A Fenton reactor

Abstract

The utility model embodiment discloses a Fenton reactor, which includes a tower body, a feeding mechanism, a flow control mechanism and an annular precipitation separation mechanism. The tower body includes a feeding area, a reaction area and a separation area arranged in sequence from a first direction. The feeding mechanism is arranged in the feeding area, and the feeding mechanism includes an air inlet assembly, a water inlet assembly and a catalyst feeding assembly; the flow control mechanism is arranged on a side of the reaction area away from the feeding area, and the flow control mechanism is provided with a plurality of water-passing gaps, wherein the width of the water-passing gaps located at the edge is smaller than the width of the water-passing gaps located at other positions; the annular precipitation separation mechanism is arranged on the inner wall of the tower body in the separation area, and a precipitation discharge port is provided at the bottom end of the annular precipitation separation mechanism, and the precipitation discharge port is adjacent to the inner wall of the tower body, and an air outlet channel is provided on the side of the inner wall of the annular precipitation separation mechanism away from the tower body, and the air outlet channel is connected to the reaction area. The utility model improves the catalyst utilization efficiency by improving the catalyst reflux mode.

Description

Technical Field

[0001] The utility model belongs to the technical field of sewage treatment, and in particular relates to a Fenton reactor. Background Art

[0002] The pharmaceutical, fine chemical, pesticide, coal chemical and other industries are important industries for national economic growth and are also major wastewater dischargers. The wastewater discharged is typical difficult-to-degrade industrial wastewater.

[0003] Fenton oxidation technology is an important technology in the treatment of refractory industrial wastewater. 2+ and H2O2 to produce ·OH, which degrades the refractory organic wastewater. The heterogeneous Fenton oxidation process introduces a solid-phase catalyst for catalysis. The catalyst is mixed with the liquid in the reactor and vortexes, so the contact between the solid and the liquid is more complete, thereby improving the wastewater treatment efficiency.

[0004] In the process of realizing the present utility model, the inventors found that the process of recovering and reusing the catalyst in the existing Fenton reactor is complicated, and a special collection tank needs to be set up to collect the catalyst and then put it back into the reactor. The catalyst utilization rate is not high, which limits the treatment efficiency of the wastewater containing difficult-to-degrade organic matter. Utility Model Content

[0005] The technical purpose of the utility model is to provide a Fenton reactor, which improves the utilization efficiency of the catalyst by improving the reflux of the catalyst.

[0006] In order to solve the above technical problems, a technical solution adopted by the utility model is: to provide a Fenton reactor, including a tower body, the tower body including a feed zone, a reaction zone and a separation zone arranged in sequence from a first direction, the first direction being the axial direction of the tower body and pointing from the bottom end of the tower body to the top end of the tower body; a feed mechanism, arranged in the feed zone, the feed mechanism including an air inlet assembly, a water inlet assembly and a catalyst feeding assembly; a flow control mechanism, arranged on a side of the reaction zone away from the feed zone, the flow control mechanism being provided with a plurality of water-passing gaps, wherein the width of the water-passing gaps located at the edge is smaller than the width of the water-passing gaps located at other positions; an annular sedimentation separation mechanism, arranged on the inner wall of the tower body in the separation zone, the bottom end of the annular sedimentation separation mechanism being provided with a sedimentation discharge port, the sedimentation discharge port being adjacent to the inner wall of the tower body, the side of the annular sedimentation separation mechanism away from the inner wall of the tower body being provided with an outlet channel, the outlet channel being connected to the reaction zone.

[0007] Optionally, the flow control mechanism includes a fixing member and a plurality of first plates and second plates alternately arranged along a second direction, wherein the first plates and the second plates are fixed to the tower body by the fixing member, and the water flow gap is located between adjacent first plates and second plates, wherein the second direction is the radial direction of the tower body.

[0008] Optionally, the first plate and the second plate are both in an inverted V shape.

[0009] Optionally, the flow control mechanism further includes at least one supporting plate, and the supporting plate is abutted against the bottom end of each of the first panels.

[0010] Optionally, the annular sedimentation separation mechanism includes an isolation member, a sedimentation component, a collecting bin and the sedimentation discharge port, a receiving cavity is provided between the isolation member and the inner wall of the tower body, the sedimentation component is received in the receiving cavity, a collecting bin is provided below the sedimentation component, and the bottom end of the collecting bin is connected to the sedimentation discharge port.

[0011] Optionally, the isolation member includes a bending member located at the bottom end of the isolation member, and the bending member is bent toward one side of the inner wall of the tower body.

[0012] Optionally, the angle between the bending member and the first direction is 50 degrees to 70 degrees.

[0013] Optionally, the Fenton reactor further comprises a blocking block fixed to the inner wall of the tower body, wherein the blocking block is located above the edge of the flow control mechanism and below the precipitation discharge port.

[0014] Optionally, the sedimentation assembly is provided with a drain pipe, and the drain pipe is connected to the outside of the tower body.

[0015] Optionally, the water inlet assembly is located above the air inlet assembly, and the catalyst feeding assembly is located above the water inlet assembly or is in the same plane as the water inlet assembly.

[0016] In the embodiment of the utility model, after the gas, liquid and catalyst enter the tower body for reaction, the catalyst is separated from the liquid in the annular precipitation separation mechanism, and the catalyst flows back through the precipitation discharge port. Due to the boundary effect of the liquid flow, the flow rate of the three-phase mixture is slow at the tower wall of the tower body, which is conducive to the reflux of the catalyst. On the one hand, the precipitation discharge port is close to the tower wall of the tower body, making it easier for the catalyst to flow back near the tower wall of the tower body. On the other hand, a flow control mechanism is set in the reaction zone, and the flow control mechanism has multiple water gaps, wherein the width of the water gap located at the edge is smaller than the width of the water gap located at other positions, so that the water flow of the water gap at the edge is further reduced, so that the catalyst falling back at the edge is easier to flow back to the reaction zone through the water gap at the edge. The structural design that the precipitation discharge port is close to the tower wall of the tower body and the width of the water gap located at the edge of the flow control mechanism is smaller than the width of the water gap located in the middle promotes the reflux of the catalyst, improves the utilization efficiency of the catalyst, and improves the treatment efficiency of wastewater. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 This is a schematic diagram of the overall structure of a Fenton reactor in an embodiment of the utility model;

[0018] Figure 2 This is a schematic diagram of the overall structure of the support plate in the embodiment of the utility model;

[0019] Figure 3 It is a schematic diagram of the overall structure of the air intake assembly in the embodiment of the utility model;

[0020] Figure 4 It is a schematic diagram of the overall structure of the water inlet assembly in the embodiment of the utility model.

[0021] In the accompanying drawings, each reference numeral represents:

[0022] 100. Fenton reactor;

[0023] 1. Tower body; 11. Feeding zone; 12. Reaction zone; 13. Separation zone; 14. First cylinder; 15. Second cylinder;

[0024] 2. Feeding mechanism; 21. Air intake assembly; 211. Main air intake pipe; 212. Branch air intake pipe; 22. Water intake assembly; 221. Main water intake pipe; 222. Branch water intake pipe; 23. Catalyst feeding assembly;

[0025] 3. Flow control mechanism; 31. First plate; 32. Second plate; 33. Water gap; 34. Support plate;

[0026] 4. annular sedimentation separation mechanism; 41. isolating member; 411. bending member; 412. flow guide member; 42. sedimentation assembly; 43. sedimentation discharge port;

[0027] 5. Exhaust channel;

[0028] 6. Blocking block. DETAILED DESCRIPTION

[0029] The embodiments of the utility model are described in detail below, and examples of the embodiments are shown in the accompanying drawings, wherein the same or similar reference numerals throughout represent the same or similar elements or elements having the same or similar functions. The embodiments described below with reference to the accompanying drawings are exemplary and are intended to be used to explain the utility model, and cannot be understood as limiting the utility model. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in the field without creative work are within the scope of protection of the utility model.

[0030] In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", "clockwise", "counterclockwise", "axial", "circumferential", "radial" and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and therefore should not be understood as a limitation on the present invention.

[0031] In addition, the terms "first" and "second" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined as "first" and "second" may explicitly or implicitly include one or more of the features. In the description of the present utility model, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0032] See also Figure 1 The Fenton reactor 100 includes a tower body 1, a feeding mechanism 2, a flow control mechanism 3 and an annular sedimentation separation mechanism 4. The feeding mechanism 2, the flow control mechanism 3 and the annular sedimentation separation mechanism 4 are arranged in sequence along a first direction, wherein the first direction is the axial direction of the tower body 1 and points from the bottom end of the tower body 1 to the top end of the tower body 1. The feeding mechanism 2, the flow control mechanism 3 and the annular sedimentation separation mechanism 4 can be installed in the tower body 1, the feeding mechanism 2 is used to input materials into the tower body 1, the flow control mechanism 3 is used to control the flow of the materials input by the feeding mechanism 2 through the flow control mechanism 3, and the annular sedimentation separation mechanism 4 is used for solid-liquid separation.

[0033] For tower 1 above, see Figure 1, the tower body 1 includes a feeding area 11, a reaction area 12, and a separation area 13 arranged in sequence in the first direction. The feeding area 11 is used for feeding, the reaction area 12 is used for material reaction, and the separation area 13 is used for the separation after material reaction. It should be noted that the Fenton reaction can occur not only in the reaction area 12, but also in the feeding area 11 and the separation area 13.

[0034] For the above feeding mechanism 2, please refer to Figure 1 , Figure 3 and Figure 4 , the feeding mechanism 2 is arranged in the feeding area 11. The feeding mechanism 2 includes an air inlet assembly 21 for inputting gas, a water inlet assembly 22 for inputting liquid, and a catalyst feeding assembly 23 for inputting catalyst. The air inlet assembly 21 is arranged at the bottom end of the feeding area 11, the water inlet assembly 22 is located above the air inlet assembly 21, and the catalyst feeding assembly 23 is located above the water inlet assembly 22 or in the same plane as the water inlet assembly 22. The air inlet assembly 21 is located below the water inlet assembly 22 and the catalyst feeding assembly 23, which is beneficial to the gas and liquid driving the catalyst to move together to form a vortex, so that the reactants can contact more fully, improve the Fenton reaction rate, and degrade refractory organic pollutants.

[0035] For the above air inlet assembly 21, in some embodiments, the air inlet assembly 21 can be set as a pipeline in the shape of "丰", ring, or "田", so that the pumped gas enters the tower body 1 through the pipeline. Figure 3 As shown in the structural schematic diagram when the air inlet assembly 21 is set as a pipeline in the shape of "丰", the air inlet assembly 21 includes a main air inlet pipe 211 and a plurality of branch air inlet pipes 212. The plurality of branch air inlet pipes 212 are evenly distributed on the pipeline of the main air inlet pipe 211, and the main air inlet pipe 211 communicates with each branch air inlet pipe 212. The gas is input into the main air inlet pipe 211 from one end of the main air inlet pipe 211 located outside the tower body 1, flows through the main air inlet pipe 211 to each branch air inlet pipe 212, and finally the gas is input into the tower body 1 at the outlets of the respective branch air inlet pipes 212, so that the gas forms a vortex at multiple positions, increasing the collision frequency of the catalyst, the reagents required for the reaction, and the refractory organic pollutants, and improving the reaction efficiency of the Fenton reaction.

[0036] For the above water inlet assembly 22, in some embodiments, the water inlet assembly 22 can be set as a pipeline in the shape of "十字形", ring, or "田", so that the pumped liquid enters the tower body 1 through the pipeline. Figure 4The figure is a structural diagram when the water inlet component 22 is configured as a "cross" shaped pipe, the water inlet component 22 includes a main water inlet pipe 221 and two branch water inlet pipes 222, and the main water inlet pipe 221 is connected to the branch water inlet pipes 222, the liquid is input into the main water inlet pipe 221 from one end of the main water inlet pipe 221 located outside the tower body 1, and flows to the branch water inlet pipes 222 through the main water inlet pipe 221, and finally the liquid is input into the tower body 1 at the outlet of each branch water inlet pipe 222, so that the liquid is output from multiple directions and vortices are formed at multiple positions, thereby increasing the collision frequency of the catalyst, the reagents required for the reaction and the difficult-to-degrade organic pollutants, and improving the reaction efficiency of the Fenton reaction.

[0037] For the above-mentioned catalyst feeding assembly 23, in some embodiments, the catalyst feeding assembly 23 can be a catalyst feeding pipe, and the catalyst is placed in the catalyst feeding pipe, and hydraulic impact is applied to the catalyst feeding pipe so that the catalyst is fed into the tower body 1 through the catalyst feeding pipe. Optionally, the catalyst can be a powder solid catalyst with a particle size of 200 to 300 meshes and a density of 2000 to 5500 kg / m3. The catalyst material can be a traditional iron ore type catalyst, a supported iron-based material, a new type of non-iron-based metal catalyst, etc., so as to catalyze the Fenton reaction.

[0038] For the above flow control mechanism 3, see Figure 1 and Figure 2 , the flow control mechanism 3 is arranged on the side of the reaction zone 12 away from the feed zone 11, and the flow control mechanism 3 includes a plurality of first plates 31 and second plates 32 alternately arranged along the second direction, so that a water gap 33 is formed between the first plates 31 and the second plates 32, and the water gap 33 is used to control the water flow rate. The second direction is the radial direction of the tower body 1. There are multiple water gaps 33, and each water gap 33 is located between adjacent first plates 31 and second plates 32, wherein the width of the water gap 33 located at the edge is smaller than the width of the water gap 33 located at other positions, so that the water flow rate of the water gap 33 at the edge position is smaller than the water flow rate at other positions, and the small water flow makes the catalyst above the water gap 33 less subjected to the water flow impact force, so that the catalyst is more likely to flow back to the reaction zone 12 from the water gap 33 at the edge position.

[0039] In some embodiments, the cross-sections of the first plate 31 and the second plate 32 are both inverted V-shaped, so that the three-phase mixture of solid, liquid and gas input by the feeding mechanism 2 collides with the bottom of the first plate 31 and the second plate 32 when rising along the tower body 1 to form a vortex, which helps the three-phase mixture to further contact and improve the reaction efficiency. In addition, the collision can also cause a portion of the catalyst to collide and fall back, thereby forming an area with a higher catalyst concentration near the bottom of the first plate 31 and the second plate 32, thereby improving the catalyst recycling efficiency.

[0040] It should be noted that the shapes of the first plate 31 and the second plate 32 are only used as examples. In other embodiments, the shapes of the first plate 31 and the second plate 32 can be set to other shapes, such as rectangle, square, etc., and the orientation of each plate can also be set arbitrarily, as long as the water flow rate at the edge position is smaller than the water flow rate at other positions.

[0041] In some embodiments, the flow control mechanism 3 further includes a fixing member (not shown), and both ends of the first plate 31 and the second plate 32 are fixed to the inner wall of the tower body 1 through the fixing members, so that the first plate 31 and the second plate 32 are fixed in the tower body 1. Optionally, the fixing member can be a threaded assembly.

[0042] In some embodiments, the cross-sectional area of ​​the first plate 31 is greater than the cross-sectional area of ​​the second plate 32. Since the first plate 31 is heavier, the flow control mechanism 3 optionally further includes at least one supporting plate 34, which abuts against the bottom end of each first plate 31, so that the supporting plate 34 provides support for each first plate 31, so that each first plate 31 is firmly installed on the inner wall of the tower body 1. Optionally, three supporting plates 34 are arranged at intervals along the third direction, and the extension direction of each supporting plate 34 is parallel to the second direction, and there is a gap between adjacent supporting plates 34, and the gap can allow the three-phase mixture to pass through. Among them, the first direction, the second direction and the third direction are perpendicular to each other.

[0043] For the above-mentioned annular sedimentation separation mechanism 4, please refer to Figure 1 The annular sedimentation separation mechanism 4 includes an isolation member 41 and a sedimentation assembly 42. The isolation member 41 surrounds the inner wall of the tower body 1, and there is a receiving cavity between the isolation member 41 and the inner wall of the tower body 1. The sedimentation assembly 42 is received in the receiving cavity. The sedimentation assembly 42 is used to separate the solid and liquid in the solid-liquid mixture.

[0044] In some embodiments, the precipitation component 42 can be an inclined tube sedimentation tank (Weifang Mingyuan Environmental Engineering Co., Ltd., model MY-55) to separate the solid and liquid in the solid-liquid mixture. It should be noted that the above-mentioned precipitation component 42 is only used for example and cannot be understood as a limitation of the present invention. In other embodiments, the precipitation component 42 can be replaced by other precipitation devices well known to those skilled in the art to separate the solid and liquid in the solid-liquid mixture.

[0045] In some embodiments, a sedimentation discharge port 43 is provided at the bottom end of the annular sedimentation separation mechanism 4, and the sedimentation discharge port 43 is located below the sedimentation assembly 42, so that the solid after solid-liquid separation can flow back to the reaction zone 12 through the sedimentation discharge port 43. Optionally, the sedimentation discharge port 43 is adjacent to the inner wall of the tower body 1. Due to the boundary effect of liquid flow, the flow rate of the three-phase mixture is slow at the tower wall of the tower body, which is conducive to the falling and reflux of the catalyst. Therefore, the sedimentation discharge port 43 is adjacent to the tower wall of the tower body 1, so that the catalyst can flow back to the reaction zone 12 more easily.

[0046] In some embodiments, the sedimentation assembly 42 is provided with a drain pipe (not shown), which is connected to the outside of the tower body 1 so that the liquid after solid-liquid separation flows out of the tower body 1 through the drain pipe.

[0047] In some embodiments, the spacer 41 includes a bending piece 411 located at the bottom of the spacer 41 and a guide piece 412 connected to the top of the bending piece 411. The guide piece 412 plays a guiding role. After the solid-liquid mixture enters from the top of the annular precipitation separation mechanism 4, it flows along the guide piece 412 to the bottom of the precipitation assembly 42. The bending piece 411 bends toward one side of the inner wall of the tower body 1, so that when the solid-liquid mixture collides with the bending piece 411, part of the catalyst falls back to the precipitation discharge port 43 due to its large inertia and difficulty in changing direction. Optionally, the angle between the bending piece 411 and the first direction is 50 degrees to 70 degrees. The larger the angle, the more obvious the catalyst falling back effect.

[0048] In some embodiments, a gas outlet channel 5 is provided on one side of the annular precipitation separation mechanism 4 away from the inner wall of the tower body 1 , and the gas outlet channel 5 connects the reaction zone 12 and the outside of the tower body 1 to allow the gas to be discharged out of the tower body 1 .

[0049] In some embodiments, the Fenton reactor 100 also includes a blocking block 6 fixed to the inner wall of the tower body 1, and the blocking block 6 is located above the edge of the flow control mechanism 3, and the blocking block 6 is located below the sedimentation discharge port 43 to prevent the three-phase mixture passing through the edge of the flow control mechanism 3 from directly impacting the sedimentation discharge port 43 and affecting the solid reflux of the sedimentation discharge port 43.

[0050] The working principle of the Fenton reactor 100 in the utility model is: after the pH of the wastewater is adjusted to 3-4, an appropriate amount of H2O2 is added to the wastewater, and then the wastewater containing acid and H2O2 is pumped into the tower body 1 from the water inlet component 22, and at the same time, an appropriate amount of solid catalyst is input into the tower body 1 through the catalyst feeding component 23. Under the action of the gas input by the air inlet component 21, the wastewater and the catalyst are fully mixed in gas, solid and liquid phases. Optionally, the input gas intensity can adopt a smaller value, preferably 0.01-0.035m 3 / (m 2*min) to control the oxygen content in the wastewater. Micro-oxygen environment is conducive to Fenton reaction and to improving the activity of the catalyst. It can also reduce the Fe 2+ Rapid reaction, production of Fe 3+ , resulting in the phenomenon of reagent waste. In the main reaction zone 12, under the action of the input liquid and gas, there are multiple cyclones and liquid vortices inside the reaction zone 12, and the three-phase mixture has collision contact in multiple different directions inside the reaction zone 12, which improves the collision frequency of the catalyst, the reagent required for the reaction and the difficult-to-degrade organic pollutants, and improves the reaction efficiency of the Fenton reaction. The three-phase mixture rises slowly in the tower body 1. When the three-phase mixture rises to the flow control mechanism 3, the width of the water gap 33 located at the edge is less than the width of the water gap 33 located at other positions, so that the flow of the three-phase mixture passing through the water gap 33 at the edge is reduced, and the impact force of the three-phase mixture on the catalyst falling back is reduced, so that the catalyst falling back is easier to flow back from the water gap 33 at the edge to the reaction zone 12. In addition, due to the boundary effect of liquid flow, at the tower wall of the tower body 1, the three-phase mixture has a slow flow rate, which is also conducive to the catalyst from the water gap 33 at the edge. Backflow, in addition, the blocking block 6 prevents the three-phase mixture from directly impacting the precipitation discharge port 43, affecting the catalyst reflux. The three-phase mixture continues to rise along the tower body 1 to the separation zone 13, and part of the catalyst hits the outer wall of the bending piece 411, and part of the catalyst may also fall back due to gravity. The gas in the three-phase mixture is discharged from the tower body 1 through the gas outlet channel 5 of the separation zone 13, and the solid-liquid mixture enters the annular sedimentation separation mechanism 4 from the top of the annular sedimentation separation mechanism 4, and flows along the guide piece 412 to the bottom of the sedimentation component 42, and the solid-liquid mixture collides with the bending piece 411. Part of the catalyst falls along the bending piece 411 due to the collision, and flows back to the reaction zone 12 along the sedimentation discharge port 43, and another part of the catalyst enters the sedimentation component 42 together with the liquid, and solid-liquid two-phase separation is realized in the sedimentation component 42. After the part of the catalyst is separated from the liquid in the sedimentation component 42, it flows back to the reaction zone 12 along the sedimentation discharge port 43, and the liquid after the solid separation is discharged from the tower body 1 through the drain pipe. Among them, the sedimentation discharge port 43 is close to the inner wall of the tower body 1. Due to the boundary effect of the liquid flow, the catalyst is more likely to flow back to the reaction zone 12 from the edge of the tower body 1. The utility model adopts the "catalytic reaction, catalyst internal circulation, solid-liquid separation, catalyst recycling" mode, which improves the utilization efficiency of the catalyst and the treatment efficiency of wastewater. It can effectively degrade the difficult-to-degrade organic matter in wastewater such as papermaking wastewater, coking wastewater, printing and dyeing wastewater, electroplating wastewater, and pharmaceutical wastewater, and the degradation efficiency is fast. The degradation can be completed in only 10 to 30 minutes, which greatly improves the degradation efficiency.

[0051] In the embodiment of the utility model, after the gas, liquid and catalyst enter the tower body 1 for reaction, the catalyst is separated from the liquid in the sedimentation separation mechanism, and the catalyst flows back through the sedimentation discharge port 43. Due to the boundary effect of the liquid flow, the flow rate of the three-phase mixture is relatively slow at the tower wall of the tower body 1, which is conducive to the reflux of the catalyst. On the one hand, the sedimentation discharge port 43 is close to the tower wall of the tower body 1, making it easier for the catalyst to flow back near the tower wall of the tower body 1. On the other hand, a flow control mechanism 3 is set in the reaction zone 12, and the flow control mechanism 3 has a plurality of water-passing gaps 33, wherein the width of the water-passing gap 33 located at the edge is smaller than the width of the water-passing gap 33 located at other positions, so that the water-passing flow rate of the water-passing gap 33 at the edge is further reduced, so that the catalyst falling back at the edge is easier to flow back to the reaction zone 12 through the water-passing gap 33 at the edge. The structural design in which the sedimentation discharge port 43 is close to the tower wall of the tower body 1 and the width of the water gap 33 at the edge of the flow control mechanism 3 is smaller than the width of the water gap 33 at the middle promotes catalyst reflux, improves catalyst utilization efficiency, and improves wastewater treatment efficiency.

[0052] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A Fenton reactor, characterized in that: include: A tower body, the tower body comprising a feed zone, a reaction zone and a separation zone arranged in sequence along a first direction, wherein the first direction is an axial direction of the tower body and points from the bottom end of the tower body to the top end of the tower body; A feeding mechanism is arranged in the feeding area, and the feeding mechanism comprises an air inlet assembly, a water inlet assembly and a catalyst feeding assembly; A flow control mechanism is arranged at a side of the reaction zone away from the feed zone, and the flow control mechanism is provided with a plurality of water-passing gaps, wherein the width of the water-passing gaps at the edge is smaller than the width of the water-passing gaps at other positions; An annular sedimentation separation mechanism is arranged on the inner wall of the tower body in the separation zone. A sedimentation discharge port is provided at the bottom end of the annular sedimentation separation mechanism, and the sedimentation discharge port is adjacent to the inner wall of the tower body. An air outlet channel is provided on the side of the annular sedimentation separation mechanism away from the inner wall of the tower body, and the air outlet channel is connected to the reaction zone.

2. A Fenton reactor according to claim 1, characterized in that: The flow control mechanism includes a fixing member and a plurality of first plates and second plates alternately arranged along a second direction, wherein the first plates and the second plates are both fixed to the tower body through the fixing member, and the water flow gap is located between adjacent first plates and second plates, wherein the second direction is the radial direction of the tower body.

3. A Fenton reactor according to claim 2, characterized in that: The first plate and the second plate are both in an inverted V shape.

4. A Fenton reactor according to claim 3, characterized in that: The flow control mechanism further includes at least one supporting plate, and the supporting plate is abutted against the bottom end of each of the first panels.

5. A Fenton reactor according to claim 1, characterized in that: The annular sedimentation separation mechanism comprises an isolating member and a sedimentation assembly. A receiving cavity is provided between the isolating member and the inner wall of the tower body. The sedimentation assembly is received in the receiving cavity. The sedimentation discharge port is provided below the sedimentation assembly.

6. A Fenton reactor according to claim 5, characterized in that: The isolating member includes a bending member located at the bottom end of the isolating member, and the bending member is bent toward one side of the inner wall of the tower body.

7. A Fenton reactor according to claim 6, characterized in that: The angle between the bending member and the first direction is 50 degrees to 70 degrees.

8. A Fenton reactor according to claim 1, characterized in that: The Fenton reactor further comprises a blocking block fixed to the inner wall of the tower body, wherein the blocking block is located above the edge of the flow control mechanism and below the precipitation discharge port.

9. A Fenton reactor according to claim 5, characterized in that: The sedimentation assembly is provided with a drainage pipe, and the drainage pipe is communicated with the outside of the tower body.

10. The Fenton reactor according to any one of claims 1 to 8, characterized in that: The water inlet assembly is located above the air inlet assembly, and the catalyst feeding assembly is located above the water inlet assembly or is in the same plane as the water inlet assembly.

Images