Apparatus for continuously producing high-purity sodium hypochlorite

Abstract

The application relates to the technical field of sodium hypochlorite production and preparation, and particularly discloses a device for continuously preparing high-purity sodium hypochlorite, which comprises a first reaction kettle, a first water inlet pipe is connected with a water inlet of the first reaction kettle, and a first conveying pump is arranged on the first water inlet pipe; a first back pressure valve is arranged on the first water inlet pipe between the first conveying pump and the first reaction kettle; a first jacketed heat exchanger is sleeved on the outer circumferential surface of the first reaction kettle, a first jacketed heat exchanger inlet and a first jacketed heat exchanger outlet are arranged on the first jacketed heat exchanger, the first jacketed heat exchanger inlet is connected with a drain outlet of the first reaction kettle through a pipeline, the first jacketed heat exchanger inlet is connected with cooling water through a pipeline, and a second back pressure valve is arranged on the pipeline between the cooling water and the first jacketed heat exchanger inlet. The application has the characteristics of being capable of reducing by-products, improving the effective content and reducing the waste of raw material chlorine.

Description

Technical Field

[0001] This invention relates to the field of sodium hypochlorite production and preparation technology, and in particular to an apparatus for the continuous preparation of high-purity sodium hypochlorite. Background Technology

[0002] Sodium hypochlorite is a colorless or pale yellow liquid with a chlorine-like odor. It has a melting point of -6°C and a boiling point of 102.2°C. It readily dissolves in water to form caustic soda and hypochlorous acid. Hypochlorous acid further decomposes to produce hydrogen chloride and nascent oxygen. Due to the strong oxidizing power of nascent oxygen, sodium hypochlorite is a strong oxidizing agent. As a truly efficient, broad-spectrum, and safe powerful sterilizing and antiviral agent, it has excellent affinity for water and is miscible with water in any proportion. It does not pose the safety hazards of liquid chlorine and chlorine dioxide, and its disinfection effect is widely recognized as comparable to chlorine. It is widely used in disinfectants, pulp bleaching, and the pharmaceutical industry, among many other fields.

[0003] Currently, the main production processes for sodium hypochlorite in China are electrolysis and sodium hydroxide absorption. Electrolysis produces products with low available chlorine content and is primarily used in applications requiring small amounts of sodium hypochlorite, such as disinfection or algae control in water treatment. Sodium hydroxide absorption produces products with high available chlorine concentrations and is mainly used as a bleaching agent in pulp, textiles, and chemical fibers; as a water purifier, bactericide, or disinfectant in water treatment; in the organic industry for manufacturing chlorinated methacrylate; in the dye industry for manufacturing indigo; and in the pharmaceutical industry for producing monochloramine or dichloramine.

[0004] Sodium hydroxide absorption methods mostly employ batch production processes, requiring continuous analysis of excess alkali levels. When the sodium hypochlorite solution meets quality standards, personnel must switch the absorption tower; failure to do so in a timely manner can lead to overchlorination. This necessitates constant monitoring and operation, placing a heavy workload on production personnel, demanding a high level of control, hindering production efficiency, and causing numerous problems for producers. Furthermore, it presents challenges such as difficulty in controlling excess chlorination or alkali levels, resulting in unstable product quality.

[0005] Based on the above problems, existing patent documents disclose methods for producing sodium hypochlorite using a continuous process (CN111732081A; CN111792625A; CN 107010599A). Continuous production of sodium hypochlorite offers advantages such as high efficiency and good product quality, while also enabling sustainable and stable production. However, these technologies also suffer from drawbacks, including the inability to obtain sodium hypochlorite solutions of accurate concentrations, the inability to monitor the entire reaction process in real time regarding temperature, pH, sodium hypochlorite concentration, and system pressure, requiring significant manpower for analysis and testing. Furthermore, existing sodium hypochlorite preparation technologies all involve adding excess chlorine gas to a reactor, where it dissolves in water under pressure and reacts with sodium hydroxide to produce chlorination. On one hand, the dissolved excess chlorine reacts with the product sodium hypochlorite, increasing byproducts and reducing the available chlorine content. On the other hand, the excess chlorine gas is often treated as tail gas, typically requiring multi-stage absorption to meet venting requirements. This not only wastes raw chlorine gas but also increases investment costs and the environmental risks associated with chlorine leaks.

[0006] Therefore, existing equipment for producing sodium hypochlorite has several drawbacks. It cannot obtain sodium hypochlorite solutions of accurate concentration, nor can it monitor the entire reaction process in real time, including temperature, pH, sodium hypochlorite concentration, and system pressure. It requires a large amount of human resources for analysis and testing, and the addition of excessive chlorine leads to increased byproducts, waste of raw chlorine, increased investment costs, and environmental risks from chlorine leaks. Summary of the Invention

[0007] In order to solve the above-mentioned technical problems existing in the existing sodium hypochlorite production equipment, the present invention provides a device for continuous preparation of high-purity sodium hypochlorite that can reduce by-products, improve the efficiency content and reduce the waste of raw material chlorine.

[0008] The first technical solution of the present invention: a method for continuously preparing high-purity sodium hypochlorite, comprising the following steps,

[0009] (a) Preparation of concentrated sodium hydroxide solution

[0010] (a1) Add a certain mass of concentrated alkali to the first reactor equipped with the first jacketed heat exchanger and turn on the circulating cooling water;

[0011] (a2) Add a certain mass of deionized water to the first reactor in step (a1) and start the stirrer in the first reactor;

[0012] (a3) Adjust the flow rate of circulating cooling water in the first jacketed heat exchanger outside the first reactor in step (a1) by adjusting the reading of the first online thermometer to control the temperature of the solution in the first reactor;

[0013] (a4) Adjust the deionized water flow rate in step (a2) by using the reading of the first densitometer to control the concentration of the sodium hydroxide solution;

[0014] (b) Preparation of dilute sodium hydroxide solution

[0015] (b1) Add the concentrated sodium hydroxide solution obtained in step (a4) to the second reactor equipped with a second jacketed heat exchanger, and turn on the circulating cooling water;

[0016] (b2) Input a certain mass of deionized water into the second reactor in step (b1) and start the stirrer in the second reactor;

[0017] (b3) Adjust the flow rate of the circulating cooling water in the second jacketed heat exchanger outside the second reactor in step (b1) by adjusting the reading of the second online thermometer to control the temperature of the solution inside the second reactor;

[0018] (b4) Adjust the deionized water flow rate in step (b2) by using the reading of the second densitometer to control the concentration of the dilute sodium hydroxide solution;

[0019] (c) Transporting dilute sodium hydroxide solution

[0020] (c1) Transfer the dilute sodium hydroxide solution obtained in step (b4) into a storage tank for later use;

[0021] (c2) The dilute sodium hydroxide solution from step (c1) is fed into a static mixer for mixing;

[0022] (d) Chlorination reaction

[0023] (d1) The sodium hydroxide dilute solution that has been mixed in step (c2) is fed into the spray tower atomizer (30) at the top of the sodium hypochlorite reactor, and the sodium hydroxide dilute solution is sprayed and atomized from the top of the spray tower atomizer downwards;

[0024] (d2) Chlorine gas is delivered to a gas distributor, and the chlorine gas is distributed in the sodium hypochlorite reactor by the gas distributor;

[0025] (d3) After the sodium hydroxide dilute solution atomized in step (d1) reacts countercurrently with the chlorine gas dispersed in step (d2), sodium hypochlorite solution is generated.

[0026] (e) Online monitoring

[0027] (e1) The pH of the sodium hypochlorite solution in step (d3) is tested online by a pH meter in the sodium hypochlorite reactor, and the opening of the back pressure valve of the dilute sodium hydroxide solution is interlocked online to keep the pH of the reaction system within a certain range.

[0028] (e2) The cooling water valve is interlocked online by a third online thermometer in the sodium hypochlorite reactor. The cooling water flow rate is adjusted by adjusting the opening of the cooling water valve online, thereby controlling the reaction temperature online.

[0029] (e3) By using the pressure gauge inside the sodium hypochlorite reactor, the inert gas valve is interlocked online. The inert gas flow rate is adjusted by regulating the opening of the inert gas valve online, thereby maintaining a constant pressure inside the sodium hypochlorite reactor.

[0030] (e4) The chlorine valve is interlocked online by the redox potential analyzer in the sodium hypochlorite reactor, and the chlorine flow rate is adjusted by adjusting the opening of the chlorine valve online;

[0031] (f) Collecting products

[0032] By observing the reading of the redox potential analyzer in step (e4), determine whether the product meets the standard; if it does, send the sodium hypochlorite solution in step (d3) to the finished product tank; if it does not meet the standard, continue to leave the sodium hypochlorite solution in the sodium hypochlorite reactor, and use the redox potential analyzer to interlock the corresponding chlorine valves online until the sodium hypochlorite solution meets the standard and is then sent to the finished product tank.

[0033] This invention utilizes a first and second reaction vessel. First, solid sodium hydroxide and deionized water are added to the first reaction vessel to prepare a concentrated sodium hydroxide solution. This concentrated solution is then transferred to the second reaction vessel, where deionized water is added to dilute it and prepare a diluted sodium hydroxide solution. Temperature control during the sodium hydroxide dissolution and dilution process is achieved by adjusting the opening of the cooling water valve and the flow rate using an online thermometer. Similarly, precise control of the sodium hydroxide mass fraction is achieved by adjusting the opening of the deionized water valve and the flow rate using an online density meter. The entire sodium hydroxide dissolution and dilution process employs online monitoring and interlocking valve technology, enabling accurate temperature and concentration control. This lays a solid foundation for the subsequent preparation of a sodium hypochlorite solution with stable mass concentration, ensuring the quality of the final sodium hypochlorite solution.

[0034] This invention provides real-time monitoring of pH, temperature, pressure, and redox potential involved in the reaction process and interlocks the opening of corresponding valves. It uses a pH meter to measure the pH of the reaction mixture online, interlocks the opening of the dilute sodium hydroxide solution valve online, and adjusts the flow rate of the dilute sodium hydroxide solution online to maintain the pH of the reaction system within a certain range. It also uses an online thermometer to interlock the cooling water valve online, and adjusts the valve opening to regulate the cooling water flow rate, thereby controlling the reaction temperature online. Finally, it uses a pressure gauge to monitor the pressure of the reaction system online, interlocks the inert gas valve online, and adjusts the inert gas flow rate by adjusting the valve opening.

[0035] This invention utilizes an oxidation-reduction potential analyzer to interlock chlorine valves online. By adjusting the valve opening and chlorine flow rate online, the online instrument interlocking valve technology ensures the controllability of the reaction process. Through coordinated control of comprehensive reaction process parameters, it successfully achieves continuous production of sodium hypochlorite with a stable mass concentration. Furthermore, this invention uses an inert gas to replace chlorine for pressurizing the reaction system, enabling online pressure compensation for the amount of chlorine consumed in the reaction. This effectively avoids the increase of byproducts and the decrease in available chlorine content caused by the reaction between chlorine and the product sodium hypochlorite. It also achieves zero chlorine emissions, completely eliminating the need for tail gas treatment, avoiding waste of raw chlorine, and effectively avoiding the investment costs of tail gas treatment devices and the environmental risks of chlorine leakage. This invention offers significant economic and social benefits.

[0036] Preferably, the following steps are also included:

[0037] (a5) The temperature of the concentrated sodium hydroxide solution in the first reactor is controlled by interlocking the reading of the first online thermometer inside the first reactor with the first jacketed heat exchanger. Through the online interlock between the first online thermometer and the first jacketed heat exchanger, the water inlet rate of the first jacketed heat exchanger can be controlled to raise or lower the temperature of the concentrated sodium hydroxide solution inside the first reactor when the temperature is lower or higher than a set value, ensuring that the temperature of the concentrated sodium hydroxide solution inside the first reactor remains within a reasonable temperature range.

[0038] Preferably, the mass concentration of the concentrated sodium hydroxide solution in step (a4) is 20% to 50%, more preferably, the mass concentration of the concentrated sodium hydroxide solution in step (a4) is 30% to 40%. This prepares for the rapid preparation of the subsequent dilute sodium hydroxide solution.

[0039] Preferably, the temperature of the concentrated sodium hydroxide solution in the first reactor is 30℃~50℃, more preferably, the temperature of the concentrated sodium hydroxide solution in the first reactor is 35℃~45℃. Controlling the temperature of the concentrated sodium hydroxide solution in the first reactor ensures that the preparation of the concentrated sodium hydroxide solution is carried out under optimal conditions.

[0040] Preferably, the following steps are also included:

[0041] (b5) The temperature of the dilute sodium hydroxide solution in the second reactor is controlled by interlocking the reading of the second online thermometer in the second reactor with the second jacketed heat exchanger. When the temperature of the dilute sodium hydroxide solution in the second jacketed heat exchanger is lower or higher than a set value, the water inlet rate of the second jacketed heat exchanger is controlled to raise or lower the temperature of the concentrated sodium hydroxide solution, ensuring that the temperature of the concentrated sodium hydroxide solution inside the second reactor remains within a reasonable temperature range.

[0042] Preferably, the mass concentration of the dilute sodium hydroxide solution in step (b4) is 13% to 18%, more preferably, the mass concentration of the dilute sodium hydroxide solution in step (b4) is 15% to 16%. This prepares the solution for subsequent processes of preparing sodium hypochlorite solution, ensuring that the sodium hypochlorite solution can be produced better and more accurately.

[0043] Preferably, the temperature of the dilute sodium hydroxide solution in the second reactor is 20°C to 40°C; more preferably, the temperature of the dilute sodium hydroxide solution in the second reactor is 25°C to 35°C. This ensures that the sodium hydroxide solution in the second reactor is at a safe and suitable temperature, preparing it for subsequent production reactions.

[0044] Preferably, the length-to-diameter ratio of the static mixer is 10-15; more preferably, it is 12-14. This ensures homogenization of the dilute sodium hydroxide solution, allowing it to be readily added to subsequent reaction processes.

[0045] Preferably, the diameter of the static mixer is 0.05m to 0.2m, and more preferably, the diameter is 0.1m to 0.15m. This allows the solution volume inside the static mixer to be controlled within a reasonable range, thereby ensuring effective mixing and homogenization and the smooth progress of subsequent reactions.

[0046] Preferably, the pressure applied to the atomizer of the spray tower is 0.2 MPa to 0.5 MPa; more preferably, the pressure applied to the atomizer of the spray tower is 0.3 MPa to 0.4 MPa. This ensures that the particle size of the atomized sodium hydroxide solution is within the acceptable range.

[0047] Preferably, the flow rate of the dilute sodium hydroxide solution in step (d1) is 20 mL / min to 40 mL / min; more preferably, the flow rate is 25 mL / min to 35 mL / min. This ensures that the amount of sodium hydroxide solution atomized and sprayed is compatible with the amount of gas blown out by the gas distributor at the bottom of the sodium hypochlorite reactor, guaranteeing sufficient and effective contact and reaction between the two, thereby ensuring the stability and reliability of the reaction.

[0048] Preferably, in step (d1), the droplet size of the atomized sodium hydroxide solution is 5 μm to 50 μm. More preferably, the droplet size is 10 μm to 45 μm. Even more preferably, the droplet size is 15 μm to 40 μm. More preferably, the droplet size is 20 μm to 35 μm. Even more preferably, the droplet size is 25 μm to 30 μm. This increases the contact area between the sodium hydroxide solution and chlorine gas, effectively improving the reaction rate between them and thus increasing the efficiency of the entire preparation process.

[0049] Preferably, the flow rate of chlorine gas in step (d2) is 5 mL / min to 25 mL / min; more preferably, the flow rate of chlorine gas in step (d2) is 10 mL / min to 20 mL / min. This allows for flexible adjustment of the chlorine gas flow rate based on the flow rate of the sprayed sodium hydroxide solution, ensuring that the reaction between the two is always complete.

[0050] Preferably, the pH of the reaction system is maintained at 12-13 in step (e1). This ensures that the reaction can proceed in a suitable acidic or alkaline environment, improving the reliability and quality of the preparation process.

[0051] Preferably, the reaction temperature in step (e2) is maintained at 30°C to 50°C. More preferably, the reaction temperature in step (e2) is maintained at 35°C to 45°C, which can ensure that the reaction is in a suitable temperature, thereby ensuring the reliability and safety of the reaction.

[0052] Preferably, the reaction pressure in step (e3) is controlled between 0.09 MPa and 0.11 MPa; more preferably, the reaction pressure in step (e3) is controlled between 0.095 MPa and 0.105 MPa. This ensures that the reaction pressure is controlled within a reasonable range, thereby guaranteeing that the reaction proceeds efficiently and in an orderly manner.

[0053] Preferably, in step (e4), the reading of the oxidation-reduction potential analyzer is controlled between 500mV and 600mV. More preferably, in step (e4), the reading of the oxidation-reduction potential analyzer is controlled between 520mV and 570mV. Based on the linear relationship between the reading of the oxidation-reduction potential analyzer and the concentration of sodium hypochlorite, the range of the reading of the oxidation-reduction potential analyzer can be determined using the concentration requirements of sodium hypochlorite in the product. If the reading is greater than the upper limit, the opening of the chlorine valve is reduced, resulting in a smaller chlorine flow rate. The back pressure valve of the product is opened synchronously, and the product is input into the finished product tank via the ninth delivery pump. If the reading is less than the lower limit, it indicates that the concentration of sodium hypochlorite in the product is too low. Through online interlocking, the opening of the chlorine valve is increased, resulting in a larger chlorine flow rate. The back pressure valve of the product is closed synchronously, and the mixture continues to react until it meets the standard and is input into the finished product tank.

[0054] Preferably, the inert gas is at least one of helium, neon, argon, krypton, or xenon. The ability to select different types of inert gases based on specific production conditions maximizes the flexibility of the method and minimizes production costs.

[0055] Preferably, in step (f), the product meets the following requirements: an available chlorine mass fraction of 6%-15% and a free alkali content of less than 0.5% by mass. This ensures that the produced sodium hypochlorite solution has a high available chlorine content, thus guaranteeing product quality.

[0056] The second technical solution of the present invention: a device for continuous preparation of high-purity sodium hypochlorite, comprising a first reaction vessel, wherein the inlet of the first reaction vessel is connected to a first inlet pipe, and a first delivery pump is provided on the first inlet pipe; a first back pressure valve is provided on the first inlet pipe between the first delivery pump and the first reaction vessel; a first jacketed heat exchanger is fitted on the outer circumference of the first reaction vessel, the first jacketed heat exchanger is provided with a first jacketed heat exchanger inlet and a first jacketed heat exchanger outlet, the first jacketed heat exchanger inlet is connected to the drain outlet of the first reaction vessel through a pipe, the first jacketed heat exchanger inlet is connected to cooling water through a pipe, and a second back pressure valve is provided on the pipe between the cooling water and the first jacketed heat exchanger inlet;

[0057] It also includes a second reactor, the inlet of which is connected to the outlet of the first reactor via a pipeline. A second delivery pump and a third back pressure valve are sequentially installed along the liquid flow direction on the pipeline between the outlet of the first reactor and the inlet of the second reactor. A second water inlet pipeline is connected to the inlet of the second reactor, and a third delivery pump is installed on the second water inlet pipeline. A fifth back pressure valve is installed on the pipeline between the third delivery pump and the second reactor. A second jacketed heat exchanger is fitted onto the outer circumference of the second reactor. The reactor is provided with a second jacketed heat exchanger inlet and a second jacketed heat exchanger outlet. The second jacketed heat exchanger inlet is connected to the drain outlet of the second reactor via a pipeline, and the second jacketed heat exchanger inlet is also connected to cooling water via a pipeline. A fourth back pressure valve is provided on the pipeline between the cooling water and the second jacketed heat exchanger inlet. The drain outlet of the second reactor is connected to a heat exchanger via a pipeline. A fourth delivery pump and a sixth back pressure valve are provided on the pipeline between the heat exchanger and the drain outlet of the second reactor. The sixth back pressure valve is closer to the heat exchanger than the fourth delivery pump.

[0058] The drain port of the heat exchanger is connected to a static mixer via a pipeline. A fifth delivery pump and a seventh back pressure valve are installed on the pipeline between the static mixer and the heat exchanger. The seventh back pressure valve is closer to the static mixer than the fifth delivery pump.

[0059] The drain port of the static mixer is connected to the sodium hypochlorite reactor via a pipeline. A sixth delivery pump and a sodium hydroxide dilute solution back pressure valve are installed on the pipeline between the sodium hypochlorite reactor and the static mixer. The sodium hydroxide dilute solution back pressure valve is closer to the sodium hypochlorite reactor than the sixth delivery pump. An atomizing jet tower is installed at the top of the sodium hypochlorite reactor.

[0060] The gas distributor’s inlet is connected to a gas buffer tank via a pipeline. An eighth back pressure valve is provided on the pipeline between the gas buffer tank and the gas distributor. The gas buffer tank’s inlet is connected to a chlorine gas inlet via a pipeline. A seventh delivery pump is provided on the pipeline between the chlorine gas inlet and the gas buffer tank.

[0061] The bottom of the sodium hypochlorite reactor is connected to an inert gas inlet via a pipeline. An eighth delivery pump and an inert gas valve are installed on the pipeline between the inert gas inlet and the sodium hypochlorite reactor. The inert gas valve is closer to the sodium hypochlorite reactor than the eighth delivery pump.

[0062] A third jacketed heat exchanger is fitted on the outer periphery of the sodium hypochlorite reactor. The third jacketed heat exchanger has a third jacketed heat exchanger inlet and a third jacketed heat exchanger outlet. The third jacketed heat exchanger inlet is connected to a cooling water interface through a pipeline. A cooling water valve is provided on the pipeline between the cooling water interface and the third jacketed heat exchanger inlet.

[0063] The discharge port of the sodium hypochlorite reactor is connected to a finished product tank via a pipeline. A ninth delivery pump and an eighth back pressure valve are installed on the pipeline between the finished product tank and the sodium hypochlorite reactor. The eighth back pressure valve is closer to the sodium hypochlorite reactor than the ninth delivery pump.

[0064] This invention utilizes a first and second reaction vessel in conjunction to first prepare a concentrated sodium hydroxide solution, which is then diluted to a dilute sodium hydroxide solution. This allows for the preparation of a concentrated sodium hydroxide solution by first pouring a large amount of solid sodium hydroxide into the first reaction vessel and adding an appropriate amount of deionized water. The concentrated sodium hydroxide solution is then passed into multiple second reaction vessels, where deionized water is added to dilute it to the desired dilute solution. This effectively reduces the time and labor required to directly prepare the dilute sodium hydroxide solution by adding solid sodium hydroxide into multiple different first reaction vessels, significantly improving the efficiency of sodium hydroxide solution preparation and reducing the workload of workers.

[0065] This invention combines a spray tower atomizer and a gas distributor. The spray tower atomizer can uniformly atomize and spray out a dilute sodium hydroxide solution through multiple atomizing nozzles, while the gas distributor uses multiple jet nozzles to uniformly disperse chlorine gas. This ensures sufficient contact and reaction between the dilute sodium hydroxide solution and chlorine gas, improving the reaction speed and thoroughness, and thus effectively improving the production efficiency of the device.

[0066] This invention utilizes a pipeline between the bottom of a sodium hypochlorite reactor and an inert gas inlet. This pipeline is equipped with an eighth delivery pump and an inert gas valve. Combined with a pressure gauge on the sodium hypochlorite reactor, after chlorine consumption, the pressure gauge detects a decrease in the internal pressure of the reactor. At this point, the pressure gauge opens the inert gas valve online, sending inert gas into the reactor to replace the chlorine and maintain the internal pressure. This ensures the smooth progress of the reaction. Furthermore, by replacing the consumed chlorine with inert gas, the reaction between chlorine and the product sodium hypochlorite is effectively prevented, thus avoiding increased byproducts and a decrease in available chlorine content. It also achieves zero chlorine emissions, completely eliminating the need for tail gas treatment and avoiding the waste of raw chlorine. This effectively avoids the investment costs associated with tail gas treatment devices and the environmental risks of chlorine leakage, resulting in significant economic and social benefits.

[0067] This invention utilizes a first jacketed heat exchanger, a second jacketed heat exchanger, and a third jacketed heat exchanger, along with a first online thermometer, a second online thermometer, and a third online thermometer, to monitor the temperature of the liquid inside the first reaction vessel, the second reaction vessel, and the sodium hypochlorite reactor in real time. When the temperature is too low or too high, this reduces or increases the amount of cooling water entering the jackets of the first, second, or third jacketed heat exchangers, thereby raising or lowering the temperature of the liquid inside the first, second, or sodium hypochlorite reactor. This maintains the temperature of the liquid inside the first, second, and sodium hypochlorite reactors within a suitable range, ensuring the smooth progress of sodium hypochlorite solution preparation.

[0068] Preferably, the first reactor is equipped with a first density meter, which is online-interlocked with a first back pressure valve. This online linkage between the first density meter and the first back pressure valve allows for timely sensing and monitoring of the concentration of the concentrated sodium hydroxide solution inside the first reactor, and the concentration of the concentrated sodium hydroxide solution inside the first reactor can be adjusted by controlling the flow rate of deionized water entering the first reactor.

[0069] Preferably, a first online thermometer is installed on the pipeline between the drain outlet of the first reactor and the inlet of the first jacketed heat exchanger. The first online thermometer allows for real-time monitoring of the sodium hydroxide solution temperature within the first reactor, ensuring the solution remains at a suitable temperature. Furthermore, in conjunction with the first jacketed heat exchanger, it allows for adjustment of the water flow rate at the inlet of the first jacketed heat exchanger when the concentrated sodium hydroxide solution temperature is abnormal, thereby regulating the temperature of the concentrated sodium hydroxide solution in the first reactor to a suitable range.

[0070] Preferably, the second reactor is equipped with a second densitometer, which is interlocked online with the fifth back pressure valve. The second densitometer is used to test the density of the dilute sodium hydroxide solution inside the second reactor, thereby allowing for timely monitoring of the sodium hydroxide solution's concentration and ensuring its smooth participation in subsequent reactions, thus guaranteeing the smooth progress of production.

[0071] Preferably, a second online thermometer is installed on the pipeline between the drain outlet of the second reactor and the inlet of the second jacketed heat exchanger. This ensures real-time monitoring of the temperature of the dilute sodium hydroxide solution and allows for timely adjustment of the solution temperature within the second reactor in conjunction with the water inlet rate at the second jacketed heat exchanger inlet.

[0072] Preferably, the sodium hypochlorite reactor is connected to a pH meter. This allows monitoring of the pH value of the sodium hypochlorite solution in the reactor, thereby determining whether the reaction between the dilute sodium hydroxide solution and chlorine gas has occurred sufficiently, enabling timely detection of problems and adjustment of the reaction.

[0073] Preferably, a pressure gauge is connected to the bottom of the sodium hypochlorite reactor, and the pressure gauge is interlocked online with an inert gas valve. The pressure gauge can detect whether the pressure inside the sodium hypochlorite reactor is within the optimal reaction pressure range. If the pressure is too high or too low, the flow rate of the inert gas entering the sodium hypochlorite reactor can be adjusted by regulating the flow rate of the online-interlocked inert gas valve, thereby quickly adjusting the pressure inside the sodium hypochlorite reactor to the optimal reaction pressure range.

[0074] Preferably, a third online thermometer is connected to the drain outlet of the sodium hypochlorite reactor, and this third online thermometer is interlocked with the cooling water valve. This allows monitoring of the temperature of the sodium hypochlorite solution inside the reactor. When the temperature is too high or too low, the interlocked cooling water valve can be controlled to increase or decrease the flow of cooling water into the third jacketed heat exchanger, thereby accelerating or slowing down the reduction of the internal temperature of the sodium hypochlorite reactor, ensuring that the temperature of the sodium hypochlorite solution in the reactor is quickly adjusted to a suitable range.

[0075] Preferably, a redox potential analyzer is installed on the pipeline between the eighth back pressure valve and the sodium hypochlorite reactor, and the redox potential analyzer is interlocked online with the chlorine valve. This allows for online interlocking of the chlorine valve, and the flow rate of chlorine entering the sodium hypochlorite reactor can be adjusted by regulating the opening degree of the chlorine valve online.

[0076] Preferably, the spray tower atomizer includes an inlet pipe, the inlet end of which is connected to a static mixer via a pipeline, and the outlet end of which is rotatably connected to an inlet horizontal pipe. Multiple inlet branch pipes are provided on the outer circumference of the inlet horizontal pipe, and multiple atomizing nozzles are provided at the top and bottom of each inlet branch pipe. Each atomizing nozzle is equipped with a solenoid valve. This allows for the uniform atomization and spraying of dilute sodium hydroxide solution through multiple atomizing nozzles, ensuring sufficient contact and reaction between the dilute sodium hydroxide solution and chlorine gas, thereby improving the completeness and speed of the reaction.

[0077] The device also includes a drive motor, which is mounted on the outer wall of the sodium hypochlorite reactor. The drive end of the drive motor has a turntable located inside the reactor and connected to one end of the inlet horizontal pipe. The drive motor can rotate the inlet horizontal pipe 180 degrees, allowing a new atomizing nozzle located on the upper side to replace the previously damaged atomizing nozzle located on the lower side for atomization spraying. This extends the replacement and maintenance cycle of the atomizing nozzles while ensuring smooth reaction, effectively improving the practicality and reliability of the device.

[0078] Preferably, the gas distributor includes an inlet pipe, the inlet end of which is connected to a gas buffer tank via a pipeline, and the outlet end of which is connected to an inlet horizontal pipe located inside the sodium hypochlorite reactor. Multiple inlet branch pipes are provided on the outer circumference of the inlet horizontal pipe, and each inlet branch pipe has multiple nozzles connected to its top. These multiple nozzles allow chlorine gas to be uniformly injected into the sodium hypochlorite reactor, maximizing the contact and reaction between the gas and the atomized dilute sodium hydroxide solution, thus improving reaction efficiency.

[0079] It also includes a primary flow divider assembly located above the nozzle, and a secondary flow divider assembly located above the primary flow divider assembly. This allows for better flow division of chlorine gas, increasing the area over which chlorine gas is evenly distributed and ensuring reaction efficiency.

[0080] Preferably, the primary diversion assembly includes multiple inverted conical first diverters, each corresponding to a jet nozzle and positioned above it. Adjacent first diverters are connected by a first connecting rod. A first fixing ring is connected to the inner wall of the sodium hypochlorite reactor, and the first diverter closest to the first fixing ring is connected to the first fixing ring via the first connecting rod. This further diverts the chlorine gas, maximizing reaction efficiency.

[0081] Preferably, the secondary diversion assembly includes multiple liquid storage boxes located above the first diverter. Each liquid storage box has a drain hole at its bottom. Multiple second diverters are connected to the top of each liquid storage box via support rods. Adjacent liquid storage boxes are connected via second connecting rods. A second fixing ring is slidably connected to the inner wall of the sodium hypochlorite reactor. The liquid storage box closest to the second fixing ring is connected to the second fixing ring via a second connecting rod. When the atomizing nozzle is corroded and damaged, the atomization effect deteriorates. Due to the reduced distribution area, the liquid storage box receives more dilute sodium hydroxide solution within the same time frame. When the receiving rate exceeds the leakage rate through the drain hole, the solution in the liquid storage box increases, generating a greater pulling force on the pull rod. When the pulling force on the tension sensor exceeds a set value, it indicates that the atomizing nozzle is severely damaged.

[0082] Preferably, the system also includes an atomization status detection component. This component comprises multiple sealed boxes mounted on the inner wall of the sodium hypochlorite reactor. Each sealed box contains a tension sensor with a straight rod extending from its base through the bottom wall of the sealed box and connected to a connecting plate. The connecting plate has a pull rod attached, the bottom of which is connected to a second fixing ring. The tension sensor is connected to a drive motor via wired or wireless connection. The connection between the pull rod and the second fixing ring allows the tension sensor to monitor the weight of the entire secondary diversion assembly. As the sodium hydroxide solution in the reservoir increases, the tension on the sensor increases, thus enabling monitoring of the atomization effect of the atomizing nozzle and determining whether a new nozzle needs to be replaced to ensure the smooth progress of the reaction.

[0083] The present invention has the following beneficial effects:

[0084] (1) By cooperating with the first and second reaction vessels, a concentrated sodium hydroxide solution can be prepared first, and then the concentrated sodium hydroxide solution can be diluted into a dilute sodium hydroxide solution. In this way, during preparation, a large amount of solid sodium hydroxide can be poured into the first reaction vessel and an appropriate amount of deionized water can be added to prepare a concentrated sodium hydroxide solution. Then, the concentrated sodium hydroxide solution can be passed into multiple second reaction vessels, and deionized water can be added to multiple second reaction vessels to dilute the concentrated sodium hydroxide solution into the required dilute sodium hydroxide solution. This can effectively reduce the time and labor required to directly prepare a dilute sodium hydroxide solution by adding solid sodium hydroxide into multiple different first reaction vessels, greatly improve the efficiency of sodium hydroxide solution preparation, and reduce the labor intensity of the staff.

[0085] (2) By combining the spray tower atomizer and the gas distributor, the spray tower atomizer can atomize and spray out the dilute sodium hydroxide solution evenly through multiple atomizing nozzles, and the gas distributor can evenly disperse the chlorine gas through multiple jet nozzles, which can ensure that the dilute sodium hydroxide solution and chlorine gas have sufficient contact and reaction, improve the reaction speed and thoroughness, and thus effectively improve the production efficiency of the device.

[0086] (3) Through the pipeline between the bottom of the sodium hypochlorite reactor and the inert gas inlet, an eighth delivery pump and an inert gas valve are installed on the pipeline. In conjunction with the pressure gauge on the sodium hypochlorite reactor, after the chlorine is consumed, the pressure gauge detects that the pressure inside the sodium hypochlorite reactor has decreased. At this time, the pressure gauge opens the inert gas valve online to send inert gas into the sodium hypochlorite reactor to replace the chlorine and maintain the pressure inside the sodium hypochlorite reactor. This ensures that the reaction can proceed smoothly. Furthermore, by replacing the consumed chlorine with inert gas, it is possible to effectively avoid the reaction between chlorine and the product sodium hypochlorite, which would lead to an increase in by-products and a decrease in the effective chlorine content. It can also achieve zero chlorine emissions, completely avoid the tail gas treatment of chlorine, avoid the waste of raw material chlorine, and effectively avoid the investment costs brought by the tail gas treatment device and the environmental risks brought by chlorine leakage. It has significant economic and social benefits.

[0087] (4) Through the first jacketed heat exchanger, the second jacketed heat exchanger and the third jacketed heat exchanger, and in conjunction with the first online thermometer, the second online thermometer and the third online thermometer, the temperature of the liquid inside the first reaction vessel, the second reaction vessel and the sodium hypochlorite reactor can be monitored in real time. When the temperature is too low or too high, this will reduce or increase the amount of cooling water entering the jacket of the first jacketed heat exchanger, the second jacketed heat exchanger or the third jacketed heat exchanger, thereby causing the temperature of the liquid inside the first reaction vessel, the second reaction vessel or the sodium hypochlorite reactor to rise or fall, thereby maintaining the temperature of the liquid inside the first reaction vessel, the second reaction vessel and the sodium hypochlorite reactor within a suitable range, and ensuring the smooth progress of the sodium hypochlorite solution preparation. Attached Figure Description

[0088] Figure 1 This is a schematic diagram of the production equipment process of the present invention;

[0089] Figure 2 This is a schematic diagram of the production equipment process of the first part of the present invention;

[0090] Figure 3 This is a schematic diagram of the production equipment process in the second part of the present invention;

[0091] Figure 4 This is a schematic diagram of a sodium hypochlorite reactor;

[0092] Figure 5 This is a schematic diagram of a partial structure of a hypochlorous acid reactor;

[0093] Figure 6 This is a front sectional view of the hypochlorous acid reactor.

[0094] Figure 7 yes Figure 4 Enlarged view of point A in the middle;

[0095] Figure 8 yes Figure 4 Enlarged view of point B in the middle;

[0096] Figure 9 This is a bottom cross-sectional view of the hypochlorous acid reactor.

[0097] Figure 10 This is a schematic diagram of the structure of the primary shunt component;

[0098] Figure 11 This is a partial structural diagram of the secondary shunt component.

[0099] The labels in the attached diagram are as follows: 100-First reactor; 101-First transfer pump; 102-First back pressure valve; 103-First density meter; 104-Second back pressure valve; 105-First online thermometer; 106-Inlet of first jacketed heat exchanger; 107-First jacketed heat exchanger; 108-Outlet of first jacketed heat exchanger; 200-Second reactor; 201-Second transfer pump; 202-Third back pressure valve; 203-Third transfer pump; 204-Fourth back pressure valve; 205-Second density meter; 206-Inlet of second jacketed heat exchanger; 207-Second... Jacketed heat exchanger; 208-Second jacketed heat exchanger outlet; 209-Second online thermometer; 2010-Fifth back pressure valve; 300-Heat exchanger; 301-Fourth transfer pump; 302-Sixth back pressure valve; 400-Static mixer; 401-Fifth transfer pump; 402-Seventh back pressure valve; 403-Sixth transfer pump; 404-Sodium hydroxide dilute solution back pressure valve; 500-Sodium hypochlorite reactor; 501-pH meter; 502-Eighth transfer pump; 503-Inert gas valve; 504-Pressure gauge; 505-Third jacketed heat exchanger; 506- 507-Third jacketed heat exchanger inlet; 508-Third jacketed heat exchanger outlet; 509-Cooling water valve; 500-Third online thermometer; 600-Buffer tank; 601-Chlorine valve; 602-Seventh transfer pump; 34-Gas distributor; 702-Eighth back pressure valve; 703-Ninth transfer pump; 704-Oxidation-reduction potential analyzer; 30-Spray tower atomizer; 3001-Inlet pipe; 3002-Inlet horizontal pipe; 303-Inlet branch pipe; 304-Atomizing nozzle; 305-Drive motor; 306-Rotary disc; 307-Atomization status detection component. 3071-Sealed box, 3072-Tension sensor, 3073-Straight rod, 3074-Connecting plate, 3075-Pull rod, 341-Inlet pipe, 342-Inlet horizontal pipe, 343-Inlet branch pipe, 344-Air nozzle, 345-First-stage diverter assembly, 3451-First diverter, 3452-First connecting rod, 3453-First fixing ring, 346-Second-stage diverter assembly, 3461-Liquid storage box, 3462-Leakage hole, 3463-Support rod, 3464-Second diverter, 3465-Second connecting rod, 3466-Second fixing ring. Detailed Implementation

[0100] The present invention will be further described below with reference to the accompanying drawings and embodiments, but this should not be construed as limiting the present invention.

[0101] like Figure 1 As shown, a method for continuously preparing high-purity sodium hypochlorite includes the following steps:

[0102] (a) Preparation of concentrated sodium hydroxide solution

[0103] (a1) Add a certain mass of concentrated alkali to the first reactor 100 equipped with the first jacketed heat exchanger 107, and turn on the circulating cooling water;

[0104] (a2) Add a certain mass of deionized water to the first reactor 100 in step (a1) and start the stirrer in the first reactor (100);

[0105] (a3) Adjust the flow rate of circulating cooling water in the first jacketed heat exchanger 107 outside the first reactor 100 in step (a1) by adjusting the reading of the first online thermometer 105, and control the solution temperature in the first reactor 100; the temperature of the concentrated sodium hydroxide solution in the first reactor 100 is 30℃~50℃;

[0106] (a4) Adjust the deionized water flow rate in step (a2) by measuring the reading of the first densitometer 103 to control the concentration of the sodium hydroxide solution; the mass concentration of the sodium hydroxide solution in step (a4) is 20% to 50%.

[0107] (a5) The temperature of the concentrated sodium hydroxide solution in the first reactor 100 is controlled by interlocking the reading of the first online thermometer 105 in the first reactor 100 with the first jacketed heat exchanger 107.

[0108] (b) Preparation of dilute sodium hydroxide solution

[0109] (b1) Add the concentrated sodium hydroxide solution obtained in step (a4) into the second reactor 200 equipped with the second jacketed heat exchanger 207, and turn on the circulating cooling water;

[0110] (b2) Input a certain mass of deionized water into the second reactor 200 in step (b1) and start the stirrer inside the second reactor 200;

[0111] (b3) Adjust the flow rate of the circulating cooling water in the second jacketed heat exchanger 207 outside the second reactor 200 in step (b1) by adjusting the reading of the second online thermometer 209, and control the solution temperature inside the second reactor 200; the temperature of the dilute sodium hydroxide solution in the second reactor 200 is 20℃~40℃;

[0112] (b4) Adjust the deionized water flow rate in step (b2) by measuring the reading of the second densitometer 205 to control the concentration of the sodium hydroxide dilute solution; the mass concentration of the sodium hydroxide dilute solution in step (b4) is 13% to 18%.

[0113] (b5) The temperature of the dilute sodium hydroxide solution in the second reactor 200 is controlled by interlocking the second jacketed heat exchanger 206 with the reading of the second online thermometer 209 in the second reactor 200;

[0114] (c) Transporting dilute sodium hydroxide solution

[0115] (c1) Transfer the dilute sodium hydroxide solution obtained in step (b4) into a storage tank for later use;

[0116] (c2) The dilute sodium hydroxide solution from step (c1) is fed into a static mixer 400 for mixing; the length-to-diameter ratio of the static mixer 400 is 10-15; the diameter of the static mixer 400 is 0.05m-0.2m.

[0117] (d) Chlorination reaction

[0118] (d1) The sodium hydroxide dilute solution mixed in step (c2) is fed into the atomizer 30 of the spray tower at the top of the sodium hypochlorite reactor 500. The sodium hydroxide dilute solution is sprayed and atomized downwards from the top of the spray tower atomizer 30. The pressure applied to the spray tower atomizer 30 is 0.2MPa to 0.5MPa. The flow rate of the sodium hydroxide dilute solution in step (d1) is 20mL / min to 40mL / min. The droplet size of the sodium hydroxide dilute solution after atomization in step (d1) is 5μm to 50μm.

[0119] (d2) Chlorine gas is delivered to gas distributor 34 and distributed in sodium hypochlorite reactor 500 by gas distributor 34; the flow rate of chlorine gas in step (d2) is 5 mL / min to 25 mL / min;

[0120] (d3) After the sodium hydroxide dilute solution atomized in step (d1) reacts countercurrently with the chlorine gas dispersed in step (d2), sodium hypochlorite solution is generated.

[0121] (e) Online monitoring

[0122] (e1) The pH of the sodium hypochlorite solution in step (d3) is tested online by pH meter 501 in sodium hypochlorite reactor 500, and the opening of back pressure valve 404 of dilute sodium hydroxide solution is interlocked online to keep the pH of the reaction system within a certain range; the pH of the reaction system in step (e1) is kept at 12-13.

[0123] (e2) The cooling water valve 508 is interlocked online by the third online thermometer 509 in the sodium hypochlorite reactor 500. The cooling water flow rate is adjusted by adjusting the opening of the cooling water valve 508 online, thereby controlling the reaction temperature online. The reaction temperature in step (e2) is maintained at 30℃~50℃.

[0124] (e3) The inert gas valve 503 is interlocked online via the pressure gauge 504 inside the sodium hypochlorite reactor 500. The inert gas flow rate is adjusted by regulating the opening of the inert gas valve 503 online, thereby maintaining a constant internal pressure in the sodium hypochlorite reactor 500. The reaction pressure in step (e3) is controlled between 0.09 MPa and 0.11 MPa. The inert gas is at least one of helium, neon, argon, krypton, or xenon.

[0125] (e4) The chlorine flow rate is adjusted by online interlocking the chlorine valve 601 through the redox potential analyzer 701 in the sodium hypochlorite reactor 500 and adjusting the opening of the chlorine valve 601 online; the reading of the redox potential analyzer 701 in step (e4) is controlled between 500mV and 600mV.

[0126] (f) Collecting products

[0127] By observing the reading of the redox potential analyzer 701 in step (e4), it is determined whether the product meets the standard. If it meets the standard, the sodium hypochlorite solution in step (d3) is sent to the finished product tank 700. If it does not meet the standard, the sodium hypochlorite solution continues to remain in the sodium hypochlorite reactor 500, and the corresponding chlorine valve 601 is interlocked online by the redox potential analyzer 701 until the sodium hypochlorite solution meets the standard and is sent to the finished product tank 700. The product compliance requirements in step (f) are that the effective chlorine mass fraction is 6%-15% and the free alkali content is less than 0.5% mass concentration.

[0128] like Figure 2 and Figure 3 As shown, the equipment for continuously preparing high-purity sodium hypochlorite includes a first reactor 100, with a first inlet pipe connected to the inlet of the first reactor 100, and a first delivery pump 101 installed on the first inlet pipe; a first back pressure valve 102 is installed on the first inlet pipe between the first delivery pump 101 and the first reactor 100; a first jacketed heat exchanger 107 is fitted onto the outer circumference of the first reactor 100, with a first jacketed heat exchanger inlet 106 and a first jacketed heat exchanger outlet 108 on the first jacketed heat exchanger 107; the first jacketed heat exchanger inlet 106 is connected to the drain outlet of the first reactor 100 through a pipe, and the first jacketed heat exchanger inlet 106 is connected to cooling water through a pipe; a second back pressure valve 104 is installed on the pipe between the cooling water and the first jacketed heat exchanger inlet 106.

[0129] It also includes a second reactor 200, whose inlet is connected to the outlet of the first reactor 100 via a pipeline. A second delivery pump 201 and a third back pressure valve 202 are sequentially installed along the liquid flow direction on the pipeline between the outlet of the first reactor 100 and the inlet of the second reactor 200. A second water inlet pipeline is connected to the inlet of the second reactor 200, and a third delivery pump 203 is installed on the second water inlet pipeline. A fifth back pressure valve 2010 is installed on the pipeline between the third delivery pump 203 and the second reactor 200. A second jacketed heat exchanger 207 is fitted onto the outer circumference of the second reactor 200, and the second jacketed heat exchanger 207 is equipped with… The second jacketed heat exchanger inlet 206 and the second jacketed heat exchanger outlet 208 are connected. The second jacketed heat exchanger inlet 206 is connected to the drain outlet of the second reactor 200 via a pipeline. The second jacketed heat exchanger inlet 206 is also connected to cooling water via a pipeline. A fourth back pressure valve 204 is provided on the pipeline between the cooling water and the second jacketed heat exchanger inlet 206. The drain outlet of the second reactor 200 is connected to the heat exchanger 300 via a pipeline. A fourth delivery pump 301 and a sixth back pressure valve 302 are provided on the pipeline between the heat exchanger 300 and the drain outlet of the second reactor 200. The sixth back pressure valve 302 is closer to the heat exchanger 300 than the fourth delivery pump 301.

[0130] The drain port of heat exchanger 300 is connected to static mixer 400 through a pipeline. A fifth delivery pump 401 and a seventh back pressure valve 402 are installed on the pipeline between static mixer 400 and heat exchanger 300. The seventh back pressure valve 402 is closer to static mixer 400 than the fifth delivery pump 401.

[0131] like Figure 4 and 6 As shown, the drain port of the static mixer 400 is connected to the sodium hypochlorite reactor 500 via a pipeline. A sixth delivery pump 403 and a sodium hydroxide dilute solution back pressure valve 404 are installed on the pipeline between the sodium hypochlorite reactor 500 and the static mixer 400. The sodium hydroxide dilute solution back pressure valve 404 is closer to the sodium hypochlorite reactor 500 than the sixth delivery pump 403. A jet tower atomizer 30 is installed at the top of the sodium hypochlorite reactor 500. A gas distributor 34 is installed at the bottom of the sodium hypochlorite reactor 500.

[0132] like Figure 5 As shown, the gas inlet of the gas distributor 34 is connected to a gas buffer tank 600 through a pipeline. A chlorine valve 601 is provided on the pipeline between the gas buffer tank 600 and the gas distributor 34. The gas inlet of the gas buffer tank 600 is connected to a chlorine inlet through a pipeline. A seventh delivery pump 602 is provided on the pipeline between the chlorine inlet and the gas buffer tank 600.

[0133] The bottom of the sodium hypochlorite reactor 500 is connected to the inert gas inlet via a pipeline. An eighth delivery pump 502 and an inert gas valve 503 are installed on the pipeline between the inert gas inlet and the sodium hypochlorite reactor 500. The inert gas valve 503 is closer to the sodium hypochlorite reactor 500 than the eighth delivery pump 502.

[0134] A third jacketed heat exchanger 505 is fitted on the outer periphery of the sodium hypochlorite reactor 500. The third jacketed heat exchanger 505 is provided with a third jacketed heat exchanger inlet 506 and a third jacketed heat exchanger outlet 507. The third jacketed heat exchanger inlet 506 is connected to a cooling water interface through a pipeline. A cooling water valve 508 is provided on the pipeline between the cooling water interface and the third jacketed heat exchanger inlet 506.

[0135] The outlet of the sodium hypochlorite reactor 500 is connected to the finished product tank 700 via a pipeline. A ninth transfer pump 703 and an eighth back pressure valve 702 are installed on the pipeline between the finished product tank 700 and the sodium hypochlorite reactor 500. The eighth back pressure valve 702 is closer to the sodium hypochlorite reactor 500 than the ninth transfer pump 703.

[0136] The first reactor 100 is equipped with a first density meter 103, which is online-locked with a first back pressure valve 102. A first online thermometer 105 is installed on the pipeline between the drain outlet of the first reactor 100 and the inlet 106 of the first jacketed heat exchanger. The second reactor 200 is equipped with a second density meter 205, which is online-locked with a fifth back pressure valve 2010. A second online thermometer 209 is installed on the pipeline between the drain outlet of the second reactor 200 and the inlet 206 of the second jacketed heat exchanger. A pH meter 501 is connected to the sodium hypochlorite reactor 500. A pressure gauge 504 is connected to the bottom of the sodium hypochlorite reactor 500, which is online-locked with an inert gas valve 503. A third online thermometer 509 is connected to the drain outlet of the sodium hypochlorite reactor 500, which is online-locked with a cooling water valve 508. An oxidation-reduction potential analyzer 701 is installed on the pipeline between the eighth back pressure valve 702 and the sodium hypochlorite reactor 500. The oxidation-reduction potential analyzer 701 is interlocked online with the chlorine valve 601.

[0137] like Figure 9As shown, the jet tower atomizer 30 includes an inlet pipe 3001, the inlet end of which is connected to the static mixer 400 via a pipeline, and an inlet horizontal pipe 3002 rotatably connected to the outlet end of the inlet pipe 3001. Multiple inlet branch pipes 303 are provided on the outer circumferential surface of the inlet horizontal pipe 3002. Multiple atomizing nozzles 304 are provided at the top and bottom of each inlet branch pipe 303, and solenoid valves are provided on the atomizing nozzles 304. The jet tower atomizer 30 also includes a drive motor 305, which is mounted on the outer wall of the sodium hypochlorite reactor 500. A turntable 306 is provided at the drive end of the drive motor 305, located inside the sodium hypochlorite reactor 500, and connected to one end of the inlet horizontal pipe 3002.

[0138] like Figure 7 , Figure 8 , Figure 10 and Figure 11As shown, the gas distributor 34 includes an inlet pipe 341, the inlet end of which is connected to the gas buffer tank 600 via a pipeline, and the outlet end of the inlet pipe 341 is connected to an inlet horizontal pipe 342. The inlet horizontal pipe 342 is located inside the sodium hypochlorite reactor 500. Multiple inlet branch pipes 343 are provided on the outer circumferential surface of the inlet horizontal pipe 342, and multiple jet nozzles 344 are connected to the top of each inlet branch pipe 343. It also includes a primary flow splitting assembly 345, which is located above the jet nozzles 344. A secondary flow splitting assembly 346 is provided above the primary flow splitting assembly 345. The primary diversion assembly 345 includes a plurality of inverted conical first diverters 3451, each corresponding to a nozzle 344. The first diverters 3451 are located above the corresponding nozzles 344. Adjacent first diverters 3451 are connected by a first connecting rod 3452. A first fixing ring 3453 is connected to the inner wall of the sodium hypochlorite reactor 500. The first diverter 3451 near the first fixing ring 3453 is connected to the first fixing ring 3453 by the first connecting rod 3452. The secondary diversion assembly 346 includes multiple liquid storage boxes 3461. The liquid storage boxes 3461 are located above the first diverter 3451. The bottom of the liquid storage box 3461 is provided with a water leakage hole 3462. The top of the liquid storage box 3461 is connected to multiple second diverters 3464 through a support rod 3463. Adjacent liquid storage boxes 3461 are connected through a second connecting rod 3465. A second fixing ring 3466 is slidably connected to the inner wall of the sodium hypochlorite reactor 500. The liquid storage box 3461 close to the second fixing ring 3466 is connected to the second fixing ring 3466 through the second connecting rod 3465. It also includes an atomization state detection component 307; the atomization state detection component 307 includes multiple sealed boxes 3071, the sealed boxes 3071 are set on the inner side wall of the sodium hypochlorite reactor 500, the sealed box 3071 is equipped with a tension sensor 3072, the tension sensor 3072 is equipped with a straight rod 3073, the bottom end of the straight rod 3073 penetrates the bottom wall of the sealed box 3071 and is connected to a connecting plate 3074, the connecting plate 3074 is equipped with a pull rod 3075, the bottom end of the pull rod 3075 is connected to a second fixing ring 3466, and the tension sensor 3072 is connected to the drive motor 305 by wire or wireless means.

[0139] Example 1:

[0140] like Figure 1 As shown, a method for continuously preparing high-purity sodium hypochlorite includes the following steps:

[0141] (a) Preparation of concentrated sodium hydroxide solution

[0142] (a1) Add a certain mass of concentrated alkali to the first reactor 100 equipped with the first jacketed heat exchanger 107, and turn on the circulating cooling water;

[0143] (a2) Add a certain mass of deionized water to the first reactor 100 in step (a1) and start the stirrer in the first reactor 100;

[0144] (a3) Adjust the flow rate of circulating cooling water in the first jacketed heat exchanger 107 outside the first reactor 100 in step (a1) by adjusting the reading of the first online thermometer 105, and control the solution temperature in the first reactor 100 to 30°C.

[0145] (a4) Adjust the deionized water flow rate in step (a2) by adjusting the reading of the first densitometer 103 to control the concentration of the sodium hydroxide solution to 20%;

[0146] (a5) The temperature of the concentrated sodium hydroxide solution in the first reactor 100 is controlled by interlocking the reading of the first online thermometer 105 in the first reactor 100 with the first jacketed heat exchanger 107.

[0147] (b) Preparation of dilute sodium hydroxide solution

[0148] (b1) Add the concentrated sodium hydroxide solution obtained in step (a4) into the second reactor 200 equipped with the second jacketed heat exchanger 207, and turn on the circulating cooling water;

[0149] (b2) Input a certain mass of deionized water into the second reactor 200 in step (b1) and start the stirrer inside the second reactor 200;

[0150] (b3) Adjust the flow rate of the circulating cooling water in the second jacketed heat exchanger 207 outside the second reactor 200 in step (b1) by adjusting the reading of the second online thermometer 209, and control the solution temperature inside the second reactor 200 to 20°C.

[0151] (b4) Adjust the deionized water flow rate in step (b2) by adjusting the reading of the second densitometer 205 to control the concentration of the sodium hydroxide dilute solution to 13%;

[0152] It also includes step (b5) interlocking the second jacketed heat exchanger 207 with the reading of the second online thermometer 209 in the second reactor 200 to control the temperature of the dilute sodium hydroxide solution in the second reactor 200;

[0153] (c) Transporting dilute sodium hydroxide solution

[0154] (c1) Transfer the dilute sodium hydroxide solution obtained in step (b4) into a storage tank for later use;

[0155] (c2) The dilute sodium hydroxide solution from step (c1) is fed into a static mixer 400 for mixing;

[0156] (d) Chlorination reaction

[0157] (d1) The sodium hydroxide dilute solution mixed in step (c2) is fed into the spray tower atomizer 30 at the top of the sodium hypochlorite reactor 500 at a flow rate of 20 mL / min. The sodium hydroxide dilute solution is sprayed and atomized from the top of the spray tower atomizer 30 downwards. The droplet size of the sodium hydroxide dilute solution after atomization in step (d1) is 5 μm.

[0158] (d2) Chlorine gas is delivered to gas distributor 34 at a flow rate of 5 mL / min, and the chlorine gas is distributed in sodium hypochlorite reactor 500 by gas distributor 34.

[0159] (d3) After the sodium hydroxide dilute solution atomized in step (d1) reacts countercurrently with the chlorine gas dispersed in step (d2), sodium hypochlorite solution is generated.

[0160] (e) Online monitoring

[0161] (e1) The pH of the sodium hypochlorite solution in step (d3) is tested online by pH meter in sodium hypochlorite reactor 500, and the opening of sodium hydroxide dilute solution back pressure valve 404 is interlocked online to keep the pH of the reaction system at 12.

[0162] (e2) The cooling water valve 508 is interlocked online by the third online thermometer 509 in the sodium hypochlorite reactor 500. The cooling water flow rate is adjusted by adjusting the opening of the cooling water valve 508 online, thereby controlling the reaction temperature to be maintained at 30℃ online.

[0163] (e3) The pressure gauge 504 inside the sodium hypochlorite reactor 500 is used to interlock the inert gas valve 503 online. The inert gas flow rate is adjusted by adjusting the opening of the inert gas valve 503 online. The inert gas is at least one of helium, neon, argon, krypton or xenon, thereby maintaining the internal pressure of the sodium hypochlorite reactor 500 at a constant 0.09 MPa.

[0164] (e4) Using the redox potential analyzer 701 in the sodium hypochlorite reactor 500, the chlorine valve 601 is interlocked online. The chlorine flow rate is adjusted by reducing the opening of the chlorine valve 601 online. In step (e4), the reading of the redox potential analyzer 701 is controlled at 500mV.

[0165] (f) Collecting products

[0166] By observing the reading of the redox potential analyzer 701 in step (e4), it is determined whether the product meets the standard. If it meets the standard, the sodium hypochlorite solution in step (d3) is sent to the finished product tank 700. If it does not meet the standard, the sodium hypochlorite solution continues to remain in the sodium hypochlorite reactor 500, and the corresponding chlorine valve 601 is interlocked online by the redox potential analyzer 701 until the sodium hypochlorite solution meets the standard and is sent to the finished product tank 700. The requirements for the product to meet the standard in step (f) are that the effective chlorine mass fraction is 6% and the free alkali content is less than 0.5% mass concentration.

[0167] Example 2:

[0168] like Figure 1 As shown, a method for continuously preparing high-purity sodium hypochlorite includes the following steps:

[0169] (a) Preparation of concentrated sodium hydroxide solution

[0170] (a1) Add a certain mass of concentrated alkali to the first reactor 100 equipped with the first jacketed heat exchanger 107, and turn on the circulating cooling water;

[0171] (a2) Add a certain mass of deionized water to the first reactor 100 in step (a1) and start the stirrer in the first reactor 100;

[0172] (a3) Adjust the flow rate of circulating cooling water in the first jacketed heat exchanger 107 outside the first reactor 100 in step (a1) by adjusting the reading of the first online thermometer 105, and control the solution temperature in the first reactor 100 to 50°C.

[0173] (a4) Adjust the deionized water flow rate in step (a2) by adjusting the reading of the first densitometer 103 to control the concentration of the sodium hydroxide solution to 50%;

[0174] (a5) The temperature of the concentrated sodium hydroxide solution in the first reactor 100 is controlled by interlocking the reading of the first online thermometer 105 in the first reactor 100 with the first jacketed heat exchanger 107.

[0175] (b) Prepare a dilute sodium hydroxide solution.

[0176] (b1) Add the concentrated sodium hydroxide solution obtained in step (a4) into the second reactor 200 equipped with the second jacketed heat exchanger 207, and turn on the circulating cooling water;

[0177] (b2) Input a certain mass of deionized water into the second reactor 200 in step (b1) and start the stirrer inside the second reactor 200;

[0178] (b3) Adjust the flow rate of the circulating cooling water in the second jacketed heat exchanger 207 outside the second reactor 200 in step (b1) by adjusting the reading of the second online thermometer 209, and control the solution temperature inside the second reactor 200 to 40°C.

[0179] (b4) Adjust the deionized water flow rate in step (b2) by adjusting the reading of the second densitometer 205 to control the concentration of the sodium hydroxide dilute solution to 18%;

[0180] (b5) The temperature of the dilute sodium hydroxide solution in the second reactor 200 is controlled by interlocking the second jacketed heat exchanger 207 with the reading of the second online thermometer 209 in the second reactor 200.

[0181] (c) Transporting dilute sodium hydroxide solution

[0182] (c1) Transfer the dilute sodium hydroxide solution obtained in step (b4) into a storage tank for later use;

[0183] (c2) The dilute sodium hydroxide solution from step (c1) is fed into a static mixer 400 for mixing;

[0184] (d) Chlorination reaction

[0185] (d1) The sodium hydroxide dilute solution mixed in step (c2) is fed into the spray tower atomizer 30 at the top of the sodium hypochlorite reactor 500 at a flow rate of 40 mL / min. The sodium hydroxide dilute solution is sprayed and atomized from the top of the spray tower atomizer 30 downwards. The droplet size of the sodium hydroxide dilute solution after atomization in step (d1) is 50 μm.

[0186] (d2) Chlorine gas is delivered to gas distributor 34 at a flow rate of 25 mL / min, and the chlorine gas is distributed in sodium hypochlorite reactor 500 by gas distributor 34.

[0187] (d3) After the sodium hydroxide dilute solution atomized in step (d1) reacts with the chlorine gas dispersed in step (d2) in a countercurrent manner, sodium hypochlorite solution is generated.

[0188] (e) Online monitoring

[0189] (e1) The pH of the sodium hypochlorite solution in step (d3) is tested online by pH meter in sodium hypochlorite reactor 500, and the opening of sodium hydroxide dilute solution back pressure valve 404 is interlocked online to keep the pH of the reaction system at 13.

[0190] (e2) The cooling water valve 508 is interlocked online by the third online thermometer 509 in the sodium hypochlorite reactor 500. The cooling water flow rate is adjusted by adjusting the opening of the cooling water valve 508 online, thereby controlling the reaction temperature to be maintained at 50℃ online.

[0191] (e3) The pressure gauge 504 inside the sodium hypochlorite reactor 500 is used to interlock the inert gas valve 503 online. The inert gas flow rate is adjusted by adjusting the opening of the inert gas valve 503 online. The inert gas is at least one of helium, neon, argon, krypton or xenon, thereby maintaining the internal pressure of the sodium hypochlorite reactor 500 at a constant 0.11 MPa.

[0192] (e4) Using the redox potential analyzer 701 in the sodium hypochlorite reactor 500, the chlorine valve 601 is interlocked online. The chlorine flow rate is adjusted by reducing the opening of the chlorine valve 601 online. In step (e4), the reading of the redox potential analyzer 701 is controlled at 600mV.

[0193] (f) Collecting products

[0194] By observing the reading of the redox potential analyzer 701 in step (e4), it is determined whether the product meets the standard. If it meets the standard, the sodium hypochlorite solution in step (d3) is sent to the finished product tank 700. If it does not meet the standard, the sodium hypochlorite solution continues to remain in the sodium hypochlorite reactor 500, and the corresponding chlorine valve 601 is interlocked online by the redox potential analyzer 701 until the sodium hypochlorite solution meets the standard and is sent to the finished product tank 700. The requirements for the product to meet the standard in step (f) are that the effective chlorine mass fraction is 15% and the free alkali content is less than 0.5% mass concentration.

[0195] Example 3:

[0196] like Figure 1 The method for continuously preparing high-purity sodium hypochlorite, as shown, includes the following steps:

[0197] (a) Preparation of concentrated sodium hydroxide solution

[0198] (a1) Add a certain mass of concentrated alkali to the first reactor 100 equipped with the first jacketed heat exchanger 107, and turn on the circulating cooling water;

[0199] (a2) Add a certain mass of deionized water to the first reactor 100 in step (a1) and start the stirrer in the first reactor 100;

[0200] (a3) Adjust the flow rate of circulating cooling water in the first jacketed heat exchanger 107 outside the first reactor 100 in step (a1) by adjusting the reading of the first online thermometer 105, and control the solution temperature in the first reactor 100 to 35°C.

[0201] (a4) Adjust the deionized water flow rate in step (a2) by adjusting the reading of the first densitometer 103 to control the concentration of the sodium hydroxide solution to 30%;

[0202] (a5) The temperature of the concentrated sodium hydroxide solution in the first reactor 100 is controlled by interlocking the reading of the first online thermometer 105 in the first reactor 100 with the first jacketed heat exchanger 107.

[0203] (b) Preparation of dilute sodium hydroxide solution

[0204] (b1) Add the concentrated sodium hydroxide solution obtained in step (a4) into the second reactor 200 equipped with the second jacketed heat exchanger 207, and turn on the circulating cooling water;

[0205] (b2) Input a certain mass of deionized water into the second reactor 200 in step (b1) and start the stirrer inside the second reactor 200;

[0206] (b3) Adjust the flow rate of the circulating cooling water in the second jacketed heat exchanger 207 outside the second reactor 200 in step (b1) by adjusting the reading of the second online thermometer 209, and control the solution temperature inside the second reactor 200 to 30°C.

[0207] (b4) Adjust the deionized water flow rate in step (b2) by adjusting the reading of the second densitometer 205 to control the concentration of the sodium hydroxide dilute solution to 15%;

[0208] (b5) The temperature of the dilute sodium hydroxide solution in the second reactor 200 is controlled by interlocking the second jacketed heat exchanger 207 with the reading of the second online thermometer 209 in the second reactor 200.

[0209] (c) Transporting dilute sodium hydroxide solution

[0210] (c1) Transfer the dilute sodium hydroxide solution obtained in step (b4) into a storage tank for later use;

[0211] (c2) The dilute sodium hydroxide solution from step (c1) is fed into a static mixer 400 for mixing;

[0212] (d) Chlorination reaction

[0213] (d1) The sodium hydroxide dilute solution mixed in step (c2) is fed into the spray tower atomizer 30 at the top of the sodium hypochlorite reactor 500 at a flow rate of 30 L / min. The sodium hydroxide dilute solution is sprayed and atomized from the top of the spray tower atomizer 30 downwards. The droplet size of the sodium hydroxide dilute solution after atomization in step (d1) is 35 μm.

[0214] (d2) Chlorine gas is delivered to the gas distributor 34 at a flow rate of 15 mL / min, and the chlorine gas is distributed in the sodium hypochlorite reactor 500 by the gas distributor 34.

[0215] (d3) After the sodium hydroxide dilute solution atomized in step (d1) reacts countercurrently with the chlorine gas dispersed in step (d2), sodium hypochlorite solution is generated.

[0216] (e) Online monitoring

[0217] (e1) The pH of the sodium hypochlorite solution in step (d3) is tested online by pH meter in sodium hypochlorite reactor 500, and the opening of sodium hydroxide dilute solution back pressure valve 404 is interlocked online to keep the pH of the reaction system at 12.5;

[0218] (e2) The cooling water valve 508 is interlocked online by the third online thermometer 509 in the sodium hypochlorite reactor 500. The cooling water flow rate is adjusted by adjusting the opening of the cooling water valve 508 online, thereby controlling the reaction temperature to be maintained at 40℃ online.

[0219] (e3) The pressure gauge 504 inside the sodium hypochlorite reactor 500 is used to interlock the inert gas valve 503 online. The inert gas flow rate is adjusted by adjusting the opening of the inert gas valve 503 online, thereby maintaining the internal pressure of the sodium hypochlorite reactor 500 at a constant 0.1 MPa. The inert gas is at least one of helium, neon, argon, krypton or xenon.

[0220] (e4) Using the redox potential analyzer 701 in the sodium hypochlorite reactor 500, the chlorine valve 601 is interlocked online. The chlorine flow rate is adjusted by reducing the opening of the chlorine valve 601 online. In step (e4), the reading of the redox potential analyzer 701 is controlled at 550mV.

[0221] (f) Collecting products

[0222] By observing the reading of the redox potential analyzer 701 in step (e4), it is determined whether the product meets the standard. If it meets the standard, the sodium hypochlorite solution in step (d3) is sent to the finished product tank 700. If it does not meet the standard, the sodium hypochlorite solution continues to remain in the sodium hypochlorite reactor 500, and the corresponding chlorine valve 601 is interlocked online by the redox potential analyzer 701 until the sodium hypochlorite solution meets the standard and is sent to the finished product tank 700. The requirements for the product to meet the standard in step (f) are that the effective chlorine mass fraction is 12% and the free alkali content is less than 0.5% mass concentration.

[0223] Example 4:

[0224] An apparatus for continuously producing high-purity sodium hypochlorite includes a first reactor 100, with a first inlet pipe connected to the inlet of the first reactor 100. A first delivery pump 101 is installed on the first inlet pipe, and a first back pressure valve 102 is installed on the first inlet pipe between the first delivery pump 101 and the first reactor 100. A first density meter 103 is installed on the first reactor 100, and the first density meter 103 is interlocked with the first back pressure valve 102 online. A first jacketed heat exchanger 107 is fitted onto the outer circumference of the first reactor 100. The first jacketed heat exchanger 107 has a first jacketed heat exchanger inlet 106 and a first jacketed heat exchanger outlet 108. The first jacketed heat exchanger inlet 106 is connected to the drain outlet of the first reactor 100 through a pipe, and a first online thermometer 105 is installed on the pipe. A second back pressure valve 104 is installed on the first jacketed heat exchanger inlet 106.

[0225] It also includes a second reactor 200. The drain port of the first reactor 100 is connected to the inlet of the second reactor 200 via a pipeline. Along the liquid flow direction, a second delivery pump 201 and a third back pressure valve 202 are sequentially installed on this pipeline. The inlet of the second reactor 200 is connected to a second inlet pipeline, which is equipped with a third delivery pump 203 and a fifth back pressure valve 2010. A second density meter 205 is installed on the second reactor 200, and the second density meter 205 is interlocked with the fifth back pressure valve 2010 online. A second jacketed heat exchanger is fitted onto the outer circumference of the second reactor 200. Heater 207, the second jacketed heat exchanger 207 is provided with a second jacketed heat exchanger inlet 206 and a second jacketed heat exchanger outlet 208. The second jacketed heat exchanger inlet 206 is connected to the drain outlet of the second reactor 200 through a pipeline, and a second online thermometer 209 is provided on the pipeline. Another pipeline is connected to the second jacketed heat exchanger inlet 206, and a fourth back pressure valve 204 is provided on the pipeline. The drain outlet of the second reactor 200 is connected to the inlet of the heat exchanger 300 through a pipeline, and a fourth delivery pump 301 and a sixth back pressure valve 302 are provided on the pipeline.

[0226] The drain port of heat exchanger 300 is connected to the inlet of static mixer 400 through a pipeline. The pipeline is equipped with a fifth delivery pump 401 and a seventh back pressure valve 402. The drain port of static mixer 400 is connected to the inlet of sodium hypochlorite reactor 500 through a pipeline. The pipeline is equipped with a 403 and a sodium hydroxide dilute solution back pressure valve 404. The sodium hypochlorite reactor 500 is equipped with a pH meter 501. The top of the sodium hypochlorite reactor 500 is equipped with a jet tower atomizer 30, and the bottom of the sodium hypochlorite reactor 500 is equipped with a gas distributor 34.

[0227] The gas distributor 34 has its inlet connected to the outlet of the buffer tank 600 via an inlet pipe. A chlorine valve 601 is installed on the inlet pipe. The chlorine inlet on the buffer tank 600 is connected to a pipe with a seventh delivery pump 602. An inert gas inlet at the bottom of the sodium hypochlorite reactor 500 is connected to a pipe with an eighth delivery pump 502 and an inert gas valve 503. A pressure gauge 504 is installed at the bottom of the sodium hypochlorite reactor 500. The pressure gauge 504 is interlocked with the inert gas valve 503 online.

[0228] A third jacketed heat exchanger 505 is fitted on the outer periphery of the sodium hypochlorite reactor 500. The third jacketed heat exchanger 505 is provided with a third jacketed heat exchanger inlet 506 and a third jacketed heat exchanger outlet 507. The drain outlet of the sodium hypochlorite reactor 500 is connected to the third jacketed heat exchanger inlet 506 through a water inlet pipe. A cooling water valve 508 and a third online thermometer 509 are provided on the water inlet pipe.

[0229] The discharge port of the sodium hypochlorite reactor 500 is connected to the finished product tank 700 through a pipeline. The pipeline is equipped with an oxidation-reduction potential analyzer 701, an eighth back pressure valve 702, and a ninth transfer pump 703. The oxidation-reduction potential analyzer 701 is interlocked with the chlorine valve 601 online.

[0230] The jet tower atomizer 30 includes an inlet pipe 3001, one end of which passes through the sodium hypochlorite reactor 500 and is rotatably connected to an inlet horizontal pipe 3002. The inlet pipe 3001 and the inlet horizontal pipe 3002 are connected. Two sets of inlet branch pipes 303 are symmetrically arranged on the outer circumference of the inlet horizontal pipe 3002. The top and bottom of the two sets of inlet branch pipes 303 are connected to multiple atomizing nozzles 304. The atomizing nozzles 304 are equipped with solenoid valves. The jet tower atomizer 30 includes a drive motor 305 and a turntable 306. The turntable 306 is located inside the sodium hypochlorite reactor 500 and is connected to the end of the inlet horizontal pipe 3002. The drive motor 305 is located outside the sodium hypochlorite reactor 500 and is connected to the turntable 306. The jet tower atomizer 30 also includes an atomization status detection component 307.

[0231] The gas distributor 34 includes an inlet pipe 341, one end of which passes through the sodium hypochlorite reactor 500 and is connected to an inlet horizontal pipe 342. Two sets of inlet branch pipes 343 are symmetrically connected to the outer circumference of the inlet horizontal pipe 342. Multiple jet nozzles 344 are connected to the top of each set of inlet branch pipes 343. The gas distributor 34 also includes a primary flow splitting component 345 and a secondary flow splitting component 346. The primary flow splitting component 345 is located above the jet nozzles 344, and the secondary flow splitting component 346 is located above the primary flow splitting component 345.

[0232] The primary diversion assembly 345 includes multiple inverted conical first diverters 3451. The number of first diverters 3451 is equal to the number of nozzles 344, and the multiple first diverters 3451 are located directly above the multiple nozzles 344. Adjacent first diverters 3451 are connected by a first connecting rod 3452. A first fixing ring 3453 is connected to the inner wall of the sodium hypochlorite reactor 500. The first diverter 3451 near the first fixing ring 3453 is connected to the first fixing ring 3453 through the first connecting rod 3452.

[0233] The secondary diversion assembly 346 includes multiple liquid storage boxes 3461, the number of which is equal to the number of multiple first diverters 3451, and the multiple liquid storage boxes 3461 are respectively located directly above the multiple first diverters 3451. A water leakage hole 3462 is provided at the bottom of the liquid storage box 3461. Multiple second diverters 3464 are connected in a ring shape to the top of the liquid storage box 3461 by a support rod 3463. Adjacent liquid storage boxes 3461 are connected by a second connecting rod 3465. A second fixing ring 3466 is slidably connected to the inner wall of the sodium hypochlorite reactor 500. The liquid storage box 3461 close to the second fixing ring 3466 is connected to the second fixing ring 3466 by the second connecting rod 3465.

[0234] Among them, the distance between the bottom end of the multiple second diverters 3464 on the reservoir 3461 and the center line of the reservoir 3461 is greater than the top surface radius of the first diverter 3451 located directly below the reservoir 3461.

[0235] The atomization status detection component 307 includes multiple sealed boxes 3071 connected in a ring to the inner wall of the sodium hypochlorite reactor 500. Each sealed box 3071 is equipped with a tension sensor 3072. The tension sensor 3072 is equipped with a straight rod 3073. The bottom end of the straight rod 3073 passes through the bottom wall of the sealed box 3071 and is connected to a connecting plate 3074. The connecting plate 3074 is equipped with a pull rod 3075. The bottom end of the pull rod 3075 is connected to a second fixing ring 3466. The tension sensor 3072 is connected to the drive motor 305 by wired or wireless means.

[0236] The working principle of this invention is as follows:

[0237] After being powered on, chlorine gas is injected upward into the sodium hypochlorite reactor 500 through the air inlet pipe 341, the horizontal air inlet pipe 342, the air inlet branch pipe 343 and the nozzle 344. Then, the chlorine gas is initially dispersed by the first distributor 3451 directly above the nozzle 344. The initially dispersed chlorine gas continues to flow upward and collides with multiple second distributors 3464, where it is dispersed again. At this point, the chlorine gas is fully and evenly distributed inside the sodium hypochlorite reactor 500.

[0238] Simultaneously, sodium hydroxide solution is atomized and sprayed into the lower part of hypochlorous acid reactor 500 through inlet pipe 3001, inlet horizontal pipe 3002, inlet branch pipe 303 and atomizing nozzle 304 until it reacts with the thoroughly dispersed and uniformly distributed chlorine gas at the interface and generates a mixed liquid.

[0239] As the atomizing nozzle 304 operates for an extended period, it will be corroded and damaged by the sodium hydroxide solution. This results in a decreased atomization effect, making it difficult for the sodium hydroxide solution to be evenly distributed within the sodium hypochlorite reactor 500. Consequently, the downward-sprayed sodium hydroxide solution becomes more concentrated, leading to an increase in the amount of sodium hydroxide solution falling into the storage box 3461 within the same timeframe. When the rate of sodium hydroxide solution entering the storage box 3461 exceeds the rate of sodium hydroxide solution exiting through the drain hole 3462, the amount of sodium hydroxide solution in the storage box 3461 will continue to increase. This increases the tension on the pull rod 3075 and the tension sensor 3072. When the tension reaches the set value, the drive motor 305 is started, which drives the air intake horizontal pipe 342 to rotate 180 degrees through the turntable 306 and the liquid inlet pipe 3001. This puts the brand-new atomizing nozzle 304, which was originally located on the upper side, into operation, while the damaged atomizing nozzle 304 rotates to the upper side and closes the solenoid valve on it to stop working. In this way, the replacement and maintenance cycle of the atomizing nozzle 304 can be extended without affecting the atomization spray effect, which effectively improves the practicality and reliability of the spray tower atomizer 30.

[0240] The foregoing has shown and described the basic principles, main features, and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments. The embodiments and descriptions in the specification are merely illustrative of the principles of the invention. Various changes and modifications can be made to the invention without departing from its spirit and scope, and all such changes and modifications fall within the scope of the claimed invention.

Claims

1. An apparatus for the continuous preparation of high-purity sodium hypochlorite, characterized in that: The system includes a first reactor (100), with a first inlet pipe connected to the inlet of the first reactor (100), and a first delivery pump (101) installed on the first inlet pipe; a first back pressure valve (102) is installed on the first inlet pipe between the first delivery pump (101) and the first reactor (100); a first jacketed heat exchanger (107) is fitted onto the outer circumference of the first reactor (100), and the first jacketed heat exchanger (107) is provided with a first jacketed heat exchanger inlet (106) and a first jacketed heat exchanger outlet (108); the first jacketed heat exchanger inlet (106) is connected to the drain outlet of the first reactor (100) through a pipe, and the first jacketed heat exchanger inlet (106) is connected to cooling water through a pipe; a second back pressure valve (104) is installed on the pipe between the cooling water and the first jacketed heat exchanger inlet (106). It also includes a second reactor (200), the inlet of which is connected to the outlet of the first reactor (100) via a pipeline. A second transfer pump (201) and a third back pressure valve (202) are sequentially installed along the liquid flow direction on the pipeline between the outlet of the first reactor (100) and the inlet of the second reactor (200). A second water inlet pipeline is connected to the inlet of the second reactor (200), and a third transfer pump (203) is installed on the second water inlet pipeline. A fifth back pressure valve (2010) is installed on the pipeline between the third transfer pump (203) and the second reactor (200). A second jacketed heat exchanger (207) is fitted onto the outer circumference of the second reactor (200), and the second jacketed heat exchanger (207) is equipped with… The second jacketed heat exchanger inlet (206) and the second jacketed heat exchanger outlet (208) are connected to the drain outlet of the second reactor (200) via a pipeline. The second jacketed heat exchanger inlet (206) is connected to the cooling water via a pipeline. A fourth back pressure valve (204) is provided on the pipeline between the cooling water and the second jacketed heat exchanger inlet (206). The drain outlet of the second reactor (200) is connected to a heat exchanger (300) via a pipeline. A fourth delivery pump (301) and a sixth back pressure valve (302) are provided on the pipeline between the heat exchanger (300) and the drain outlet of the second reactor (200). The sixth back pressure valve (302) is closer to the heat exchanger (300) than the fourth delivery pump (301). The drain port of the heat exchanger (300) is connected to a static mixer (400) via a pipeline. A fifth delivery pump (401) and a seventh back pressure valve (402) are provided on the pipeline between the static mixer (400) and the heat exchanger (300). The seventh back pressure valve (402) is closer to the static mixer (400) than the fifth delivery pump (401). The drain port of the static mixer (400) is connected to the sodium hypochlorite reactor (500) via a pipeline. A sixth delivery pump (403) and a sodium hydroxide dilute solution back pressure valve (404) are provided on the pipeline between the sodium hypochlorite reactor (500) and the static mixer (400). The sodium hydroxide dilute solution back pressure valve (404) is closer to the sodium hypochlorite reactor (500) than the sixth delivery pump (403). A jet tower atomizer (30) is provided at the top of the sodium hypochlorite reactor (500). A gas distributor (34) is provided at the bottom of the sodium hypochlorite reactor (500). The gas distributor (34) has an inlet connected to a gas buffer tank (600) via a pipeline. A chlorine valve (601) is provided on the pipeline between the gas buffer tank (600) and the gas distributor (34). The gas buffer tank (600) has an inlet connected to a chlorine inlet via a pipeline. A seventh delivery pump (602) is provided on the pipeline between the chlorine inlet and the gas buffer tank (600). The bottom of the sodium hypochlorite reactor (500) is connected to an inert gas inlet via a pipeline. An eighth delivery pump (502) and a chlorine valve (601) are provided on the pipeline between the inert gas inlet and the sodium hypochlorite reactor (500). The chlorine valve (601) is closer to the sodium hypochlorite reactor (500) than the eighth delivery pump (502). The sodium hypochlorite reactor (500) is fitted with a third jacketed heat exchanger (505) on its outer periphery. The third jacketed heat exchanger (505) is provided with a third jacketed heat exchanger inlet (506) and a third jacketed heat exchanger outlet (507). The third jacketed heat exchanger inlet (506) is connected to a cooling water interface through a pipeline. A cooling water valve (508) is provided on the pipeline between the cooling water interface and the third jacketed heat exchanger inlet (506). The outlet of the sodium hypochlorite reactor (500) is connected to a finished product tank (700) via a pipeline. A ninth transfer pump (703) and an eighth back pressure valve (702) are installed on the pipeline between the finished product tank (700) and the sodium hypochlorite reactor (500). The eighth back pressure valve (702) is closer to the sodium hypochlorite reactor (500) than the ninth transfer pump (703). The gas distributor (34) includes an inlet pipe (341), the inlet end of which is connected to a gas buffer tank (600) via a pipeline, and the outlet end of which is connected to an inlet horizontal pipe (342). The inlet horizontal pipe (342) is located inside the sodium hypochlorite reactor (500). Multiple inlet branch pipes (343) are provided on the outer circumferential surface of the inlet horizontal pipe (342), and multiple jet nozzles (344) are connected to the top of each inlet branch pipe (343). It also includes a primary flow splitter assembly (345), which is located above the jet nozzle (344), and a secondary flow splitter assembly (346) is provided above the primary flow splitter assembly (345). The primary diversion assembly (345) includes a plurality of inverted conical first diverters (3451), each first diverter (3451) corresponding to a nozzle (344), the first diverter (3451) being located above the corresponding nozzle (344), adjacent first diverters (3451) being connected by a first connecting rod (3452), a first fixing ring (3453) being connected to the inner wall of the sodium hypochlorite reactor (500), and the first diverter (3451) near the first fixing ring (3453) being connected to the first fixing ring (3453) by the first connecting rod (3452); The secondary diversion assembly (346) includes multiple liquid storage boxes (3461). The liquid storage boxes (3461) are located above the first diverter (3451). The bottom of the liquid storage box (3461) is provided with a water leakage hole (3462). The top of the liquid storage box (3461) is connected to multiple second diverters (3464) through a support rod (3463). Adjacent liquid storage boxes (3461) are connected through a second connecting rod (3465). A second fixing ring (3466) is slidably connected to the inner wall of the sodium hypochlorite reactor (500). The liquid storage box (3461) close to the second fixing ring (3466) is connected to the second fixing ring (3466) through the second connecting rod (3465).

2. The apparatus for continuous preparation of high-purity sodium hypochlorite according to claim 1, characterized in that: The first reactor (100) is equipped with a first densitometer (103), which is online interlocked with the first back pressure valve (102); a first online thermometer (105) is installed on the pipeline between the drain outlet of the first reactor (100) and the inlet (106) of the first jacketed heat exchanger; the second reactor (200) is equipped with a second densitometer (205), which is online interlocked with the fifth back pressure valve (2010); a second online thermometer (209) is installed on the pipeline between the drain outlet of the second reactor (200) and the inlet (206) of the second jacketed heat exchanger.

3. The apparatus for continuous preparation of high-purity sodium hypochlorite according to claim 1, characterized in that: A pH meter (501) is connected to the sodium hypochlorite reactor (500); a pressure gauge (504) is connected to the bottom of the sodium hypochlorite reactor (500), and the pressure gauge (504) is online interlocked with the inert gas valve (503); a third online thermometer (509) is connected to the drain outlet of the sodium hypochlorite reactor (500), and the third online thermometer (509) is online interlocked with the cooling water valve (508); an oxidation-reduction potential analyzer (701) is installed on the pipeline between the eighth back pressure valve (702) and the sodium hypochlorite reactor (500), and the oxidation-reduction potential analyzer (701) is online interlocked with the chlorine valve (601).

4. The apparatus for continuous preparation of high-purity sodium hypochlorite according to claim 1, characterized in that: The jet tower atomizer (30) includes an inlet pipe (3001), the inlet end of which is connected to a static mixer (400) via a pipeline, and the outlet end of which is rotatably connected to an inlet horizontal pipe (3002). Multiple inlet branch pipes (303) are provided on the outer circumferential surface of the inlet horizontal pipe (3002). Multiple atomizing nozzles (304) are provided at the top and bottom of the inlet branch pipes (303), and a solenoid valve is provided on the atomizing nozzles (304).

5. The apparatus for continuous preparation of high-purity sodium hypochlorite according to claim 4, characterized in that: It also includes a drive motor (305), which is disposed on the outer wall of the sodium hypochlorite reactor (500). The drive end of the drive motor (305) is provided with a turntable (306), which is located inside the sodium hypochlorite reactor (500). The turntable (306) is connected to one end of the liquid inlet horizontal pipe (3002).

6. The apparatus for continuous preparation of high-purity sodium hypochlorite according to claim 1, characterized in that: It also includes an atomization state detection component (307); the atomization state detection component (307) includes multiple sealed boxes (3071), the sealed boxes (3071) are set on the inner wall of the sodium hypochlorite reactor (500), the sealed boxes (3071) are provided with a tension sensor (3072), the tension sensor (3072) is provided with a straight rod (3073), the bottom end of the straight rod (3073) penetrates the bottom wall of the sealed box (3071) and is connected to a connecting plate (3074), the connecting plate (3074) is provided with a pull rod (3075), the bottom end of the pull rod (3075) is connected to a second fixing ring (3466), and the tension sensor (3072) is connected to a drive motor (305) by wire or wireless means.

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