Efficient defluorination agent as well as production method and equipment thereof

Abstract

The invention discloses an efficient defluorination agent as well as a production method and equipment thereof, and relates to the technical field of fluorine-containing wastewater treatment. The efficient defluorination agent disclosed by the invention is prepared from HEDTA (Hydroxyethylene Diamine Tetraacetic Acid), DTPA (Diethylene Triamine Pentacetate Acid), Fe2 (SO4) 3, FeCl3, NaHCO3, NaH2PO4, Fe-MOFs (Metal-Organic Frameworks), Zn-MOFs (Zn-Metal-Organic Frameworks), propylene glycol The fluorine removal agent disclosed by the invention can efficiently remove fluorine ions in water through a plurality of action mechanisms such as stable chelation, fluorine removal by precipitation, catalytic oxidation, fluorine removal by adsorption, pH buffer adjustment and the like; the microchannel reactor is adopted for continuous production, so that the uniformity and the stability of the medicament are improved, and the defluorination effect is ensured; the defluorination agent is suitable for defluorination treatment of drinking water, industrial wastewater and underground water; after low-fluorine and medium-fluorine water treatment, the fluorine ion concentration is reduced to below 1mg / L, and the water quality recovery standard of drinking water and underground water is met; and less sludge is generated in the defluorination process.

Description

Technical Field

[0001] The invention relates to the technical field of fluorine-containing wastewater treatment, and in particular to a high-efficiency defluorination agent and a production method and equipment thereof. Background Art

[0002] Fluoride-containing wastewater refers to industrial wastewater containing fluoride ions. Fluoride-containing wastewater is almost everywhere in multiple industrial fields, and such wastewater may be produced from basic material production to high-tech manufacturing. Fluoride ions are highly corrosive and toxic, posing a serious threat to the ecological environment and human health. Long-term contact with or drinking water with high fluoride concentrations may have adverse effects on human health, such as chronic diseases such as dental caries, dental fluorosis, and fluorosis, and even damage to human brain nerves. The treatment of fluoride-containing wastewater faces many challenges, including large water volume, complex composition, and high treatment costs. With the rapid development of industry, the discharge of fluoride-containing wastewater is increasing, which has brought tremendous pressure to treatment facilities. In addition, wastewater may contain a variety of other pollutants, such as heavy metals, organic matter, etc., which makes the treatment process more complicated. Therefore, it is necessary to continuously develop and innovate more efficient and economical wastewater treatment technologies to meet these challenges.

[0003] In the treatment of fluoride-containing wastewater, precipitation and adsorption are two commonly used treatment methods. Although they have certain effects, they also have some defects. The precipitation method usually involves adding lime (CaO) and calcium hydroxide (Ca(OH) 2 ) or aluminum salts (such as alum) and other agents react with fluoride ions in the wastewater to form a precipitate of calcium fluoride or aluminum fluoride; this method is difficult to achieve the effect of deep defluoridation, and for occasions requiring high-precision defluoridation, the precipitation method may not meet the requirements. The adsorption method usually uses adsorbents such as activated alumina, bone char, and modified zeolite to adsorb fluoride ions in wastewater. However, these adsorbents need to be regenerated after adsorbing a certain amount of fluoride ions, and the regeneration process may be complicated and costly. The adsorption capacity of the adsorbent is limited. When the adsorbent is saturated, it needs to be replaced with a new adsorbent, which increases the treatment cost and may cause secondary pollution. Although the adsorption method has a certain treatment effect on wastewater with a low fluoride concentration, when the fluoride ion concentration in the wastewater is very low, the treatment effect of the adsorption method may be limited. Summary of the invention

[0004] In view of this, the present invention aims to provide a high-efficiency defluorination agent and a production method and equipment thereof, wherein the defluorination agent can reduce the fluoride ion content of fluoride-containing wastewater to below 10 ppm.

[0005] In order to achieve the above object, the present invention adopts the following technical solution:

[0006] In the first aspect, the present invention provides a highly efficient defluorination agent, which comprises, by weight percentage, 2-4% HEDTA, 1-2% DTPA, Fe 2 (SO 4 ) 3 6-7%, FeCl 3 2-3%, NaHCO 3 3-5%, NaH 2 PO 4 1-2%, Fe-MOFs 0.5-1%, Zn-MOFs 0.5-1%, propylene glycol 4-5% and deionized water 70-80%.

[0007] In a preferred embodiment of the present invention, the Fe-MOFs is MIL-101(Fe).

[0008] In a preferred embodiment of the present invention, the Zn-MOFs is ZIF-8.

[0009] In a second aspect, the present invention provides a method for producing the above-mentioned high-efficiency defluorination agent, comprising the following steps:

[0010] (1) Dissolve HEDTA and DTPA in an appropriate amount of deionized water and stir evenly to obtain an organic chelating agent solution; 2 (SO 4 ) 3 、FeCl 3 Dissolve in an appropriate amount of deionized water and stir evenly to obtain an iron-containing complex solution; add NaHCO 3 and NaH 2 PO 4 Dissolve in an appropriate amount of deionized water and stir evenly to obtain a pH regulator solution; disperse Fe-MOFs and Zn-MOFs in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension;

[0011] (2) The organic chelating agent solution, the iron-containing complex solution, the pH adjusting agent solution, and the bifunctional catalyst suspension are pumped into the microchannel reactor in proportion through the four feed ports of the microchannel reactor. In the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor reacts at a constant temperature to generate a high-efficiency defluorination agent.

[0012] Preferably, the temperature of the isothermal reaction is controlled at 40-60°C.

[0013] In a third aspect, the present invention provides a production device for the above-mentioned high-efficiency defluorination agent, comprising:

[0014] A first venturi mixer, wherein the inlet section of the first venturi mixer is provided with an iron-containing complex solution injection port, and the side wall of the inlet section is provided with an organic chelating agent solution injection port;

[0015] A second venturi mixer, wherein the inlet section of the second venturi mixer is provided with a dual-function catalyst suspension injection port, and the side wall of the inlet section is provided with a pH regulator solution injection port;

[0016] A microchannel reaction device, the microchannel reaction device comprises a shell and a microchannel spiral reactor arranged in the shell, a first venturi mixer and a second venturi mixer are connected to a buffer chamber arranged in the upper part of the shell through a Y-type mixer, an inlet end of the microchannel spiral reactor is connected to the buffer chamber, and an outlet end thereof is connected to a liquid collecting chamber arranged in the lower part of the shell; a heat medium outlet, a heat medium inlet, and a reagent outlet are arranged on the shell, and the reagent outlet is connected to the liquid collecting chamber.

[0017] Furthermore, the microchannel spiral reactor comprises a spiral countercurrent microreaction channel, a spiral downstream microreaction channel, and a maturation chamber. The maturation chamber is a circular tube and is located at the center of the spiral countercurrent microreaction channel and the spiral downstream microreaction channel. The inlet end of the spiral countercurrent microreaction channel is connected to the buffer chamber, and its outlet end is connected to the maturation chamber. The inlet end of the spiral downstream microreaction channel is connected to the maturation chamber, and its outlet end is connected to the liquid collecting chamber. An axial through heat exchange channel is formed between the spiral countercurrent microreaction channel and the spiral downstream microreaction channel. A plurality of first baffles are arranged in the spiral countercurrent microreaction channel and the spiral downstream microreaction channel, so that the spiral countercurrent microreaction channel and the spiral downstream microreaction channel are subdivided into a plurality of layers of microreaction channels.

[0018] Preferably, a plurality of second partitions are provided in the maturation chamber, and the second partitions subdivide the maturation chamber into a plurality of layers of micro-maturation chambers.

[0019] Furthermore, a liquid distributor is provided in the buffer chamber, the liquid distributor is located at the bottom of the buffer chamber, a groove is provided on the top surface of the liquid distributor, a plurality of liquid distribution holes are provided in the groove, and each liquid distribution hole corresponds to a micro-reaction channel of the spiral countercurrent micro-reaction channel.

[0020] Compared with the prior art, the beneficial technical effects of the present invention are:

[0021] (1) The defluorination agent of the present invention can efficiently remove fluoride ions from water through multiple mechanisms such as chelation stabilization, precipitation defluorination, catalytic oxidation, adsorption defluorination and pH buffering adjustment. HEDTA and DTPA are multidentate ligands that can bind to metal ions (such as Ca 2+ Mg 2+ , Fe 3+ By chelating metal ions, it prevents them from forming insoluble precipitates with fluoride ions (such as CaF 2), thereby improving the removal efficiency of fluoride ions; chelating agents can stabilize Fe 3+ , to prevent its hydrolysis to form Fe(OH)3 precipitation, and ensure Fe 3+ Can fully react with fluoride ions. Fe 2 (SO 4 ) 3 With FeCl 3 Forming composite iron salts to improve the solubility and reactivity of iron ions, Fe 3+ Reacts with fluoride ions to form insoluble FeF 3 Precipitation, thereby achieving the removal of fluoride ions, Fe in water 3+ Oxidized to Fe under the action of catalyst 3+ , further enhancing the defluorination effect. NaHCO 3 and NaH 2 PO 4 It can form a buffer system to maintain the pH of the agent in the range of 7-9, avoiding local pH being too high or too low. The appropriate pH condition is conducive to Fe 3+ Reaction with fluoride ions while preventing Fe(OH) 3 The active metal centers Fe and Zn in MOFs can catalyze Fe 2+ Oxidized to Fe 3+ , enhance the defluorination effect, MOFs have a high specific surface area and rich pore structure, can adsorb fluoride ions, and further improve the defluorination efficiency. Propylene glycol can improve the solubility of the agent, ensure the uniform dispersion of each component, improve the fluidity of the agent, facilitate transmission and mixing in the microchannel reactor, and prevent the agent from stratification or precipitation during storage and use.

[0022] (2) The defluorination agent of the present invention adopts a microchannel reactor for continuous production, thereby improving the uniformity and stability of the agent and ensuring its defluorination effect; improving production efficiency, reducing the interval time of batch production, and increasing output.

[0023] (3) The defluorination agent of the present invention is suitable for defluorination treatment of drinking water, industrial wastewater and groundwater. After being used for treating low-fluoride and medium-fluoride concentration water bodies, the fluoride ion concentration is reduced to below 1 mg / L, meeting the water quality recovery standards for drinking water and groundwater. The amount of sludge generated during the defluorination process is relatively small. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 It is a main cross-sectional view of the production equipment of the high-efficiency defluorination agent of the present invention;

[0025] Figure 2 It is a left view of the production equipment of the high-efficiency defluorination agent of the present invention;

[0026] Figure 3 for Figure 1 A three-dimensional image of a microchannel spiral reactor;

[0027] Figure 4 for Figure 3 A top cross-sectional view of the microchannel spiral reactor;

[0028] Figure 5 for Figure 1 A three-dimensional diagram of the liquid distributor;

[0029] Figure markings: 1-first venturi mixer, 101-iron-containing complex solution injection port, 102-organic chelating agent solution injection port, 2-second venturi mixer, 201-bifunctional catalyst suspension injection port, 202-pH adjuster solution injection port, 3-Y-type mixer, 4-microchannel reaction device, 401-buffer chamber, 402-liquid distributor, 403-microchannel spiral reactor, 4031-spiral countercurrent microreaction channel, 4032-spiral downstream microreaction channel, 4033-maturation chamber, 4034-first partition, 4035-second partition, 404-liquid collecting chamber, 405-agent outlet, 406-heat medium outlet, 407-heat medium inlet. DETAILED DESCRIPTION

[0030] The technical solution of the present invention will be described clearly and completely in conjunction with the embodiments below. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0031] Example 1

[0032] The high-efficiency defluorination agent provided in this embodiment is composed, by weight percentage, of 2% HEDTA (N,N'-bis(2-hydroxyethyl)ethylenediamine-N,N'-diacetic acid), 1% DTPA (diethylenetriaminepentaacetic acid), and Fe 2 (SO 4 ) 3 (Ferric sulfate) 6%, FeCl 3 (Ferric chloride) 2%, NaHCO 3 (Sodium bicarbonate) 3%, NaH 2 PO 4 (sodium dihydrogen phosphate) 1%, Fe-MOFs 0.5%, Zn-MOFs 0.5%, propylene glycol 4% and deionized water 80%, wherein Fe-MOFs adopts MIL-101(Fe) and Zn-MOFs adopts ZIF-8.

[0033] The preparation method of the high-efficiency defluorination agent provided in this embodiment is as follows: HEDTA and DTPA are dissolved in an appropriate amount of deionized water, and stirred evenly to obtain an organic chelating agent solution; Fe 2 (SO 4 ) 3 、FeCl 3 Dissolve in an appropriate amount of deionized water and stir evenly to obtain an iron-containing complex solution; add NaHCO 3 and NaH 2 PO 4 Dissolve in an appropriate amount of deionized water, stir evenly to obtain a pH regulator solution; disperse Fe-MOFs and Zn-MOFs in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension; pump the organic chelating agent solution, the iron-containing complex solution, the pH regulator solution, and the bifunctional catalyst suspension into the microchannel reactor in proportion through the four feed ports of the microchannel reactor, and in the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor reacts at a constant temperature at 40°C to generate a high-efficiency defluorination agent.

[0034] The high-efficiency defluoridation agent of this embodiment is a low-concentration formula, which is suitable for the treatment of low-fluoride concentration water (such as drinking water). In actual application, the defluoridation agent of this embodiment is added to the drinking water treatment system, and the dosage of the agent is 0.8-1kg / m 3 .

[0035] Example 2

[0036] The high-efficiency defluorination agent provided in this embodiment is composed of 3% HEDTA, 1.5% DTPA, and Fe 2 (SO 4 ) 3 6.5%, FeCl 3 2.5%, NaHCO 3 4%, NaH 2 PO 4 1.5%, Fe-MOFs 0.75%, Zn-MOFs 0.75%, propylene glycol 4.5% and deionized water 75%, wherein Fe-MOFs adopts MIL-101(Fe) and Zn-MOFs adopts ZIF-8.

[0037] The preparation method of the high-efficiency defluorination agent provided in this embodiment is as follows: HEDTA and DTPA are dissolved in an appropriate amount of deionized water, and stirred evenly to obtain an organic chelating agent solution; Fe 2 (SO 4 ) 3 、FeCl 3 Dissolve in an appropriate amount of deionized water and stir evenly to obtain an iron-containing complex solution; add NaHCO3 and NaH 2 PO 4 Dissolve in an appropriate amount of deionized water, stir evenly to obtain a pH regulator solution; disperse Fe-MOFs and Zn-MOFs in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension; pump the organic chelating agent solution, the iron-containing complex solution, the pH regulator solution, and the bifunctional catalyst suspension into the microchannel reactor in proportion through the four feed ports of the microchannel reactor, and in the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor reacts at a constant temperature of 50°C to generate a high-efficiency defluorination agent.

[0038] The high-efficiency defluoridation agent of this embodiment is a medium-concentration formula, which is suitable for the treatment of medium-fluoride concentration water (such as groundwater). In actual application, the defluoridation agent of this embodiment is added to the groundwater recovery treatment system at a dosage of 1kg / m 3 .

[0039] Example 3

[0040] The high-efficiency defluorination agent provided in this embodiment is composed of 4% HEDTA, 2% DTPA, and Fe 2 (SO 4 ) 3 7%, FeCl 3 3%, NaHCO 3 5%, NaH 2 PO 4 2%, Fe-MOFs 1%, Zn-MOFs 1%, propylene glycol 5% and deionized water 70%, wherein Fe-MOFs adopts MIL-101(Fe) and Zn-MOFs adopts ZI F-8.

[0041] The preparation method of the high-efficiency defluorination agent provided in this embodiment is as follows: HEDTA and DTPA are dissolved in an appropriate amount of deionized water, and stirred evenly to obtain an organic chelating agent solution; Fe 2 (SO 4 ) 3 、FeCl 3 Dissolve in an appropriate amount of deionized water and stir evenly to obtain an iron-containing complex solution; add NaHCO 3 and NaH 2 PO 4Dissolve in an appropriate amount of deionized water, stir evenly to obtain a pH regulator solution; disperse Fe-MOFs and Zn-MOFs in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension; pump the organic chelating agent solution, the iron-containing complex solution, the pH regulator solution, and the bifunctional catalyst suspension into the microchannel reactor in proportion through the four feed ports of the microchannel reactor, and in the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor reacts at a constant temperature of 60°C to generate a high-efficiency defluorination agent.

[0042] The high-efficiency defluorination agent of this embodiment is a high-concentration formula, which is suitable for the preliminary treatment of high-fluorine concentration water (such as industrial wastewater). In practical applications, the defluorination agent of this embodiment is added to the industrial wastewater treatment system, and the agent dosage is 1-1.5kg / m 3 .

[0043] Comparative Example 1

[0044] A defluorination agent, calculated by weight percentage, consisting of CaCl 2 (Calcium chloride) 10kg, NaOH (sodium hydroxide) 5kg, deionized water 85kg.

[0045] The defluoridation agent is a formula used in the traditional chemical precipitation method (calcium salt method).

[0046] Comparative Example 2

[0047] A defluorination agent is composed of 10 kg of activated alumina and 90 kg of deionized water in terms of weight percentage.

[0048] The defluorination agent is a formula used in the activated alumina adsorption method.

[0049] Test example: Fluorine removal performance test

[0050] The defluorination effects of the defluorination agents of Examples 1-3 and Comparative Examples 1-2 were tested, and the results are shown in the following table.

[0051]

[0052] The test results show that: (1) the defluorination efficiency of the defluorination agents of Examples 1 and 2 is significantly higher than that of the defluorination agents of Comparative Examples 1 and 2. After treatment with the defluorination agent of Example 1, the fluoride ion concentration reaches 0.9 mg / L, which is reduced to below 1 mg / L and meets the drinking water standard. After treatment with the defluorination agent of Example 2, the fluoride ion concentration reaches 0.8 mg / L, which is reduced to below 1 mg / L and meets the groundwater quality recovery standard. (2) The defluorination agents of Examples 1 and 2 are suitable for water bodies with low and medium fluoride concentrations, while the applicable scenarios of Comparative Examples 1 and 2 are limited. (3) Although the cost of Examples 1 and 2 is slightly higher than that of Comparative Example 1, it is much lower than that of Comparative Example 2. (4) The defluorination agent of Comparative Example 1 not only has a low defluorination efficiency, but also produces a large amount of sludge. The defluorination agents of Examples 1 and 2 produce less sludge during the defluorination process, and are more environmentally friendly than Comparative Example 1. It can be seen that although the cost of the defluorination agent of the present invention is slightly higher than that of the traditional calcium salt method, it has significant advantages in terms of high defluorination efficiency, fluoride ion concentration after treatment and environmental protection, making it a better choice.

[0053] Example 4

[0054] Please see attached Figure 1-5 As shown, the production equipment of a high-efficiency defluorination agent provided in this embodiment includes a first Venturi mixer, a second Venturi mixer, a Y-type mixer and a microchannel reaction device.

[0055] Specifically, the inlet section of the first venturi mixer is provided with an iron-containing complex solution injection port, and the side wall of the inlet section is provided with an organic chelating agent solution injection port; the inlet section of the second venturi mixer is provided with a dual-function catalyst suspension injection port, and the side wall of the inlet section is provided with a pH regulator solution injection port.

[0056] Specifically, the microchannel reaction device includes a shell and a microchannel spiral reactor arranged in the shell, the first venturi mixer and the second venturi mixer are connected to the buffer chamber arranged in the upper part of the shell through a Y-type mixer, the inlet end of the microchannel spiral reactor is connected to the buffer chamber, and its outlet end is connected to the liquid collecting chamber arranged in the lower part of the shell; a heat medium outlet, a heat medium inlet, and a reagent outlet are provided on the shell, and the reagent outlet is connected to the liquid collecting chamber; the microchannel spiral reactor includes a spiral countercurrent microreaction channel, a spiral downstream microreaction channel, and a maturation chamber, the maturation chamber is a circular tube, and is located at the center of the spiral countercurrent microreaction channel and the spiral downstream microreaction channel, the inlet end of the spiral countercurrent microreaction channel is connected to the buffer chamber, and its outlet end is connected to A maturation chamber, an inlet end of the spiral downstream micro-reaction channel is connected to the maturation chamber, and an outlet end thereof is connected to the liquid collecting chamber, an axial through heat exchange channel is formed between the spiral countercurrent micro-reaction channel and the spiral downstream micro-reaction channel, a plurality of first partitions are arranged in the spiral countercurrent micro-reaction channel and the spiral downstream micro-reaction channel, so that the spiral countercurrent micro-reaction channel and the spiral downstream micro-reaction channel are both subdivided into a plurality of layers of micro-reaction channels, a plurality of second partitions are arranged in the maturation chamber, and the second partitions subdivide the maturation chamber into a plurality of layers of micro-maturation chambers, a liquid distributor is arranged in the buffer chamber, the liquid distributor is located at the bottom of the buffer chamber, a groove is arranged on the top surface of the liquid distributor, a plurality of liquid distribution holes are arranged in the groove, and each liquid distribution hole corresponds to a micro-reaction channel of the spiral countercurrent micro-reaction channel.

[0057] In this embodiment, the width of the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel is 1-2 mm, and the first partition plate subdivides the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel into several layers of micro-reaction channels with a length of 1-2 mm.

[0058] In actual applications, each injection port is equipped with a precision flow meter and a pump to ensure that each component is added in proportion. A pH sensor and a temperature sensor can be set in each micro-ripening chamber, and a PLC control system is used to monitor the pH and temperature of the mixed liquid in real time.

[0059] In this embodiment, the heat medium enters the shell from the heat medium inlet, heats the spiral countercurrent microreaction channel and the spiral downstream microreaction channel through the axially connected heat exchange flow channel, and then flows out from the heat medium outlet; the iron-containing complex solution and the organic chelating agent solution are premixed through the first Venturi mixer, and at the same time, the bifunctional catalyst suspension and the pH adjuster solution injection port are premixed through the second Venturi mixer, and the two premixed solutions are mixed again through the Y-type mixer and enter the buffer chamber, and enter the spiral countercurrent microreaction channel after being distributed by the liquid distributor, and enter the maturation chamber after counterclockwise swirling from the outside to the inside, and the mixed liquid in the maturation chamber enters the liquid collecting chamber after clockwise swirling from the inside to the outside through the spiral downstream microreaction channel; the mixture is fully reacted in the spiral countercurrent microreaction channel and the spiral downstream microreaction channel to generate a defluorination agent, and the heat medium maintains the temperature of the microchannel spiral reactor at 40-60°C.

[0060] 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 technical solution and conceptual invention of the present invention should be included in the protection scope of the present invention.

Claims

1. A highly efficient defluorination agent, characterized in that: Calculated by weight percentage, it includes: HEDTA 2-4%, DTPA 1-2%, Fe2(SO4)36-7%, FeCl32-3%, NaHCO33-5%, NaH2PO41-2%, Fe-MOFs0.5-1%, Zn-MOFs0.5-1%, propylene glycol4-5% and deionized water70-80%.

2. A highly efficient defluorination agent according to claim 1, characterized in that: The Fe-MOFs adopts MIL-101(Fe).

3. A highly efficient defluorination agent according to claim 1, characterized in that: The Zn-MOFs described herein adopts ZIF-8.

4. A method for producing a highly efficient defluorination agent according to any one of claims 1 to 3, characterized in that: The following steps are involved: (1) Dissolving HEDTA and DTPA in an appropriate amount of deionized water and stirring evenly to obtain an organic chelating agent solution; dissolving Fe2(SO4)3 and FeCl3 in an appropriate amount of deionized water and stirring evenly to obtain an iron-containing complex solution; dissolving NaHCO3 and NaH2PO4 in an appropriate amount of deionized water and stirring evenly to obtain a pH regulator solution; dispersing Fe-MOFs and Zn-MOFs in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension; (2) The organic chelating agent solution, the iron-containing complex solution, the pH adjusting agent solution, and the bifunctional catalyst suspension are pumped into the microchannel reactor in proportion through the four feed ports of the microchannel reactor. In the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor reacts at a constant temperature to generate a high-efficiency defluorination agent.

5. The production method according to claim 4, characterized in that: The temperature of the isothermal reaction is controlled at 40-60°C.

6. A production equipment for a high-efficiency defluorination agent as claimed in any one of claims 1 to 3, characterized in that: include: A first venturi mixer, wherein the inlet section of the first venturi mixer is provided with an iron-containing complex solution injection port, and the side wall of the inlet section is provided with an organic chelating agent solution injection port; A second venturi mixer, wherein the inlet section of the second venturi mixer is provided with a dual-function catalyst suspension injection port, and the side wall of the inlet section is provided with a pH regulator solution injection port; A microchannel reaction device, the microchannel reaction device comprises a shell and a microchannel spiral reactor arranged in the shell, a first venturi mixer and a second venturi mixer are connected to a buffer chamber arranged in the upper part of the shell through a Y-type mixer, an inlet end of the microchannel spiral reactor is connected to the buffer chamber, and an outlet end thereof is connected to a liquid collecting chamber arranged in the lower part of the shell; a heat medium outlet, a heat medium inlet, and a reagent outlet are arranged on the shell, and the reagent outlet is connected to the liquid collecting chamber.

7. The production equipment according to claim 6, characterized in that: The microchannel spiral reactor comprises a spiral countercurrent microreaction channel, a spiral downstream microreaction channel, and a maturation chamber. The maturation chamber is a circular tube and is located at the center of the spiral countercurrent microreaction channel and the spiral downstream microreaction channel. The inlet end of the spiral countercurrent microreaction channel is connected to the buffer chamber, and the outlet end thereof is connected to the maturation chamber. The inlet end of the spiral downstream microreaction channel is connected to the maturation chamber, and the outlet end thereof is connected to the liquid collecting chamber. An axially through heat exchange channel is formed between the spiral countercurrent microreaction channel and the spiral downstream microreaction channel. A plurality of first baffles are arranged in the spiral countercurrent microreaction channel and the spiral downstream microreaction channel, so that the spiral countercurrent microreaction channel and the spiral downstream microreaction channel are subdivided into a plurality of layers of microreaction channels.

8. The production equipment according to claim 7, characterized in that: A plurality of second partitions are arranged in the ripening chamber, and the second partitions subdivide the ripening chamber into a plurality of layers of micro-ripening chambers.

9. The production equipment according to claim 8, characterized in that: A liquid distributor is arranged in the buffer cavity, the liquid distributor is located at the bottom of the buffer cavity, a groove is provided on the top surface of the liquid distributor, a plurality of liquid distribution holes are provided in the groove, and each liquid distribution hole corresponds to a micro-reaction channel of the spiral countercurrent micro-reaction channel.

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