Continuous light salt brine ammonium removal reaction device and method

Abstract

The invention discloses a continuous light salt brine ammonium removal reaction device and method, and relates to the technical field of light salt brine treatment in the chlor-alkali industry. The device mainly comprises a raw material storage unit, a dechlorination tower, a vertical strong turbulent flow reaction tank, an ammonium blow-off tower, a continuous liquid separator, an alkali liquor absorption tower and a conveying and control module. Light salt brine enters the reaction tank after being subjected to vacuum dechlorination; the method comprises the following steps: continuously adding chlorine water, sodium hypochlorite and other composite oxidants under precise metering, and reacting with light salt brine under the superposed action of vertical strong turbulent flow and compressed air to generate volatilizable chloramine; after a reaction material is subjected to air stripping and liquid separation, qualified light salt brine is discharged, and an organic phase is refluxed and reused. According to the invention, dechlorination-ammonium removal-absorption-circulation integrated continuous operation is realized, the precipitation and scaling risks of equipment are thoroughly eliminated by using a composite system, the ammonium removal thoroughness and production continuity are greatly improved, and the energy consumption and environmental protection pressure are reduced.

Description

Technical Field

[0001] This invention relates to the field of brine treatment technology in the chlor-alkali industry, and particularly to a continuous brine ammonium removal reaction device and method. Background Technology

[0002] Existing brine deammonium removal technologies have several shortcomings in actual production. Traditional processes commonly use a 32% NaOH solution combined with sodium hypochlorite for deammonium removal. This method readily reacts with calcium and magnesium ions in the brine, forming precipitates that cause scaling and clogging of equipment, requiring frequent shutdowns for cleaning and severely impacting production continuity. Furthermore, some existing processes heavily rely on manual adjustment of the oxidant dosage, which is prone to error, leading not only to incomplete deammonium removal but also potential equipment corrosion. Additionally, using a single oxidant system results in a slow reaction rate and requires a long reaction time, thus reducing equipment efficiency.

[0003] Regarding equipment operation, existing devices are mostly intermittent, leading to significant heat loss from the brine and high overall energy consumption. Furthermore, some processes require the use of highly toxic chemical reagents (such as barium chloride and sulfur dioxide), posing significant safety hazards and imposing heavy environmental burdens. The existing dechlorination and ammonium removal processes are often disconnected, resulting in a complex overall process and high operating costs. Therefore, the industry urgently needs a continuous, efficient, low-consumption, and environmentally safe brine ammonium removal reactor. Summary of the Invention

[0004] One objective of this invention is to provide a continuous demineralized water ammonium removal reaction device to solve the technical problems of scaling, low precision of oxidant addition, and slow reaction rate in the prior art.

[0005] To achieve the above objectives, the technical solution adopted by the present invention is: to provide a continuous desalinated water ammonium removal reaction device, wherein the continuous desalinated water ammonium removal reaction device includes a pretreatment module, a reaction module and a gas-liquid separation module connected in sequence; The pretreatment module includes a dechlorination tower, which is kept under vacuum to perform dechlorination. The reaction module includes a vertical high-turbulence reaction tank, which receives dechlorinated brine and is connected to an oxidant delivery pipeline; the bottom of the vertical high-turbulence reaction tank is connected to a compressed air supply source, and an internal stirring device is provided to create a high-turbulence reaction environment. The gas-liquid separation module includes an ammonium stripping tower and a continuous separator; the ammonium stripping tower receives the reacted material and strips it, and the bottom outlet of the ammonium stripping tower is connected to the continuous separator; the organic phase outlet of the continuous separator is returned to the vertical strong turbulence reaction tank, and the brine outlet is used to discharge qualified dilute brine.

[0006] In one embodiment, a control module is also included; a pH detector, an online ORP detection device, and an automatic regulating valve are sequentially installed on the pipeline from the dechlorination tower to the vertical turbulent reaction tank.

[0007] In one embodiment, the end of the oxidant delivery pipeline is connected to a baffle tank located above the vertical turbulent reaction tank; the baffle tank is connected to a chlorine water source, a sodium hypochlorite source, and a chlorine dioxide source respectively through pipelines equipped with a mass flow meter and a horizontal flow pump.

[0008] In one embodiment, the system further includes an absorption module and a raw material storage unit; the top of the ammonium stripping tower is connected to the alkaline absorption tower via a pipeline; the raw material storage unit includes a chlorine water storage tank, a sodium hypochlorite storage tank, and a chlorine dioxide storage tank, which are respectively connected to the baffled channel via pipelines, as well as a brine storage tank connected to the inlet of the dechlorination tower.

[0009] In one embodiment, the baffle channel includes: The outer shell has a chamber inside which liquid can flow. The two ends of the outer shell are respectively provided with a liquid inlet and a liquid outlet. The liquid inlet is connected to the dechlorination tower to receive dechlorinated brine, and the liquid outlet is connected to the vertical strong turbulence reaction tank. Multiple adaptive baffles, one end of which is hinged to the inner wall of the chamber, are staggered on opposite inner walls of the chamber along the water flow direction to create an S-shaped flow channel with variable cross-section within the chamber. An arc-shaped groove is formed on the top wall and / or bottom wall of the chamber. The center of the arc-shaped groove coincides with the hinge point of the corresponding adaptive baffle. The movable end of the adaptive baffle is slidably engaged in the arc-shaped groove. An elastic reset member is located within the arc-shaped groove. One end of the elastic reset member is connected to the adaptive baffle, and the other end is connected to the housing, so as to provide the adaptive baffle with an elastic buffering force to resist the impact of water flow. The graded dosing assembly has a chlorine water dosing tube, a sodium hypochlorite dosing tube, and a chlorine dioxide dosing tube sequentially connected to the housing along the fluid flow direction within the chamber. Adjacent dosing tubes are separated by at least one adaptive baffle to form a graded dosing zone. The dosing ports of the chlorine water dosing tube, sodium hypochlorite dosing tube, and chlorine dioxide dosing tube are all directly opposite the high-velocity shear zone where the movable end of the adaptive baffle is located.

[0010] In one embodiment, the vertical high-turbulence reaction tank is further provided with a baffle plate, and the stirring device is a vertical mixer, and its stirring part is superimposed with the flow range of compressed air.

[0011] Another aspect of the present invention provides a continuous desalinated water ammonium removal method, employing the continuous desalinated water ammonium removal reactor described in any of the above embodiments, the continuous desalinated water ammonium removal method comprising the following steps: S1. The brine is first dechlorinated under vacuum to control the free chlorine content within a preset range; S2. After adjusting the pH value of the dechlorinated brine, it is continuously fed into a strong turbulent reaction environment, and a composite oxidant system is continuously added in proportion to react and generate volatile chloramine; the composite oxidant system contains at least chlorine water and sodium hypochlorite. S3. After the reaction material is stripped by gas, the liquid phase enters the continuous separation stage. S4. The separated organic phase is recycled to the strongly turbulent reaction environment of S2, while the aqueous phase is discharged as qualified brine.

[0012] In one embodiment, in S1, the free chlorine content is controlled at 100~150ppm and the vacuum degree is controlled at 82~93kPa; in S2, the pH is adjusted to 5.0~10.5, the reaction temperature is controlled at 30℃~60℃, and the reaction time is 1~3h.

[0013] In one embodiment, the composite oxidant system further comprises chlorine dioxide; wherein the added sodium hypochlorite solution has a mass percentage concentration of 10% and the amount added is 0.1~0.3% of the total mass of the brine; the amount of chlorine water added is dynamically adjusted to ensure that the hypochlorite content is 10~80ppm after the reaction; the amount of chlorine dioxide added is 0.01~0.5% of the total mass of the brine, calculated based on available chlorine.

[0014] The above-described technical solutions in the embodiments of the present invention have at least the following technical effects or advantages: The continuous demineralized water ammonium removal reactor and method provided in this invention use a composite oxidant system of chlorine water and sodium hypochlorite to replace the traditional NaOH solution, completely eliminating the risk of precipitation and scaling, while realizing the resource utilization of chlorine waste liquid and effectively reducing production costs.

[0015] Furthermore, this invention integrates a vertical strong turbulent flow reaction module and a vacuum dechlorination module, which enhances the mass transfer process through the superposition of compressed air aeration and vertical stirring, and, in conjunction with a negative pressure deammonium removal design, significantly improves the reaction rate and the thoroughness of ammonium removal.

[0016] Furthermore, this invention is equipped with a mass flow meter and an online detection interlocking system (including a pH detector and an online ORP detection device), which enables precise metering of the oxidant and real-time control of reaction parameters, fundamentally avoiding errors caused by manual operation.

[0017] Furthermore, this invention designs a continuous closed-loop process that integrates dechlorination, ammonium removal, gas-liquid separation, and waste liquid absorption into a single unit, reducing heat loss, eliminating redundant steps such as chemical dechlorination, and significantly improving production continuity and energy utilization.

[0018] Finally, by adopting a staged absorption and material recycling design, the emission of harmful gases is reduced, material loss is minimized, and the requirements of green chemical engineering are fully met. The continuous desalinated water ammonium removal reactor provided by this invention achieves integrated continuous operation of dechlorination-ammonia removal-absorption-recycling. Attached Figure Description

[0019] To more clearly illustrate the technical solutions in the embodiments of the present invention, 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 some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0020] Figure 1 A schematic diagram of a continuous brine deammonium removal reactor provided in an embodiment of the present invention; Figure 2 This is a schematic diagram of the baffle channel provided in an embodiment of the present invention.

[0021] The labels for the various figures are as follows: 1. Dechlorination tower; 2. Vertical turbulent reaction tank; 3. Ammonium stripping tower; 4. Continuous separator; 5. Baffle; 6. Alkali absorption tower; 7. Chlorine water storage tank; 8. Sodium hypochlorite storage tank; 9. Chlorine dioxide storage tank; 10. Dilute brine storage tank; 51. Shell; 52. Self-adaptive baffle; 53. Arc-shaped chute; 54. Elastic reset component; 55. Chlorine water addition pipe; 56. Sodium hypochlorite addition pipe; 57. Chlorine dioxide addition pipe; 58. Inlet; 59. Outlet. Detailed Implementation

[0022] Embodiments of the present invention are described in detail below, examples of which are illustrated in the accompanying drawings, wherein the same or similar reference numerals denote the same or similar elements or elements having the same or similar functions throughout. The embodiments described below with reference to the accompanying drawings are exemplary and intended to explain the present invention, and should not be construed as limiting the present invention.

[0023] In the description of this invention, it should be understood that the terms "length", "width", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0024] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of this invention, "a plurality of" means two or more, unless otherwise explicitly specified.

[0025] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0026] Please see Figure 1 The continuous brine deammonium removal reactor of the present invention includes a raw material storage unit, a pretreatment module, a reaction module, a gas-liquid separation module, an absorption module, and a conveying and control module. During system operation, the brine first enters the dechlorination tower 1 for vacuum dechlorination, controlling the free chlorine content to 100-150 ppm. Then, the pH is adjusted to 5.0-10.5 via an automatic regulating valve and an online detection device on the pipeline before being sent to the reaction tank. Chlorine water, sodium hypochlorite, and chlorine dioxide are continuously added to the baffle tank 5 by a horizontal flow pump and a mass flow meter in a specific ratio, and then enter the strong turbulence reaction tank. In the reaction tank, the gas, liquid, and solid phases react under strong turbulence, generating volatile chloramines. The reaction product overflows or is pumped to the ammonium stripping tower 3. Under the stripping effect of compressed air at the bottom, the gas phase enters the alkaline absorption tower 6 for treatment; the liquid phase enters the continuous separator 4 for separation. Qualified brine is discharged and sent to subsequent processes, while the organic phase is recycled back to the reaction tank for reuse.

[0027] The reason why this invention can achieve efficient, continuous, and scale-free ammonium removal is due to the synergistic effect of the following technical principles: 1. Scale prevention using a composite oxidant system: Existing technologies use a 32% NaOH solution in combination with sodium hypochlorite to remove ammonium, which introduces a large concentration of hydroxide ions (OH-). - It readily reacts with calcium ions (Ca²⁺) in a slightly saline system. + ), magnesium ions (Mg²) + These substances combine to form calcium hydroxide and magnesium hydroxide precipitates, leading to scaling and clogging of the equipment.

[0028] This invention innovatively employs a composite oxidant system composed of chlorine water and sodium hypochlorite (or supplemented with chlorine dioxide). This system can operate under relatively mild pH conditions (5.0~10.5), thermodynamically avoiding the formation of localized strongly alkaline environments and breaking the solubility product condition for calcium and magnesium ion precipitation, thus completely eliminating the risk of precipitation and scaling. Simultaneously, the chlorine wastewater is utilized as an oxidant, reducing costs.

[0029] 2. Enhanced mass transfer through strong turbulence and gas-liquid separation: This invention overcomes the mass transfer bottleneck of traditional static or low-speed stirring. The vertical high-turbulence reaction tank 2 is equipped with a vertical stirrer and baffles, and the bottom is connected to a compressed air supply source. During operation, the high-speed rotating stirring blades and the rising compressed air flow at the bottom overlap and collide in space (the stirring part and the compressed air flow range overlap).

[0030] This process further breaks the bubbles into micron-sized microbubbles, greatly increasing the gas-liquid contact surface area and creating a strong turbulent dissipation field (strong turbulent environment). This significantly reduces the interphase mass transfer resistance, allowing the oxidant and ammonium ions to mix and react instantly and uniformly.

[0031] Furthermore, the product generated by the reaction is volatile chloramine. This invention then utilizes a vacuum deammoniation design and compressed air aeration at the bottom of the ammonium stripping tower 3, employing the principle of air stripping, to rapidly remove the generated volatile chloramine from the liquid phase. According to Le Chatelier's principle (the principle of chemical equilibrium shift), the continuous removal of the product drives the ammonium removal reaction forward, thereby greatly improving the reaction rate and the thoroughness of ammonium removal.

[0032] 3. Online interlocking control and corrosion / leak prevention: Traditional processes rely on manual adjustment of the oxidant. Due to fluctuations in the concentration of reactants, this often results in either an excessive amount of oxidant added (causing severe equipment corrosion and reagent waste) or an insufficient amount (incomplete ammonium removal).

[0033] This invention employs a mass flow meter for precise metering and installs a pH detector and an online ORP (oxidation-reduction potential) monitoring device on the dechlorinated brine pipeline. The ORP value can accurately reflect the oxidation potential state of free chlorine and hypochlorite ions in the system in real time. Through a PLC or DCS control system, the ORP / pH value is interlocked with the automatic regulating valve and the parallel flow pump, achieving millisecond-level dynamic response of the dosage. This ensures that the oxidant is always at the optimal stoichiometric ratio, guaranteeing both the ammonium removal rate and preventing corrosion of the equipment by excessive free chlorine.

[0034] Process parameter control range: Solvents and oxidants can be replaced according to the composition of the brine, and chlorine dioxide can be added as needed. The sodium hypochlorite solution mass percentage concentration is usually 10%, and the addition amount is set to 0.1~0.3% of the total brine mass. The amount of chlorine water added is dynamically adjusted according to its chlorine content, and is combined with sodium hypochlorite to ensure that the hypochlorite content is between 10~80 ppm after the reaction. The chlorine dioxide addition amount is calculated based on available chlorine and is 0.01~0.5% of the total brine mass. The vacuum degree of dechlorination tower 1 is controlled at 82~93 kPa, the reaction tank temperature is controlled at 30℃~60℃, the pH value is maintained at 5.0~10.5, and the reaction time is controlled at 1~3 h. The concentration of caustic soda solution in alkali absorption tower 6 is 5%~15%. The ammonium removal efficiency can be calculated by determining the ammonium content after ammonium removal using ion chromatography.

[0035] 4. Comprehensive energy utilization and continuous closed-loop system: In traditional intermittent operations, the brine suffers significant heat loss, resulting in high energy consumption. This invention constructs a continuous closed-loop process, integrating dechlorination, ammonium removal, gas-liquid separation, and wastewater absorption into a single unit. The dechlorination tower 1 is connected to the reaction tank via an insulated pipe, maximizing the retention of the heat (sensible heat) carried by the brine itself. The higher system temperature (30℃~60℃) not only reduces steam consumption for subsequent heating but also, according to the Arrhenius equation, increases the rate constant of the chemical reaction, further shortening the reaction time (to 1~3 hours).

[0036] In a preferred embodiment of the present invention, in response to technical biases such as flow fluctuations, uneven mixing, and easy scaling during the dosing process of multiphase composite oxidants, the present invention has carried out a special "electromechanical-chemical synergistic" structural design for the baffle trough 5.

[0037] Specifically, please refer to Figure 2 The interior of the baffle 5 is constructed with multiple staggered, hinged adaptive baffles 52 to form a variable cross-section S-shaped baffle channel. Its core working principle and beneficial technical effects are reflected in the following three dimensions: Firstly, the mechanical adaptive flow stabilization and buffering mechanism: In continuous production, when the brine inflow surges instantaneously or the upstream pump pressure pulses, traditional fixed baffles can cause severe liquid level fluctuations and pressure buildup. The adaptive baffle 52 of this invention, through the cooperation of its movable end with the arc-shaped chute 53 and the elastic reset member 54, achieves "flow adaptation": When operating at high flow rates, the water flow impact force overcomes the elastic force of the elastic reset member 54, pushing the adaptive baffle 52 towards the water flow direction, spontaneously increasing the cross-sectional area of ​​the baffle channel, thus playing a pressure relief and buffering role and ensuring system safety; when operating at low flow rates, the elastic reset member 54 pushes the baffle back, reducing the channel cross-sectional area, thereby maintaining a sufficiently high local flow velocity even under low-production conditions, preventing oxidant deposition in dead zones.

[0038] Furthermore, the invention employs a high-shear micro-mixing mechanism at the fluid dynamics level: It innovatively positions the injection ports of the chlorine water addition pipe 55, sodium hypochlorite addition pipe 56, and chlorine dioxide addition pipe 57 precisely opposite the movable end of the adaptive baffle 52. According to fluid dynamics principles, when the fluid flows through the narrow gap formed between the movable end of the baffle and the sidewall of the shell, the flow velocity increases sharply, generating strong shear forces and micro-eddies. Injecting the oxidant into this "high-velocity shear zone" instantly tears the drug droplets into micron-sized particles, which then rapidly diffuse into the brine with the turbulent flow, achieving instantaneous uniform mixing at the molecular level and significantly improving interphase mass transfer efficiency.

[0039] Finally, the spatiotemporal gradient anti-scaling and anti-escape mechanism at the chemical level: This embodiment cleverly utilizes the spatial extension of the S-shaped channel to physically isolate the three oxidants through the adaptive baffle 52, achieving a strict "acid first, then alkali, then strong oxidation" stepwise dosing time difference: The first step (chlorine water acidification and scale prevention). Chlorine water is first injected into the first chamber. Because chlorine water is slightly acidic, it first lowers the pH value of the brine in a localized area, eliminating the highly alkaline environment that would easily lead to the precipitation of calcium and magnesium ions and scale formation.

[0040] The second step (sodium hypochlorite synergistic neutralization). Subsequently, strongly alkaline sodium hypochlorite is injected into the second chamber. At this time, the hydroxide ions carried by the sodium hypochlorite are instantly neutralized by the slightly acidic brine flowing from upstream, perfectly avoiding the scaling threshold; at the same time, the hypochlorite ions are rapidly converted into hypochlorous acid molecules with extremely strong oxidizing activity in the slightly acidic environment, achieving in-situ synergistic enhancement.

[0041] The third stage (chlorine dioxide to prevent escape). Chlorine dioxide is highly volatile, so it is injected in the last chamber. As soon as it is mixed into the system, it immediately enters the vertical strong turbulence reaction tank 2 below with the fluid to participate in the main reaction. This "shortest residence time" design maximizes the preservation of the strong oxidizing energy of chlorine dioxide and avoids gas blockage caused by the precipitation of microbubbles due to prolonged residence in the baffle tank 5.

[0042] In this application, the detailed process parameters are controlled as follows: the solvent and oxidant can be replaced according to the composition of the brine, and chlorine dioxide can be added as needed. The sodium hypochlorite solution concentration is usually 10% by mass, and the amount added is set to 0.1~0.3% of the total brine mass. The amount of chlorine water added is dynamically adjusted according to its chlorine content, in combination with sodium hypochlorite, to ensure that the hypochlorite content is between 10~80 ppm after the reaction. The amount of chlorine dioxide added is calculated based on available chlorine and is 0.01~0.5% of the total brine mass.

[0043] The vacuum level of dechlorination tower 1 is controlled at 82~93 kPa, the temperature of the reaction tank is controlled at 30℃~60℃, the pH value is maintained at 5.0~10.5, and the reaction time is controlled at 1~3 hours. The concentration of caustic soda solution in alkali absorption tower 6 is 5%~15%.

[0044] To verify the technical effect of the present invention, the following examples are provided (the ammonium removal efficiency can be calculated by measuring the ammonium content after ammonium removal using ion chromatography): Example 1: This example did not add chlorine dioxide, but only used a sodium hypochlorite and chlorine water composite system. The brine flow rate was 130 m³ / h, and the initial ammonium content was 5.9 mg / L. The reaction conditions were controlled as follows: temperature 50℃, pH 5.5, and vacuum degree of 88 kPa in dechlorination tower 1. The oxidant addition parameters were: sodium hypochlorite 160 L / h, chlorine water 860 L / h. Under mild pH conditions, after 8 hours of continuous operation, the ammonium content after ammonium removal decreased to 0.49 ppm, the ammonium removal efficiency reached 99.92%, and there was no scaling on the equipment.

[0045] Example 2: In this example, chlorine dioxide was added as an auxiliary oxidant. The brine flow rate was 130 m³ / h, and the initial ammonium content was 4.3 mg / L. The oxidant addition parameters were: sodium hypochlorite 200 L / h, chlorine water 650 L / h, and chlorine dioxide 0.03% (based on available chlorine). After 5 hours of continuous operation, due to the increased reaction rate, the ammonium content after removal was as low as 0.17 ppm, with an ammonium removal efficiency as high as 99.96%. During operation, the free chlorine content remained stable within the controllable range, and no equipment corrosion was observed.

[0046] Example 3: In this example, the brine flow rate was increased to 150 m³ / h, with an initial ammonium content of 8.5 mg / L. The oxidant ratio was adjusted to: sodium hypochlorite 240 L / h, chlorine water 500 L / h, and chlorine dioxide 0.05% (based on available chlorine). After 12 hours of continuous operation, the ammonium content decreased to 0.35 ppm after ammonium removal, while still maintaining a high ammonium removal efficiency of 99.96%. Heat loss was reduced by 30% compared to traditional devices.

[0047] Example 4: The brine flow rate was 120 m³ / h, and the initial ammonium content was 6.4 mg / L. The pH was optimized to 6.0, and the oxidant addition parameters were: sodium hypochlorite 180 L / h and chlorine water 720 L / h. After 10 hours of continuous operation, the ammonium content after removal was 0.28 ppm, and the ammonium removal effect was stable. Due to the synergistic effect of chlorine water and sodium hypochlorite, this process saves more than 30% of the sodium hypochlorite usage compared to the traditional process.

[0048] The above are merely preferred embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A continuous saline solution ammonium removal reaction device, characterized in that, The continuous demineralized water ammonium removal reactor includes a pretreatment module, a reaction module, and a gas-liquid separation module connected in sequence. The pretreatment module includes a dechlorination tower, which is kept under vacuum to perform dechlorination. The reaction module includes a vertical high-turbulence reaction tank, which receives dechlorinated brine and is connected to an oxidant delivery pipeline; the bottom of the vertical high-turbulence reaction tank is connected to a compressed air supply source, and an internal stirring device is provided to create a high-turbulence reaction environment. The gas-liquid separation module includes an ammonium stripping tower and a continuous separator; the ammonium stripping tower receives the reacted material and strips it, and the bottom outlet of the ammonium stripping tower is connected to the continuous separator; the organic phase outlet of the continuous separator is returned to the vertical strong turbulence reaction tank, and the brine outlet is used to discharge qualified dilute brine.

2. The continuous desalinated water ammonium removal reaction device according to claim 1, characterized in that: It also includes a control module; a pH detector, an online ORP detection device, and an automatic regulating valve are sequentially installed on the pipeline from the dechlorination tower to the vertical turbulent reaction tank.

3. The continuous desalinated water ammonium removal reaction device according to claim 1, characterized in that: The end of the oxidant delivery pipeline is connected to a baffle tank located above the vertical strong turbulent reaction tank; the baffle tank is connected to a chlorine water source, a sodium hypochlorite source, and a chlorine dioxide source respectively through pipelines equipped with a mass flow meter and a horizontal flow pump.

4. The continuous desalinated water ammonium removal reaction device according to claim 3, characterized in that: It also includes an absorption module and a raw material storage unit; the top of the ammonium stripping tower is connected to the alkaline absorption tower via a pipeline; the raw material storage unit includes a chlorine water storage tank, a sodium hypochlorite storage tank and a chlorine dioxide storage tank that are respectively connected to the baffle through pipelines, as well as a brine storage tank that is connected to the inlet of the dechlorination tower.

5. The continuous desalinated water ammonium removal reaction device according to claim 3, characterized in that, The baffle channel includes: The outer shell has a chamber inside which liquid can flow. The two ends of the outer shell are respectively provided with a liquid inlet and a liquid outlet. The liquid inlet is connected to the dechlorination tower to receive dechlorinated brine, and the liquid outlet is connected to the vertical strong turbulence reaction tank. Multiple adaptive baffles, one end of which is hinged to the inner wall of the chamber, are staggered on opposite inner walls of the chamber along the water flow direction to create an S-shaped flow channel with variable cross-section within the chamber. An arc-shaped groove is formed on the top wall and / or bottom wall of the chamber. The center of the arc-shaped groove coincides with the hinge point of the corresponding adaptive baffle. The movable end of the adaptive baffle is slidably engaged in the arc-shaped groove. An elastic reset member is located within the arc-shaped groove. One end of the elastic reset member is connected to the adaptive baffle, and the other end is connected to the housing, so as to provide the adaptive baffle with an elastic buffering force to resist the impact of water flow. The graded dosing assembly has a chlorine water dosing tube, a sodium hypochlorite dosing tube, and a chlorine dioxide dosing tube sequentially connected to the housing along the fluid flow direction within the chamber. Adjacent dosing tubes are separated by at least one adaptive baffle to form a graded dosing zone. The dosing ports of the chlorine water dosing tube, sodium hypochlorite dosing tube, and chlorine dioxide dosing tube are all directly opposite the high-velocity shear zone where the movable end of the adaptive baffle is located.

6. The continuous desalinated water ammonium removal reaction device according to claim 1, characterized in that: The vertical high-turbulence reaction tank is also equipped with a baffle plate, and the stirring device is a vertical mixer, and its stirring part is superimposed with the flow range of compressed air.

7. A continuous desalinated water ammonium removal method, employing the continuous desalinated water ammonium removal reactor described in any one of claims 1-6, characterized in that, The continuous demineralized water ammonium removal method includes the following steps: S1. The brine is first dechlorinated under vacuum to control the free chlorine content within a preset range; S2. After adjusting the pH value of the dechlorinated brine, it is continuously fed into a strong turbulent reaction environment, and a composite oxidant system is continuously added in proportion to react and generate volatile chloramine; the composite oxidant system contains at least chlorine water and sodium hypochlorite. S3. After the reaction material is stripped by gas, the liquid phase enters the continuous separation stage. S4. The separated organic phase is recycled to the strongly turbulent reaction environment of S2, while the aqueous phase is discharged as qualified brine.

8. The continuous demineralized water ammonium removal method according to claim 7, characterized in that: In S1, the free chlorine content is controlled at 100~150ppm, and the vacuum degree is controlled at 82~93kPa; in S2, the pH is adjusted to 5.0~10.5, the reaction temperature is controlled at 30℃~60℃, and the reaction time is 1~3h.

9. The continuous demineralized water ammonium removal method according to claim 7, characterized in that: The composite oxidant system also includes chlorine dioxide; wherein, the added sodium hypochlorite solution has a mass percentage concentration of 10% and the amount added is 0.1~0.3% of the total mass of the brine; the amount of chlorine water added is dynamically adjusted to ensure that the hypochlorite content is 10~80ppm after the reaction; the amount of chlorine dioxide added is 0.01~0.5% of the total mass of the brine, calculated based on available chlorine.

Images