High-efficiency fluoride removal agent and production method and equipment thereof

Abstract

The application discloses a high-efficiency fluorine removal agent and a production method and equipment thereof, and relates to the technical field of fluorine-containing wastewater treatment. The high-efficiency fluorine removal agent comprises HEDTA, DTPA, Fe2(SO4)3, FeCl3, NaHCO3, NaH2PO4, Fe-MOFs, Zn-MOFs, propylene glycol and deionized water. The fluorine removal agent can efficiently remove fluorine ions in water through multiple action mechanisms such as chelation stability, fluorine removal by precipitation, catalytic oxidation, fluorine removal by adsorption and pH buffer adjustment. The micro-channel reactor is used for continuous production, the uniformity and stability of the agent are improved, and the fluorine removal effect is ensured. The fluorine removal agent is suitable for fluorine removal treatment of drinking water, industrial wastewater and groundwater. After the fluorine removal agent is used for low-fluorine and medium-fluorine concentration water body treatment, the fluorine ion concentration is reduced to below 1 mg / L, and the drinking water and groundwater quality recovery standards are reached. The amount of sludge generated in the fluorine removal process is small.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of fluorine-containing wastewater treatment, and particularly relates to a high-efficiency defluorination agent and a production method and equipment thereof. BACKGROUND

[0002] Fluorine-containing wastewater refers to industrial wastewater containing fluoride ions. Fluoride ion-containing wastewater is almost ubiquitous in various industrial fields, from basic material production to high-tech manufacturing. Fluoride ions have strong corrosive and toxic properties, posing a serious threat to the ecological environment and human health. Long-term contact or drinking of water with high fluoride concentration can adversely affect human health, such as chronic diseases such as dental caries, fluorosis, and fluorosis, and even damage to the human brain. The treatment of fluoride-containing wastewater faces many challenges, including large water volume, complex composition, and high treatment cost. With the rapid development of industry, the discharge of fluoride-containing wastewater is increasing, which puts a huge pressure on treatment facilities. In addition, wastewater may contain other pollutants such as heavy metals and organic matter, making the treatment process more complex. Therefore, it is necessary to continuously develop and innovate more efficient and economical wastewater treatment technologies to meet these challenges.

[0003] In the treatment process of fluoride-containing wastewater, precipitation and adsorption are two commonly used treatment methods, which have certain effects but also have some defects. Precipitation usually adds lime (CaO), calcium hydroxide (Ca(OH)2), or aluminum salts (such as alum) to react with fluoride ions in wastewater to form calcium fluoride or aluminum fluoride precipitates; this method is difficult to achieve deep defluorination, and for applications that require high-precision defluorination, precipitation may not meet the requirements. Adsorption usually uses activated alumina, bone charcoal, modified zeolite, etc. as adsorbents 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 complex and costly. The adsorption capacity of the adsorbent is limited, and when the adsorbent is saturated, new adsorbents need to be replaced, which increases the treatment cost and may cause secondary pollution. Although adsorption has certain treatment effect on wastewater with low fluoride concentration, when the fluoride ion concentration in wastewater is very low, the treatment effect of adsorption may be limited. SUMMARY

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

[0005] To achieve the above-mentioned purpose, the present application adopts the following technical solutions:

[0006] In a first aspect, the present application provides a high-efficiency fluoride removal agent, comprising, in percentage by weight: HEDTA 2-4%, DTPA 1-2%, Fe2(SO4)3 6-7%, FeCl3 2-3%, NaHCO3 3-5%, NaH2PO4 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 application, the Fe-MOFs are MIL-101(Fe).

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

[0009] In a second aspect, the present application provides a production method of the high-efficiency fluoride removal agent described above, comprising the following steps:

[0010] (1) Dissolve HEDTA and DTPA in an appropriate amount of deionized water, stir until uniform, to obtain an organic chelating agent solution; dissolve Fe2(SO4)3 and FeCl3 in an appropriate amount of deionized water, stir until uniform, to obtain an iron-containing complex solution; dissolve NaHCO3 and NaH2PO4 in an appropriate amount of deionized water, stir until uniform, to obtain a pH adjuster 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) Pump the organic chelating agent solution, the iron-containing complex solution, the pH adjuster solution, and the bifunctional catalyst suspension through the four feed ports of the micro-channel reactor in proportion, mix the components in the mixing channel to form a uniform agent precursor, and perform constant-temperature reaction of the agent precursor in the reaction channel to generate the high-efficiency fluoride removal agent.

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

[0013] In a third aspect, the present application provides a production device of the high-efficiency fluoride removal agent described above, comprising:

[0014] a first Venturi mixer, an iron-containing complex solution injection port being arranged at an inlet section of the first Venturi mixer, and an organic chelating agent solution injection port being arranged at a side wall of the inlet section of the first Venturi mixer;

[0015] a second Venturi mixer, a bifunctional catalyst suspension injection port being arranged at an inlet section of the second Venturi mixer, and a pH adjuster solution injection port being arranged at a side wall of the inlet section of the second Venturi mixer;

[0016] The micro-channel reaction device comprises a shell and a micro-channel spiral reactor arranged in the shell, a first Venturi mixer and a second Venturi mixer are connected to the shell through a Y-type mixer and an upper buffer cavity arranged in the shell, an inlet end of the micro-channel spiral reactor is connected to the buffer cavity, and an outlet end thereof is connected to a liquid collecting cavity arranged in a lower part of the shell; a hot medium outlet, a hot medium inlet and a medicament outlet are arranged on the shell, and the medicament outlet is communicated with the liquid collecting cavity.

[0017] Further, the micro-channel spiral reactor comprises a spiral countercurrent micro-reaction channel, a spiral cocurrent micro-reaction channel and a maturation chamber, the maturation chamber is a circular tube and is located at the center of the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, an inlet end of the spiral countercurrent micro-reaction channel is connected to the buffer cavity, and an outlet end thereof is connected to the maturation chamber, an inlet end of the spiral cocurrent micro-reaction channel is connected to the maturation chamber, and an outlet end thereof is connected to the liquid collecting cavity, an axial through heat exchange flow channel is formed between the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, and a plurality of first partitions are arranged in the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, so that the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel are subdivided into a plurality of layers of micro-reaction channels.

[0018] Preferably, 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 cavities.

[0019] Further, a liquid distributor is arranged in the buffer cavity, the liquid distributor is located at the bottom of the buffer cavity, a groove is formed in the top surface of the liquid distributor, a plurality of liquid distribution holes are formed in the groove, and each liquid distribution hole corresponds to one micro-reaction channel of the spiral countercurrent micro-reaction channel.

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

[0021] (1) The defluorination medicament of the present application can efficiently remove fluorine ions in water through multiple action mechanisms such as chelation stabilization, precipitation defluorination, catalytic oxidation, adsorption defluorination and pH buffer adjustment. HEDTA and DTPA are polydentate ligands, which can form stable chelates with metal ions (such as Ca 2+ , Mg 2+ , Fe 3+ , etc.) in water, chelate metal ions, prevent them from forming insoluble precipitates (such as CaF2) with fluorine ions, and thus improve the removal efficiency of fluorine ions; the chelating agent can stabilize Fe 3+ , prevent it from hydrolyzing to form Fe(OH)3 precipitate, and ensure that Fe 3+ can fully react with fluorine ions. Fe2(SO4)3 and FeCl3 form a complex iron salt, which improves the solubility and reactivity of iron ions, and Fe 3+ reacts with fluorine ions to form insoluble FeF3 precipitate, thereby achieving the removal of fluorine ions, and Fe 3+Fe 3+ , further enhancing the defluorination effect. NaHCO3 and NaH2PO4 can form a buffer system to maintain the pH of the medicament in the range of 7-9, avoiding excessive or excessive local pH, and suitable pH conditions are conducive to the reaction of Fe 3+ with fluoride ions, while preventing the formation of Fe(OH)3 precipitate. The active metal centers Fe and Zn in MOFs can catalyze the oxidation of Fe 2+ to Fe 3+ , enhancing the defluorination effect. MOFs have high specific surface area and rich pore structure, which can adsorb fluoride ions, further improving the defluorination efficiency. Propylene glycol can improve the solubility of the medicament, ensure uniform dispersion of each component, and improve the flowability of the medicament, facilitating transportation and mixing in the micro-channel reactor, preventing stratification or precipitation of the medicament during storage and use.

[0022] (2) The defluorination medicament of the present application is produced continuously in a micro-channel reactor, improving the uniformity and stability of the medicament and ensuring its defluorination effect; improving production efficiency, reducing the interval time of batch production, and increasing yield.

[0023] (3) The defluorination medicament of the present application is suitable for defluorination treatment of drinking water, industrial wastewater and groundwater; after treatment of low-fluorine and medium-fluorine concentration water bodies, the concentration of fluoride ions is reduced to below 1 mg / L, meeting the drinking water and groundwater quality restoration standards; the amount of sludge generated during defluorination is less. BRIEF DESCRIPTION OF DRAWINGS

[0024] Figure 1 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application;

[0025] Figure 2 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application;

[0026] Figure 3 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application; Figure 1 is a perspective view of the micro-channel spiral reactor;

[0027] Figure 4 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application; Figure 3 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application;

[0028] Figure 5 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application; Figure 1 is a front view of the production equipment of the high-efficiency defluorination medicament of the present application;

[0029] Reference signs: 1-first venturi mixer, 101-iron complex solution injection port, 102-organic chelating agent solution injection port, 2-second venturi mixer, 201-bifunctional catalyst suspension injection port, 202-pH regulator solution injection port, 3-Y mixer, 4-micro-channel reaction device, 401-buffer cavity, 402-distributing device, 403-micro-channel spiral reactor, 4031-spiral countercurrent micro-reaction channel, 4032-spiral cocurrent micro-reaction channel, 4033-maturation chamber, 4034-first partition, 4035-second partition, 404-liquid collecting cavity, 405-drug outlet, 406-thermal medium outlet, 407-thermal medium inlet. DETAILED DESCRIPTION

[0030] The technical solutions in the present application will be clearly and completely described in combination with the embodiments below. Obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative work fall within the protection scope of the present application.

[0031] Embodiment 1

[0032] The high-efficiency fluoride removal agent provided in the embodiment is composed of HEDTA (N,N'-bis(2-hydroxyethyl)ethylenediamine-N,N'-diacetic acid) 2%, DTPA (diethylene triamine pentaacetic acid) 1%, Fe2(SO4)3 (ferric sulfate) 6%, FeCl3 (ferric chloride) 2%, NaHCO3 (sodium bicarbonate) 3%, NaH2PO4 (sodium dihydrogen phosphate) 1%, Fe-MOFs 0.5%, Zn-MOFs 0.5%, propylene glycol 4% and deionized water 80% by weight percentage, wherein the Fe-MOFs adopts MIL-101 (Fe) and the Zn-MOFs adopts ZIF-8.

[0033] The preparation method of the high-efficiency fluoride removal agent provided in the embodiment is as follows: dissolving HEDTA and DTPA in a proper amount of deionized water, stirring uniformly to obtain an organic chelating agent solution; dissolving Fe2(SO4)3 and FeCl3 in a proper amount of deionized water, stirring uniformly to obtain an iron complex solution; dissolving NaHCO3 and NaH2PO4 in a proper amount of deionized water, stirring uniformly 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; pumping the organic chelating agent solution, the iron complex solution, the pH regulator solution and the bifunctional catalyst suspension into a micro-channel reactor through four feeding ports of the micro-channel reactor in proportion, fully mixing the components in a mixing channel to form a uniform drug precursor; and reacting the drug precursor at 40℃ in a reaction channel to generate the high-efficiency fluoride removal agent.

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

[0035] Embodiment 2

[0036] The high-efficiency fluoride removal agent provided in the embodiment consists of, by weight percentage, HEDTA 3%, DTPA 1.5%, Fe2(SO4)3 6.5%, FeCl3 2.5%, NaHCO3 4%, NaH2PO4 1.5%, Fe-MOFs 0.75%, Zn-MOFs 0.75%, propylene glycol 4.5%, and deionized water 75%, wherein the Fe-MOFs adopt MIL-101 (Fe), and the Zn-MOFs adopt ZIF-8.

[0037] The preparation method of the high-efficiency fluoride removal agent provided in the embodiment is as follows: HEDTA and DTPA are dissolved in an appropriate amount of deionized water, and stirred uniformly to obtain an organic chelating agent solution; Fe2(SO4)3 and FeCl3 are dissolved in an appropriate amount of deionized water, and stirred uniformly to obtain an iron-containing complex solution; NaHCO3 and NaH2PO4 are dissolved in an appropriate amount of deionized water, and stirred uniformly to obtain a pH adjusting agent solution; Fe-MOFs and Zn-MOFs are dispersed in a mixture of propylene glycol and deionized water to form a uniform bifunctional catalyst suspension; the organic chelating agent solution, the iron-containing complex solution, the pH adjusting agent solution, and the bifunctional catalyst suspension are pumped into a micro-channel reactor through four feed ports of the micro-channel reactor in proportion, and in the mixing channel, the components are fully mixed to form a uniform agent precursor; in the reaction channel, the agent precursor is reacted at a constant temperature of 50°C to generate the high-efficiency fluoride removal agent.

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

[0039] Embodiment 3

[0040] The high-efficiency fluoride removal agent provided in the embodiment is composed of HEDTA 4%, DTPA 2%, Fe2(SO4)3 7%, FeCl3 3%, NaHCO3 5%, NaH2PO4 2%, Fe-MOFs 1%, Zn-MOFs 1%, propylene glycol 5% and deionized water 70% by weight percentage, wherein the Fe-MOFs adopts MIL-101(Fe) and the Zn-MOFs adopts ZIF-8.

[0041] The preparation method of the high-efficiency fluoride removal agent provided in the embodiment is as follows: dissolving HEDTA and DTPA in a proper amount of deionized water, stirring uniformly to obtain an organic chelating agent solution; dissolving Fe2(SO4)3 and FeCl3 in a proper amount of deionized water, stirring uniformly to obtain an iron-containing compound solution; dissolving NaHCO3 and NaH2PO4 in a proper amount of deionized water, stirring uniformly 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; pumping the organic chelating agent solution, the iron-containing compound solution, the pH regulator solution and the bifunctional catalyst suspension into a micro-channel reactor through four feed ports of the micro-channel reactor in proportion, fully mixing the components in a mixing channel to form a uniform agent precursor; and reacting the agent precursor at 60°C in a reaction channel to generate the high-efficiency fluoride removal agent.

[0042] The high-efficiency fluoride removal agent of the embodiment is a high-concentration formula, which is suitable for the preliminary treatment of high-fluorine-concentration water bodies (such as industrial wastewater). In actual application, the fluoride removal agent of the embodiment is added to an industrial wastewater treatment system, and the agent addition amount is 1-1.5 kg / m 3 .

[0043] Comparative Example 1

[0044] A fluoride removal agent is composed of CaCl2(calcium chloride) 10 kg, NaOH (sodium hydroxide) 5 kg and deionized water 85 kg by weight percentage.

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

[0046] Comparative Example 2

[0047] A fluoride removal agent is composed of active alumina 10 kg and deionized water 90 kg by weight percentage.

[0048] The fluoride removal agent is a formula used in the active alumina adsorption method.

[0049] Test Example Fluoride 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] From the test results, it can be seen 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, wherein the fluorine ion concentration after treatment of the defluorination agent of Example 1 reaches 0.9 mg / L, and is reduced to below 1 mg / L, reaching the drinking water standard, and the fluorine ion concentration after treatment of the defluorination agent of Example 2 reaches 0.8 mg / L, and is reduced to below 1 mg / L, reaching the groundwater quality recovery standard; (2) the defluorination agents of Examples 1 and 2 are suitable for low-fluorine and medium-fluorine concentration water bodies, while the application 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 low defluorination efficiency, but also produces a large amount of sludge, and the amount of sludge produced during the defluorination process of the defluorination agents of Examples 1 and 2 is less, and the environmental protection performance is better than that of Comparative Example 1. It can be seen that although the defluorination agent of the present application has a slightly higher cost than the traditional calcium salt method, it has significant advantages in defluorination efficiency, fluorine ion concentration after treatment, and environmental protection, making it a better choice.

[0053] Example 4

[0054] Please refer to the accompanying Figures 1-5 The production equipment of the high-efficiency defluorination agent provided by the present embodiment comprises a first Venturi mixer, a second Venturi mixer, a Y-shaped mixer, and a micro-channel reaction device.

[0055] Specifically, the inlet section of the first Venturi mixer is provided with an iron 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 bifunctional catalyst suspension injection port, and the side wall of the inlet section is provided with a pH adjuster solution injection port.

[0056] Specifically, the micro-channel reaction device comprises a shell and a micro-channel spiral reactor arranged in the shell, a first Venturi mixer and a second Venturi mixer are connected to an upper buffer cavity arranged in the shell through a Y-type mixer, an inlet end of the micro-channel spiral reactor is connected to the buffer cavity, and an outlet end of the micro-channel spiral reactor is connected to a lower liquid collecting cavity arranged in the shell; a hot medium outlet, a hot medium inlet and a medicament outlet are arranged on the shell, and the medicament outlet is communicated with the liquid collecting cavity; the micro-channel spiral reactor comprises a spiral countercurrent micro-reaction channel, a spiral cocurrent micro-reaction channel and a maturation chamber, the maturation chamber is a circular tube and is located at the center of the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, the inlet end of the spiral countercurrent micro-reaction channel is connected to the buffer cavity, and the outlet end of the spiral countercurrent micro-reaction channel is connected to the maturation chamber, the inlet end of the spiral cocurrent micro-reaction channel is connected to the maturation chamber, and the outlet end of the spiral cocurrent micro-reaction channel is connected to the liquid collecting cavity, an axial through heat exchange flow channel is formed between the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, a plurality of first partitions are arranged in the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, so that the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel are 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 cavities, and a liquid distributor is arranged in the buffer cavity, the liquid distributor is located at the bottom of the buffer cavity, a groove is formed in the top surface of the liquid distributor, a plurality of liquid distribution holes are formed in the groove, and each liquid distribution hole corresponds to one micro-reaction channel of the spiral countercurrent micro-reaction channel.

[0057] In the embodiment, the width of the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel is 1-2 mm, and the first partitions subdivide the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel into a plurality of layers of micro-reaction channels with a length of 1-2 mm.

[0058] In actual application, a precise flowmeter and a pump are arranged at each injection port to ensure that the components are added into each micro-maturation cavity in proportion, a pH sensor and a temperature sensor can be arranged, and a PLC control system is used to monitor the pH and temperature of the mixed solution in real time.

[0059] In the embodiment, the hot medium enters the shell from the hot medium inlet, is heated through the axial through heat exchange flow channel to heat the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, and then flows out from the hot medium outlet; the iron-containing compound solution and the organic chelating agent solution are premixed through the first Venturi mixer, at the same time, the bifunctional catalyst suspension and the pH adjuster solution are premixed through the second Venturi mixer, the two kinds of premixed solutions are mixed again through the Y-type mixer, and then enter the buffer cavity, are distributed through the liquid distributor, enter the spiral countercurrent micro-reaction channel, flow counterclockwise from outside to inside, enter the maturation chamber, the mixed solution in the maturation chamber flows clockwise from inside to outside through the spiral cocurrent micro-reaction channel, and then enters the liquid collecting cavity; the mixture is fully reacted in the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel to generate the defluorination medicament, and the temperature of the micro-channel spiral reactor is maintained at 40-60°C by the hot medium.

[0060] The above merely provides the preferred embodiments of the present application, and is not intended to limit the present application. Any modification, equivalent replacement, and improvement made within the technical concept and spirit of the present application should be included in the protection scope of the present application.

Claims

1. A highly efficient fluoride removal agent, characterized by, By weight percentage, it comprises: HEDTA 2-4%, DTPA 1-2%, Fe2(SO4)3 6-7%, FeCl3 2-3%, NaHCO3 3-5%, NaH2PO4 1-2%, Fe-MOFs 0.5-1%, Zn-MOFs 0.5-1%, propylene glycol 4-5%, and deionized water 70-80%.

2. The high-efficiency fluorine removal agent according to claim 1, characterized in that: The Fe-MOFs are MIL-101(Fe).

3. The high-efficiency fluorine removal agent according to claim 1, characterized in that: The Zn-MOFs are ZIF-8.

4. The method for producing a high-efficiency fluorine removal agent according to any one of claims 1 to 3, characterized by, It comprises the following steps: (1) Dissolve HEDTA and DTPA in a proper amount of deionized water, stir uniformly to obtain an organic chelating agent solution; dissolve Fe2(SO4)3 and FeCl3 in a proper amount of deionized water, stir uniformly to obtain an iron-containing compound solution; dissolve NaHCO3 and NaH2PO4 in a proper amount of deionized water, stir uniformly 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; (2) Pump the organic chelating agent solution, the iron-containing compound solution, the pH regulator solution, and the bifunctional catalyst suspension into the micro-channel reactor through the four feed ports of the micro-channel reactor in proportion, mix the components in the mixing channel to form a uniform medicament precursor, and react the medicament precursor at a constant temperature in the reaction channel to generate a high-efficiency fluorine removal medicament.

5. The production method according to claim 4, characterized in that: The constant temperature reaction is controlled at 40-60℃.

6. An apparatus for producing a high-performance fluorine removal agent as claimed in any one of claims 1 to 3, characterized by It comprises: A first Venturi mixer, the inlet section of which is provided with an iron-containing compound 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, the inlet section of which is provided with a bifunctional catalyst suspension injection port, and the side wall of the inlet section is provided with a pH regulator solution injection port; A micro-channel reaction device, which comprises a shell and a micro-channel spiral reactor arranged in the shell, the first Venturi mixer and the second Venturi mixer are connected to the upper part of the buffer cavity in the shell through a Y-type mixer, the inlet end of the micro-channel spiral reactor is connected to the buffer cavity, and the outlet end is connected to the liquid collecting cavity arranged in the lower part of the shell; the shell is provided with a heat medium outlet, a heat medium inlet, and a medicament outlet, and the medicament outlet communicates with the liquid collecting cavity.

7. The production apparatus according to claim 6, characterized by: The micro-channel spiral reactor comprises a spiral countercurrent micro-reaction channel, a spiral cocurrent micro-reaction channel, and a maturation chamber, the maturation chamber is a circular tube and is located in the center of the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, the inlet end of the spiral countercurrent micro-reaction channel is connected to the buffer cavity, and the outlet end is connected to the maturation chamber, the inlet end of the spiral cocurrent micro-reaction channel is connected to the maturation chamber, and the outlet end is connected to the liquid collecting cavity, an axial through heat exchange flow channel is formed between the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, and a plurality of first partitions are arranged in the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel, so that the spiral countercurrent micro-reaction channel and the spiral cocurrent micro-reaction channel are subdivided into a plurality of layers of micro-reaction channels.

8. The production apparatus according to claim 7, characterized by: 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.

9. The production apparatus according to claim 8, characterized by: The buffer cavity is provided with a liquid distributor, the liquid distributor is located at the bottom of the buffer cavity, a groove is formed on the top surface of the liquid distributor, and a plurality of liquid distribution holes are formed in the groove, each liquid distribution hole corresponding to one micro-reaction channel of the spiral counter-flow micro-reaction channel.

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