporative precipitator (4) is used to perform salt precipitation on the waste liquid discharged from the liquid phase outlet of the three-phase separator (3) according to the steam discharged from the gas phase outlet of the three-phase separator (3), the liquid outlet of the evaporative precipitator (4) is connected to the crystallizer (5) through a pipeline, and is used to discharge the supernatant generated after the salt precipitation into the crystallizer (5), and the crystallizer (5) is used to perform salt crystallization on the supernatant discharged from the liquid outlet of the evaporative precipitator (4) according to the steam discharged from the gas phase outlet of the three-phase separator (3); The liquid outlet of the crystallizer (5) is connected to the feed unit (18) via a pipeline, so as to provide condensed water to the feed unit (18).

2. The organic waste liquid treatment system according to claim 1, characterized in that: The oxidation and salt removal device (1) comprises a reactor (1.2) and a particle separator (1.3); the reactor (1.2) is used for performing a supercritical water oxidation reaction; salt precipitation particles (1.21) are arranged in the reactor (1.2); the salt precipitation particles (1.21) are used for precipitating inorganic salts in waste liquid after the oxidation reaction; the inlet of the particle separator (1.3) is connected to the particle outlet of the reactor (1.2); the particle separator (1.3) is provided with a particle outlet and a drain outlet; the particle separator (1.3) is used for separating salt water and the salt precipitation particles (1.21); The reactor (1.2) is provided with a reactant inlet and a reactant outlet. The reactant inlet is connected to the feed unit (18) via a pipeline, and the reactant outlet is connected to the inlet end of the pressure-reducing energy storage unit (2) via a pipeline.

3. The organic waste liquid treatment system according to claim 2, characterized in that: The oxidation and salt removal devices (1) are provided with two, one of the oxidation and salt removal devices (1) is a main device (101), and the other oxidation and salt removal device (1) is a backup device (102); The organic waste liquid treatment system further comprises a three-way feed valve (6), a first three-way valve (7), a second three-way valve (8), a feed pipeline, a main discharge pipeline and a spare discharge pipeline, wherein the feed pipeline is connected between the feed unit (18), the feed port of the main device (101) and the feed port of the spare device (102); the three-way feed valve (6) is arranged on the feed pipeline; the main discharge pipeline is connected between the reactant outlet of the main device (101), the inlet end of the step-down energy storage unit (2) and the discharge port of the spare device (102); the first three-way valve (7) is arranged on the main discharge pipeline; the spare discharge pipeline is connected between the reactant outlet of the spare device (102), the inlet end of the step-down energy storage unit (2) and the feed port of the main device (101); and the second three-way valve (8) is arranged on the spare discharge pipeline.

4. The organic waste liquid treatment system according to claim 2, characterized in that: The invention also comprises a particle conveyor (9) and a particle valve (10); one end of the particle conveyor (9) is connected to the particle outlet via a pipeline, and the other end of the particle conveyor (9) is connected to the reactant outlet of the reactor (1.2) via a pipeline; the particle valve (10) is arranged between the particle conveyor (9) and the reactant outlet of the reactor (1.2); the particle conveyor (9) is used to convey the salt precipitation particles (1.21) discharged from the particle outlet to the reactor (1.2).

5. The organic waste liquid treatment system according to claim 2, characterized in that: The invention also comprises a drain valve (11), a salt water tank (12) and a salt separation unit (13); the two ends of the drain valve (11) are respectively connected to the drain port and the inlet of the salt water tank (12) through pipelines; the outlet of the salt water tank (12) is connected to the salt separation unit (13) through a pipeline; the salt separation unit (13) is used to separate salt from the salt water discharged from the drain port; the salt separation unit (13) is connected to the crystallizer (5) through a pipeline; and the crystallizer (5) is used to separate and crystallize the salt water after separation.

6. The organic waste liquid treatment system according to claim 1, characterized in that: It also includes a condensate tank (14), the inlet of which is connected to the liquid outlet of the crystallizer (5) and the liquid outlet of the evaporation precipitator (4) through a pipeline, and the outlet of the condensate tank (14) is connected to the feed unit (18) through a pipeline.

7. The organic waste liquid treatment system according to claim 6, characterized in that: The feed unit (18) comprises an oxidant pump (18.1), a gas heater (18.2), a starter fuel pump (18.3), a waste liquid inlet valve (18.4) and a mixed feed pump (18.5); one end of the oxidant pump (18.1) is connected to the reactant inlet of the oxidation and salt removal device (1) through a pipeline, and the other end is connected to the oxidant material source through a pipeline; the gas heater (18.2) is arranged between the oxidant pump (18.1) and the oxidation and salt removal device (1); The inlet of the starting fuel pump (18.3) is connected to the starting fuel source through a pipeline, the inlet of the waste liquid inlet valve (18.4) is connected to the waste liquid source, one end of the mixed feed pump (18.5) is connected to the outlet of the starting fuel pump (18.3) and the outlet of the waste liquid inlet valve (18.4) through a pipeline, and the other end is connected to the reactant inlet of the oxidation and salt removal device (1) through a pipeline.

8. The organic waste liquid treatment system according to claim 6, characterized in that: The evaporation precipitator (4) comprises a low-temperature evaporation unit (4.1) and a precipitation separation unit (4.2); the inlet of the low-temperature evaporation unit (4.1) is respectively connected to the liquid phase outlet of the three-phase separator (3) and the gas phase outlet of the three-phase separator (3); the low-temperature evaporation unit (4.1) is used to evaporate and concentrate the waste liquid discharged from the liquid phase outlet of the three-phase separator (3) according to the steam discharged from the gas phase outlet of the three-phase separator (3); the outlet of the low-temperature evaporation unit (4.1) is connected to the inlet of the precipitation separation unit (4.2); the outlet of the precipitation separation unit (4.2) is connected to the condensed water tank (14); and the precipitation separation unit (4.2) is used to precipitate and separate the waste liquid after evaporation and concentration.

9. The organic waste liquid treatment system according to claim 1, characterized in that: It also includes a pH detector (15), a cooling water pump (16) and an alkali liquid pump (17), wherein the pH detector (15) is arranged between the pressure-reducing energy storage unit (2) and the three-phase separator (3), the alkali liquid pump (17) is connected to the cooling water pump (16) and an alkali liquid source via a pipeline, the pH detector (15) is electrically connected to the alkali liquid pump (17), and the outlet of the cooling water pump (16) is connected to the cooling water inlet of the oxidation and salt removal device (1) via a pipeline.

10. The organic waste liquid treatment system according to claim 1, characterized in that: The oxidation and salt removal device (1) further comprises a differential pressure gauge (1.4) and a temperature gauge, wherein the differential pressure gauge (1.4) is connected between the reactant inlet of the oxidation and salt removal device (1) and the reactant outlet of the oxidation and salt removal device (1), and the temperature gauge is arranged at the lower part of the reactant inlet of the oxidation and salt removal device (1).

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