Zero-valent iron fenton reaction device with enhanced mass transfer by impinging stream coupled with agitator

Abstract

The utility model discloses a zero valence iron fenton reaction device of impingement stream coupling stirrer reinforced mass transfer belongs to wastewater treatment equipment technical field, including device body, wastewater liquid inlet and reagent adding mouth, and the upper portion of device body inner chamber is equipped with impingement stream reactor, one side of impingement stream reactor is equipped with first tapering nozzle, and the other side is equipped with second tapering nozzle, and wastewater liquid inlet is connected first tapering nozzle liquid inlet end through pipeline, and reagent adding mouth is connected second tapering nozzle liquid inlet end through pipeline, and the first tapering nozzle is left with reinforced mixing area between second tapering nozzle, and the lower portion of device body inner chamber is equipped with axial flow stirrer, and the lower portion of device body is equipped with liquid outlet symmetrically, and is connected first tapering nozzle and second tapering nozzle respectively through circulating pipeline. The utility model discloses through the impingement stream reactor of upper portion realizes instantaneous strong mixing, realizes sustained steady mass transfer through the axial flow stirrer of lower portion and circulating pipeline to realize all cycle mass transfer reinforcement.

Description

Technical Field

[0001] This utility model relates to the technical field of wastewater treatment equipment, specifically a zero-valent iron Fenton reaction device with an impingement flow coupled agitator to enhance mass transfer. Background Technology

[0002] The core kinetics of the Fenton reaction depend on the efficiency of ·OH formation, while the mass transfer process directly determines the reactants (Fe). 0 The microscopic contact probability of H2O2 and organic matter. According to the two-film theory, mass transfer resistance is mainly concentrated in the stagnant film layer at the liquid-solid / liquid-liquid interface. Traditional single enhancement methods (such as mechanical stirring or impingement flow) can only act on fluid motion at a specific scale. Existing technologies mainly have the following drawbacks:

[0003] 1. Traditional stirred reactors: Insufficient macroscopic mixing and operational pain points

[0004] Relying on mechanical stirring to achieve liquid-liquid-solid three-phase mixing, for micron-sized zero-valent iron (Fe) 0 The reaction system between hydroxyl radicals and hydrogen peroxide (H2O2) exhibits a significant local concentration gradient, leading to low efficiency in the generation of hydroxyl radicals. Studies have shown that the mass transfer coefficient under traditional stirring conditions is only 0.1-0.3 cm / s, requiring a mixing time of 5-10 minutes. For example, the patented "Stirred Fenton Reactor (CN107555579A)" has the following disadvantages: limited zoning function; once stirring is activated, the water quality in each zone easily becomes homogenized, failing to fully achieve its intended function; high sealing requirements for the stirring shaft; the stirring shaft penetrates from the bottom of the reactor, and if the stirring shaft malfunctions, the entire reactor must be emptied for maintenance, making operation difficult. For example, the patent "High-efficiency anti-clogging pulse-type Fenton oxidation tower (CN109761336A)" describes a reactor that uses pulse-type water inlet to achieve intermittent pulse water supply, resulting in more uniform mixing. However, its main drawbacks are: difficulty in synchronizing reagent addition; the rapid Fenton reaction requires consideration of pH, ferrous salt, and hydrogen peroxide dosage ratios; while pulse-type water inlet solves the clogging problem, the reagent addition for the Fenton reaction must be synchronized with the water inlet pulse, making operation difficult; and the equipment is complex, with the pulse-type water inlet system increasing the complexity and cost of the equipment. These shortcomings severely limit the operability and practicality of this device in actual production applications.

[0005] 2. Single-impact flow device: Instantaneous mixing advantages and persistent defects

[0006] Although initial mixing enhancement can be achieved through fluid impaction, the lack of sustained stirring leads to accelerated settling of micron-sized zero-valent iron particles (settling rate approximately 0.5-1.0 mm / s), resulting in a sharp drop in mass transfer efficiency in the later stages of the reaction, making it difficult to maintain a high-efficiency reaction throughout the entire cycle. For example, the patent "An Impinging Flow Reactor Device (CN209302727U)" suffers from the following problems: complex equipment requiring precise design of the guide tube and fluid flow rate, resulting in high manufacturing and maintenance costs; uneven fluid distribution, affecting reaction performance; high operational difficulty requiring precise control of fluid flow rate and volume; and limited applicability. It is mainly suitable for liquid-phase reactions; other types of reactions require design adjustments. For example, the patent "A High-Efficiency Plug-Flow Fenton Reactor (CN202122138242.5)" has the following problems: the reactor has multiple compartments and aeration devices, resulting in a complex structure; high energy consumption: it requires power from the aeration devices and jet devices, leading to high operating costs; the jet devices and aeration devices wear out quickly after long-term operation; and it requires precise control of aeration and jet intensity, making operation difficult. Therefore, it has certain limitations in practical applications.

[0007] 3. Other types of reactors: limitations in specific scenarios

[0008] Other types of reactors, such as point Fenton reactors and fluidized bed Fenton reactors, while providing Fenton reaction solutions, still have some shortcomings and deficiencies, requiring optimization and improvement based on specific application scenarios.

[0009] For example, the patent "An Electromagnetized Fenton Reaction Device (CN222042901U)" has the following main disadvantages: the equipment is complex, and the structure becomes more complex after the introduction of an electric field, which increases the difficulty of manufacturing and maintenance; it requires additional power to maintain the electric field, which increases the operating cost; it requires precise control of the electric field strength and reaction conditions, which makes operation more difficult; and its scope of application is limited, mainly applicable to specific types of wastewater treatment, and parameters may need to be adjusted for other types of wastewater.

[0010] For example, the patent "Three-dimensional electro-Fenton water treatment device (ZL201410201495.4)" aims to improve the efficiency of heterogeneous Fenton micron zero-valent iron. However, the current efficiency of heterogeneous Fenton micron zero-valent iron still cannot fully meet the needs of industrial applications. In addition, this technology requires the selection of a suitable carrier to load the active components or oxides. In terms of current practical applications, the selection and preparation process of the carrier is relatively complex, which is another problem faced by this treatment device and greatly limits its practical production application.

[0011] For example, the patent "An Improved Fenton Fluidized Bed Reactor (CN209654321U)" shows that although the Fenton fluidized bed reactor has certain advantages in wastewater treatment, further technological improvements are still needed to overcome problems such as operational complexity, energy consumption, sludge treatment, and equipment wear. This reactor has the following drawbacks: the improved fluidized bed reactor has a relatively complex structure, requiring precise design of the packing layer and aeration device, increasing the manufacturing and maintenance costs; it requires power from the aeration device, increasing energy consumption and resulting in higher operating costs; the mutual impact and wear between packing particles are severe, potentially shortening the packing's lifespan and requiring frequent replacement; and it requires precise control of aeration intensity and fluid velocity, placing high demands on the operator's skills and expertise.

[0012] In summary, a single mass transfer enhancement method cannot meet the mixing requirements throughout the entire reaction cycle. There is an urgent need to design a synergistic reactor that integrates "initial impact strong mixing" and "continuous stirring stable mass transfer". Utility Model Content

[0013] To solve the above-mentioned technical problems, this utility model provides the following technical solution: a zero-valent iron Fenton reaction device with impinging flow coupled agitator to enhance mass transfer, comprising a device body, a wastewater inlet, and a reagent addition port. An impinging flow reactor is provided in the upper part of the inner cavity of the device body. A first tapered nozzle is provided on one side of the impinging flow reactor, and a second tapered nozzle is symmetrically provided on the other side. The wastewater inlet is connected to the inlet end of the first tapered nozzle via a pipe, and the reagent addition port is connected to the inlet end of the second tapered nozzle via a pipe. An enhanced mixing zone is provided between the first and second tapered nozzles. A flow guide notch is provided at the bottom of the impinging flow reactor, and an axial flow agitator is provided in the lower part of the inner cavity of the device body.

[0014] The device body has a first liquid outlet and a second liquid outlet symmetrically arranged on the lower side wall. The first liquid outlet is connected to the liquid inlet of the first converging nozzle through a circulation pipeline, and the second liquid outlet is connected to the liquid inlet of the second converging nozzle through a circulation pipeline. Both sets of circulation pipelines are equipped with circulation pumps and valves.

[0015] Furthermore, the nozzle contraction angle of both the first and second tapered nozzles is 30°-60°, and the outlet diameter is 2-5mm; the length of the enhanced mixing zone is 1 / 2-2 / 3 of the inner diameter of the impinging flow reactor.

[0016] Furthermore, the heights of both the first and second liquid outlets are 2 / 3 of the height of the axial flow agitator.

[0017] Furthermore, the axial flow agitator adopts a three-bladed propulsion impeller, with the impeller diameter being 1 / 3 to 1 / 2 of the lower inner diameter of the device body.

[0018] Furthermore, the blade edges of the axial flow agitator are provided with an anti-scaling coating with a thickness of 0.1-0.3 mm.

[0019] Furthermore, it also includes a pH adjustment liquid inlet and a pH sensor. The pH adjustment liquid inlet is connected to the lower part of the inner cavity of the device body through a pipe, and the monitoring end of the pH sensor extends into the lower part of the inner cavity of the device body.

[0020] Furthermore, an electromagnetic metering pump is provided at the pH adjustment solution addition port, and the pH sensor is electrically connected to the electromagnetic metering pump.

[0021] Furthermore, the device body is provided with a pressure monitoring port on the top, a pressure sensor is installed in the pressure monitoring port, and a sludge discharge port is provided at the bottom of the device body.

[0022] Furthermore, the device body has a removable filter screen in its internal cavity. The removable filter screen is located between the flow guide notch and the axial flow stirrer. The pore size of the removable filter screen is 50-100μm, which is used to prevent the accumulation of micron-sized zero-valent iron particles.

[0023] Furthermore, the edge of the flow guide notch is provided with a beveled flow guide plate to prevent fluid stagnation.

[0024] The beneficial effects of this utility model are as follows:

[0025] In this invention, the impact flow reactor in the upper cavity forms high-speed fluid impacts in opposite directions through symmetrically arranged first and second converging nozzles, completing the initial mixing of wastewater, micron-sized zero-valent iron, and hydrogen peroxide, significantly improving mass transfer efficiency, accelerating the Fenton reaction rate, and enabling faster degradation of organic matter in wastewater.

[0026] This invention utilizes an axial flow agitator in the lower cavity to create a macroscopic flow field with vertical circulation, extending the suspension time of micron-sized zero-valent iron (ZFI) and preventing reaction interruption due to particle settling. Simultaneously, a "impact-stirring-re-impact" loop is constructed through the circulation pipeline to adapt to different wastewater treatment loads. The axial flow agitator allows for better control of key parameters such as temperature and pH in the reaction system, resulting in more stable and suitable reaction conditions. This contributes to improved reaction selectivity and efficiency, and reduces the occurrence of side reactions. The stirring action of the axial flow agitator ensures uniform dispersion of ZFI particles within the reactor, preventing aggregation and scaling on the reactor walls or in localized areas, extending the lifespan of the ZFI and maintaining its activity.

[0027] This invention couples an impinging flow reactor with an axial flow agitator to achieve enhanced mass transfer throughout the entire cycle through "initial impingement to break the gradient + continuous stirring to prevent sedimentation." This improves reagent utilization, allowing Fenton's reagent (micron-sized zero-valent iron and hydrogen peroxide) to mix more thoroughly with the wastewater, reducing ineffective reagent consumption and lowering treatment costs. It also reduces reaction time; the efficient mass transfer process shortens the time required for the Fenton reaction to reach equilibrium, thereby improving the overall wastewater treatment system efficiency and reducing treatment time, enabling faster completion of wastewater treatment tasks at the same treatment scale. Attached Figure Description

[0028] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.

[0029] Figure 1 This is a schematic diagram of the structure of a zero-valent iron Fenton reactor with an impingement flow coupled stirrer to enhance mass transfer according to the present invention.

[0030] Figure 2 This is a longitudinal sectional view of the impinging flow reactor in this utility model.

[0031] In the figure:

[0032] 1-Purpose device body; 11-Pressure monitoring port; 12-First liquid outlet; 13-Second liquid outlet; 14-Sludge discharge port; 2-Impact flow reactor; 21-First converging nozzle; 22-Second converging nozzle; 23-Enhanced mixing zone; 3-Axial flow agitator; 4-pH sensor; 5-pH adjustment solution addition port; 6-Wastewater inlet; 7-Reagent addition port; 8-Circulation pump; 9-Valve. Detailed Implementation

[0033] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model.

[0034] See appendix Figure 1-2This utility model discloses a zero-valent iron Fenton reaction device with mass transfer enhanced by an impinging flow coupled stirrer, including a device body 1, a wastewater inlet 6, and a reagent addition port 7. An impinging flow reactor 2 is provided in the upper part of the inner cavity of the device body 1. A first tapered nozzle 21 is provided on one side of the impinging flow reactor 2, and a second tapered nozzle 22 is symmetrically provided on the other side. The wastewater inlet 6 is connected to the inlet end of the first tapered nozzle 21 through a pipe, and the reagent addition port 7 is connected to the inlet end of the second tapered nozzle 22 through a pipe. An enhanced mixing zone 23 is left between the first tapered nozzle 21 and the second tapered nozzle 22. A flow guide notch is provided at the bottom of the impinging flow reactor 2, and an axial flow stirrer 3 is provided in the lower part of the inner cavity of the device body 1.

[0035] The lower part of the side wall of the device body 1 is symmetrically provided with a first liquid outlet 12 and a second liquid outlet 13. The first liquid outlet 12 is connected to the liquid inlet of the first converging nozzle 21 through a circulation pipeline, and the second liquid outlet 13 is connected to the liquid inlet of the second converging nozzle 22 through a circulation pipeline. Both sets of circulation pipelines are provided with circulation pumps 8 and valves 9.

[0036] In this embodiment, the device body 1 is made of corrosion-resistant stainless steel 316L, and the inner wall roughness Ra≤0.8μm.

[0037] In this embodiment, the impinging flow reactor 2 has a cylindrical structure with a 90° arc-shaped flow guide notch. The width of the notch is in the ratio of 1:4 to 1:3 to the diameter of the impinging flow reactor 2. It is used to guide the impinging mixture into the lower part of the inner cavity of the device body 1 by gravity at a flow rate of 0.5-1.2 m / s.

[0038] In this embodiment, the wastewater inlet 6 is connected to a wastewater pipe and has a built-in micron zero-valent iron premixing chamber. The volume of the premixing chamber accounts for 15%-20% of the volume of the impinging flow reactor 2, and can form a micron zero-valent iron suspension with a concentration of 1-5 g / L.

[0039] In this embodiment, reagent addition port 7 is used to add hydrogen peroxide separately, and the pipeline is equipped with a one-way check valve, which is connected 5-10cm upstream of the liquid inlet end of the second converging nozzle 22.

[0040] In this embodiment, the liquid ejected by the first tapered nozzle 21 and the second tapered nozzle 22, after being impacted in the enhanced mixing zone 23, flows through the guide notch to the lower part of the inner cavity of the device body 1, and is stirred by the axial flow stirrer 3.

[0041] In this embodiment, the flow rate of the circulation pipeline ranges from 5 to 20 m³ / h. 3 / h, head 1-3m, forming a "lower chamber-upper chamber" cross-unit circulation loop, with a total fluid residence time of 1-3h.

[0042] The nozzle contraction angles of the first tapering nozzle 21 and the second tapering nozzle 22 are both 30°-60°, and the outlet diameters are both 2-5mm; the length of the enhanced mixing zone 23 is 1 / 2-2 / 3 of the inner diameter of the impinging flow reactor 2.

[0043] In this embodiment, the outlet diameters of the first tapered nozzle 21 and the second tapered nozzle 22 are 2-5 mm, the center distance between the two nozzles is 1 / 2-2 / 3 of the inner diameter of the impinging flow reactor 2, the outlet flow velocity is 1-3 m / s, and the micro vortex size generated is ≤500 μm. Compared with the millimeter-level vortex of traditional stirring, the mass transfer coefficient is increased to 0.8-1.2 cm / s, which is 2-4 times higher than that of traditional stirring. The initial mixing of wastewater, micron-sized zero-valent iron and hydrogen peroxide is completed within 0.5 min.

[0044] In this embodiment, the inner surfaces of both the first tapered nozzle 21 and the second tapered nozzle 22 are mirror polished (Ra≤0.2μm).

[0045] The heights of the first liquid outlet 12 and the second liquid outlet 13 are both 2 / 3 of the height of the axial flow agitator 3.

[0046] The axial flow agitator 3 adopts a three-blade propulsion impeller, and the diameter of the impeller is 1 / 3 to 1 / 2 of the inner diameter of the lower part of the inner cavity of the device body 1.

[0047] In this embodiment, the axial flow agitator 3 rotates at a speed of 50-200 r / min, forming a fluid circulation with an upper and lower circulating flow rate of 0.2-0.8 m / s. This extends the suspension time of micron-sized zero-valent iron from 1-2 hours in traditional devices to over 4 hours, preventing reaction interruption caused by particle settling. Simultaneously, a "impact-stirring-re-impact" loop is constructed through the circulation pipeline, allowing the total fluid residence time to be flexibly adjusted to 1-3 hours to adapt to different wastewater treatment loads. The circulation pump 8 pumps the stirred liquid from the lower part of the device body 1 at a speed of 5-20 m... 3 The flow rate is returned to the impinging flow reactor 2 at a rate of / h, forming a dynamic concentration gradient control: the unreacted micron-sized zero-valent iron in the return liquid is mixed with the newly input wastewater again by impact, which increases the ·OH generation rate by 25%-40% compared with the non-circulation condition, while reducing the ineffective decomposition of hydrogen peroxide (the decomposition rate is reduced from 15% in the traditional process to <8%).

[0048] The blade edge of the axial flow agitator 3 is provided with an anti-scaling coating (such as a polytetrafluoroethylene coating) with a coating thickness of 0.1-0.3mm. The shaft seal of the axial flow agitator 3 adopts a double mechanical seal structure with a leakage rate of ≤5ml / h.

[0049] It also includes a pH adjustment liquid addition port 5 and a pH sensor 4. The pH adjustment liquid addition port 5 is connected to the lower part of the inner cavity of the device body 1 through a pipe, and the monitoring end of the pH sensor 4 extends into the lower part of the inner cavity of the device body 1.

[0050] An electromagnetic metering pump is installed at pH adjustment liquid addition port 5, and pH sensor 4 is electrically connected to the electromagnetic metering pump.

[0051] In this embodiment, the inner diameter of the pipe for adding pH adjustment liquid 5 is 4-8mm, and the flow rate adjustment range of the electromagnetic metering pump is 0.1-5L / min.

[0052] In this embodiment, the pH sensor 4 monitors the pH value of the liquid in the inner cavity of the device body 1 in real time, and controls the electromagnetic metering pump according to the pH value to adjust the addition ratio of the pH adjustment liquid. The adjustment response time is ≤30s, and the pH value is controlled to be 3.0±0.2. When the pH deviates from the set value ±0.5, an alarm is automatically triggered and the addition of the medicine is cut off.

[0053] The device body 1 has a pressure monitoring port 11 at the top, and a pressure sensor is installed in the pressure monitoring port 11. The device body 1 has a sludge discharge port 14 at the bottom.

[0054] In this embodiment, the pressure sensor has a range of -0.1 to 0.5 MPa, and the pressure relief valve is automatically opened when the internal pressure of the device body 1 exceeds 0.3 MPa.

[0055] In this embodiment, the diameter of the sludge discharge port 14 is DN50-DN80, and it is connected to a pulse backwashing system. The flushing cycle can be set to 4-8 hours.

[0056] The device body 1 has a removable filter screen inside its cavity. The removable filter screen is located between the flow guide notch and the axial flow agitator 3. The pore size of the removable filter screen is 50-100μm, which is used to prevent the accumulation of micron-sized zero-valent iron particles.

[0057] The flow guide notch is equipped with a beveled flow guide plate to prevent fluid stagnation.

[0058] In this embodiment, the device body 1 can be designed as an upper or lower part connected by a flange, wherein the impinging flow reactor 2 is located at the upper part and the axial flow agitator 3 is located at the lower part. This design allows for quick disassembly and maintenance.

[0059] The above description is only a preferred embodiment of the present utility model, but the protection scope of the present utility model is not limited thereto. Any equivalent substitutions or changes made by those skilled in the art within the technical scope disclosed in the present utility model, based on the technical solution and concept of the present utility model, should be included within the protection scope of the present utility model.

Claims

1. A zero-valent iron Fenton-like reaction device for enhancing mass transfer by impinging stream coupling agitator, characterized in that, The device includes a main body (1), a wastewater inlet (6), and a reagent addition port (7). The upper part of the inner cavity of the main body (1) is provided with an impingement flow reactor (2). The impingement flow reactor (2) has a first tapered nozzle (21) on one side and a second tapered nozzle (22) symmetrically provided on the other side. The wastewater inlet (6) is connected to the inlet end of the first tapered nozzle (21) through a pipe. The reagent addition port (7) is connected to the inlet end of the second tapered nozzle (22) through a pipe. An enhanced mixing zone (23) is left between the first tapered nozzle (21) and the second tapered nozzle (22). The bottom of the impingement flow reactor (2) is provided with a flow guide notch. The lower part of the inner cavity of the main body (1) is provided with an axial flow stirrer (3). The device body (1) has a first liquid outlet (12) and a second liquid outlet (13) symmetrically arranged on the lower side wall. The first liquid outlet (12) is connected to the liquid inlet of the first converging nozzle (21) through a circulation pipeline, and the second liquid outlet (13) is connected to the liquid inlet of the second converging nozzle (22) through a circulation pipeline. Both sets of circulation pipelines are equipped with circulation pumps (8) and valves (9).

2. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupling agitator according to claim 1, characterized in that, The nozzle contraction angle of the first tapering nozzle (21) and the second tapering nozzle (22) are both 30°-60°, and the outlet diameter is 2-5mm; the length of the enhanced mixing zone (23) is 1 / 2-2 / 3 of the inner diameter of the impinging flow reactor (2).

3. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupled agitator according to claim 1, characterized in that, The heights of the first liquid outlet (12) and the second liquid outlet (13) are both 2 / 3 of the height of the axial flow agitator (3).

4. The zero-valent iron Fenton reactor with mass transfer enhanced by an impinging flow coupled stirrer according to claim 1, characterized in that, The axial flow agitator (3) adopts a three-blade propulsion impeller, and the diameter of the impeller is 1 / 3 to 1 / 2 of the inner diameter of the lower part of the inner cavity of the device body (1).

5. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupled agitator according to claim 4, characterized in that, The blade edge of the axial flow agitator (3) is provided with an anti-scaling coating with a thickness of 0.1-0.3 mm.

6. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupled agitator according to claim 1, characterized in that, It also includes a pH adjustment liquid addition port (5) and a pH sensor (4). The pH adjustment liquid addition port (5) is connected to the lower part of the inner cavity of the device body (1) through a pipe, and the monitoring end of the pH sensor (4) extends into the lower part of the inner cavity of the device body (1).

7. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupled agitator according to claim 6, characterized in that, An electromagnetic metering pump is provided at the pH adjustment liquid addition port (5), and the pH sensor (4) is electrically connected to the electromagnetic metering pump.

8. The zero-valent iron Fenton-like reaction device with intensified mass transfer by impinging stream coupled agitator according to claim 1, characterized in that, The device body (1) is provided with a pressure monitoring port (11) at the top, and a pressure sensor is installed in the pressure monitoring port (11). The device body (1) is provided with a sludge discharge port (14) at the bottom.

9. The zero-valent iron Fenton-like reaction device with intensified mass transfer by impinging stream coupled agitator according to claim 1, characterized in that, The device body (1) has a detachable filter screen in its inner cavity. The detachable filter screen is located between the flow guide notch and the axial flow stirrer (3). The pore size of the detachable filter screen is 50-100μm, which is used to prevent the accumulation of micron zero-valent iron particles.

10. The zero-valent iron Fenton-like reaction device for intensifying mass transfer by impinging stream coupled agitator according to claim 1, characterized in that, The flow guide notch is provided with a beveled flow guide plate at its edge to prevent fluid stagnation.

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