Chloride ion removal integrated device

Abstract

The utility model discloses a chloride ion removal integrated device, relates to the technical field of industrial wastewater treatment, and aims to solve the problems that most of existing chloride ion removal methods and equipment are relatively high in operation cost and high in manufacturing cost, and a chloride ion removal integrated device adopting an ultrahigh calcium and aluminum method chloride ion removal technology is lacked in the market. Comprising a support and a treatment tank, the treatment tank is installed on the support, and multiple sets of partition plates are arranged in the treatment tank; the treatment tank is divided into a plurality of independent units through partition plates, liquid is conveyed among the independent units through a pipeline system, a stirrer, a salt adding port and a water outlet cofferdam which are arranged in the treatment tank are matched, the device achieves the effect of purifying sewage through the principle that chloride ions are removed through an ultrahigh calcium-aluminum method, the integration degree of the device is high, and operation is convenient. The structure is simple, cost is economical and practical, and maintenance is convenient.

Description

Technical Field

[0001] This utility model relates to the field of industrial wastewater treatment technology, and in particular to an integrated device for chloride ion removal. Background Technology

[0002] High chloride ion concentrations pose significant risks to drinking water, irrigation, industrial equipment, human health, and the ecological environment. When chloride ion levels in drinking water exceed 250 mg / L (National Drinking Water Quality Standard GB5749-2006), the water will taste bitter or salty, and in severe cases, it can cause poisoning. When chloride ion levels in irrigation water exceed 350 mg / L (Evaluation Standard for Environmental Quality of Edible Agricultural Products Origin Areas HJ332-2006), it will seriously affect crop growth. In refining and chemical enterprises, chloride ions cause irreversible corrosion damage to equipment, especially pitting corrosion and other localized corrosion, which are difficult to predict and highly destructive. Treating chlorinated wastewater can not only alleviate the pressure of water scarcity in my country but also increase the reuse rate of industrial wastewater.

[0003] Currently, chloride ion emissions from the pharmaceutical and chemical industries exceed 100,000 mg / L. With increasingly stringent environmental pollution control measures, the discharge of chlorinated wastewater will inevitably face stricter restrictions. Methods for removing chloride ions used domestically and internationally include aerobic biological treatment, anaerobic biological treatment, ion exchange, incineration, electrochemical methods, electrodialysis, and reverse osmosis. Each method has its drawbacks. For example, ion exchange technology offers advantages such as good screening, low cost, and high recovery rate in purifying and enriching metals, and it has a strong ability to remove inorganic anions and cations. However, it generates a significant amount of wastewater during the regeneration of ion exchange resins. Electroadsorption technology can remove Cl- from reclaimed water with a removal rate of up to 70%, but its operating costs are high. Static adsorption experiments have explored the effectiveness of electroadsorption in removing chloride ions from reclaimed water, showing good removal results, but the electrode materials often have stringent requirements and are expensive. A comparison of these chloride removal technologies reveals that high cost, high operating costs, and the potential for secondary pollution limit their industrial application in treating large-scale high-chlorine wastewater. In recent years, ultra-high calcium aluminum method for chloride ion removal technology has received increasing theoretical research, but there is a lack of integrated chloride ion removal devices on the market that are compatible with it.

[0004] Therefore, this application provides an integrated chloride ion removal device to meet the requirements. Utility Model Content

[0005] The purpose of this application is to provide an integrated chloride ion removal device, which aims to solve the problems that most existing chloride ion removal methods and equipment have high operating costs and expensive construction costs, and there is a lack of integrated chloride ion removal devices on the market that use ultra-high calcium aluminum method for chloride ion removal technology.

[0006] To achieve the above objectives, this application provides the following technical solution: an integrated chloride ion removal device, comprising a support frame and a treatment tank, the treatment tank being mounted on the support frame, and multiple sets of partitions being provided inside the treatment tank; the internal space of the treatment tank being divided into several independent units by the partitions, with multiple sets of partitions, and a liquid level detection rod connected to the partition, one end of the liquid level detection rod passing through the side wall of the treatment tank; the partitions also include a first partition, a second partition, and a third partition, and each of the multiple sets of independent units is provided with an independent inlet and outlet; the treatment tank is also provided with a maintenance port for maintaining the treatment tank; the treatment tank is provided with a salt addition port for adding reactants and a stirring port for stirring the liquid inside the tank; multiple sets of maintenance ports, salt addition ports, and stirring ports are provided; the support frame is provided with a piping system for connecting the inlets and outlets of adjacent independent units; adjacent independent units are connected by the piping system, achieving the effect of integrated chloride ion removal and purification of wastewater.

[0007] Preferably, the independent unit also includes a first unit, a second unit, a third unit, and a fourth unit. The inner bottom surface of the second unit, the third unit, and the fourth unit are all provided with sludge discharge ports. The sludge discharge ports are connected to the sludge treatment unit through pipes, so that the generated sediment can be recycled.

[0008] Preferably, the pipeline system further includes a first liquid pump, a second liquid pump, and a third liquid pump. The outlet of the first unit is connected to the inlet of the second unit through the first liquid pump, the outlet of the second unit is connected to the inlet of the third unit through the second liquid pump, and the outlet of the third unit is connected to the inlet of the fourth unit through the third liquid pump, making it easier to transport liquid between adjacent units.

[0009] Preferably, the top surface of the first unit is provided with an inspection port, a salt addition port and a stirring port. The water outlet of the first unit is connected to the water inlet of the second unit through a first liquid pump, so that additives can be added into the equipment through the salt addition port.

[0010] Preferably, the second unit is further provided with a first outlet weir in the middle. The top surface of the second unit is provided with an inspection port, a salt addition port and a stirring port. A guide pipe is connected to the water inlet of the second unit. The water inlet and the sludge discharge port of the second unit are both located on the left side of the first outlet weir. The water outlet of the second unit is located on the right side of the first outlet weir. The water outlet of the second unit is connected to the water inlet of the third unit through a second liquid pump. The outlet weir ensures that the liquid in the tank can be discharged only after sedimentation.

[0011] Preferably, a second outlet weir is provided in the middle of the third unit. The top surface of the third unit is provided with an inspection port, a salt addition port and a stirring port. A guide pipe is connected to the inlet of the third unit. The inlet and the sludge discharge port of the third unit are both located on the left side of the second outlet weir. The outlet of the third unit is located on the right side of the second outlet weir. The outlet of the third unit is connected to the inlet of the fourth unit through a third liquid pump. The guide pipe ensures that the liquid does not mix with the bottom sediment when it is input.

[0012] Preferably, a guide pipe is connected to the water inlet of the fourth unit, and an inspection port is provided on the top surface of the fourth unit to facilitate maintenance of the tank interior.

[0013] Preferably, a mixer is installed inside the mixing port to accelerate the mixing speed of the liquid and the additives.

[0014] In summary, the technical effects and advantages of this utility model are as follows:

[0015] In this invention, a treatment tank is provided, which is divided into several independent units by partitions. The independent units are connected by a pipeline system for liquid transportation. With the help of a mixer, salt addition port and effluent weir installed in the treatment tank, the effect of purifying sewage is achieved. The equipment has a high degree of integration, simple structure, economical cost and easy maintenance.

[0016] In this invention, by setting a sludge discharge port in the treatment tank, which is connected to the sludge treatment unit through a pipe, the precipitate produced by the reaction of the wastewater inside the treatment tank with the additives can be discharged to the sludge treatment unit through the sludge discharge port, so that the precipitate can be recycled. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in the embodiments of this application 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 only some embodiments of this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 This is a schematic diagram of the structure of this utility model;

[0019] Figure 2 This is a schematic diagram of the internal cross-sectional structure of this utility model;

[0020] Figure 3 This is an enlarged view of point A in this utility model;

[0021] Figure 4 This is an enlarged view of section B of this utility model;

[0022] Figure 5 This is a schematic diagram of the sewage flow direction of this utility model.

[0023] In the diagram: 1. Support frame; 2. Treatment tank; 3. Baffle plate; 4. Independent unit; 5. First baffle plate; 6. Second baffle plate; 7. Third baffle plate; 8. Liquid level detection rod; 10. Inspection port; 11. Piping system; 12. Salt addition port; 13. Stirring port; 41. First unit; 42. Second unit; 43. Third unit; 44. Fourth unit; 111. First liquid pump; 112. Second liquid pump; 113. Third liquid pump; 421. First effluent weir; 431. Second effluent weir. Detailed Implementation

[0024] The technical solutions of the present utility model will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of the present utility model, and not all embodiments. Based on the embodiments of the present utility model, all other embodiments obtained by those of ordinary skill in the art without creative effort are within the protection scope of the present utility model. Example

[0025] refer to Figure 1-5 The illustrated integrated chloride ion removal device includes a support frame 1 and a treatment tank 2. The support frame 1 supports the treatment tank 2. The treatment tank 2 is also equipped with partitions 3, and liquid level detection rods 8 are connected to the partitions 3. There are three sets of partitions 3, namely a first partition 5, a second partition 6, and a third partition 7. The treatment tank 2 is divided into four independent units 4 by the first partition 5, the second partition 6, and the third partition 7. The four independent units 4 are the first unit 41, the second unit 42, the third unit 43, and the fourth unit 44. Each of the four independent units 4 is equipped with its own inlet and outlet. The support 1 is also equipped with a piping system 11, which is used to connect the outlet of the independent unit 4 to the inlet of the adjacent independent unit 4. The treatment tank 2 is also equipped with an inspection port 10, a salt addition port 12 and a stirring port 13. There are six sets of inspection ports 10. The first unit 41 and the fourth unit 44 are each equipped with one set of inspection ports 10, and the second unit 42 and the third unit 43 are each equipped with two sets of inspection ports 10. There are three sets of salt addition ports 12 and stirring ports 13. The first unit 41, the second unit 42 and the third unit 43 are each equipped with one set of salt addition ports 12 and stirring ports 13.

[0026] As one implementation method in this embodiment, the ultra-high calcium aluminum method for removing chloride ions from wastewater is environmentally friendly and energy-efficient. The added Ca(OH)₂ and NaAlO₂ are both inexpensive and readily available, and the resulting FS salt is inexpensive and has low toxicity. The process is also simple to operate. Compared to other chloride ion removal technologies, it requires less initial investment, is simple to operate, and the resulting precipitate can be used as an adsorbent for heavy metal ions in wastewater, meeting the requirements of green chemistry and avoiding secondary pollution. Therefore, it has good industrial application prospects and promotional value compared to other treatment technologies.

[0027] The ultra-high calcium-aluminum method is a technology that uses aluminum and calcium salts to remove chloride ions. Its principle is that aluminum and calcium salts combine with free chloride ions to form FS salt precipitates that adsorb chloride ions. The precipitate is then filtered to remove chloride. Specifically, this involves adding Ca(OH)₂ or Ca(OH)₂ and NaAlO₂ to high-chlorine wastewater to generate a calcium-aluminum chloride compound with extremely low solubility, Ca₄Al₂Cl₂(OH)₁₂ (Friedel's salt), thus achieving chloride ion removal.

[0028] The specific reaction mechanism is as follows:

[0029] NaAlO2 dissolves in water to form Al(OH)3, and Ca(OH)2 dissolves in water to form Ca(OH)2, which reacts with Al(OH)3 to form Ca4Al2(OH)14. The precipitation equilibrium constant of Ca4Al2(OH)14 is 10⁻²⁵.0², and the precipitation equilibrium constant of Ca4Al2Cl2(OH)12 is...

[0030] 10-27.10, and the order of easy exchange of anions between layers is OH- > F- > Cl- > Br- > NO3-. Therefore, Ca4Al2(OH)14 is formed first, and Ca4Al2(OH)14 further reacts with Cl- to form Ca4Al2Cl2(OH)12 precipitate. This is illustrated by the following reaction equation:

[0031] 4Ca(OH)2+2Al(OH)3=Ca4Al2(OH)14↓

[0032] Ca4Al2(OH)14+2Cl-=2OH-+Ca4Al2Cl2(OH)12↓

[0033] 3Ca4Al2Cl2(OH)12+2Al(OH)4-+4OH-

[0034] =4Ca3Al2(OH)12+6Cl-

[0035] 3Ca4Al2(OH)14+2Al(OH)4-

[0036] =4Ca3Al2(OH)12↓+2OH-

[0037] As the reaction proceeds, the pH of the solution slowly increases. Once the chloride ion exchange reaches equilibrium, the pH stops changing. If the amount of NaAlO2 exceeds the amount needed to completely form Ca4Al2(OH)14, excess NaAlO2 will react with Ca4Al2Cl2(OH)12, reducing the chloride ion removal rate. Therefore, the amount of NaAlO2 added must be strictly controlled. The Ca4Al2Cl2(OH)12↓ structure is mainly composed of [Ca2Al(OH)6]+ as the main layer and OH- as the interlayer ion. The interlayer ions are maintained with the main layer by ionic hydrogen bonds. Therefore, the interlayer ions are exchangeable. When chloride ions are present in the solution, they will enter the interlayer and exchange with OH- in the Ca4Al2(OH)14 interlayer. Cl- enters the interlayer in the form of [Cl-, 2H2O], forming Ca4Al2Cl2(OH)12.

[0038] Research on the removal of chloride ions from wastewater using the ultra-high calcium aluminum method mainly focuses on the effects of raw material ratio, reaction time, reaction temperature, chloride ion concentration, and other anions on the chloride removal effect, as well as the chloride ion removal efficiency in different water systems.

[0039] The removal of Cl- from a simulated water system was studied using the lime-aluminate precipitation method. Calcium hydroxide and sodium aluminate were used as basic raw materials. The effects of SO42- and CO32- on Cl- removal efficiency were investigated. SO42- and CO32- had a significant impact on Cl- removal, with the removal rate increasing as the concentrations of SO42- and CO32- decreased. In a laboratory study, the ultra-high lime-aluminate method for treating low-concentration chlorine-containing wastewater was investigated. The effects of the addition ratio of aluminum and calcium salts, reaction time, reaction temperature, and chloride ion concentration on the final chlorine removal efficiency were studied. The maximum removal rate was 70.1%. Adding sodium aluminate and calcium oxide in two separate additions significantly improved the chloride ion removal efficiency, reaching a maximum removal rate of 80.5%.

[0040] Studies on chloride ion removal in actual water systems have also been reported. The authors applied the ultra-high calcium aluminum method to treat high-chlorine wastewater from a polysilicon plant in Luoyang, using simulated wastewater to find the optimal reaction conditions. They then applied the ultra-high calcium aluminum method to dechlorinate desulfurization wastewater from a power plant in Yangquan City, Shanxi Province. When n(Ca):n(Al):n(Cl) = 10:4:1, and the reagents were added in two doses at a molar concentration ratio of 1:2, the chloride ion removal rate reached 90.0%. The FS salt precipitate obtained by the ultra-high calcium aluminum method exhibits porous adsorption characteristics. After drying and grinding, the authors added it to the original desulfurization wastewater, where it adsorbed and removed heavy metals, with a manganese removal rate reaching 99.7%. Zhang Qiang et al. applied the ultra-high calcium-aluminum method for chloride ion removal to gas field wastewater. They selected calcium hydroxide and sodium aluminate as calcium and aluminum salts, respectively. When the reaction temperature was 40℃, the initial pH was 8, and the molar ratio of calcium hydroxide to sodium aluminate was 13 and 4, respectively, the chloride ion removal rate reached 92.3% after 2 hours of reaction.

[0041] As one implementation method in this embodiment, the second unit 42 and the third unit 43 are respectively provided with a first outlet cofferdam 421 and a second outlet cofferdam 431. The two sets of inspection ports 10 on the second unit 42 are respectively located on both sides of the first outlet cofferdam 421, and the two sets of inspection ports 10 on the third unit 43 are respectively located on both sides of the second outlet cofferdam 431. The setting of the first outlet cofferdam 421 and the second outlet cofferdam 431 enables the sediment to be initially filtered.

[0042] As one implementation method in this embodiment, the inner bottom surfaces of the second unit 42, the third unit 43 and the fourth unit 44 are all provided with sludge discharge ports, and the three sets of sludge discharge ports are connected to each other through pipes and uniformly connected to the sludge treatment unit.

[0043] As one implementation method in this embodiment, in order to facilitate the liquid transportation in adjacent independent units 4, the pipeline system 11 further includes a first liquid pump 111, a second liquid pump 112, and a third liquid pump 113. The outlet of the first unit 41 is connected to the inlet of the second unit 42 through the first liquid pump 111, the outlet of the second unit 42 is connected to the inlet of the third unit 43 through the second liquid pump 112, and the outlet of the third unit 43 is connected to the inlet of the fourth unit 44 through the third liquid pump 113. Moreover, only guide pipes are provided at the inlets of the second unit 42, the third unit 43, and the fourth unit 44, so that when the liquid is input into the corresponding independent unit 4 through the inlet, the liquid is higher than the sediment, while avoiding the sediment from blocking the inlet. The height of the inlet of the first unit 41 and the outlet of the fourth unit 44 is matched with the height of the first outlet weir 421.

[0044] As one embodiment of this example, a stirrer is provided in each stirring port 13 in order to quickly mix the liquid and the reactants.

[0045] As one implementation method in this embodiment, the multiple sludge discharge ports installed in the treatment tank 2 can facilitate the reuse of FS salt, thereby reducing the cost of ultra-high calcium aluminum method in actual industrial wastewater treatment. FS salt, due to its structure similar to layered bimetallic hydroxides, is mainly used as an adsorbent, and adsorption studies of various metal ions have been conducted.

[0046] Adsorption of nitrates

[0047] The adsorption characteristics of nitrates by FS salt in a landfill environment were investigated. FS salt was first synthesized using the ultra-high calcium-aluminum method and characterized by XRD and FT-IR. Adsorption kinetics and adsorption isotherms were studied, and the effects of different landfill environments on adsorption were discussed. The results showed that the adsorption capacity of FS salt for nitrates was 2.494 mg / g. The adsorption process was exothermic and could be described by the pseudo-second-order kinetic Langmuir-Freundlich equation. In the landfill environment, Cl- enhanced adsorption, while SO42-, PO43-, and organic matter inhibited the adsorption effect. These results indicate that FS salt can alter the migration of nitrates in landfills, which is related to changes in the landfill environment.

[0048] Adsorption of heavy metal ions

[0049] A: A novel calcium aluminate-rich cementitious material (FS salt adsorbent) was studied for the removal of hexavalent chromium (Cr(VI)) from water. Adsorption kinetics results showed that the maximum adsorption capacity of FA was 3.36 mg / g, 14.66 mg / g, and 26.17 mg / g at initial Cr(VI) concentrations of 10 mg / L, 50 mg / L, and 100 mg / L, respectively. The adsorption efficiency was also related to the Cr(VI) concentration in the influent. The adsorption followed a pseudo-second-order kinetic model, indicating that intercalation plays an important role in the adsorption process with increasing Cr(VI) concentration. This adsorbent exhibits good adaptability and effectiveness in removing Cr(VI) from polluted groundwater. The removal behavior and adsorption mechanism of the FS salt adsorbent for Cr(VI) further demonstrate its feasibility as a remediation agent for Cr(VI) in soil and groundwater.

[0050] The adsorption behavior of FS salt for Cr(VI) at different concentrations and initial pH conditions was carefully investigated. The adsorption kinetics data all conformed to the first-order Lagerren equation. Experimental and simulation data showed that within the pH range of 4–10, FS salt adsorbed a large amount of Cr(VI) (1.4 mM / g) rapidly (t = 2–3 min) with high efficiency (removing 99% of Cr(VI). When the [Cr] concentration was below 4 mM, the adsorbent dosage was 4.00 g / L). In particular, the competitive adsorption experiments showed that the coexistence of Cl- and HCO3- ions had a relatively small impact on the Cr(VI) removal rate. Solid solution stability tests of Cr(VI) showed that, under pH conditions of 4–10, the leaching rate of Cr(VI) was only 0.2% within 24 hours. This is because the adsorption / exchange of Cr(VI) by FS salt led to the formation of a new stable phase 3Ca(OH)2·Al2O3·CaCrO4·10H2O, which resulted in the following reaction:

[0051] Ca4Al2(OH)12Cl2(H2O).xH2O+CrO42-

[0052] →Ca4Al2(OH)12CrO4(H2O)4.xH2O+2Cl-

[0053] This study demonstrates that Friedel salt is a potentially economically viable adsorbent for wastewater treatment.

[0054] b: Developing novel, low-cost, and efficient mineral adsorbents has been a research hotspot in recent years. In the laboratory, FS salt, a hexagonal layered inorganic adsorbent, was synthesized using sodium aluminate and calcium hydroxide for the removal of Cd²⁺ from water. The adsorption process was simulated using the Langmuir and Freundlich models. The adsorption mechanism was further analyzed through TEM, XRD, FT-IR analysis, and monitoring of released metal cations and solution pH changes. The results showed that the FS adsorbent has a good adsorption capacity for Cd(II), with a maximum adsorption capacity of 671.14 mg / g. The adsorbed Cd²⁺ and released Ca²⁺ were almost equal, indicating that ion exchange (surface and interior) plays an important role in the adsorption process of Cd(II). The adsorption behavior of FS for Cd(II) is significantly affected by surface reactions. The adsorption mechanism of Cd²⁺ by FS mainly involves surface complexation and surface precipitation, indicating that FS has good ion exchange capacity and is a promising layered inorganic adsorbent.

[0055] c: The adsorption performance of layered double hydroxide FS salt (FS: 3Ca(OH)2-Al2O3·CaCl2·10H2O) for arsenic in water was investigated. A well-crystallized FS salt was prepared from calcium chloride and sodium aluminate using a conventional hot-pressing method at a relatively low temperature (50℃). Kinetic studies showed that the FS salt exhibited rapid adsorption of arsenate in the first 12 hours, reaching equilibrium within 48 hours. Based on Langmuir isotherms, the adsorption capacities of the synthesized adsorbent for arsenate at pH 4 and 7 were 11.85 mg / g and 7.80 mg / g, respectively. Furthermore, the adsorbent showed higher removal rates for arsenate in both acidic and alkaline media than for arsenite. Phosphate and silicate significantly reduced the arsenate removal rate, especially at higher pH values. Sulfate inhibited arsenate adsorption at lower pH values, but this adverse effect disappeared at pH 6. Common metal cations in water (Ca2+, Mg2+) enhance the adsorption of arsenate, indicating that FS salt is a potentially economically viable adsorbent for arsenic in water treatment.

[0056] The authors synthesized Friedel salt using sodium aluminate and calcium chloride in the laboratory and studied its adsorption behavior on cobalt (Co(II)) in aqueous solution, investigating the effects of different concentrations and initial pH values ​​on the adsorption efficiency. Experimental results showed that the Friedel salt exhibited a high adsorption capacity for Co(II) (3.682 mmol Co(II) / g) and strong adsorption efficiency (greater than 99.98% when using 4.0 g / L adsorbent to adsorb [Co] containing less than 16.00 mM chlorine). Due to isomorphic substitution behavior, the leaching amount of Co(II) from the newly formed co-adsorbed gibbsite was less than 0.2% in the ion stability test. This study demonstrates that Friedel salt can serve as a low-cost, high-efficiency adsorbent for removing cobalt from wastewater. XRD analysis of the resulting precipitate was performed, and the cobalt removal mechanism was hypothesized as follows:

[0057] Ca4Al2(OH)12Cl2(H2O)·4H2O

[0058] →4Ca2++2Al(OH)4-+2Cl-+4OH-+5H2O

[0059] 4Co2++2Al(OH)4-+2Cl-+4OH-+4H2O

[0060] →Co4Al2Cl2(OH)12·4H2O

[0061] Furthermore, FS salts can be calcined at high temperatures to obtain a mixture of calcium oxide and aluminum oxide. This mixture can then be further reacted with chlorine-containing substances under acidic or alkaline conditions to yield FS salts again. Therefore, the calcination products can also be used for dechlorination research. Alternatively, the obtained calcium oxide and aluminum oxide can be used as components in cement, which can also reduce the cost of industrial-scale application of the calcium-aluminum precipitation method for dechlorination.

[0062] The working principle of this utility model is as follows: First, wastewater is input into treatment tank 2 via external equipment. The wastewater is introduced into the tank body through the inlet of the first unit 41 of treatment tank 2. The liquid level detection rod 8 connected to the partition 3 monitors the liquid volume in treatment tank 2 in real time. Then, additives are added into the pipe body of treatment tank 2 through the salt addition port 12. The additives are thoroughly mixed with the wastewater by the agitator installed in the stirring port 13 of the first unit 41. Finally, the first liquid pump 111 inputs the primary mixed liquid from the first unit 41 from the outlet of the first unit 41 to the inlet of the second unit 42, completing the primary mixing process. The liquid is fed into the second unit 42 through a guide pipe connected to the inlet of the second unit 42 for sedimentation. The sediment is fed into the sludge treatment unit through the sludge discharge port on the second unit 42. At the same time, the primary mixed liquor is continuously fed into the second unit 42. When the liquid level of the primary mixed liquor is higher than the first effluent weir 421, the sedimented primary mixed liquor flows to the other side of the first effluent weir 421. Then, additives are added into the second unit 42 through the salt addition port 12. At the same time, the agitator in the second unit 42 mixes the liquid and the additives to obtain a secondary mixed liquor. The secondary mixed liquor is then pumped by the second liquid pump 11. 2. The secondary mixed liquor is transported from the outlet of the second unit 42 to the inlet of the third unit 43. It is then fed into the third unit 43 through a guide pipe connected to the inlet of the third unit 43 for sedimentation. The sediment is discharged through the sludge discharge port on the third unit 43 and piped to the sludge treatment unit. Simultaneously, the secondary mixed liquor continues to be fed into the third unit 43. When the liquid level of the secondary mixed liquor is higher than the second effluent weir 431, the sedimented secondary mixed liquor flows to the other side of the second effluent weir 431. Then, additives are added to the third unit 43 through the salt addition port 12. Simultaneously, the mixture in the third unit 43 is stirred... The machine mixes the liquid with additives to obtain a tertiary mixture. The tertiary mixture is transported from the outlet of the third unit 43 to the inlet of the fourth unit 44 through the third liquid pump 113. The tertiary mixture is then fed into the fourth unit 44 through the guide pipe for sedimentation. The sediment is fed into the sludge treatment unit through the sludge discharge port on the fourth unit 44. At the same time, the tertiary mixture is continuously fed into the fourth unit 44. When the liquid level in the fourth unit 44 is higher than the outlet of the fourth unit 44, the liquid that has settled on the surface of the tertiary mixture is discharged through the outlet of the fourth unit 44, thus completing the entire process of wastewater purification.

[0063] The electromechanical connections involved in this utility model are common practices used by those skilled in the art, and technical inspiration can be obtained through a limited number of experiments; they are common knowledge.

[0064] Components not described in detail in this article are existing technologies.

[0065] Finally, it should be noted that the above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Although the present utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.

Claims

1. An integrated chloride ion removal device, characterized in that: It includes a support (1) and a processing tank (2), the processing tank (2) is mounted on the support (1), and the processing tank (2) is provided with a partition (3), the partition (3) being provided with multiple sets; The internal space of the processing tank (2) is divided into several independent units (4) by the partition (3). The partition (3) is provided with multiple sets, and a liquid level detection rod (8) is connected to the partition (3). One end of the liquid level detection rod (8) passes through the side wall of the processing tank (2). The partition (3) also includes a first partition (5), a second partition (6) and a third partition (7), and each of the multiple independent units (4) is provided with an independent inlet and outlet. The treatment tank (2) is also provided with an inspection port (10) for maintaining the treatment tank (2). The processing tank (2) is provided with a salt addition port (12) for adding reactants and a stirring port (13) for stirring the liquid in the tank. The inspection port (10), salt addition port (12) and stirring port (13) are each provided with multiple sets; The bracket (1) is provided with a pipe system (11) for connecting the inlet and outlet of the adjacent independent unit (4). The adjacent independent units (4) are connected by the piping system (11).

2. The integrated chloride ion removal device according to claim 1, characterized in that: The independent unit (4) also includes a first unit (41), a second unit (42), a third unit (43) and a fourth unit (44). The inner bottom surfaces of the second unit (42), the third unit (43) and the fourth unit (44) are provided with sludge discharge ports, which are connected to the sludge treatment unit through pipes.

3. The integrated chloride ion removal device according to claim 2, characterized in that: The pipeline system (11) further includes a first liquid pump (111), a second liquid pump (112) and a third liquid pump (113). The outlet of the first unit (41) is connected to the inlet of the second unit (42) through the first liquid pump (111). The outlet of the second unit (42) is connected to the inlet of the third unit (43) through the second liquid pump (112). The outlet of the third unit (43) is connected to the inlet of the fourth unit (44) through the third liquid pump (113).

4. The integrated chloride ion removal device according to claim 3, characterized in that: The top surface of the first unit (41) is provided with the inspection port (10), the salt addition port (12) and the stirring port (13).

5. The integrated chloride ion removal device according to claim 3, characterized in that: The second unit (42) is also provided with a first outlet weir (421) in the middle. The top surface of the second unit (42) is provided with the inspection port (10), the salt addition port (12) and the stirring port (13). A guide pipe is connected to the water inlet of the second unit (42). The water inlet and the sludge discharge port of the second unit (42) are both located on the left side of the first outlet weir (421). The water outlet of the second unit (42) is located on the right side of the first outlet weir (421).

6. The integrated chloride ion removal device according to claim 3, characterized in that: The third unit (43) is also provided with a second outlet weir (431) in the middle. The top surface of the third unit (43) is provided with the inspection port (10), the salt addition port (12) and the stirring port (13). The inlet of the third unit (43) is connected to a guide pipe. The inlet of the third unit (43) and the sludge discharge port of the third unit (43) are both located on the left side of the second outlet weir (431).

7. The integrated chloride ion removal device according to claim 3, characterized in that: The fourth unit (44) is connected to a guide pipe at its inlet, and the inspection port (10) is provided on the top surface of the fourth unit (44).

8. The integrated chloride ion removal device according to claim 1, characterized in that: A mixer is installed inside the mixing port (13).

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