Resource utilization method and device system for high-salt organic wastewater

Abstract

The invention relates to a resource utilization method and device system for high-salinity organic wastewater, and the resource utilization method comprises the following steps: sequentially carrying out pH value adjustment and preheating on the high-salinity organic wastewater, and then carrying out wet catalytic oxidation reaction on the high-salinity organic wastewater and an oxidant under the action of a copper-based composite metal catalyst to obtain a vapor-liquid mixture; performing first gas-liquid separation on the gas-liquid mixture to obtain a first gas phase and a first liquid phase; the first gas phase is sequentially subjected to condensation and second gas-liquid separation, a second gas phase and a second liquid phase are obtained, and the second gas phase enters a turbine to do work; and sequentially carrying out cooling, ion exchange impurity removal and solid-liquid separation on the first liquid phase, carrying out alkali washing on the obtained filtrate to obtain purified saline water, and carrying out electrolysis on the purified saline water in an ion membrane electrolysis device. According to the method, the TOC concentration and the metal ion content of the high-salt organic wastewater can be effectively reduced, the treated water meets the water inlet requirement of the ion membrane electrolysis device, and resource utilization of the high-salt organic wastewater can be achieved.

Description

Technical Field

[0001] The invention relates to the technical field of wastewater resource recovery, and in particular to a resource utilization method and device system for high-salt organic wastewater. Background Art

[0002] Epichlorohydrin is an important organic chemical raw material and is widely used in chemical, light industry, medicine, electronic and electrical industries. In the production process of epichlorohydrin, a large amount of organic wastewater that is difficult to treat and has a high salt content will inevitably be produced. At present, wet oxidation is usually used to solve the problem of treating the above wastewater. The wet oxidation treatment process usually uses an oxidant to convert organic matter in the wastewater into carbon dioxide and water under high temperature (150-350°C) and high pressure (5-20MPa) conditions, thereby removing pollutants. Compared with traditional treatment methods, the wet oxidation method has the advantages of wide application scenarios, high treatment efficiency, almost no secondary pollution, and fast oxidation speed. It is an ideal choice for treating epichlorohydrin wastewater.

[0003] CN105645624A discloses a technology for resource utilization of high-salt wastewater from epichlorohydrin preparation by glycerol process, including three operating units: catalytic wet oxidation, acetic acid recovery and catalyst recovery. The technology can reduce the TOC concentration in sodium chloride solution, but the oxidation temperature is high, the pressure is high, the equipment is seriously corrosive, and the metal in the catalyst, especially Cu 2+ The dissolution volume is large, the catalyst recovery unit is complex, and other metal ions are introduced. The resulting sodium chloride brine cannot be directly used in the electrolysis device to achieve the recycling of brine.

[0004] Therefore, developing a treatment method with low energy consumption, high treatment efficiency and the ability to realize resource utilization of epichlorohydrin wastewater is a technical problem that needs to be solved in the current field. Summary of the invention

[0005] In view of the above problems, the purpose of the present invention is to provide a method and device system for resource utilization of high-salt organic wastewater. Compared with the prior art, the present invention can effectively reduce the TOC concentration of high-salt organic wastewater and avoid the introduction of excessive metal ions. The treated water obtained meets the water inlet requirements of the ion membrane electrolysis device, can realize the resource utilization of high-salt organic wastewater, and has the advantages of high treatment efficiency and low operating energy consumption, which is conducive to industrial application.

[0006] In order to achieve the purpose of the invention, the present invention adopts the following technical solutions:

[0007] In a first aspect, the present invention provides a method for resource utilization of high-salt organic wastewater, the resource utilization method comprising the following steps:

[0008] (1) adjusting the pH value and preheating the high-salt organic wastewater in sequence, and subjecting the preheated high-salt organic wastewater and an oxidant to a wet catalytic oxidation reaction under the action of a copper-based composite metal catalyst to obtain a vapor-liquid mixture;

[0009] (2) performing a first gas-liquid separation on the vapor-liquid mixture obtained in step (1) to obtain a first gas phase and a first liquid phase;

[0010] (3) condensing the first gas phase obtained in step (2) and performing a second gas-liquid separation in sequence to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work, and the second liquid phase returns to a wet catalytic oxidation reaction;

[0011] (4) cooling the first liquid phase obtained in step (2), performing ion exchange to remove impurities, and performing solid-liquid separation in sequence, and washing the liquid phase obtained after solid-liquid separation with alkali to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis;

[0012] There is no order relationship between step (3) and step (4).

[0013] The resource utilization method provided by the present invention is aimed at high-salt organic wastewater with high alkalinity and high TOC content. First, the pH value is adjusted, and then it is preheated to the reaction temperature. Under the catalytic action of the copper-based composite metal catalyst, the oxidant is used to accelerate the oxidation of organic matter in the high-salt organic wastewater, and the organic matter is oxidized into carbon dioxide and water, etc., to obtain a gas-liquid mixture; the first gas phase after the first gas-liquid separation is condensed, and then the second gas-liquid separation is performed. The second gas phase after the second gas-liquid separation enters the turbine to do work and generates mechanical energy or electrical energy; the first liquid phase is cooled, ion exchanged, impurities removed, and solid-liquid separated in sequence, and the liquid phase after the solid-liquid separation absorbs the acidic gas contained therein through alkali washing, and finally purified brine is obtained, and the purified brine can meet the water inlet requirements of the ion membrane electrolysis device. It can be seen that the present invention can realize the resource utilization of high-salt organic wastewater, simplify the wastewater treatment process, and ensure the economy, safety and environmental protection of the treatment process.

[0014] Preferably, the high-salt organic wastewater in step (1) comprises epichlorohydrin production wastewater.

[0015] In the present invention, the resource utilization method is preferably used to treat the production wastewater of epichlorohydrin, and is particularly suitable for the production wastewater obtained from the preparation of epichlorohydrin by the glycerol method.

[0016] Preferably, the mass percentage of sodium chloride in the high-salt organic wastewater is 18-25%, for example, it can be 18%, 19%, 20%, 21%, 22%, 23%, 24% or 25%, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0017] Preferably, the TOC concentration in the high-salt organic wastewater is 5000-12000 mg / L, for example, it can be 5000 mg / L, 6000 mg / L, 7000 mg / L, 8000 mg / L, 9000 mg / L, 10000 mg / L, 11000 mg / L or 12000 mg / L, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0018] Preferably, the pH value of the high-salt organic wastewater is 9-12, for example, it can be 9, 9.5, 10, 10.5, 11, 11.5 or 12, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0019] Preferably, the end point of the pH adjustment in step (1) is 2-7, for example, 2, 3, 4, 5, 6 or 7, but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable, preferably 3-6.

[0020] Preferably, the pH value adjusting agent used includes hydrochloric acid.

[0021] Preferably, the oxidant comprises oxygen.

[0022] In the present invention, the mass concentration of oxygen is generally ≥93%.

[0023] Preferably, the temperature of the wet catalytic oxidation reaction is 150-220°C, for example, it can be 150°C, 160°C, 170°C, 180°C, 190°C, 200°C, 210°C or 220°C, but is not limited to the listed values. Other unlisted values ​​within the numerical range are also applicable, preferably 150-180°C.

[0024] Preferably, the pressure of the wet catalytic oxidation reaction is 2.2-4.0 MPa, for example, it can be 2.2 MPa, 2.4 MPa, 2.6 MPa, 2.8 MPa, 3 MPa, 3.2 MPa, 3.4 MPa, 3.6 MPa, 3.8 MPa or 4 MPa, but is not limited to the listed values. Other unlisted values ​​within the numerical range are also applicable, preferably 2.2-2.7 MPa.

[0025] Preferably, the copper-based composite metal catalyst in step (1) contains Cu and auxiliary metal elements.

[0026] Preferably, the auxiliary metal element includes any one of Ce, Fe, Ni, Zn or Al or a combination of at least two thereof, preferably a combination of Zn and Ce.

[0027] In the present invention, by controlling the addition of auxiliary metal elements, such as using a combination of Zn and Ce, the interaction between the auxiliary metal elements and Cu can be utilized, so that the active components can be uniformly dispersed on the catalyst surface and the loss of metal active centers can be suppressed, thereby overcoming the problems of complex catalyst recovery and difficult treatment of lost metal ions in existing wet oxidation catalysts, and synergistically improving the catalytic oxidation effect.

[0028] Preferably, in the copper-based composite metal catalyst, the molar ratio of the metal elements contained in the catalyst to the corresponding oxides is n(CuO):n(CeO2):n(ZnO) (0.5-1.5):(1-4):(1-6), for example, it can be 0.5:1:1, 0.8:2:3, 1.0:3:4, 1.2:4:5 or 1.5:4:6, but is not limited to the listed values. Other values ​​not listed within the numerical range are also applicable, preferably 1:(1-3):(1-2).

[0029] Preferably, the preparation method of the copper-based composite metal catalyst includes any one of a hydrothermal method, a coprecipitation method or a sol-gel method, preferably a sol-gel method.

[0030] In the present invention, the sol-gel method is preferably used to further promote the uniform mixing and dispersion of the catalyst synthesis raw materials, and form a metal nanocluster structure, which is further beneficial to avoid Cu 2+ It can prevent the dissolution and loss of auxiliary metal elements and enhance the catalytic activity of the reaction.

[0031] Preferably, the step of preparing the copper-based composite metal catalyst by the sol-gel method includes: adding citric acid and ammonia water to the metal source solution, the molar ratio of citric acid to copper ions is (0.5-2):1, the ammonia water is added to the pH value of 4-7, and then stirring at 70-90°C for 2-5h, and then filtering to obtain a gel; drying the gel at 80-100°C for 1-3h, and then calcining at 700-900°C for 2-4h to obtain a copper-based composite metal catalyst.

[0032] In the present invention, the metal source solution is a mixed solution of a copper precursor and an auxiliary metal element precursor, for example, a salt solution, and the salt solution may be a nitrate solution. In the present invention, the citric acid is generally added in the form of an aqueous solution prepared at a volume ratio of 1:1.

[0033] In the present invention, the steps of preparing the copper-based composite metal catalyst by the coprecipitation method include: mixing the metal source solution evenly to obtain a mixed solution, then slowly dripping the mixed solution into an excess Na2CO3 solution, controlling the pH value to 8-9 for coprecipitation reaction, aging at 10-40°C for 12-24h after the coprecipitation reaction is completed, then filtering, drying the obtained filter residue at 80-100°C for 8-12h, then roasting at 700-900°C for 2-5h, mixing the product evenly with the ZSM-5 carrier, and pressing the tablets to obtain a copper-based composite metal catalyst. In the present invention, the copper-based composite metal catalyst prepared by the coprecipitation method also contains a carrier, wherein the loading amount of Cu is 10-50%, preferably 15-25%.

[0034] Preferably, the wet catalytic oxidation reaction in step (1) is carried out in a microchannel reactor.

[0035] In the present invention, by preferably controlling the wet catalytic oxidation reaction to be carried out in a microchannel reactor, the mass transfer and heat transfer effects in the catalytic reaction can be enhanced compared to other catalytic oxidation devices, and the reaction conditions are milder, thereby improving the catalytic effect, reaction efficiency and safety, and reducing the energy consumption during the operation of the device.

[0036] Preferably, the residence time of the material in the microchannel reactor is 1-5 min, for example, 1 min, 2 min, 3 min, 4 min or 5 min, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0037] Preferably, a spirally curved channel structure is arranged inside the microchannel reactor.

[0038] Preferably, the material of the channel structure includes silicon carbide.

[0039] Preferably, the inner diameter of the channel structure is 1-2 mm, for example, 1 mm, 1.2 mm, 1.4 mm, 1.6 mm, 1.8 mm or 2 mm, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0040] Preferably, the effective volume of the channel structure is 20-80 mL, for example, 20 mL, 30 mL, 40 mL, 50 mL, 60 mL, 70 mL or 80 mL, but is not limited to the listed values, and other unlisted values ​​within the numerical range are also applicable.

[0041] Preferably, the copper-based composite metal catalyst is loaded into the channel structure of the microchannel reactor.

[0042] Preferably, the particle size of the copper-based composite metal catalyst in step (1) is 50-60 mesh, for example, 50 mesh, 52 mesh, 54 mesh, 56 mesh, 58 mesh or 60 mesh, but is not limited to the listed values, and other values ​​not listed within the numerical range are also applicable.

[0043] Preferably, the resin used for ion exchange impurity removal in step (4) comprises a cation exchange resin.

[0044] Preferably, the cation exchange resin comprises any one of the strongly acidic styrene-based ion exchange resins 001×7, 001×7MB or 001×7FC, or a combination of at least two thereof.

[0045] Preferably, the solid-liquid separation method includes filtration.

[0046] Preferably, the cooling method of the first liquid phase includes: preheating the high-salt organic wastewater using the first liquid phase as a heat source.

[0047] In the present invention, by preferably using the first liquid phase as a heat source to preheat the high-salt organic wastewater, the high-salt organic wastewater can be heated while the first liquid phase can be cooled, which can further improve the energy utilization rate and reduce the energy consumption of the system.

[0048] As a preferred technical solution of the first aspect of the present invention, the resource utilization method comprises the following steps:

[0049] (1) adding hydrochloric acid to the high-salt organic wastewater to adjust the pH value to 2-7, and then preheating to the reaction temperature, and subjecting the preheated high-salt organic wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 150-220° C. and a pressure of 2.2-4.0 MPa to obtain a vapor-liquid mixture;

[0050] The high-salt organic wastewater includes epichlorohydrin production wastewater, in which the mass percentage of sodium chloride is 18-25%, the TOC concentration is 5000-12000 mg / L, and the pH value is 9-12;

[0051] The copper-based composite metal catalyst contains Cu and an auxiliary metal element, wherein the auxiliary metal element includes any one of Ce, Fe, Ni, Zn or Al or a combination of at least two thereof. In the copper-based composite metal catalyst, the molar ratio of the metal elements to the oxides is n(CuO):n(CeO2):n(ZnO) is 1:(1-3):(1-2). The preparation method of the copper-based composite metal catalyst includes any one of a hydrothermal method, a coprecipitation method or a sol-gel method. The particle size of the copper-based composite metal catalyst is 50-60 meshes.

[0052] The wet catalytic oxidation reaction is carried out in a microchannel reactor, the residence time of the material in the microchannel reactor is 1-5 min, a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure includes silicon carbide, the inner diameter is 1-2 mm, and the copper-based composite metal catalyst is loaded into the channel structure of the microchannel reactor;

[0053] (2) performing a first gas-liquid separation on the vapor-liquid mixture obtained in step (1) to obtain a first gas phase and a first liquid phase;

[0054] (3) condensing the first gas phase obtained in step (2), and then performing a second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work, and the second liquid phase returns to a wet catalytic oxidation reaction;

[0055] (4) The first liquid phase obtained in step (2) is used as a heat source for preheating high-salt organic wastewater and the first liquid phase is cooled, and then ion exchange and impurity removal are performed using a cation exchange resin, followed by filtration. The filtrate is washed with alkali to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

[0056] In a second aspect, the present invention provides a high-salt organic wastewater resource utilization device system, the resource utilization device system is used for the high-salt organic wastewater resource utilization method as described in the first aspect of the present invention, the resource utilization device system comprises a high-salt organic wastewater storage device, a delivery pump, a first heat exchange device, a reactor, an oxygen production device, a first gas-liquid separator, a second heat exchange device, a second gas-liquid separator, a circulation pump, an ion exchange impurity removal device, a solid-liquid separation device, an alkali washing device, an ion membrane electrolysis device and a turbine;

[0057] Along the flow direction of the high-salt organic wastewater, the outlet of the high-salt organic wastewater storage device is connected to the cold source inlet of the first heat exchange device via a delivery pump, and the cold source outlet of the first heat exchange device is connected to the reactor;

[0058] The inlet of the reactor is also connected to an oxygen production device;

[0059] The outlet of the reactor is connected to the first gas-liquid separator;

[0060] The liquid phase outlet of the first gas-liquid separator is connected to the heat source inlet of the first heat exchange device, the heat source outlet of the first heat exchange device is connected to the ion exchange impurity removal device and the solid-liquid separation device in sequence, the liquid phase outlet of the solid-liquid separation device is connected to the alkali washing device, and the outlet of the alkali washing device is connected to the ion membrane electrolysis device;

[0061] The gas phase outlet of the first gas-liquid separator is connected to the heat source inlet of the second heat exchange device, and the heat source outlet of the second heat exchange device is connected to the second gas-liquid separator;

[0062] The gas phase outlet of the second gas-liquid separator is connected to a turbine;

[0063] The liquid phase outlet of the second gas-liquid separator is connected to the reactor via a circulation pump.

[0064] In the device system provided by the present invention, high-salt organic wastewater is stored in a storage device and its pH value is adjusted, and then sent to a cold source inlet of a first heat exchange device through a delivery pump and flows out from a cold source outlet to be preheated, the preheated high-salt organic wastewater is sent to a reactor, the reactor is pre-filled with a catalyst and a wet catalytic oxidation reaction is carried out in the reactor, the vapor-liquid mixture obtained by the reaction is sent to a first gas-liquid separator for first gas-liquid separation to obtain a first gas phase and a first liquid phase, the first gas phase is condensed through a second heat exchange device to produce condensed water, and then sent to a second gas exchange device. A second gas-liquid separation is carried out in the liquid separator to obtain a second gas phase and a second liquid phase. The second gas phase is sent to the turbine to do work, and the second liquid phase is returned to the reactor through a circulation pump; the first liquid phase enters the heat source inlet of the first heat exchange device and flows out from the heat source outlet to achieve cooling, and then enters the ion exchange impurity removal device to further remove the metal ion impurities contained therein, and then the insoluble impurities are removed by the solid-liquid separation device, and then the acidic gas in the liquid phase is absorbed by alkaline washing, and the purified brine is finally sent to the ion membrane electrolysis device, thereby realizing the resource utilization of high-salt organic wastewater.

[0065] Preferably, the reactor comprises a microchannel reactor.

[0066] Preferably, the solid-liquid separation device comprises a filtering device.

[0067] Preferably, the filtering device comprises a basket filter.

[0068] Preferably, the oxygen generator comprises a VPSA oxygen generator.

[0069] Compared with the prior art, the present invention has the following beneficial effects:

[0070] (1) The copper-based composite metal catalyst used in the resource utilization method of high-salt organic wastewater provided by the present invention has excellent catalytic activity and anti-toxicity, and can avoid Cu 2+ The present invention can control the dissolution of Cu and the loss of auxiliary metal elements under optimal conditions, and has a good service life and can be recycled. 2+ The dissolution amount of Cu is less than 20ppb, the residual amount of auxiliary metal elements is less than 30ppb, and the TOC removal rate is more than 98.0%. Under better conditions, Cu2+ The dissolution amount reaches less than 10ppb, the residual amount of auxiliary metal elements reaches less than 28ppb, and the TOC removal rate reaches more than 99.85%. The purified brine meets the water inlet requirements of the ion membrane electrolysis device, simplifies the wastewater treatment process, and realizes the resource utilization of high-salt organic wastewater, especially epichlorohydrin production wastewater.

[0071] (2) The method and device system for resource utilization of high-salt organic wastewater provided by the present invention adopts a microchannel reactor, which can enhance the mass transfer and heat transfer effects in the catalytic reaction, and the reaction conditions are milder, thereby improving the catalytic effect, reaction efficiency and safety, and reducing the energy consumption during the operation of the device.

[0072] (3) The method and device system for resource utilization of high-salt organic wastewater provided by the present invention can reduce the system's operating energy consumption and operating costs by setting up material recycling and energy recycling, which is conducive to industrial application. BRIEF DESCRIPTION OF THE DRAWINGS

[0073] Figure 1 A schematic diagram of the structure of a high-salt organic wastewater resource utilization device system provided in Example 1 of the present invention;

[0074] Among them, 1-high-salt organic wastewater storage device; 2-transfer pump; 3-first heat exchange device; 4-oxygen production device; 5-reactor; 6-first gas-liquid separator; 7-second heat exchange device; 8-second gas-liquid separator; 9-turbine; 10-circulation pump; 11-ion exchange impurity removal device; 12-solid-liquid separation device; 13-ion membrane electrolysis device; 14-alkali washing device. DETAILED DESCRIPTION

[0075] The technical solution of the present invention is further described below by specific implementation methods. It should be understood by those skilled in the art that the embodiments are only to help understand the present invention and should not be regarded as specific limitations of the present invention.

[0076] In a specific embodiment, the resource utilization method of high-salt organic wastewater provided by the present invention is carried out in a resource utilization device system of high-salt organic wastewater, such as Figure 1As shown, the resource utilization device system includes a high-salt organic wastewater storage device 1, a delivery pump 2, a first heat exchange device 3, a reactor 5, an oxygen production device 4, a first gas-liquid separator 6, a second heat exchange device 7, a second gas-liquid separator 8, a circulation pump 10, an ion exchange impurity removal device 11, a solid-liquid separation device 12, an alkali washing device 14, an ion membrane electrolysis device 13 and a turbine 9. Along the flow direction of the high-salt organic wastewater, the outlet of the high-salt organic wastewater storage device 1 is connected to the cold source inlet of the first heat exchange device 3 through the delivery pump 2, the cold source outlet of the first heat exchange device 3 is connected to the reactor 5, the inlet of the reactor 5 is also connected to the oxygen production device 4, and the outlet of the reactor 5 is connected to the first gas-liquid separator 6. The first gas-liquid separator 6 is connected to the heat source inlet of the first heat exchange device 3, the heat source outlet of the first heat exchange device 3 is connected to the ion exchange impurity removal device 11 and the solid-liquid separation device 12 in sequence, the liquid phase outlet of the solid-liquid separation device 12 is connected to the alkali washing device 14, the outlet of the alkali washing device 14 is connected to the ion membrane electrolysis device 13, the gas phase outlet of the first gas-liquid separator 6 is connected to the heat source inlet of the second heat exchange device 7, the heat source outlet of the second heat exchange device 7 is connected to the second gas-liquid separator 8, the gas phase outlet of the second gas-liquid separator 8 is connected to the turbine 9, and the liquid phase outlet of the second gas-liquid separator 8 is connected to the reactor 5 via the circulation pump 10;

[0077] The reactor 5 is a microchannel reactor, the solid-liquid separation device 12 is a basket filter, the oxygen generator 4 is a VPSA oxygen generator, and the second heat exchange device uses condensed water to condense and generate steam.

[0078] The device system provided by the present invention can simplify the wastewater treatment process, realize the resource utilization of high-salt organic wastewater, especially epichlorohydrin production wastewater, can reduce the system operation energy consumption and operation cost, and is conducive to industrial application.

[0079] In the following examples and comparative examples, water quality tests were performed on epichlorohydrin wastewater, reactor effluent and purified brine, respectively, wherein TOC was tested by supercritical oxidation method and the content of metal ions was tested by inductively coupled plasma spectrometer.

[0080] Example 1

[0081] This embodiment provides a method and device system for resource utilization of high-salt organic wastewater. The structural diagram of the device system is as follows: Figure 1As shown, the device system includes a high-salt organic wastewater storage device 1, a delivery pump 2, a first heat exchange device 3, a reactor 5, an oxygen production device 4, a first gas-liquid separator 6, a second heat exchange device 7, a second gas-liquid separator 8, a circulation pump 10, an ion exchange impurity removal device 11, a solid-liquid separation device 12, an alkali washing device 14, an ion membrane electrolysis device 13 and a turbine 9. The resource utilization method includes the following steps:

[0082] (1) epichlorohydrin wastewater is prepared by the glycerol method to obtain high-salt organic wastewater (the mass percentage of sodium chloride is 22.5%, the pH value is 9, and the TOC content is 7985 mg / L), which is stored in a high-salt organic wastewater storage device 1, and hydrochloric acid is added to adjust the pH value to 4, and then it is sent to the cold source inlet of the first heat exchange device 3 through a delivery pump 2 and flows out from the cold source outlet to be preheated to the reaction temperature, and the preheated wastewater, oxygen and a copper-based composite metal catalyst are subjected to a wet catalytic oxidation reaction at a temperature of 180° C. and a pressure of 2.7 MPa. The reactor 5 is a microchannel reactor, and the residence time of the material is 2 min. A spirally curved channel structure is arranged inside the microchannel reactor. The material of the channel structure is silicon carbide, the inner diameter is 1.2 mm, and the effective volume is 40 mL, to obtain a vapor-liquid mixture;

[0083] The copper-based composite metal catalyst contains Cu and auxiliary metal elements (Ce and Zn). In the copper-based composite metal catalyst, according to the molar ratio of the metal elements corresponding to the oxides, n(CuO):n(CeO2):n(ZnO) is 1:2:3. The preparation method of the copper-based composite metal catalyst is as follows: adding ammonia water to a mixed metal source solution composed of copper nitrate, zinc nitrate and cerium nitrate to adjust the pH value to 6, and adding citric acid at a molar ratio of citric acid to copper ions of 1:1, and then stirring at a constant temperature of 85°C in a water bath for 5h, at which time a large amount of gel appears in the solution, and then filtering and collecting the gel, and then drying the gel at 90°C for 3h, and then putting it into a muffle furnace and roasting it at 900°C for 2h to obtain a copper-based composite metal catalyst, and the particle size of the catalyst screened is 50-60 mesh and filled into a microchannel reactor;

[0084] (2) sending the vapor-liquid mixture obtained in step (1) into a first gas-liquid separator 6 for first gas-liquid separation to obtain a first gas phase and a first liquid phase;

[0085] (3) sending the first gas phase obtained in step (2) into a second heat exchange device 7 for condensation to produce condensed water, and then sending it into a second gas-liquid separator 8 for second gas-liquid separation to obtain a second gas phase and a second liquid phase, the second gas phase entering a turbine 9 to perform work to produce mechanical energy or electrical energy, and the second liquid phase returning to the reactor 5 via a circulation pump 10 to perform a wet catalytic oxidation reaction;

[0086] (4) The first liquid phase obtained in step (2) is sent to the heat source inlet of the first heat exchange device 3 as a heat source for preheating high-salt organic wastewater and flows out from the heat source outlet to cool the first liquid phase, and then sent to the ion exchange impurity removal device 11 for ion exchange impurity removal using a strong acid styrene-based ion exchange resin 001×7MB, and then sent to the solid-liquid separation device 12 for filtration to remove insoluble impurities. The obtained filtrate enters the alkaline washing device 14 for alkaline washing to absorb acidic gases to obtain purified brine, and the purified brine enters the ion membrane electrolysis device 13 for electrolysis.

[0087] The epichlorohydrin wastewater, reactor effluent and purified brine in this embodiment were tested for water quality. The results are shown in Table 1. The removal rate of TOC in this embodiment reached 99.9%.

[0088] Table 1

[0089]

[0090] In Table 1, “ / ” means that the ion is not contained.

[0091] Example 2

[0092] This embodiment provides a method and device system for resource utilization of high-salt organic wastewater. The device system is the same as that in Example 1. The resource utilization method includes the following steps:

[0093] (1) preparing epichlorohydrin wastewater by a glycerol process to obtain high-salt organic wastewater (the mass percentage of sodium chloride is 25%, the pH value is 10, and the TOC content is 7905 mg / L), storing it in a high-salt organic wastewater storage device, adding hydrochloric acid to adjust the pH value to 3, and then feeding it into a cold source inlet of a first heat exchange device through a delivery pump and flowing out from a cold source outlet to be preheated to a reaction temperature, and subjecting the preheated wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 150° C. and a pressure of 2.2 MPa, wherein the reactor is a microchannel reactor, the residence time of the material is 3 min, and a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure is silicon carbide, the inner diameter is 1 mm, and the effective volume is 20 mL, to obtain a vapor-liquid mixture;

[0094] The copper-based composite metal catalyst contains Cu and auxiliary metal elements (Ce and Zn). In the copper-based composite metal catalyst, according to the molar ratio of the metal elements corresponding to the oxides, n(CuO):n(CeO2):n(ZnO) is 1:2:2. The preparation method of the copper-based composite metal catalyst is as follows: adding ammonia water to a mixed metal source solution composed of copper nitrate, zinc nitrate and cerium nitrate to adjust the pH value to 5, and adding citric acid at a molar ratio of citric acid to copper ions of 1.2:1, and then stirring at a constant temperature of 70°C in a water bath for 3h, at which time a large amount of gel appears in the solution, and then filtering and collecting the gel, and then drying the gel at 100°C for 1h, and then putting it into a muffle furnace and roasting it at 800°C for 2h to obtain a copper-based composite metal catalyst, screening the catalyst particle size of 50-60 mesh and filling it into a microchannel reactor;

[0095] (2) sending the vapor-liquid mixture obtained in step (1) into a first gas-liquid separator for first gas-liquid separation to obtain a first gas phase and a first liquid phase;

[0096] (3) sending the first gas phase obtained in step (2) into a second heat exchange device for condensation to produce condensed water, and then sending it into a second gas-liquid separator for second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work to produce mechanical energy or electrical energy, and the second liquid phase returns to the reactor via a circulation pump for wet catalytic oxidation reaction;

[0097] (4) The first liquid phase obtained in step (2) is sent to the heat source inlet of the first heat exchange device as a heat source for preheating high-salt organic wastewater and flows out from the heat source outlet to cool the first liquid phase, and then sent to an ion exchange impurity removal device for ion exchange and impurity removal using a strong acid styrene-based ion exchange resin 001×7MB, and then sent to a solid-liquid separation device for filtration to remove insoluble impurities. The obtained filtrate enters an alkali washing device for alkali washing to absorb acidic gases to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

[0098] The epichlorohydrin wastewater, reactor effluent and purified brine in this embodiment were tested for water quality. The results are shown in Table 2. The removal rate of TOC in this embodiment reached 99.85%.

[0099] Table 2

[0100]

[0101] In Table 2, “ / ” means that the ion is not contained.

[0102] Example 3

[0103] This embodiment provides a method and device system for resource utilization of high-salt organic wastewater. The device system is the same as that in Example 1. The resource utilization method includes the following steps:

[0104] (1) preparing epichlorohydrin wastewater by a glycerol process to obtain high-salt organic wastewater (the mass percentage of sodium chloride is 21%, the pH value is 9, and the TOC content is 9732 mg / L), storing it in a high-salt organic wastewater storage device, adding hydrochloric acid to adjust the pH value to 3, and then feeding it into a cold source inlet of a first heat exchange device through a delivery pump and flowing out from a cold source outlet to be preheated to a reaction temperature, and subjecting the preheated wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 200° C. and a pressure of 3.5 MPa, wherein the reactor is a microchannel reactor, the residence time of the material is 5 min, and a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure includes silicon carbide, the inner diameter is 2 mm, and the effective volume is 80 mL, to obtain a vapor-liquid mixture;

[0105] The copper-based composite metal catalyst contains Cu and auxiliary metal elements (Ce and Zn). In the copper-based composite metal catalyst, according to the molar ratio of the metal elements corresponding to the oxides, n(CuO):n(CeO2):n(ZnO) is 2:2:3. The preparation method of the copper-based composite metal catalyst is as follows: adding ammonia water to a mixed metal source solution composed of copper nitrate, zinc nitrate and cerium nitrate to adjust the pH value to 6, and adding citric acid at a molar ratio of citric acid to copper ions of 1.5:1, and then stirring at a constant temperature of 90°C in a water bath for 3h, at which time a large amount of gel appears in the solution, and then filtering and collecting the gel, and then drying the gel at 90°C for 3h, and then putting it into a muffle furnace and roasting it at 800°C for 4h to obtain a copper-based composite metal catalyst, and the particle size of the catalyst screened is 50-60 mesh and filled into a microchannel reactor;

[0106] (2) sending the vapor-liquid mixture obtained in step (1) into a first gas-liquid separator for first gas-liquid separation to obtain a first gas phase and a first liquid phase;

[0107] (3) sending the first gas phase obtained in step (2) into a second heat exchange device for condensation to produce condensed water, and then sending it into a second gas-liquid separator for second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work to produce mechanical energy or electrical energy, and the second liquid phase returns to the reactor via a circulation pump for wet catalytic oxidation reaction;

[0108] (4) The first liquid phase obtained in step (2) is sent to the heat source inlet of the first heat exchange device as a heat source for preheating high-salt organic wastewater and flows out from the heat source outlet to cool the first liquid phase, and then sent to an ion exchange impurity removal device for ion exchange and impurity removal using a strong acid styrene-based ion exchange resin 001×7MB, and then sent to a solid-liquid separation device for filtration to remove insoluble impurities. The obtained filtrate enters an alkali washing device for alkali washing to absorb acidic gases to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

[0109] The epichlorohydrin wastewater, reactor effluent and purified brine in this embodiment were tested for water quality. The results are shown in Table 3. The removal rate of TOC in this embodiment reached 99.8%.

[0110] Table 3

[0111]

[0112] In Table 3, “ / ” means that the ion is not contained.

[0113] Example 4

[0114] This embodiment provides a method and device system for resource utilization of high-salt organic wastewater. The device system is the same as that in Example 1. The resource utilization method includes the following steps:

[0115] (1) preparing epichlorohydrin wastewater by a glycerol process to obtain high-salt organic wastewater (the mass percentage of sodium chloride is 18%, the pH value is 10, and the TOC content is 10623 mg / L), storing it in a high-salt organic wastewater storage device, adding hydrochloric acid to adjust the pH value to 4, and then feeding it into a cold source inlet of a first heat exchange device through a delivery pump and flowing out from a cold source outlet to be preheated to a reaction temperature, and subjecting the preheated wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 160° C. and a pressure of 2.5 MPa, wherein the reactor is a microchannel reactor, the residence time of the material is 4 min, and a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure includes silicon carbide, the inner diameter is 1.5 mm, and the effective volume is 60 mL, to obtain a vapor-liquid mixture;

[0116] The copper-based composite metal catalyst contains Cu and auxiliary metal elements (Al and Ce), and the molar ratio of the metal elements corresponding to the oxides in the copper-based composite metal catalyst is n(CuO):n(Al2O3):n(CeO2) is 2:4:3. The preparation method of the copper-based composite metal catalyst is as follows: slowly dripping a mixed solution of copper nitrate, aluminum nitrate and cerium nitrate into a solution containing excess Na2CO3, controlling the pH value to be 8, aging at 25°C for 24h after the coprecipitation reaction is completed, and then filtering, drying the obtained filter residue at 100°C for 8h, and then calcining at 900°C for 2h, the Cu loading is 15%, and the product is mixed evenly with a ZSM-5 carrier and then pressed into tablets, and the particle size is screened to be 50-60 meshes, and the copper-based composite metal catalyst is filled into a microchannel reactor;

[0117] (2) sending the vapor-liquid mixture obtained in step (1) into a first gas-liquid separator for first gas-liquid separation to obtain a first gas phase and a first liquid phase;

[0118] (3) sending the first gas phase obtained in step (2) into a second heat exchange device for condensation to produce condensed water, and then sending it into a second gas-liquid separator for second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work to produce mechanical energy or electrical energy, and the second liquid phase returns to the reactor via a circulation pump for wet catalytic oxidation reaction;

[0119] (4) The first liquid phase obtained in step (2) is sent to the heat source inlet of the first heat exchange device as a heat source for preheating high-salt organic wastewater and flows out from the heat source outlet to cool the first liquid phase, and then sent to an ion exchange impurity removal device for ion exchange and impurity removal using a strong acid styrene-based ion exchange resin 001×7MB, and then sent to a solid-liquid separation device for filtration to remove insoluble impurities. The obtained filtrate enters an alkali washing device for alkali washing to absorb acidic gases to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

[0120] The epichlorohydrin wastewater, reactor effluent and purified brine in this embodiment were tested for water quality. The results are shown in Table 4. The removal rate of TOC in this embodiment reached 99.5%.

[0121] Table 4

[0122]

[0123] In Table 4, “ / ” means that the ion is not contained.

[0124] Example 5

[0125] This embodiment provides a method and device system for resource utilization of high-salt organic wastewater. The device system is the same as that in Example 1. The resource utilization method includes the following steps:

[0126] (1) preparing epichlorohydrin wastewater by a glycerol process to obtain high-salt organic wastewater (the mass percentage of sodium chloride is 19.5%, the pH value is 11, and the TOC content is 8296 mg / L), storing it in a high-salt organic wastewater storage device, adding hydrochloric acid to adjust the pH value to 4, and then feeding it into a cold source inlet of a first heat exchange device through a delivery pump and flowing out from a cold source outlet to be preheated to a reaction temperature, and subjecting the preheated wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 220° C. and a pressure of 4.0 MPa, wherein the reactor is a microchannel reactor, the residence time of the material is 1 min, and a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure includes silicon carbide, the inner diameter is 1.8 mm, and the effective volume is 70 mL, to obtain a vapor-liquid mixture;

[0127] The copper-based composite metal catalyst contains Cu and auxiliary metal elements (Al and Ce), and the molar ratio of the metal elements corresponding to the oxides in the copper-based composite metal catalyst is n(CuO):n(Al2O3):n(CeO2) of 1:3:2. The preparation method of the copper-based composite metal catalyst is as follows: slowly dripping a mixed solution of copper nitrate, aluminum nitrate and cerium nitrate into a solution containing excess Na2CO3, controlling the pH value to be 8, aging at 20°C for 20h after the coprecipitation reaction is completed, and then filtering, drying the obtained filter residue at 80°C for 10h, and then calcining at 900°C for 4h, the Cu loading is 25%, and the product is mixed evenly with a ZSM-5 carrier and then pressed into tablets, and the particle size is screened to be 50-60 meshes, and the copper-based composite metal catalyst is filled into a microchannel reactor;

[0128] (2) sending the vapor-liquid mixture obtained in step (1) into a first gas-liquid separator for first gas-liquid separation to obtain a first gas phase and a first liquid phase;

[0129] (3) sending the first gas phase obtained in step (2) into a second heat exchange device for condensation to produce condensed water, and then sending it into a second gas-liquid separator for second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work to produce mechanical energy or electrical energy, and the second liquid phase returns to the reactor via a circulation pump for wet catalytic oxidation reaction;

[0130] (4) The first liquid phase obtained in step (2) is sent to the heat source inlet of the first heat exchange device as a heat source for preheating high-salt organic wastewater and flows out from the heat source outlet to cool the first liquid phase, and then sent to an ion exchange impurity removal device for ion exchange and impurity removal using a strong acid styrene-based ion exchange resin 001×7MB, and then sent to a solid-liquid separation device for filtration to remove insoluble impurities. The obtained filtrate enters an alkali washing device for alkali washing to absorb acidic gases to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

[0131] The epichlorohydrin wastewater, reactor effluent and purified brine in this embodiment were tested for water quality. The results are shown in Table 5. The removal rate of TOC in this embodiment reached 99.6%.

[0132] Table 5

[0133]

[0134] In Table 5, “ / ” means that the ion is not contained.

[0135] Example 6

[0136] This embodiment provides a method for resource utilization of high-salt organic wastewater, which is different from Embodiment 1 only in that the auxiliary metal elements are Zn and Al;

[0137] The only difference between the preparation method of the copper-based composite metal catalyst and Example 1 is that cerium nitrate is replaced by aluminum nitrate, and the molar amount of aluminum ions is controlled to be equal to the molar amount of cerium ions.

[0138] Example 7

[0139] This embodiment provides a method for resource utilization of high-salt organic wastewater, which is different from Embodiment 1 only in that the copper-based composite metal catalyst is prepared by a hydrothermal method;

[0140] The preparation method of the copper-based composite metal catalyst comprises: slowly dripping a mixed solution consisting of copper nitrate, zinc nitrate and cerium nitrate into a solution containing excess Na2CO3, controlling the pH value to be 8, aging at 25°C for 24 hours after the coprecipitation reaction is completed, filtering, drying the obtained filter residue at 90°C for 12 hours, and then roasting at 900°C for 5 hours, mixing the product with a ZSM-5 carrier evenly, and then pressing the tablets to obtain a copper-based composite metal catalyst, wherein the amounts of the copper nitrate, zinc nitrate and cerium nitrate are the same as those in Example 1, and the copper loading amount in the copper-based composite metal catalyst is 30%.

[0141] Example 8

[0142] This embodiment provides a method for resource utilization of high-salt organic wastewater. The only difference compared with Example 1 is that the molar ratio of the metal elements contained in the copper-based composite metal catalyst to the corresponding oxides is n(CuO):n(CeO2):n(ZnO) is 1:4:4.

[0143] Example 9

[0144] This embodiment provides a method for resource utilization of high-salt organic wastewater. The only difference compared with Example 1 is that the molar ratio of the metal elements contained in the copper-based composite metal catalyst to the corresponding oxides is n(CuO):n(CeO2):n(ZnO) is 1.5:2:5.

[0145] Example 10

[0146] This comparative example provides a method for treating high-salt organic wastewater. The only difference compared with Example 1 is that the microchannel reactor is replaced by a traditional intermittent wet oxidation reactor, and the reaction time is 5 hours.

[0147] Comparative Example 1

[0148] This comparative example provides a method for treating high-salt organic wastewater, which is different from Example 1 only in that the copper-based composite metal catalyst is replaced by a copper chloride catalyst with an equal molar amount of copper ions.

[0149] The water quality of the effluent from the reactor in Example 1, Examples 6-10 and Comparative Example 1 was tested respectively, and the results are shown in Table 6.

[0150] Table 6

[0151]

[0152]

[0153] The following points can be seen from the contents of Table 1-6:

[0154] (1) From the data of Examples 1-6, it can be seen that the resource utilization method provided by the present invention can control Cu under optimal conditions. 2+ The dissolution amount of Cu is less than 20ppb, the residual amount of auxiliary metal elements is less than 30ppb, and the TOC removal rate is more than 98.0%. Under better conditions, Cu 2+ The dissolution amount reaches below 10ppb, the residual amount of auxiliary metal elements reaches below 28ppb, and the TOC removal rate reaches above 99.85%.

[0155] (2) A comprehensive comparison of the data of Example 1 and Comparative Example 1 shows that the copper-based composite metal catalyst used in the present invention not only has a higher TOC removal rate than the copper chloride catalyst, but also can significantly avoid the dissolution of copper ions; the data of Example 1 and Example 6 show that the present invention can better exert the interaction between elements by preferably using a combination of Cu, Zn and Ce, especially the introduction of Ce, which can further avoid the dissolution of copper elements and auxiliary metal elements; a comprehensive comparison of the data of Example 1 and Example 7 shows that the present invention preferably uses a sol-gel method to prepare the catalyst. Compared with the hydrothermal method, the sol-gel method can synthesize a catalyst with a metal nanocluster structure, which can further avoid Cu 2+ It can reduce the dissolution and loss of auxiliary metal elements and improve the removal effect of TOC.

[0156] (3) Comprehensive comparison of the data of Example 1 and Examples 8-9 shows that the present invention can further promote the interaction between Cu, Zn and Ce by preferentially controlling the molar ratio of n(CuO):n(CeO2):n(ZnO), so that the active components can be uniformly dispersed on the catalyst surface and the loss of metal active centers can be inhibited, thereby further improving the TOC removal effect and reducing the residues of copper and auxiliary metal elements.

[0157] (4) A comprehensive comparison of the data of Example 1 and Example 10 shows that the present invention preferably controls the use of a microchannel reactor. Compared with a conventional intermittent wet oxidation reactor, not only is the reaction time shorter than that of a conventional reactor, but a higher TOC removal rate can also be achieved.

[0158] In summary, the present invention can effectively reduce the TOC concentration and metal ion content of high-salt organic wastewater, and the obtained treated water meets the water inlet requirements of the ion membrane electrolysis device, and can realize the resource utilization of high-salt organic wastewater.

[0159] The applicant declares that the above is only a specific implementation mode of the present invention, but the protection scope of the present invention is not limited thereto. Those skilled in the art should understand that any changes or substitutions that can be easily thought of by those skilled in the art within the technical scope disclosed by the present invention shall fall within the protection scope and disclosure scope of the present invention.

Claims

1. A method for resource utilization of high-salt organic wastewater, characterized in that: The resource utilization method comprises the following steps: (1) adjusting the pH value and preheating the high-salt organic wastewater in sequence, and subjecting the preheated high-salt organic wastewater and an oxidant to a wet catalytic oxidation reaction under the action of a copper-based composite metal catalyst to obtain a vapor-liquid mixture; (2) performing a first gas-liquid separation on the vapor-liquid mixture obtained in step (1) to obtain a first gas phase and a first liquid phase; (3) condensing the first gas phase obtained in step (2) and performing a second gas-liquid separation in sequence to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work, and the second liquid phase returns to a wet catalytic oxidation reaction; (4) cooling the first liquid phase obtained in step (2), performing ion exchange to remove impurities, and performing solid-liquid separation in sequence, and washing the liquid phase obtained after solid-liquid separation with alkali to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis; There is no order relationship between step (3) and step (4).

2. The resource utilization method according to claim 1, characterized in that: The high-salt organic wastewater in step (1) includes epichlorohydrin production wastewater; Preferably, the mass percentage of sodium chloride in the high-salt organic wastewater is 18-25%; Preferably, the TOC concentration in the high-salt organic wastewater is 5000-12000 mg / L; Preferably, the pH value of the high-salt organic wastewater is 9-12.

3. The resource utilization method according to claim 1 or 2, characterized in that: The end point of the pH adjustment in step (1) is 2-7, preferably 3-6; Preferably, the pH value adjusting agent used comprises hydrochloric acid; Preferably, the oxidant comprises oxygen; Preferably, the temperature of the wet catalytic oxidation reaction is 150-220°C, preferably 150-180°C; Preferably, the pressure of the wet catalytic oxidation reaction is 2.2-4.0 MPa, preferably 2.2-2.7 MPa.

4. The resource utilization method according to any one of claims 1 to 3, characterized in that: The copper-based composite metal catalyst in step (1) contains Cu and an auxiliary metal element; Preferably, the auxiliary metal element includes any one or a combination of at least two of Ce, Fe, Ni, Zn or Al, preferably a combination of Zn and Ce; Preferably, in the copper-based composite metal catalyst, the molar ratio of the metal elements to the oxides contained is n(CuO):n(CeO2):n(ZnO) is (0.5-1.5):(1-4):(1-6), preferably 1:(1-3):(1-2); Preferably, the preparation method of the copper-based composite metal catalyst includes any one of a hydrothermal method, a coprecipitation method or a sol-gel method, preferably a sol-gel method.

5. The resource utilization method according to any one of claims 1 to 4, characterized in that: The wet catalytic oxidation reaction in step (1) is carried out in a microchannel reactor; Preferably, the residence time of the material in the microchannel reactor is 1-5 min; Preferably, a spirally curved channel structure is provided inside the microchannel reactor; Preferably, the material of the channel structure includes silicon carbide; Preferably, the inner diameter of the channel structure is 1-2 mm; Preferably, the copper-based composite metal catalyst is loaded into the channel structure of the microchannel reactor.

6. The resource utilization method according to any one of claims 1 to 5, characterized in that: The particle size of the copper-based composite metal catalyst in step (1) is 50-60 mesh.

7. The resource utilization method according to any one of claims 1 to 6, characterized in that: The resin used for ion exchange impurity removal in step (4) includes a cation exchange resin; Preferably, the cation exchange resin comprises any one of the strongly acidic styrene ion exchange resins 001×7, 001×7MB or 001×7FC, or a combination of at least two thereof; Preferably, the solid-liquid separation method includes filtration; Preferably, the cooling method of the first liquid phase includes: preheating the high-salt organic wastewater using the first liquid phase as a heat source.

8. The resource utilization method according to any one of claims 1 to 7, characterized in that: The resource utilization method comprises the following steps: (1) adding hydrochloric acid to the high-salt organic wastewater to adjust the pH value to 2-7, and then preheating to the reaction temperature, and subjecting the preheated high-salt organic wastewater, oxygen and a copper-based composite metal catalyst to a wet catalytic oxidation reaction at a temperature of 150-220° C. and a pressure of 2.2-4.0 MPa to obtain a vapor-liquid mixture; The high-salt organic wastewater includes epichlorohydrin production wastewater, in which the mass percentage of sodium chloride is 18-25%, the TOC concentration is 5000-12000 mg / L, and the pH value is 9-12; The copper-based composite metal catalyst contains Cu and an auxiliary metal element, wherein the auxiliary metal element includes any one of Ce, Fe, Ni, Zn or Al or a combination of at least two thereof. In the copper-based composite metal catalyst, the molar ratio of the metal elements to the oxides is n(CuO):n(CeO2):n(ZnO) is 1:(1-3):(1-2). The preparation method of the copper-based composite metal catalyst includes any one of a hydrothermal method, a coprecipitation method or a sol-gel method. The particle size of the copper-based composite metal catalyst is 50-60 meshes. The wet catalytic oxidation reaction is carried out in a microchannel reactor, the residence time of the material in the microchannel reactor is 1-5 min, a spirally curved channel structure is arranged inside the microchannel reactor, the material of the channel structure includes silicon carbide, the inner diameter is 1-2 mm, and the copper-based composite metal catalyst is loaded into the channel structure of the microchannel reactor; (2) performing a first gas-liquid separation on the vapor-liquid mixture obtained in step (1) to obtain a first gas phase and a first liquid phase; (3) condensing the first gas phase obtained in step (2), and then performing a second gas-liquid separation to obtain a second gas phase and a second liquid phase, wherein the second gas phase enters a turbine to perform work, and the second liquid phase returns to a wet catalytic oxidation reaction; (4) The first liquid phase obtained in step (2) is used as a heat source for preheating high-salt organic wastewater and the first liquid phase is cooled, and then ion exchange and impurity removal are performed using a cation exchange resin, followed by filtration. The filtrate is washed with alkali to obtain purified brine, and the purified brine enters an ion membrane electrolysis device for electrolysis.

9. A resource utilization device system for high-salt organic wastewater, characterized in that: The resource utilization device system is used for the resource utilization method of high-salt organic wastewater as claimed in any one of claims 1 to 8, and the resource utilization device system comprises a high-salt organic wastewater storage device, a delivery pump, a first heat exchange device, a reactor, an oxygen production device, a first gas-liquid separator, a second heat exchange device, a second gas-liquid separator, a circulation pump, an ion exchange impurity removal device, a solid-liquid separation device, an alkali washing device, an ion membrane electrolysis device and a turbine; Along the flow direction of the high-salt organic wastewater, the outlet of the high-salt organic wastewater storage device is connected to the cold source inlet of the first heat exchange device via a delivery pump, and the cold source outlet of the first heat exchange device is connected to the reactor; The inlet of the reactor is also connected to an oxygen production device; The outlet of the reactor is connected to the first gas-liquid separator; The liquid phase outlet of the first gas-liquid separator is connected to the heat source inlet of the first heat exchange device, the heat source outlet of the first heat exchange device is connected to the ion exchange impurity removal device and the solid-liquid separation device in sequence, the liquid phase outlet of the solid-liquid separation device is connected to the alkali washing device, and the outlet of the alkali washing device is connected to the ion membrane electrolysis device; The gas phase outlet of the first gas-liquid separator is connected to the heat source inlet of the second heat exchange device, and the heat source outlet of the second heat exchange device is connected to the second gas-liquid separator; The gas phase outlet of the second gas-liquid separator is connected to a turbine; The liquid phase outlet of the second gas-liquid separator is connected to the reactor via a circulation pump.

10. The resource utilization device system according to claim 9, characterized in that: The reactor comprises a microchannel reactor; Preferably, the solid-liquid separation device comprises a filtering device; Preferably, the filtering device comprises a basket filter; Preferably, the oxygen generator comprises a VPSA oxygen generator.

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