Regeneration wastewater recovery system for ion exchange water production

Abstract

The utility model relates to the technical field of wastewater retreatment, and provides an ion exchange water production regeneration wastewater recovery system. The ion exchange water-making regenerated wastewater recovery system comprises an ion exchange water-making regenerated wastewater pretreatment device, a salt separation device and a resource utilization device. The ion exchange water-making regenerated wastewater pretreatment device is used for removing impurities in regenerated wastewater; the salt separation device is communicated with the ion exchange water production regeneration wastewater pretreatment device and is used for carrying out nanofiltration separation on the regeneration wastewater to obtain a monovalent salt solution and a divalent salt solution and treating sulfate ions in the divalent salt solution; and the resource utilization device is communicated with the salt separation device and is used for preparing acid and alkali from the monovalent salt solution. The utility model overcomes the defect of low resource utilization rate in the ion exchange water-making regeneration wastewater in the prior art, realizes the ion exchange water-making regeneration wastewater recovery system, and can be used for recovering the ion exchange water-making regeneration wastewater in a resource manner to prepare acid and alkali.

Description

Technical Field

[0001] This utility model relates to the field of wastewater reprocessing technology, and in particular to an ion exchange water regeneration wastewater recovery system. Background Technology

[0002] Ion exchange water production technology is one of the current methods for industrial production of demineralized water. Its water production principle is to use resin ion exchange to adsorb other anions and cations in the water. After the adsorption is saturated, acid and alkali are used for desorption and regeneration. The pure water production rate of ion exchange is over 95%.

[0003] The wastewater from ion exchange water regeneration is highly complex and requires treatment before discharge. Current methods involve using the regenerated wastewater to treat blast furnace slag and power plant fly ash, which can then be utilized in concrete production.

[0004] However, the high chloride ion content in the wastewater from ion exchange water regeneration affects the quality of the slag used in lime production. Considering overall economic benefits, it is necessary to design an ion exchange water regeneration wastewater recovery system to recover the wastewater and produce acids and alkalis. Utility Model Content

[0005] This utility model provides an ion exchange water regeneration wastewater recovery system to solve the problem of low resource utilization rate in ion exchange water regeneration wastewater in the prior art. It realizes an ion exchange water regeneration wastewater recovery system that can recover ion exchange water regeneration wastewater to produce acid and alkali.

[0006] This utility model provides an ion exchange water regeneration wastewater recovery system, comprising:

[0007] Ion exchange water regeneration wastewater pretreatment device is used to remove impurities from regeneration wastewater;

[0008] The salt separation device is connected to the ion exchange water regeneration wastewater pretreatment device, and is used to perform nanofiltration to separate monovalent salt solution and divalent salt solution from the regeneration wastewater, and to treat sulfate ions in the divalent salt solution.

[0009] A resource utilization device, connected to the salt separation device, is used to produce acid and alkali from the monovalent salt solution.

[0010] According to the ion exchange water regeneration wastewater recovery system provided by this utility model, the salt separation device includes:

[0011] The nanofiltration unit is connected to the ion exchange water production and regeneration wastewater pretreatment device and is used to separate monovalent salt solution and divalent salt solution from the regeneration wastewater by nanofiltration.

[0012] A room-temperature crystallization reaction assembly, connected to the nanofiltration assembly, is used to treat sulfate ions in the divalent salt solution;

[0013] The SRB component, connected to the room temperature crystallization reaction component, is used to further process sulfate ions in the divalent salt solution.

[0014] According to the present invention, an ion exchange water treatment and regeneration wastewater recovery system is provided, wherein the nanofiltration component includes:

[0015] The first nanofiltration component has a first inlet water pipe, a first product water pipe and a first concentrate water pipe that are interconnected, and the first inlet water pipe is connected to the ion exchange water production and regeneration wastewater pretreatment device.

[0016] The second nanofiltration unit has a second inlet pipe, a second product water pipe, and a second concentrate pipe that are interconnected, with the second inlet pipe connected to the first product water pipe; the second nanofiltration unit is used to separate the monovalent salt solution, and the monovalent salt solution flows out through the second product water pipe.

[0017] The third nanofiltration unit has a third inlet water pipe, a third product water pipe, and a third concentrate water pipe that are interconnected. The first concentrate water pipe and the second concentrate water pipe are both connected to the third inlet water pipe, and the third concentrate water pipe is connected to the first product water pipe. The third nanofiltration unit is used to separate the divalent salt solution. The divalent salt solution flows out through the third product water pipe, which is connected to the room temperature crystallization reaction component.

[0018] A booster pump, located in the third inlet pipe, drives the regenerated wastewater to circulate.

[0019] According to the ion exchange water treatment and regeneration wastewater recovery system provided by this utility model, the resource utilization device includes:

[0020] The first reverse osmosis component is connected to the second product water pipeline and is used to concentrate the monovalent salt solution to a first concentration.

[0021] An ultrafiltration membrane module, connected to the first reverse osmosis module, is used to filter the monovalent salt solution;

[0022] The second reverse osmosis component is connected to the ultrafiltration membrane component and is used to concentrate the monovalent salt solution to a second concentration.

[0023] A bipolar membrane electrodialysis unit, connected to the second reverse osmosis unit, is used to treat the monovalent salt solution of the second concentration and produce sodium hydroxide and hydrochloric acid.

[0024] According to the ion exchange water production and regeneration wastewater recovery system provided by this utility model, the salt separation device further includes a product water pump, a heat exchanger, a security filter and a nanofiltration circulation pump arranged in sequence.

[0025] The water pump is connected to the ion exchange water production and regeneration wastewater pretreatment device, and the nanofiltration circulating pump is connected to the first inlet pipe.

[0026] The third water production pipeline is connected to the divalent saline tank, and the second water production pipeline is connected to the monovalent saline tank.

[0027] According to the ion exchange water production and regeneration wastewater recycling system provided by this utility model, the first reverse osmosis component is connected to the single-valent brine tank, and a first water supply pump, a first filter and a second water supply pump are sequentially connected between the first reverse osmosis component and the single-valent brine tank.

[0028] According to the present invention, an ion exchange water production and regeneration wastewater recovery system is provided, wherein a concentrate tank and a third water supply pump are sequentially connected between the first reverse osmosis component and the ultrafiltration membrane component, and a first circulation pipe is provided between the ultrafiltration membrane component and the concentrate tank.

[0029] According to the present invention, an ion exchange water production and regeneration wastewater recovery system is provided, wherein an ultrafiltration membrane module and a second reverse osmosis module are sequentially connected to an ultrafiltration product water tank, a fourth water supply pump, a second filter, and a fifth water supply pump.

[0030] According to the ion exchange water production and regeneration wastewater recycling system provided by this utility model, a reverse osmosis water tank, a sixth water supply pump and a circulating water supply pump are sequentially connected between the second reverse osmosis component and the bipolar membrane electrodialysis component, and a second circulation pipeline is also provided between the circulating water supply pump and the bipolar membrane electrodialysis component.

[0031] The ion exchange water treatment and regeneration wastewater recovery system provided by this invention achieves effective removal of impurities, separation of salts, and reuse of resources in the regeneration wastewater through an ion exchange water treatment and regeneration wastewater pretreatment device, a salt separation device, and a resource utilization device. This invention solves the problems of incomplete impurity removal, difficulty in effectively separating mixed salts, and resource waste that exist in traditional regeneration wastewater treatment processes. Attached Figure Description

[0032] To more clearly illustrate the technical solutions in this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of this utility model. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0033] Figure 1 This is a schematic diagram of the ion exchange water treatment and wastewater recycling system provided by this utility model.

[0034] Figure 2 This is a schematic diagram of the nanofiltration component of the ion exchange water treatment and wastewater recycling system provided by this utility model.

[0035] Figure 3 This is a schematic diagram of the working principle of the ion exchange water regeneration wastewater pretreatment device in the ion exchange water regeneration wastewater recovery system provided by this utility model.

[0036] Figure 4 This is a schematic diagram of the working principle of the salt separation device in the ion exchange water regeneration wastewater recovery system provided by this utility model.

[0037] Figure 5 This is a schematic diagram of the working principle of the resource utilization device of the ion exchange water regeneration wastewater recovery system provided by this utility model.

[0038] Figure 6 This is a cross-sectional view of the sedimentation tank in the ion exchange water treatment and regeneration wastewater recovery system provided by this utility model.

[0039] Figure 7 This is a top view of the sedimentation tank of the ion exchange water regeneration wastewater recovery system provided by this utility model.

[0040] Figure 8 This is a cross-sectional view of the ion exchange component of the ion exchange water treatment and wastewater recycling system provided by this utility model.

[0041] Figure 9 This is a schematic diagram of the strong oxidizer structure of the ion exchange water treatment and wastewater recycling system provided by this utility model.

[0042] Figure 10 This is a schematic diagram of the structure of the tubular reactor in the ion exchange water treatment and wastewater recycling system provided by this utility model.

[0043] Reference numerals: 100: Ion exchange water treatment and regeneration wastewater pretreatment device; 200: Salt separation device; 300: Resource utilization device; 210: Nanofiltration module; 220: Room temperature crystallization reaction module; 230: SRB module; 310: First reverse osmosis module; 320: Ultrafiltration membrane module; 330: Second reverse osmosis module; 340: Bipolar membrane electrodialysis module; 211: First nanofiltration component; 212: Second nanofiltration component; 213: Third nanofiltration component; 214: Booster pump;

[0044] 110: Wastewater equalization tank; 120: Ambient temperature crystallization reactor; 130: Sedimentation tank; 140: Precision filter; 150: Self-cleaning filter; 160: Ultrafiltration module; 170: Ion exchange module; 180: Strong oxidizer; 190: Ultrafiltration product water tank;

[0045] 131: Sedimentation shell; 1311: Shell body; 1312: First inlet pipe; 1313: Water distribution trough; 1314: Toothed weir; 1315: Sludge discharge pipe; 132: Sedimentation component; 1321: Support plate; 1322: Inclined pipe; 1323: Internal water collection trough; 1324: Support platform; 133: Cleaning component; 1331: Motor; 1332: Rotating rod; 1333: Scraper; 134: External water receiving trough; 135: First product water pipe;

[0046] 1711: Exchange shell; 1712: First filter plate; 1713: Second filter plate; 1714: Third filter plate; 1721: First cavity; 1722: Second cavity; 1723: Third cavity; 1724: Fourth cavity; 1731: First single-sided filter cap; 1732: Double-sided filter cap; 1733: Second single-sided filter cap; 174: Second inlet pipe; 175: Baffle; 176: Perforated plate; 177: Second product water pipe; 1781: Weak acid cation exchange resin layer; 1782: White ball resin pressing layer; 1783: Chelating resin layer;

[0047] 181: Tubular reactor; 1811: Inlet pipe; 1812: Packed reaction tube; 1813: Chemical dosing pipe; 1814: Arc-shaped connecting pipe; 182: Oxidation water tank; 1821: Water supply unit; 1822: Ozone generator; 1823: Pipeline ejector; 1824: Circulating water pump; 183: Oxygen release tank; 1831: Nitrogen explosion unit; 1832: Booster pump; 1833: Tail gas absorber; 184: Ejector; 185: Hydrogen peroxide dosing unit. Detailed Implementation

[0048] The embodiments of this utility model will be described in further detail below with reference to the accompanying drawings and examples. The following examples are for illustrative purposes only and should not be construed as limiting the scope of this utility model.

[0049] In the description of the embodiments of this utility model, it should be noted that the terms "center," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing the embodiments of this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on the embodiments of this utility model. In addition, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0050] In the description of the embodiments of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "connected" and "linked" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium. Those skilled in the art can understand the specific meaning of the above terms in the embodiments of this utility model based on the specific circumstances.

[0051] In this embodiment of the utility model, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "on top of," and "over" the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0052] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0053] The following is combined Figures 1-10 Describe the structure and working principle of this utility model.

[0054] Reference Figure 1 This utility model provides an ion exchange water regeneration wastewater recovery system, comprising an ion exchange water regeneration wastewater pretreatment device 100, a salt separation device 200, and a resource utilization device 300. The ion exchange water regeneration wastewater pretreatment device 100 is used to remove impurities from the regeneration wastewater; the salt separation device 200, connected to the ion exchange water regeneration wastewater pretreatment device 100, is used to perform nanofiltration to separate monovalent salt solutions and divalent salt solutions from the regeneration wastewater, and to treat sulfate ions in the divalent salt solutions; the resource utilization device 300, connected to the salt separation device 200, is used to produce acids and bases from the monovalent salt solutions.

[0055] This invention, through its three core components—an ion exchange water treatment and regeneration wastewater pretreatment device 100, a salt separation device 200, and a resource utilization device 300—achieves effective removal of impurities, separation of salts, and reuse of resources in regeneration wastewater. This invention solves the problems of incomplete impurity removal, difficulty in effectively separating mixed salts, and resource waste that exist in traditional regeneration wastewater treatment processes.

[0056] Specifically, firstly, the ion exchange water regeneration wastewater pretreatment unit 100 is responsible for removing most of the impurities from the regeneration wastewater. This unit includes multiple treatment units, such as an ambient temperature crystallization reactor, a sedimentation tank, and filter components, ensuring that the wastewater entering subsequent treatment steps has undergone preliminary purification. After pretreatment, the impurity content in the regeneration wastewater is significantly reduced, providing excellent influent conditions for subsequent nanofiltration separation.

[0057] Next, the salt separation device 200 is connected to the ion exchange water regeneration wastewater pretreatment device 100 for nanofiltration separation of the pretreated regeneration wastewater. In this process, the salt separation device 200 can separate the wastewater into monovalent salt solutions and divalent salt solutions, and specifically treats sulfate ions in the divalent salt solutions. This separation method not only improves the purity of the salts but also simplifies subsequent treatment processes, allowing different types of salts to be treated or recovered more effectively.

[0058] Finally, the resource utilization unit 300 processes the monovalent salt solution separated by the salt separation unit 200. This unit converts the monovalent salt solution into acids and bases through a series of chemical treatment processes. This step not only achieves resource recycling and reduces waste emissions but also creates valuable chemicals, improving the overall economic efficiency of the system.

[0059] In the above structure, the close collaboration between the components solves several key problems in the treatment of regenerated wastewater. The ion exchange water treatment and regeneration wastewater pretreatment unit 100 ensures that the wastewater is fully purified before entering the salt separation unit 200, avoiding the impact of impurities on the nanofiltration membrane. The salt separation unit 200 achieves effective separation of salts through precise nanofiltration separation technology, especially the treatment of sulfate ions, laying the foundation for subsequent resource utilization. The resource utilization unit 300 further converts the separated monovalent salt solution into acids and bases, maximizing resource utilization.

[0060] Reference Figure 1 In some embodiments of this utility model, the salt separation device 200 includes a nanofiltration component 210, a room temperature crystallization reaction component 220, and an SRB (Sulfate-Reducing Bacteria) component 230. The nanofiltration component 210 is connected to the ion exchange water treatment and regeneration wastewater pretreatment device 100, and is used to separate monovalent salt solutions and divalent salt solutions from the regeneration wastewater through nanofiltration.

[0061] The room temperature crystallization reaction component 220 is connected to the nanofiltration component 210 and is used to treat sulfate ions in divalent salt solutions. Calcium oxide slurry is added to the room temperature crystallization reaction component 220, and the sulfate ions are removed by reacting calcium ions and sulfate ions to form calcium sulfate precipitate. Due to the principle of co-dissolution of calcium sulfate and sodium chloride, the solubility of calcium sulfate deviates. The co-crystallization principle of the room temperature crystallizer is adopted to promote the precipitation and growth of calcium sulfate crystals.

[0062] SRB component 230 is connected to room temperature crystallization reaction component 220 for further treatment of sulfate ions in divalent salt solution. SRB component 230 utilizes sulfate-reducing bacteria to further digest and remove sulfate ions. Sulfate-reducing bacteria are strictly anaerobic heterotrophic organisms, requiring the isolation of oxygen and the addition of organic matter during the treatment process. SRB component 230 includes a baffle-type anaerobic reactor and a flocculation sedimentation tank. A certain concentration of polyacrylamide is added at the inlet of the anaerobic reactor. Polyacrylamide provides carbon and nitrogen sources for the bacteria, while the remaining portion participates in the flocculation sedimentation reaction, resulting in low residual levels.

[0063] In this embodiment, the salt separation device 200 is designed to ensure the efficient separation of different types of salts and the effective treatment of specific ions such as sulfate ions by precisely separating and treating the reclaimed wastewater. The device includes a nanofiltration component 210, a room-temperature crystallization reaction component 220, and a sulfate-reducing bacteria reaction component. These three components are connected sequentially to form a continuous and efficient treatment process.

[0064] First, the nanofiltration module 210 is connected to the ion exchange water treatment and regeneration wastewater pretreatment device 100, receiving the pre-purified regeneration wastewater. The nanofiltration module 210 uses nanofiltration membrane technology to separate the regeneration wastewater into monovalent salt solutions and divalent salt solutions. Through the nanofiltration module 210, monovalent and divalent salts in the regeneration wastewater can be initially distinguished, solving the problem of ineffective separation in traditional treatment methods. This separation not only improves the purity of the salts but also provides conditions for subsequent treatment of different salts.

[0065] Next, the separated divalent salt solution flows into the ambient temperature crystallization reactor 220. The ambient temperature crystallization reactor 220 is specifically designed to treat sulfate ions in the divalent salt solution. At this stage, by adding appropriate chemical reagents or altering the solution conditions, sulfate ions are encouraged to crystallize and precipitate from the solution. This process not only reduces the sulfate ion content in the solution but also generates recyclable solid products, achieving preliminary resource reuse.

[0066] Subsequently, the divalent salt solution, after being treated by the ambient temperature crystallization reaction unit 220, enters the sulfate-reducing bacteria reaction unit. The sulfate-reducing bacteria reaction unit further treats the sulfate ions in the divalent salt solution. Under the action of sulfate-reducing bacteria, sulfate ions are reduced to sulfides, thereby significantly reducing the sulfate concentration in the solution. This biological treatment method is not only environmentally friendly but also removes residual sulfate ions more thoroughly, improving the purity and quality of the final product. Furthermore, the sulfate-reducing bacteria reaction unit can also produce byproducts such as hydrogen sulfide, which can be further processed or utilized in subsequent processes.

[0067] Reference Figure 2 In some embodiments of this utility model, the nanofiltration assembly 210 includes a first nanofiltration component 211, a second nanofiltration component 212, a third nanofiltration component 213, and a pressure pump 214.

[0068] The first nanofiltration component 211 has a first inlet pipe, a first product water pipe and a first concentrate water pipe that are interconnected, and the first inlet pipe is connected to the ion exchange water production and regeneration wastewater pretreatment device 100; the second nanofiltration component 212 has a second inlet pipe, a second product water pipe and a second concentrate water pipe that are interconnected, and the second inlet pipe is connected to the first product water pipe.

[0069] The second nanofiltration unit 212 is used to separate monovalent salt solutions, which flow out through the second product water pipe; the third nanofiltration unit 213 has a third inlet water pipe, a third product water pipe and a third concentrate water pipe that are interconnected, the first concentrate water pipe and the second concentrate water pipe are both connected to the third inlet water pipe, and the third concentrate water pipe is connected to the first product water pipe.

[0070] The third nanofiltration unit 213 is used to separate divalent salt solutions, which flow out through the third product water pipe and are connected to the room temperature crystallization reaction component 220. The pressure pump 214 is located in the third inlet water pipe to drive the circulation of the regenerated wastewater.

[0071] In this embodiment, the nanofiltration component 210 is designed to ensure that different types of salts can be efficiently distinguished and treated through multi-stage nanofiltration separation of reclaimed wastewater. Specifically, when the pretreated reclaimed wastewater enters the first nanofiltration component 211, some monovalent salt solutions and divalent salt solutions are initially separated by nanofiltration membrane technology. The separated solutions flow out from the first product water pipe and the first concentrate pipe, respectively, providing a basis for subsequent treatment.

[0072] Next, the second nanofiltration unit 212 receives the fluid from the first product water pipe and further separates a purer monovalent salt solution. The monovalent salt solution flows out through the second product water pipe, achieving efficient separation of the monovalent salt solution. Meanwhile, the remaining concentrate flows to the next processing unit through the second concentrate pipe.

[0073] Subsequently, the third nanofiltration unit 213 is responsible for processing the mixed solution flowing in from the first and second concentrate pipes. In the third nanofiltration unit 213, the divalent salt solution is further separated by nanofiltration membrane technology. The divalent salt solution flows out through the third product water pipe and is directly connected to the ambient temperature crystallization reaction unit 220 for subsequent sulfate ion treatment.

[0074] To maintain the stable operation of the entire system, a booster pump 214 is installed in the third inlet pipe to drive the circulation of the regenerated wastewater. The booster pump 214 not only ensures the continuity of water flow and pressure stability, but also promotes effective connection between the various nanofiltration components, ensuring the smooth progress of each treatment step.

[0075] Overall, the nanofiltration module 210 optimizes the treatment process of reclaimed wastewater, improves salt separation efficiency and resource utilization, and meets the requirements of modern environmental protection and resource recycling. This system not only solves the problems of impurity removal and salt separation in reclaimed wastewater treatment, but also achieves more thorough and efficient salt treatment through multi-stage nanofiltration separation technology. The nanofiltration module 210 features high water recovery rate and high chloride and sulfate ion rejection rates. The chloride and sulfate ion rejection rates are 99.7% and -13.7%, respectively, with an average water recovery rate of 81.9%. During continuous operation, the water recovery rate and operating pressure fluctuations are small, indicating high system stability.

[0076] Reference Figure 1In some embodiments of this utility model, the resource utilization device 300 includes a first reverse osmosis component 310, an ultrafiltration membrane component 320, a second reverse osmosis component 330, and a bipolar membrane electrodialysis component 340. The first reverse osmosis component 310 is connected to a second product water pipeline and is used to concentrate the monovalent salt solution to a first concentration, which is greater than 65%. The ultrafiltration membrane component 320 is connected to the first reverse osmosis component 310 and is used to filter the monovalent salt solution. The second reverse osmosis component 330 is connected to the ultrafiltration membrane component 320 and is used to concentrate the monovalent salt solution to a second concentration, which is greater than 60%. The bipolar membrane electrodialysis component 340 is connected to the second reverse osmosis component 330 and is used to treat the monovalent salt solution of the second concentration, producing sodium hydroxide and hydrochloric acid.

[0077] In the above structure, the first reverse osmosis component 310 is connected to the second product water pipe of the nanofiltration component 210, receiving the monovalent salt solution after nanofiltration separation. The first reverse osmosis component 310 concentrates the monovalent salt solution to a first concentration, which is greater than 65%, using reverse osmosis technology. This preliminary concentration process not only increases the salt concentration in the solution but also provides purer feed conditions for subsequent treatment steps.

[0078] Next, the pre-concentrated monovalent salt solution flows into the ultrafiltration membrane module 320. The ultrafiltration membrane module 320 is connected to the first reverse osmosis module 310 and is used for fine filtration of the monovalent salt solution. The ultrafiltration membrane removes any suspended particles and other impurities that may be present in the solution, ensuring that the presence of impurities does not affect efficiency or damage the equipment during subsequent treatment processes.

[0079] Subsequently, the monovalent salt solution filtered by the ultrafiltration membrane module 320 enters the second reverse osmosis module 330. The second reverse osmosis module 330 further concentrates the solution to a second concentration greater than 60%. Through two reverse osmosis concentrations, the concentration of the monovalent salt solution is significantly increased, while ensuring a high degree of purification of the salts in the solution.

[0080] Finally, the concentrated monovalent salt solution enters the bipolar membrane electrodialysis unit 340. The bipolar membrane electrodialysis unit 340 is connected to the second reverse osmosis unit 330 and is specifically designed to treat high-concentration monovalent salt solutions, decomposing them into sodium hydroxide and hydrochloric acid through an electrochemical reaction. This treatment method not only achieves resource reuse but also creates two valuable chemicals, improving the overall economic efficiency of the system.

[0081] Reference Figure 1In some embodiments of this utility model, the salt separation device 200 further includes a product water pump, a heat exchanger, a security filter, and a nanofiltration circulation pump arranged in sequence; the water supply pump is connected to the ultrafiltration product water tank 190, the nanofiltration circulation pump is connected to the first inlet water pipe; the third product water pipe is connected to the divalent saline tank, and the second product water pipe is connected to the monovalent saline tank.

[0082] Before entering the nanofiltration module 210, the wastewater in the ultrafiltration permeate tank 190 undergoes pretreatment sequentially through a permeate pump, a heat exchanger, and a security filter. The permeate pump provides the necessary pressure to ensure smooth flow of wastewater through each treatment unit; the heat exchanger regulates the wastewater temperature to provide suitable operating conditions for the subsequent nanofiltration process; and the security filter removes fine particulate matter and other impurities from the wastewater, protecting the nanofiltration membrane from contamination and damage. It should be noted that a reducing agent needs to be added to the regenerated wastewater before it enters the nanofiltration module 210. The working principles of the regenerated wastewater in the nanofiltration module 210, the ambient temperature crystallization reaction module 220, and the sulfate-reducing bacteria reaction module can be found in the aforementioned embodiments and will not be repeated here.

[0083] Reference Figure 5 In some embodiments of this utility model, the first reverse osmosis component 310 is connected to the monovalent brine tank, and a first water supply pump, a first filter, and a second water supply pump are sequentially connected between the first reverse osmosis component 310 and the monovalent brine tank. Specifically, the first water supply pump can be a low-pressure water supply pump, the first filter can be a 5µm security filter, and the second water supply pump can be a medium-pressure water supply pump.

[0084] Specifically, the first reverse osmosis module 310 can use Dow's anti-fouling high-efficiency membrane elements and is equipped with an online flushing and chemical cleaning system. The high-pressure water supply pump of the online flushing and chemical cleaning system is equipped with a frequency converter. Alternatively, the first reverse osmosis module 310 can have a separate chemical cleaning device, which includes a cleaning water pump and a 5µm security filter. The chemical cleaning system should have a thorough flushing device to prevent cross-contamination of chemicals. The operation of the first reverse osmosis module 310 is controlled by signals from the flow rate and conductivity meters, and the operation is automatically controlled. Conductivity meters, pH meters, residual chlorine meters, ORP meters, pressure gauges, and flow meters can be installed on the inlet pipe of the security filter. Each security filter outlet is equipped with an SDI membrane detection device. The security filter adopts a horizontal high-flow filtration system with a filter element featuring a pleated surface design.

[0085] Reference Figure 5In some embodiments of this utility model, a concentrate tank and a third water supply pump are sequentially connected between the first reverse osmosis component 310 and the ultrafiltration membrane component 320, and a first circulation pipe is provided between the ultrafiltration membrane component 320 and the concentrate tank. An ultrafiltration permeate tank, a fourth water supply pump, a second filter, and a fifth water supply pump are sequentially connected between the ultrafiltration membrane component 320 and the second reverse osmosis component 330. A reverse osmosis water tank, a sixth water supply pump, and a circulating water supply pump are sequentially connected between the second reverse osmosis component 330 and the bipolar membrane electrodialysis component 340, and a second circulation pipe is also provided between the circulating water supply pump and the bipolar membrane electrodialysis component 340.

[0086] Specifically, the bipolar membrane electrodialysis module 340 is composed of a combination of bipolar and monopolar membranes. This technology utilizes bipolar membranes for water dissociation, which is more economical than direct water electrolysis. The combination of bipolar and monopolar membranes not only enables multiple functions but also has wide applications in various fields, especially in the treatment of typical chemical wastewater.

[0087] In the bipolar membrane electrodialysis module 340, under the influence of an electric field, water dissociation occurs in the intermediate layer of the bipolar membrane, generating H+ and OH- ions. This process enables the separation of salts in chemical wastewater and simultaneously converts them into corresponding acids and bases. Specifically, when wastewater containing salts passes through the bipolar membrane, under the influence of the electric field, cations move towards the cathode, and anions move towards the anode. The presence of the bipolar membrane causes water molecules to decompose into hydrogen ions (H+) and hydroxide ions (OH-) in the intermediate layer of the membrane. These ions migrate in opposite directions, thereby achieving effective separation of salts.

[0088] Due to the unique mechanism of the bipolar membrane electrodialysis module 340, it can not only efficiently remove salts from wastewater, but also convert the salts contained in the wastewater into valuable acid and alkali products. For example, sodium chloride can be converted into hydrochloric acid and sodium hydroxide, both of which have wide industrial applications. Therefore, this method not only solves the wastewater treatment problem, but also realizes resource recovery and reuse, improving the economic efficiency and environmental friendliness of the entire treatment process.

[0089] In the resource utilization device 300, a bipolar membrane electrodialysis unit 340 is connected to a second reverse osmosis unit 330, receiving a monovalent salt solution after two rounds of reverse osmosis concentration. This unit further processes the high-concentration monovalent salt solution, decomposing it into sodium hydroxide and hydrochloric acid through an electrochemical reaction. In this way, the previously difficult-to-treat high-concentration salt solution is not only effectively treated but also transformed into a commercially valuable product, further enhancing the overall efficiency of the system.

[0090] The following points should be noted regarding the influent water quality of the 340 bipolar membrane electrodialysis module, as these are essential for ensuring adequate wastewater pretreatment:

[0091] 1. Based on the fundamental principle of bipolar membranes, bipolar membranes are only suitable for monovalent cation salt systems such as Li, Na, K, and ammonium;

[0092] 2. Salt concentration requirement: 1.5N-2.5N concentration is optimal (in terms of concentration equivalents).

[0093] 3. Total amount of divalent and higher cations: <1ppm (the lower the better, technically demanding);

[0094] 4. Total oil and surfactant content <2ppm (the lower the better). For organic solvent types and content, please consult the manufacturer.

[0095] 5. Silicon content < 200 ppm, TSS index < 0.1 ppm.

[0096] Water quality of the effluent from the 340 bipolar membrane electrodialysis module:

[0097] 1. If the influent is a mixture of salts, the effluent will be a mixture of acids or alkalis. For example, if the influent is a mixture of sodium chloride and sodium sulfate wastewater, the resulting alkali will be sodium hydroxide, and the acid will be a mixture of sulfuric acid and hydrochloric acid. The ion ratio will be similar to that of the influent.

[0098] 2. Acid concentration in effluent: adjustable from 0.5N to 3N, with 1N to 2N being the most economical, except for acids with strong oxidizing properties, for which the concentration is limited.

[0099] 3. Effluent alkalinity concentration: adjustable from 0.5N to 3N, with 1N to 2N being the most economical.

[0100] 4. Purity of acid and alkali in effluent: Both acids and alkalis contain a small amount of salt. According to the manufacturer, there is generally about 0-1g / L of salt (which is related to the salt concentration of the influent and the acid and alkali concentration of the effluent).

[0101] The structure and working principle of the ion exchange water regeneration wastewater pretreatment device 100 are described below:

[0102] Reference Figure 1 This utility model provides an ion exchange water regeneration wastewater pretreatment device, comprising a room temperature crystallization reactor 120, a sedimentation tank 130, a filter assembly, an ion exchange assembly 170, and a strong oxidizer 180. The room temperature crystallization reactor 120 is used to crystallize and separate some impurities in the regeneration wastewater; the sedimentation tank 130 is connected to the room temperature crystallization reactor 120 and is used to precipitate and purify the crystallized regeneration wastewater; the filter assembly is connected to the sedimentation tank 130 and is used to filter the purified regeneration wastewater; the ion exchange assembly 170 is connected to the filter assembly and is used to remove calcium and magnesium ions from the regeneration wastewater; the strong oxidizer 180 is connected to the ion exchange assembly 170 and is used to kill microorganisms in the regeneration wastewater.

[0103] Specifically, the reclaimed wastewater enters the ambient temperature crystallization reactor 120. Alkali solution, sodium carbonate, and seed crystals are added to the reactor, ensuring the pH value is >11.5 throughout the reactor. This process generates calcium carbonate, magnesium hydroxide, and metal hydroxide crystals. The ambient temperature crystallization reactor 120 consists of an influent circulation section, a chemical reaction center zone, a slag discharge system, and a sedimentation and clarification section. A special crystal growth mechanism design ensures rapid and complete crystal growth, with sufficient reaction of calcium and magnesium impurities. No flocculant is needed (as this would increase other impurities). The crystals are automatically screened and discharged, completing the treatment process. At this stage, over 97% of calcium and magnesium ions, over 99% of heavy metals, 100% of total silicon, and over 75% of organic and inorganic reducing substances are removed.

[0104] The regenerated wastewater, after being treated in the ambient temperature crystallization reactor 120, flows naturally to the sedimentation tank 130 due to the elevation difference. In the sedimentation tank 130, due to gravity, the heavier crystal particles will settle to the bottom, thus achieving preliminary solid-liquid separation. The wastewater, after sedimentation and purification, continues to flow to the filter assembly, where even finer suspended solids are trapped, further purifying the water quality.

[0105] Next, the treated wastewater flows into ion exchange module 170, which thoroughly removes heavy metal ions such as calcium and magnesium from the wastewater. This step is crucial for subsequent treatment because the presence of heavy metal ions such as calcium and magnesium can affect the final water quality or damage downstream equipment. Finally, a strong oxidizer 180 is connected after the ion exchange module 170. Its function is to inactivate microorganisms in the wastewater through strong oxidation, ensuring the biological safety of the treated water.

[0106] This invention promotes impurity crystallization through a room-temperature crystallization reactor 120, removing over 97% of calcium and magnesium ions, over 99% of heavy metals, 100% of total silicon, and over 75% of organic and inorganic reducing substances. Effective sedimentation is achieved in the sedimentation tank 130, fine filtration is achieved through the filtration components, calcium and magnesium ions are completely removed through the ion exchange components 170, and microorganisms are inactivated through the strong oxidizer 180. The entire process is closely interconnected, with each step preparing for the next. The coordinated work between the components not only solves the problem of excessive impurity ions in the regenerated wastewater but also ensures the effectiveness and economy of the treatment process.

[0107] In some possible embodiments, the present invention further includes a wastewater equalization tank 110 and an ultrafiltration product water tank 190. The wastewater equalization tank 110 is located one stage above the ambient temperature crystallization reactor 120, meaning that the regenerated wastewater first passes through the wastewater equalization tank 110 before entering the ambient temperature crystallization reactor 120. The wastewater equalization tank 110 has a certain function of adjusting the water quantity and quality balance, and is equipped with high and low level gauges, as well as an alkali addition device, a pneumatic stirring device, and a temperature regulating cooling water facility. The cooling water equipment controls the influent water temperature at a low level, which is beneficial to the crystallization mechanism of the ambient temperature crystallizer. The ultrafiltration product water tank 190 is located one stage after the strong oxidizer 180, meaning that the regenerated wastewater treated by the strong oxidizer 180 enters the ultrafiltration product water tank 190 for storage, in order to be processed in the next stage.

[0108] Reference Figure 6 and Figure 7 In some embodiments of this utility model, the sedimentation tank 130 includes a sedimentation shell 131, a sedimentation component 132, a cleaning component 133, an external water receiving tank 134, and a first product water pipe 135. The sedimentation shell 131 has an internal cavity for sedimenting reclaimed wastewater; the sedimentation component 132 has a sedimentation chamber located at the top of the cavity, used to settle impurities at the top of the reclaimed wastewater; the cleaning component 133 is located in the sedimentation shell 131 for cleaning the sediment at the bottom of the cavity; the external water receiving tank 134 is connected to the sedimentation chamber for guiding the settled liquid in the sedimentation chamber; and the first product water pipe 135 is connected to the external water receiving tank 134.

[0109] Specifically, the sedimentation shell 131 forms the basic framework of the sedimentation tank 130, and its interior has a cavity that provides the necessary space for the regenerated wastewater to complete the sedimentation process. To improve sedimentation efficiency, a sedimentation component 132 is located at the top of the cavity and has a sedimentation chamber inside, specifically designed to effectively settle impurities on the top of the regenerated wastewater entering the sedimentation tank 130. When wastewater flows into the sedimentation component 132, lighter impurities gradually settle in the sedimentation chamber, while the clearer water continues to flow downwards into the cavity of the sedimentation shell 131.

[0110] To further enhance the system's automation and maintenance convenience, a cleaning component 133 is installed on the sedimentation shell 131, enabling regular or on-demand cleaning of the sediment accumulated at the bottom of the chamber. This design not only helps maintain the long-term stable operation of the sedimentation tank 130 but also reduces the need for manual intervention, thereby improving overall operational efficiency.

[0111] In the above structure, the external water receiving tank 134 is connected to the sedimentation chamber of the sedimentation component 132. Its main function is to guide the liquid after preliminary sedimentation out of the tank, ensuring smooth water flow while preventing impurities that have not been completely settled from being carried out. The first water production pipe 135 is connected to the external water receiving tank 134 and is responsible for exporting the purified water to the sedimentation tank 130, thereby effectively improving the water quality.

[0112] This invention, through the close cooperation between the components of the sedimentation tank 130, effectively solves the problem of simultaneously and efficiently treating top impurities and bottom sediments in reclaimed wastewater. The design of the sedimentation tank 130 ensures that when reclaimed wastewater flows through this stage, it can not only fully remove top suspended impurities but also promptly clean bottom sediments, thereby providing better influent conditions for subsequent treatment steps.

[0113] Reference Figure 6 and Figure 7 In some embodiments of this utility model, the sedimentation shell 131 includes a shell body 1311, a first inlet pipe 1312, a water distribution trough 1313, a toothed weir 1314, and a sludge discharge pipe 1315. The shell body 1311 can be a cuboid structure with a funnel-shaped bottom to facilitate sediment collection. A cavity is located inside the shell body 1311, and the top of the shell body 1311 has an opening. The toothed weir 1314 is located at the left end of the opening. The water distribution trough 1313 is located outside the toothed weir 1314, and the bottom of the water distribution trough 1313 is lower than the top of the toothed weir 1314. The first inlet pipe 1312 is connected to the side of the water distribution trough 1313 opposite to the toothed weir 1314. The sludge discharge pipe 1315 is used for sediment discharge, connected to the bottom of the shell body 1311, and located at the lowest part of the funnel structure to facilitate sediment discharge.

[0114] Specifically, the water distribution trough 1313 is located outside the toothed weir 1314, with its bottom end lower than the top end of the toothed weir 1314. This height difference allows the regenerated wastewater entering from the first inlet pipe 1312 to be fully dispersed within the water distribution trough 1313, and the toothed weir 1314 can withstand the impact of the regenerated wastewater, eliminating the inlet potential energy and achieving uniform water distribution. This allows the regenerated wastewater to flow into the cavity through the toothed weir 1314 in a relatively gentle manner. This arrangement helps reduce the impact of the inlet water on the cavity, ensuring the stability of the sedimentation process. The first inlet pipe 1312 is connected to the side of the water distribution trough 1313 away from the toothed weir 1314, ensuring that the regenerated wastewater entering the system is first distributed by the water distribution trough 1313, thereby achieving uniform water intake. The sludge discharge pipe 1315 is located at the bottom end of the shell body 1311, used to promptly discharge the sediment settled at the bottom of the cavity, preventing sediment accumulation from affecting treatment efficiency.

[0115] In the above structure, this embodiment solves the problem of effective sedimentation of suspended solids in reclaimed wastewater. The combination of the water distribution trough 1313 and the toothed weir 1314 achieves uniform distribution of the reclaimed wastewater, reduces turbulence, and promotes rapid settling of larger particles. Simultaneously, the presence of the sludge discharge pipe 1315 ensures that sediment does not remain at the bottom of the cavity for extended periods, maintaining the system's continuous and efficient operation. Furthermore, the opening at the top of the shell body 1311 combined with the toothed weir 1314 not only simplifies the structure but also improves the convenience of operation and maintenance, ensuring the smooth progress of the entire sedimentation process.

[0116] Reference Figure 6 and Figure 7 In some embodiments of this utility model, the sedimentation component 132 includes a support plate 1321, a plurality of inclined tubes 1322, at least one internal water collection tank 1323, and at least one support platform 1324. The support plate 1321 is fixedly installed at the end of the opening away from the toothed weir 1314, that is, at the right end of the opening, and the top of the support plate 1321 is flush with the top of the opening. The shape of the support plate 1321 is not specifically limited, as long as the support plate 1321 and the inner wall of the inclined tube 1322 form a cavity, which can serve as a sedimentation chamber. Multiple inclined tubes 1322 are fixedly and inclinedly arranged at the bottom of the sedimentation chamber. The angle between the bottom ends of the inclined tubes 1322 can be 60 degrees, and the bottom ends of the inclined tubes 1322 are connected to the internal cavity of the inclined tubes 1322. The internal water collection tank 1323 is located at the top of the inclined tubes 1322 and is connected to the external water receiving tank 134. The support platform 1324 is fixedly or detachably arranged at the top of the support plate 1321, and its function is to install the cleaning component 133.

[0117] In the above structure, when the regenerated wastewater enters the cavity inside the shell body 1311 through the opening, it undergoes preliminary sedimentation. The liquid at the top enters the sedimentation chamber through the inclined tube 1322. According to the principle of shallow sedimentation, the suspended matter settles on the surface of the inclined tube 1322. When the sediment layer accumulates to a certain thickness, it will fall to the bottom of the cavity inside the shell body 1311 according to its own gravity.

[0118] Inclined tube 1322 is fixedly installed at the bottom of the sedimentation chamber at an angle of 60 degrees between the bottom ends of inclined tube 1322. This design increases the effective sedimentation area, allowing suspended particles in the wastewater to settle more quickly to the bottom of inclined tube 1322 and then be smoothly discharged through the internal cavity of inclined tube 1322. This structure not only improves sedimentation efficiency but also reduces the possibility of the sediment being re-stirred.

[0119] An internal water collection tank 1323 is located at the top of the inclined tube 1322 and is connected to the external water receiving tank 134. This allows the clearer water, after sedimentation treatment, to flow smoothly into the external water receiving tank 134 and further to subsequent treatment units or the discharge system. The support platform 1324 is fixedly or detachably mounted on the top of the support plate 1321, ensuring the stable installation of the cleaning component 133 while also providing flexibility for maintenance and replacement, facilitating cleaning operations as needed by the operators.

[0120] Reference Figure 6 and Figure 7 In some embodiments of this utility model, the cleaning component 133 includes a motor 1331, a rotating rod 1332, and a scraper 1333. The motor 1331 is detachably mounted on the support platform 1324 by means of bolts or other means; the rotating rod 1332 is splinedly connected to the output shaft of the motor 1331, and the bottom end of the rotating rod 1332 extends towards the bottom end of the cavity; the scraper 1333 is mounted on the bottom end of the rotating rod 1332 by welding or bolting, and is used to agitate the sediment at the bottom end of the cavity so that the sediment is discharged through the sludge discharge pipe 1315. It should be noted that the shape of the scraper 1333 is adapted to the bottom end of the shell body 1311, so that the scraper 1333 can rotate normally while uniformly agitating the sediment at the bottom end of the shell body 1311, causing the sediment to gather towards the sludge discharge pipe 1315.

[0121] The cleaning component 133 is designed to ensure effective cleaning of sediment inside the sedimentation shell 131, preventing its accumulation at the bottom of the cavity and thus affecting processing efficiency and long-term operating performance of the equipment. The motor 1331 is mounted on the support platform 1324 by means of bolts or other detachable methods. This installation method ensures the stability of the motor 1331 and facilitates maintenance and replacement.

[0122] The rotating rod 1332 and the output shaft of the motor 1331 are connected by a spline, ensuring reliable power transmission. The bottom end of the rotating rod 1332 extends towards the bottom of the cavity, transmitting the power of the motor 1331 to the bottom of the cavity. The scraper 1333 is installed at the bottom end of the rotating rod 1332 by welding or bolting, and is used to agitate the sediment at the bottom of the cavity. To ensure that the scraper 1333 can effectively perform cleaning work, its shape is adapted to the shape of the bottom of the shell body 1311. This not only allows the scraper 1333 to rotate normally, but also to evenly agitate the sediment at the bottom of the shell body 1311, causing the sediment to gather towards the sludge discharge pipe 1315 and be smoothly discharged.

[0123] In the above structure, the coordinated operation of the components of the cleaning unit 133 solves the problem of ineffective removal of sediment. The motor 1331 provides power, transmitting rotational motion to the scraper 1333 via the rotating rod 1332, enabling the scraper 1333 to agitate the sediment along a predetermined path. Because the scraper 1333 is designed to match the shape of the bottom of the shell body 1311, it can cover the entire bottom area during rotation, ensuring that all sediment is agitated and moves towards the sludge discharge pipe 1315. This process avoids long-term accumulation of sediment at the bottom of the cavity, reduces the need for manual cleaning, and improves the system's automation and operational stability.

[0124] Furthermore, this design ensures that the sedimentation tank 130 can operate continuously and efficiently, maintaining good water treatment results, while simplifying maintenance procedures and enhancing the reliability and ease of operation of the system.

[0125] Reference Figure 8 In some embodiments of this utility model, the ion exchange assembly 170 includes an exchange shell 1711. Specifically, the exchange shell 1711 has a cylindrical structure with a rubber-lined anti-corrosion layer on its inner wall. The top of the exchange shell 1711 is provided with a second product water pipe 177, and the bottom is provided with a second inlet water pipe 174. A baffle 175 is provided on the top of the second inlet water pipe 174 located inside the exchange shell 1711.

[0126] The interior of the exchange housing 1711 is provided with a first filter plate 1712, a second filter plate 1713, and a third filter plate 1714 arranged sequentially from top to bottom. These three filter plates divide the interior of the exchange housing 1711 into a first cavity 1721, a second cavity 1722, a third cavity 1723, and a fourth cavity 1724. The first filter plate 1712 has multiple first single-sided filter caps 1731, the second filter plate 1713 has multiple double-sided filter caps 1732, and the third filter plate 1714 has multiple second single-sided filter caps 1733. It should be noted that the first single-sided filter caps 1731, the double-sided filter caps 1732, and the second single-sided filter caps 1733 are all configured for dual flow rates. That is, when the flow rate is downward, the damping device reduces the flow rate, while when the flow rate is upward, the flow rate is unaffected.

[0127] The interior of the third cavity 1723 is provided with a weak acid cation resin layer 1781 and a white sphere resin pressing layer 1782 (the thickness of the white sphere resin pressing layer 1782 can be about 200 mm) from bottom to top, and there is a gap between the white sphere resin pressing layer 1782 and the second filter plate 1713 (the thickness of the gap can be about 100 mm). This gap is reserved for the expansion of the white sphere resin pressing layer 1782. The interior of the second cavity 1722 is provided with a chelating resin layer 1783 and a white sphere resin pressing layer 1782 (the thickness of the white sphere resin pressing layer 1782 can be about 200 mm) from bottom to top, and there is a gap between the white sphere resin pressing layer 1782 and the first filter plate 1712 (the thickness of the gap can be about 100 mm). This gap is reserved for the expansion of the white sphere resin pressing layer 1782. The first filter plate 1712 is provided with at least one porous plate 176.

[0128] In this embodiment, firstly, the regenerated wastewater enters the bottom of the exchange housing 1711 through the second inlet pipe 174, and the potential energy of the inlet water is eliminated by the baffle 175, thereby making the inlet water evenly distributed on the third filter plate 1714.

[0129] Subsequently, the wastewater flows upwards, passing through the second single-sided filter cap 1733 and entering the third chamber 1723, where it begins to contact the weak acid cation exchange resin layer 1781. The weak acid cation exchange resin layer 1781 adsorbs calcium and magnesium ions of equal alkalinity from the water, undergoing a preliminary ion exchange process. As the wastewater continues to rise, it passes through the white sphere resin pressing layer 1782, which sits above the weak acid cation exchange resin layer 1781 and has a gap between it and the second filter plate 1713. The main function of the white sphere resin pressing layer 1782 is to maintain the stability and integrity of the weak acid cation exchange resin layer 1781, preventing resin particle loss.

[0130] The wastewater then flows through the double-sided filter caps 1732 into the second chamber 1722, and further passes through the chelating resin layer 1783. This layer performs deeper adsorption and exchange of calcium and magnesium heavy metal ions. Similarly, after passing through the chelating resin layer 1783, the wastewater encounters the white sphere resin pressing layer 1782 again. The latter also has a gap between it and the first filter plate 1712 to ensure smooth water flow and resin layer stability.

[0131] As the wastewater continues to move upwards, it enters the first cavity 1721 through the first single-sided filter cap 1731. Here, the water flow path is affected by the porous plate 176 inside the first filter plate 1712. The porous plate 176 eliminates the potential energy of the wastewater, making its distribution more uniform. Finally, it flows out from the second product water pipe 177, completing the entire treatment process.

[0132] Reference Figure 9In some embodiments of this utility model, the strong oxidizer 180 includes a tubular reactor 181, an oxidation water tank 182, and an oxygen release tank 183. The tubular reactor 181 has an inlet and a dosing port that are interconnected. The inlet is connected to the water supply unit 1821, and the dosing port is connected to the hydrogen peroxide dosing unit 185 via an injector 184. The oxidation water tank 182 has an inlet, an outlet, and an overflow. The inlet is connected to the tubular reactor 181, and the outlet is connected to a circulating water pump 1824. The circulating water pump 1824 is connected to a pipeline injector 1823, and the negative pressure port of the pipeline injector 1823 is connected to an ozone generator 1822. The outlet of the pipeline injector 1823 is connected to the water supply unit 1821. The oxygen release tank 183 is connected to the overflow and has a nitrogen aeration unit 1831 inside. The first outlet of the oxygen release tank 183 is connected to a booster pump 1832, and the second outlet of the oxygen release tank 183 is connected to a tail gas absorber 1833.

[0133] The design of the strong oxidizer 180 aims to effectively inactivate microorganisms and remove harmful substances from reclaimed wastewater through a series of tightly connected components, ensuring the biological safety of the treated water. The tubular reactor 181, as the front-end treatment unit of the strong oxidizer 180, has an interconnected inlet and a dosing port. The inlet is connected to the water supply component 1821 to introduce the wastewater to be treated. The dosing port is connected to the hydrogen peroxide dosing component 185 via an injector 184, ensuring that hydrogen peroxide is evenly added to the wastewater flowing through the tubular reactor 181 to begin the initial oxidation process. Simultaneously, oxidation-reduction potential measuring instruments are installed at different locations within the tubular reactor 181 to adjust the dosage of hydrogen peroxide and ozone based on the oxidation potential.

[0134] Wastewater flowing from the tubular reactor 181 then enters an oxidation tank 182, which has an inlet, an outlet, and an overflow outlet, with the inlet directly connected to the tubular reactor 181. The wastewater continues its oxidation reaction in the oxidation tank 182 to further destroy residual organic matter and microorganisms. To enhance the oxidation effect, a circulating water pump 1824 is connected to the outlet, which pumps a portion of the treated water back into the jet injector 1823, where ozone generated by the ozone generator 1822 is drawn in under negative pressure. The water, after enhanced oxidation treatment, returns to the tubular reactor 181, forming a closed-loop system that ensures the sufficiency and continuity of the oxidation reaction.

[0135] The regenerated wastewater treated by the tubular reactor 181 enters the oxygen release tank 183 through the overflow port. The oxygen release tank 183 is equipped with a nitrogen aeration component 1831. After aeration, the gas mixed with residual ozone enters the tail gas absorber 1833. After the ozone is adsorbed, the gas is discharged into the atmosphere. The wastewater after ozone release is supplied to the next process by the booster pump 1832.

[0136] Reference Figure 10 In some embodiments of this utility model, the tubular reactor 181 includes multiple direct current sections and multiple arc-shaped connecting pipes 1814. The multiple direct current sections are connected end to end through the arc-shaped connecting pipes 1814. The direct current section includes an inlet pipe 1811 and a packing reaction pipe 1812 connected in sequence. The packing reaction pipe 1812 is fitted with at least one reagent inlet pipe 1813, and the reagent inlet pipe 1813 is connected to the packing reaction pipe 1812.

[0137] Specifically, multiple DC sections are connected end to end through an arc-shaped connecting pipe 1814 to form a flow channel, and the water inlet pipes 1811 at both ends are connected to the water supply component 1821 and the water inlet of the oxidation water tank 182, respectively, while the chemical injection pipe 1813 is connected to the chemical injection port through an injector 184.

[0138] Reference Figure 1 In some embodiments of this utility model, the filtration assembly includes a precision filter 140, a self-cleaning filter 150, and an ultrafiltration assembly 160 connected in sequence. The precision filter 140 is connected to the sedimentation tank 130, and the ultrafiltration assembly 160 is connected to the ion exchange assembly 170.

[0139] Specifically, the precision filter 140 can be a comet fiber filter, which has the characteristics of high dirt-holding depth, strong dirt-holding capacity, high filtration accuracy, interception capacity of more than 85% of organic matter such as oil, thorough backwashing, and good recovery of filter media filtration capacity.

[0140] The self-cleaning filter 150 consists of a cylinder, filter screen, filter screen support structure, filter cleaning device, control system, differential pressure switch, and drain valve. It uses a 100um high-precision filter element, and the filter control system can meet the requirements of long-term continuous operation. It can automatically clean the filter screen and clean it thoroughly.

[0141] The ultrafiltration module 160 can employ a reverse osmosis protection device to intercept fine suspended solids, colloids, and large organic molecules in the water, ensuring that the effluent SDI is ≤3. This meets the requirements of the reverse osmosis system for SDI value and suspended solids, extending the cleaning cycle of the reverse osmosis system and thus its service life. The membrane element uses the Asahi Kasei UNA-620A ultrafiltration membrane from Japan, with an absolute filtration accuracy of 0.1µm. It is equipped with an online backwashing device and a chemical cleaning device, achieving a 90% water production rate. The backwash water includes a NaClO metering dosing device, with a dosing standard of 10–15 mg / L (based on available chlorine).

[0142] A method for recycling ion exchange water regeneration wastewater includes the following steps:

[0143] S1. Impurities in the regenerated wastewater are removed by the ion exchange water treatment pretreatment device 100.

[0144] S2. The regenerated wastewater after impurities are removed is separated into monovalent salt solution and divalent salt solution by nanofiltration through the salt separation device 200, and the sulfate ions in the divalent salt solution are treated.

[0145] S3. The monovalent salt solution is processed into acid and alkali through the resource utilization device 300.

[0146] Step S1 includes the following steps:

[0147] S1.1. Some impurities in the regenerated wastewater are crystallized and separated using a room temperature crystallization reactor 120;

[0148] S1.2 The crystallized regenerated wastewater is purified by sedimentation in sedimentation tank 130;

[0149] S1.3 Filter the purified regenerated wastewater through a filtration assembly;

[0150] S1.4. Remove calcium and magnesium ions from the regenerated wastewater through ion exchange component 170;

[0151] S1.5. The microorganisms in the regenerated wastewater are killed by the strong oxidizer 180.

[0152] Specifically, a wastewater supply pump is installed between the wastewater equalization tank 110 and the ambient temperature crystallization reactor 120. The wastewater supply pump is also connected to a sludge thickening component, used to thicken the sludge removed from the supply pump. The thickened liquid is then resupplyed to the wastewater equalization tank 110, while the remaining sludge is transported to the sludge treatment plant. During operation, air and seed crystals (NaOH and Na₂CO₃) can be supplied to the ambient temperature crystallization reactor 120. An ultrafiltration water supply pump is installed between the sedimentation tank 130 and the filter assembly. A Na-weak acid resin layer is also installed between the filter assembly and the ion exchange assembly 170. During operation, a suitable amount of regenerated acid is added to the ion exchange assembly 170. An appropriate amount of air is added to the strong oxidizer 180 during operation. The strong oxidizer 180 is connected to the ultrafiltration product water tank 190, which is also equipped with a first reflux pipe and a second manifold. The first reflux pipe is connected to the ultrafiltration assembly 160 and is also equipped with a backwash pump. The second manifold connects to the precision filter 140 and is equipped with a cleaning water pump. The precision filter 140 requires the addition of HCl during operation. The ultrafiltration unit 160 requires the addition of cleaning agent, HCl, NaOH, and NaClO during operation.

[0153] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and not to limit it. Although this utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some of the technical features. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the spirit and scope of the technical solutions of the embodiments of this utility model.

Claims

1. An ion exchange water production regeneration waste water recovery system characterized by, The application relates to a resource utilization device for ion exchange water regeneration wastewater, which comprises the following parts: an ion exchange water regeneration wastewater pretreatment device (100) for removing impurities in the regeneration wastewater; a salt separation device (200) in communication with the ion exchange water regeneration wastewater pretreatment device (100) and used for separating monovalent salt solution and divalent salt solution from the regeneration wastewater through nanofiltration and treating sulfate ions in the divalent salt solution; a resource utilization device (300) in communication with the salt separation device (200) and used for preparing acid and alkali from the monovalent salt solution. The salt separation device (200) comprises: a nanofiltration assembly (210) in communication with the ion exchange water regeneration wastewater pretreatment device (100) and used for separating monovalent salt solution and divalent salt solution from the regeneration wastewater through nanofiltration; a normal-temperature crystallization reaction assembly (220) in communication with the nanofiltration assembly (210) and used for treating sulfate ions in the divalent salt solution; an SRB assembly (230) in communication with the normal-temperature crystallization reaction assembly (220) and used for further treating the sulfate ions in the divalent salt solution.

2. The ion exchange water service regeneration waste water recovery system of claim 1, wherein, The nanofiltration assembly (210) comprises: a first nanofiltration part (211) with a first water inlet pipeline, a first water production pipeline and a first concentrated water pipeline which are in communication with each other, wherein the first water inlet pipeline is in communication with the ion exchange water regeneration wastewater pretreatment device (100); a second nanofiltration part (212) with a second water inlet pipeline, a second water production pipeline and a second concentrated water pipeline which are in communication with each other, wherein the second water inlet pipeline is in communication with the first water production pipeline; the second nanofiltration part (212) is used for separating the monovalent salt solution, and the monovalent salt solution flows out through the second water production pipeline; a third nanofiltration part (213) with a third water inlet pipeline, a third water production pipeline and a third concentrated water pipeline which are in communication with each other, wherein the first concentrated water pipeline and the second concentrated water pipeline are both in communication with the third water inlet pipeline, and the third concentrated water pipeline is in communication with the first water production pipeline; the third nanofiltration part (213) is used for separating the divalent salt solution, and the divalent salt solution flows out through the third water production pipeline, wherein the third water production pipeline is in communication with the normal-temperature crystallization reaction assembly (220); a pressurizing pump (214) arranged in the third water inlet pipeline and used for driving the circulation of the regeneration wastewater.

3. The ion exchange service water regeneration waste water recovery system of claim 2, wherein, The resource utilization device (300) comprises: a first reverse osmosis assembly (310) in communication with the second water production pipeline and used for concentrating the monovalent salt solution to a first concentration; an ultrafiltration membrane assembly (320) in communication with the first reverse osmosis assembly (310) and used for filtering the monovalent salt solution; a second reverse osmosis assembly (330) in communication with the ultrafiltration membrane assembly (320) and used for concentrating the monovalent salt solution to a second concentration; a bipolar membrane electrodialysis assembly (340) in communication with the second reverse osmosis assembly (330) and used for treating the monovalent salt solution with the second concentration and generating sodium hydroxide and hydrochloric acid.

4. The ion exchange service water regeneration waste water recovery system of claim 3, wherein, The salt separation device (200) further comprises a water production pump, a heat exchanger, a security filter and a nanofiltration circulating pump which are sequentially arranged in communication. The water production pump is communicated with the ion exchange water production regeneration wastewater pretreatment device (100), and the nanofiltration circulating pump is communicated with the first water inlet pipeline; The third water production pipeline is communicated with a divalent salt water tank, and the second water production pipeline is communicated with a monovalent salt water tank.

5. The ion exchange service water regeneration waste water recovery system of claim 4, wherein, The first reverse osmosis component (310) is communicated with the monovalent salt water tank, and a first water supply pump, a first filter and a second water supply pump are sequentially arranged between the first reverse osmosis component (310) and the monovalent salt water tank.

6. The ion exchange service water regeneration waste water recovery system of claim 5, wherein, A concentrated water tank and a third water supply pump are sequentially arranged between the first reverse osmosis component (310) and the ultrafiltration membrane component (320), and a first circulating pipeline is arranged between the ultrafiltration membrane component (320) and the concentrated water tank.

7. The ion exchange service water regeneration waste water recovery system of claim 6, wherein, An ultrafiltration water production tank, a fourth water supply pump, a second filter and a fifth water supply pump are sequentially arranged between the ultrafiltration membrane component (320) and the second reverse osmosis component (330).

8. The ion exchange water production regeneration waste water recovery system according to any one of claims 5-7, characterized in that, A reverse osmosis water tank, a sixth water supply pump and a circulating water supply pump are sequentially arranged between the second reverse osmosis component (330) and the bipolar membrane electrodialysis component (340), and a second circulating pipeline is further arranged between the circulating water supply pump and the bipolar membrane electrodialysis component (340).

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