Fenton reactor, application thereof and method for treating DMSO wastewater

Abstract

The invention relates to the field of wastewater treatment, and discloses a Fenton reactor and application thereof and a method for treating DMSO wastewater, the Fenton reactor comprises a shell, a catalyst filling column, a filter part and a heat source, the shell surrounds a defined reaction cavity and is provided with a material inlet and a material outlet; the catalyst filling column is positioned in the reaction cavity and is used for filling a Fenton catalyst; the filter piece is sleeved in the catalyst filling fence, and a discharge part of the filter piece is communicated with the material outlet; the heat source is used for providing heat required by reaction. The method has the characteristics of simple process, low cost, high treatment depth, zero emission and the like.

Description

Technical Field

[0001] The invention relates to the field of wastewater treatment, in particular to a Fenton reactor and an application thereof and a method for treating DMSO wastewater. Background Art

[0002] The Fenton process has unique advantages in treating refractory organic pollutants. The generated OH is the strongest inorganic oxidant except for fluorine. The oxidation product is generally CO 2 and water, is a wastewater treatment technology with great application prospects. For the traditional Fenton reaction, it can only show excellent degradation performance under acidic conditions, and it is necessary to continuously adjust the pH value of the wastewater, consuming a large amount of acid; at the same time, it is necessary to add excess iron salts and hydrogen peroxide. After the reaction is completed, there will still be a large amount of iron salts and iron sludge in the wastewater, which is difficult to carry out subsequent treatment and easily causes secondary pollution of the water body. In order to reduce secondary pollution and the generation of iron sludge, domestic and foreign researchers have proposed the preparation of heterogeneous Fenton reaction catalysts for heterogeneous Fenton reaction, that is, biomass materials or inorganic materials are used as carriers to carry out Fe 2+ , Fe 3+ Or solidify the iron oxide so that it is evenly dispersed on the surface of the carrier, which can reduce the amount of iron ions in the solution after the reaction, avoid secondary pollution and reduce costs.

[0003] CN105948216A proposes an airlift heterogeneous Fenton reactor, which allows homogeneous and heterogeneous Fenton reactions to occur simultaneously; CN113044950A discloses a heterogeneous Fenton reactor, in which the catalyst can rotate along the rotating shaft; CN205151957U discloses a heterogeneous Fenton reactor, which utilizes the flow state of wastewater in the reactor to fully mix the reagents; CN205258186U provides a heterogeneous Fenton reactor that can achieve uninterrupted continuous Fenton reaction. When the heterogeneous Fenton reactor in the prior art is used in sewage treatment, it has the disadvantages of easy loss of catalyst, sludge generation, high degradation efficiency and treatment cost. At present, the operating cost of a single heterogeneous Fenton process is still higher than that of the existing conventional homogeneous Fenton, and it has not yet been widely promoted to practical applications. Summary of the invention

[0004] The purpose of the present invention is to overcome the problems of easy loss of catalyst, sludge generation, low degradation efficiency and high treatment cost when the heterogeneous Fenton reactor in the prior art is used for sewage treatment, and to provide a Fenton reactor and its application and a method for treating DMSO wastewater, which have the characteristics of simple process, low cost, high treatment depth and zero emission.

[0005] In order to achieve the above object, the present invention provides a Fenton reactor on one hand, wherein the Fenton reactor comprises:

[0006] A shell, the shell surrounds the defined reaction chamber and is provided with a material inlet and a material outlet;

[0007] A catalyst loading column, located in the reaction chamber, for loading Fenton catalyst;

[0008] A filter element is sleeved in the catalyst loading column, and a discharge portion of the filter element is connected to the material outlet;

[0009] Heat source, used to provide the heat required for the reaction.

[0010] The second aspect of the present invention discloses an application of the Fenton reactor described in the present invention in wastewater treatment.

[0011] A third aspect of the present invention provides a method for treating DMSO wastewater, the method using the Fenton reactor of the present invention, comprising:

[0012] A mixed solution of DMSO wastewater and an oxidant is fed into the material inlet, and the mixed solution is brought into contact with a Fenton catalyst to degrade the DMSO wastewater, which is then filtered through a filter element and discharged from the material outlet.

[0013] Through the above technical scheme, the Fenton reactor of the present invention integrates heterogeneous catalysis and filtration in one reactor, effectively preventing the loss of catalyst; further, the DMSO wastewater treatment method of the present invention solves the problem that DMSO wastewater is difficult to biodegrade, and the final effluent can be reused, turning waste into treasure, the process is simple and efficient, and has the advantages of good effect, technical applicability, and economic feasibility. BRIEF DESCRIPTION OF THE DRAWINGS

[0014] Figure 1 is a schematic diagram of the structure of a Fenton reactor in some embodiments of the present invention;

[0015] Figure 2 yes Figure 1 A top view of the Fenton reactor.

[0016] Description of Reference Numerals

[0017] 1. First inlet; 2. Second inlet; 3. Heat source; 4. Catalyst addition inlet; 5. Material inlet; 6. Catalyst loading column; 7. Filter element; 8. Slag discharge port; 9. Pressure gauge port; 10. Exhaust port; 11. Material outlet. DETAILED DESCRIPTION

[0018] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0019] In the present invention, unless otherwise specified, directional words such as "up, down, top, bottom" are usually used with reference to the directions shown in the drawings or are used to describe the relative positional relationships of components in the vertical, perpendicular or gravity direction.

[0020] The present invention discloses a Fenton reactor for treating DMSO wastewater, the Fenton reactor comprising:

[0021] A shell, the shell surrounds the defined reaction chamber and is provided with a material inlet and a material outlet 11;

[0022] A catalyst loading column 6, located in the reaction chamber, for loading Fenton catalyst;

[0023] The filter element 7 is sleeved in the catalyst loading column 6, the feed portion of the filter element is connected to the discharge portion of the catalyst loading column 6, and the discharge portion of the filter element is connected to the material outlet;

[0024] Heat source 3 is used to provide the heat required for treating DMSO wastewater.

[0025] like Figure 1 As shown, the Fenton reactor of the present invention is nested with a filter element 7, a catalyst loading column 6 and a shell from the inside out, a feed pipe passes through the shell and is connected to the bottom of the reaction chamber, a material inlet is set to be connected to the first inlet 1 and the second inlet 2 on the feed pipe, and a material outlet 11 is opened at the top of the shell and is connected to the top of the filter element. In this way, heterogeneous catalysis and filtration are integrated in one reactor, and the DMSO wastewater and hydrogen peroxide fed through the first inlet 1 and the second inlet 2, respectively, contact with the Fenton catalyst in the catalyst loading column 6 under the action of a heat source, and a Fenton reaction occurs to degrade TOC in the wastewater. The reaction product is discharged out of the reactor after intercepting the residue dropped by the heterogeneous Fenton catalyst through the filter element, which can effectively prevent the loss of the catalyst.

[0026] It is understandable that a material port 5 communicating with the top of the filter element may be provided on the housing for back-flushing the filter element, or for discharging the filter aid through the material port for regeneration and recycling to reduce costs.

[0027] In some embodiments of the present invention, Figure 1As shown, a top end dosing port connected to the catalyst loading column 6 is provided at the top end of the shell. The dosing port can be used as a catalyst addition port 4, as an exhaust port 10, or as a pressure gauge port 9 for installing a pressure gauge. The aforementioned is a commonly used setting method in the prior art, and the present invention will not elaborate on this.

[0028] In some embodiments of the present invention, a slag discharge port 8 is also provided at the bottom of the reactor. It can be understood that, according to the needs, the various inlets and outlets of the reactor of the present invention can be installed with control valves, pumps or detection elements (such as temperature measurement) and other components using existing technologies. The present invention has no special requirements for this and will not go into details.

[0029] In some embodiments of the present invention, the filter element 7 includes an integral filter element or a porous filter column, and the material after the Fenton reaction is filtered through the integral filter element or the porous filter column and then discharged from the material outlet 11.

[0030] In some embodiments of the present invention, the filter element 7 is filled with a filter aid, which is evenly distributed on the filter cloth before the oxidation experiment begins. The filter cloth and the filter aid can be filled in the integral filter element or the porous filter column using existing technology to further adsorb organic matter and improve the filtration efficiency.

[0031] In some embodiments of the present invention, the catalyst loading column 6 is configured as an annular mesh column, and preferably the catalyst loading column 6 is configured as at least one circle of mesh fixed to the top cover of the shell, wherein when the number of the mesh is greater than one circle, multiple circles of mesh are nested inside and outside; more preferably, the mesh diameter of the catalyst loading column 6 is smaller than the minimum particle size of the loaded catalyst, so as to prevent the catalyst from clogging the water outlet under the impact of water flow, or to prevent the catalyst from destroying the distribution of filter aids on the filter cloth.

[0032] In some embodiments of the present invention, the heat source 3 is located between the filter element 7 and the catalyst loading column 6, and the heat source 3 includes one of a microwave probe, an ultrasonic probe, an electric heating rod, an infrared heating probe or a steam heating jacket.

[0033] In some embodiments of the present invention, the integral filter element includes an upper fixing plate, an upper filter element sleeve, a candle-type filter element corresponding to the upper filter element sleeve, a clamping assembly corresponding to the candle-type filter element, and a lower clamping plate. The upper fixing plate is detachably connected to the top cover, the upper ends of the upper filter element sleeves are respectively connected to the upper fixing plates, each candle-type filter element is respectively mounted on each upper filter element sleeve, the upper ends of each clamping assembly are respectively connected to the lower ends of each candle-type filter element, and the lower ends of each clamping assembly are respectively connected to the lower clamping plate.

[0034] In some embodiments of the present invention, the porous filter column is configured as a hollow cylindrical tube with a closed lower end, the upper end of which is fixed to the top cover, the outer sleeve of the hollow cylindrical tube is provided with a filter cloth, and the upper and lower ends are provided with filter cloth fixing members in the prior art; preferably, the pore size of the filter cloth is 5 μm-100 μm, for example, 10 μm, 20 μm, 30 μm, 50 μm, 100 μm. In some embodiments of the present invention, the pore size of the filter cloth is more preferably 10 μm-30 μm.

[0035] The second aspect of the present invention discloses an application of the Fenton reactor described in the present invention in wastewater treatment.

[0036] The third aspect of the present invention discloses a method for treating DMSO wastewater, the method using the Fenton reactor of the present invention, comprising:

[0037] A mixed solution of DMSO wastewater and an oxidant is fed into the material inlet, and the mixed solution is brought into contact with the catalyst to degrade the DMSO wastewater, which is then filtered through a filter element and discharged from the material outlet.

[0038] In the present invention, the reactor of the present invention is applied to the oxidation treatment of DMSO wastewater, the heterogeneous Fenton catalyst is activated by heating to improve the degradation efficiency, and the residue dropped by the heterogeneous Fenton catalyst is intercepted by filtering, which has the advantages of simple process, high treatment depth and zero emission.

[0039] In some embodiments of the present invention, the composition of DMSO wastewater includes, by mass percentage, 0.1%-5% dimethyl sulfoxide, 0.0001%-0.0005% azobisisobutyronitrile, 0.00001%-0.00005% 3-(methyl)propionitrile and other trace organic matter.

[0040] In some embodiments of the present invention, the TOC content in the DMSO wastewater is 70 ppm-3500 ppm, for example, 100 ppm, 500 ppm, 1000 ppm, 1500 ppm, 2000 ppm, 2500 ppm, 3000 ppm, 3500 ppm or any value therebetween.

[0041] In some embodiments of the present invention, the pH of the mixed solution is adjusted to 2-5, for example, 2.5, 3, 3.5, 4, 4.5, 5 or any value therebetween.

[0042] In some embodiments of the present invention, the molar ratio of the oxidant calculated as oxidizing substance to the DMSO wastewater calculated as total organic carbon is 100:1-1:1.

[0043] In some embodiments of the present invention, the oxidant comprises hydrogen peroxide, 3, one or more of persulfates, wherein the persulfate can be at least one of potassium monopersulfate (PMS), potassium double persulfate, ammonium persulfate, and sodium persulfate.

[0044] In some embodiments of the present invention, the oxidant preferably comprises hydrogen peroxide and O 3 , where hydrogen peroxide and O 3 The molar ratio is 10:1-10;

[0045] In some embodiments of the present invention, it is more preferred that the oxidant comprises hydrogen peroxide, 3 and persulfates, wherein hydrogen peroxide and O 3 The molar ratio of the persulfate to the persulfate is 10:1-10:1-4.

[0046] In some embodiments of the present invention, the conditions of the Fenton reaction include: a temperature of 50°C-100°C, preferably 60°C-90°C, and a pressure of 0.1 MPa at normal pressure. The temperature of the Fenton reaction in the present invention can be 50°C, 60°C, 70°C, 80°C, 90°C, 100°C or any value therebetween.

[0047] In some embodiments of the present invention, the volume space velocity of DMSO wastewater is 0.1h -1 -2.0h -1 .

[0048] In some embodiments of the present invention, the Fenton catalyst loaded in the catalyst loading column 6 is a heterogeneous catalyst.

[0049] In some embodiments of the present invention, the Fenton catalyst comprises an active component and a carrier, wherein the mass content of the active component is 0.5%-15% in terms of metal elements, and the mass content of the carrier is 70%-90%.

[0050] In some embodiments of the present invention, the carrier is preferably selected from at least one of a spherical shape, a strip shape, or a clover leaf shape.

[0051] In some embodiments of the present invention, the active components of the Fenton catalyst include Fe and / or Cu, preferably include Fe and Cu, more preferably the molar ratio of Fe to Cu in the active components of the Fenton catalyst is (1-10): 1, further preferably (1-2): 1. The above has the advantage of good oxidation effect.

[0052] In some embodiments of the present invention, the filter element is filled with a filter aid, and the filter aid is selected from at least one of diatomaceous earth, perlite, cellulose, asbestos, graphite powder, sawdust, magnesium oxide, gypsum, activated carbon or clay.

[0053] In some embodiments of the present invention, the working pressure of filtration is 0.1 MPa-0.6 MPa.

[0054] In some embodiments of the present invention, the method further comprises adjusting the pH of the effluent from the material outlet to 7-9.

[0055] In the present invention, there is no special requirement for the pH adjusting agent added to the mixed solution, as long as it can achieve the adjustment within the target range. Commonly used adjusting agents can be used in the present invention, such as sulfuric acid, calcium oxide, etc., and the present invention will not go into details.

[0056] The advantages of the present invention are described below by way of examples, but the present invention is not limited thereto.

[0057] In the present invention, the treatment effect of DMSO wastewater is represented by the total organic carbon (TOC) of the effluent, and the DMSO removal rate is defined as the value of TOC reduced after treatment divided by the value of TOC in the raw water.

[0058] In the examples and comparative examples of the present invention, the DMSO wastewater is derived from wastewater generated during the distillation process of carbon fiber wastewater.

[0059] The reagents used in the following examples are commercially available and analytically pure. The wastewater reuse standard refers to a TOC removal rate greater than 90%.

[0060] Example 1

[0061] This embodiment adopts Figure 1 The Fenton reactor shown comprises a filter element 7, a catalyst loading column 6 and a shell which are nested in sequence from the inside to the outside, wherein the heat source 3 is an electric heating rod and is installed between the filter element 7 and the catalyst loading column 6, the filter element 7 is a porous filter column, the pore size of the filter cloth is 20 μm, and the catalyst loading column 6 is an annular mesh column in which a spherical heterogeneous Fenton catalyst is loaded to form a catalyst bed, and the mesh aperture is smaller than the catalyst diameter.

[0062] (1) 50 g of activated carbon as a filter aid is prepared into a 2 L solution, which is pumped in under pressure from a first inlet 1, and the activated carbon is evenly distributed on the surface of the filter cloth to form a filter cake; after the pressure is released, 2 L of a heterogeneous Fenton catalyst is added from a catalyst addition port 4, wherein the composition of the Fenton catalyst is as follows: the mass content of the active component is 3% in terms of Fe, the mass content of the carrier is 86%, the carrier is selected from a spherical shape, and the molar ratio of Fe to Cu in the active component is 1.9:1; the heating temperature of the heat source 3 is controlled to be 80° C., and the pressure is controlled to be normal pressure.

[0063] (2) DMSO wastewater (DMSO content of about 0.7wt%, TOC = 500ppm) and hydrogen peroxide were respectively added with sulfuric acid to adjust the pH to 3 and introduced into the reaction chamber from the first inlet 1 and the second inlet 2, respectively. The molar ratio of hydrogen peroxide to wastewater was 9:1 with respect to total organic carbon. The volume space velocity of wastewater passing through the catalyst bed was 0.5h -1 The working pressure of the filtration is normal pressure. The effluent is collected at the material outlet 11, and the pH is adjusted to 8.5 with 10wt% sodium hydroxide. The TOC is measured to be 30ppm. The active components of the catalyst Fe and Cu are not detected in the effluent, and the effluent is clear and can be reused.

[0064] Example 2

[0065] This embodiment adopts Figure 1 The Fenton reactor shown comprises a filter element 7, a catalyst loading column 6 and a shell which are nested in sequence from the inside to the outside, wherein the heat source 3 is a microwave probe and is installed between the filter element 7 and the catalyst loading column 6, the filter element 7 is an integral filter element, the pore size of the filter cloth is 10 μm, and the catalyst loading column 6 is an annular mesh column in which strip-shaped heterogeneous Fenton catalyst is loaded to form a catalyst bed, and the mesh pore size is smaller than the catalyst diameter.

[0066] (1) 50 g of perlite as a filter aid is prepared into a 2 L solution, which is pumped in under pressure from the first inlet 1, and the perlite is evenly distributed on the surface of the filter cloth to form a filter cake; after the pressure is released, 2 L of a heterogeneous Fenton catalyst is added from the catalyst addition port 4, wherein the composition of the Fenton catalyst is as follows: the mass content of the active component is 4% in terms of Fe, the mass content of the carrier is 85%, the carrier is selected from a spherical shape, and the molar ratio of Fe to Cu in the active component is 1.5:1; the heating temperature of the heat source 3 is controlled to be 80° C., and the pressure is controlled to be normal pressure.

[0067] (2) DMSO wastewater (DMSO content of about 0.7wt%, TOC = 500ppm) and hydrogen peroxide were respectively added with sulfuric acid to adjust the pH to 3 and introduced into the reaction chamber from the first inlet 1 and the second inlet 2, respectively. The molar ratio of hydrogen peroxide to wastewater in terms of total organic carbon was 5:1, and the volume space velocity of wastewater passing through the catalyst bed was 0.5h -1 The working pressure of the filtration is 0.3Mpa. The effluent is collected at the material outlet 11, and the pH is adjusted to 8.5 with 10wt% sodium hydroxide. The TOC is measured to be 25ppm. The active components of the catalyst Fe and Cu are not detected in the effluent, and the effluent is clear and can be reused.

[0068] Example 3

[0069] This embodiment adopts Figure 1The Fenton reactor shown in the figure comprises a filter element 7, a catalyst loading column 6 and a shell which are nested in sequence from the inside to the outside, wherein the heat source 3 is an infrared heating probe and is installed between the filter element 7 and the catalyst loading column 6, the filter element 7 is an integral filter element, the pore size of the filter cloth is 30 μm, and the catalyst loading column 6 is an annular mesh column, in which a clover-shaped heterogeneous Fenton catalyst is loaded to form a catalyst bed, and the mesh aperture is smaller than the catalyst diameter.

[0070] (1) 50 g of graphite powder as a filter aid is prepared into a 2 L solution, which is pumped in under pressure from a first inlet 1, and the graphite powder is evenly distributed on the surface of the filter cloth to form a filter cake; after the pressure is released, 2 L of a heterogeneous Fenton catalyst is added from a catalyst addition port 4, wherein the composition of the Fenton catalyst is as follows: the mass content of the active component is 2.5% in terms of Fe, the mass content of the carrier is 89%, the carrier is selected from a spherical shape, and the molar ratio of Fe to Cu in the active component is 1:1; the heating temperature of the heat source 3 is controlled to be 80° C., and the pressure is controlled to be normal pressure.

[0071] (2) DMSO wastewater (DMSO content of about 0.7wt%, TOC = 500ppm) and hydrogen peroxide were respectively added with sulfuric acid to adjust the pH to 3 and introduced into the reaction chamber from the first inlet 1 and the second inlet 2, respectively. The molar ratio of hydrogen peroxide to wastewater in terms of total organic carbon was 4.5:1, and the volume space velocity of wastewater passing through the catalyst bed was 0.5h -1 The working pressure of the filtration is 0.5 MPa. The effluent is collected at the material outlet 11 and the pH is adjusted to 8.5 with 10 wt% sodium hydroxide. The TOC is measured to be 28 ppm. The active components of the catalyst, Fe and Cu, are not detected in the effluent. The effluent is clear and can be reused.

[0072] Example 4

[0073] Different from Example 1, the molar ratio of Fe to Cu in the active components of the Fenton catalyst is 5:1, the TOC of the effluent is measured to be 37 ppm, and the effluent is clear and can be reused.

[0074] Example 5

[0075] The difference from Example 1 is that the incoming raw water is landfill leachate with TOC=550ppm, and the TOC of the effluent is measured to be 8ppm, indicating that the treatment effect is good.

[0076] Example 6

[0077] The difference from Example 1 is that O is introduced into the second inlet 2. 3 , O 3 The molar ratio of total organic carbon to wastewater is 9:1, and the effluent TOC is measured to be 45ppm. The effluent is clear and can be reused.

[0078] Example 7

[0079] The difference from Example 1 is that O is introduced into the second inlet 2. 3 , O 3 The molar ratio of total organic carbon to wastewater is 0.5:1, the effluent TOC is measured at 88ppm, and the effluent cannot be reused.

[0080] Example 8

[0081] The difference from Example 1 is that hydrogen peroxide and O are added to the reaction chamber. 3 , where hydrogen peroxide and O 3 The molar ratio is 10:5.

[0082] The measured effluent TOC is 23ppm, and the effluent is clear and can be reused.

[0083] Example 9

[0084] The difference from Example 1 is that hydrogen peroxide and O are added to the reaction chamber. 3 and potassium monopersulfate (PMS), wherein hydrogen peroxide, O 3 The molar ratio of MgO and PMS is 10:5:2.

[0085] The measured effluent TOC is 20ppm, and the effluent is clear and can be reused.

[0086] Comparative Example 1

[0087] Different from Example 1, no catalyst loading was performed, and the TOC of the effluent was measured to be 450 ppm, so the effluent could not be reused.

[0088] Comparative Example 2

[0089] Different from Example 1, the filter element 7 is not provided in the Fenton reactor, but 2 L of heterogeneous Fenton catalyst is added from the catalyst addition port 4 .

[0090] The effluent is collected at the material outlet 11, and the pH is adjusted to 8.5 with 10% calcium oxide. The TOC is measured to be 480 ppm. The effluent is turbid and needs to be filtered. This effluent cannot be reused.

[0091] Comparative Example 3

[0092] The pH of 1L DMSO wastewater (DMSO content is about 0.7wt%, TOC=500ppm) is adjusted to 3, and hydrogen peroxide and ferrous sulfate heptahydrate are added at the same time. The molar ratio of hydrogen peroxide to total organic carbon in the wastewater is 9:1, and the molar ratio of hydrogen peroxide to ferrous sulfate heptahydrate is 10:1. After reacting for 1h, the pH is adjusted to 8.5 with 10% calcium oxide. After filtration, the TOC is measured to be 93ppm. This effluent cannot be reused, and a large amount of iron sludge will be produced, increasing the cost of hazardous waste treatment.

[0093] The preferred embodiments of the present invention are described in detail above in conjunction with the accompanying drawings, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various specific technical features in any appropriate manner. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations. However, these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to the protection scope of the present invention.

Claims

1. A Fenton reactor, It is characterized in that The Fenton reactor comprises: A shell, the shell surrounds the defined reaction chamber and is provided with a material inlet and a material outlet; A catalyst loading column (6), located in the reaction chamber, for loading Fenton catalyst; A filter element (7) is sleeved in the catalyst loading column (6), and a discharge portion of the filter element is connected to the material outlet; The heat source (3) is used to provide the heat required for the reaction.

2. The Fenton reactor according to claim 1, It is characterized in that The filter element (7) is filled with a filter aid; and / or The catalyst loading bar (6) is configured as an annular mesh column, preferably the catalyst loading bar (6) is configured as at least one circle of mesh fixed to the top cover of the shell; more preferably, the mesh diameter of the catalyst loading bar (6) is smaller than the minimum particle size of the loaded catalyst; and / or The filter element (7) comprises an integral filter element or a porous filter column; and / or The heat source (3) comprises one of a microwave probe, an ultrasonic probe, an electric heating rod, an infrared heating probe or a steam heating jacket.

3. The Fenton reactor according to claim 2, It is characterized in that The integral filter element comprises an upper fixing plate, an upper filter element sleeve, a candle-type filter element corresponding to the upper filter element sleeve, a clamping assembly corresponding to the candle-type filter element, and a lower clamping plate. The upper fixing plate is detachably connected to the top cover, the upper ends of the upper filter element sleeves are respectively connected to the upper fixing plate, the candle-type filter elements are respectively mounted on the upper filter element sleeves, the upper ends of the clamping assemblies are respectively connected to the lower ends of the candle-type filter elements, and the lower ends of the clamping assemblies are respectively connected to the lower clamping plate.

4. The Fenton reactor according to claim 2, It is characterized in that The porous filter column is configured as a hollow cylindrical tube with a closed lower end and an upper end fixed to a top cover. The outer portion of the hollow cylindrical tube is covered with a filter cloth; preferably, the pore size of the filter cloth is 5 μm-100 μm.

5. Use of the Fenton reactor according to any one of claims 1 to 4 in wastewater treatment.

6. A method for treating DMSO wastewater, It is characterized in that The method adopts the Fenton reactor described in any one of claims 1 to 4, comprising: A mixed solution of DMSO wastewater and an oxidant is fed into the material inlet, and the mixed solution is brought into contact with a Fenton catalyst to degrade the DMSO wastewater, which is then filtered by the filter element and discharged from the material outlet.

7. The method according to claim 6, in, The TOC content in the DMSO wastewater is 70ppm-3500ppm; and / or Adjusting the pH of the mixed solution to 2-5; and / or The molar ratio of the oxidant calculated as oxidizing substances to the DMSO wastewater calculated as total organic carbon is 100:1-1:1; and / or The oxidant includes hydrogen peroxide, 3 or one or more of persulfates; Preferably, the oxidant comprises hydrogen peroxide and O 3 , where hydrogen peroxide and O 3 The molar ratio is 10:1-1:1; More preferably, the oxidant comprises hydrogen peroxide, 3 and persulfates, wherein hydrogen peroxide and O 3 The molar ratio of the persulfate to the persulfate is 10:1-10:1-4.

8. The method according to claim 6 or 7, in, The reaction conditions include: a temperature of 50°C-100°C, preferably 60°C-90°C, and normal pressure; and / or The volume space velocity of the DMSO wastewater is 0.1h -1 -2.0h -1 .

9. The method according to any one of claims 5 to 8, in, The Fenton catalyst loaded in the catalyst loading column (6) is a heterogeneous catalyst; and / or The Fenton catalyst comprises an active component and a carrier, wherein the mass content of the active component is 0.5%-15% in terms of metal element, and the mass content of the carrier is 70%-90%, and the carrier is preferably selected from at least one of spherical, strip-shaped or clover-shaped; and / or The active components of the Fenton catalyst include Fe and / or Cu, preferably include Fe and Cu, more preferably the molar ratio of Fe to Cu in the active components of the Fenton catalyst is (1-10):1, further preferably (1-2):

1.

10. The method according to any one of claims 5 to 9, in, The filter element is filled with a filter aid, and the filter aid is selected from at least one of diatomaceous earth, perlite, cellulose, asbestos, graphite powder, sawdust, magnesium oxide, gypsum, activated carbon or clay; and / or The working pressure of the filtration is 0.1MPa-0.6Mpa; and / or The method further comprises adjusting the pH of the effluent from the material outlet to 7-9.

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