Dimethylisoborneol removal device for drinking water production

Abstract

The invention belongs to the technical field of 2-MIB removal, and discloses a removal device for dimethyl isoborneol produced by drinking water, which comprises a dissolved air pump and an air floatation treatment machine, a water delivery pipe and a dissolved air pipe of the dissolved air pump are communicated with the air floatation treatment machine, and fine bubbles are dissolved in water and conveyed to the air floatation treatment machine; the dimethyl isoborneol removal device is characterized by further comprising a secondary removal module, and the secondary removal module is communicated with the dissolved air pump and used for further filtering soluble impurities including dimethyl isoborneol in water subjected to air flotation treatment. According to the multi-layer secondary removal module disclosed by the invention, a parallel treatment mode with relatively high initial efficiency and a series treatment mode with relatively high removal rate can be switched through cooperation among the stop valves I, the three-way pipes and the stop valves II of the multi-layer secondary removal module. After the adsorption efficiency is reduced, a series treatment method is adopted, and the removal rate of 2-MIB is further increased through at least two adsorption processes. Compared with the prior art, the removal strategy is changeable, and the working condition adaptability is high.

Description

Technical Field

[0001] The present invention belongs to the technical field of 2-MIB removal, and specifically relates to a device for removing dimethylisoborneol in drinking water production. Background Art

[0002] Dimethylisoborneol (hereinafter all replaced by 2-MIB) is a common harmful substance in drinking water, which can stimulate the eyes and respiratory tract, causing conditions such as tearing, coughing, and even shortness of breath. Moreover, it is also a potential carcinogen, and long-term exposure to it will increase the risk of cancer and cause damage to kidney function. Therefore, it is one of the harmful substances that need to be removed with emphasis in drinking water.

[0003] Currently, most of the removal devices used are continuous treatment devices, that is, the drinking water is passed through the filter layer of the device, and the 2-MIB in it is adsorbed and removed by activated carbon. Usually, after hundreds of hours of continuous operation, the adsorption effect will significantly decline, and then the filter layer is replaced to continue the removal work, with relatively low efficiency. Or the adsorbent is directly mixed with water, and after adsorption, filtration treatment is carried out to separate the adsorbent and water. Compared with the previous method, its removal efficiency is relatively high, but due to the addition of a filtration process, the post-treatment speed is relatively slow (such as the invention patent disclosed in the application number: 202210843678.0).

[0004] Therefore, this application proposes a device for removing dimethylisoborneol in drinking water production to overcome the above-mentioned defects. Summary of the Invention

[0005] To solve the problems raised in the above background art, the present invention provides a device for removing dimethylisoborneol in drinking water production.

[0006] To achieve the above purpose, the present invention provides the following technical solution: A device for removing dimethylisoborneol in drinking water production, including a dissolved air pump and an air flotation processor. The water delivery pipe and the dissolved air pipe of the dissolved air pump are connected to the air flotation processor to dissolve fine air bubbles in water and transport it to the air flotation processor. The dimethylisoborneol removal device further includes a secondary removal module, and the secondary removal module is connected to the dissolved air pump for further filtering soluble impurities including dimethylisoborneol in the water treated by air flotation;

[0007] An aerator, which is connected to the output end of the secondary removal module to aerate the water filtered by it;

[0008] The secondary removal module is provided with at least four layers for continuous treatment or parallel treatment of drinking water;

[0009] The adjacent two secondary removal modules are connected between a stop valve I and a tee pipe. The connection between the adjacent two tee pipes is controlled to be cut off or connected through a stop valve II. A handwheel valve is arranged at the connection port between the tee pipe and the secondary removal module.

[0010] Preferably, one end of the secondary removal module can be used as the input port of the water to be treated. The filtered water enters through one end tee pipe and is discharged through the other end tee pipe for parallel processing.

[0011] Preferably, the secondary removal module located at the topmost layer can be used as the output port of the water to be treated. The filtered water is input through the water inlet at its top, and after being processed once inside, the water is introduced into other secondary removal modules through the cooperation between the stop valve I and the tee pipe or the cooperation between the tee pipe and the stop valve II.

[0012] Preferably, the air flotation processor includes three chambers, namely a scum chamber, a slag removal chamber, and a drainage tank, arranged inside it. The partition is connected to the scum chamber. The water input into the scum chamber enters the slag removal chamber by crossing the top of the partition. The slag removal chamber injects the water treated by air flotation into the drainage tank through a water pipe arranged at the bottom of the chamber. The air flotation processor also includes a slag conveying line arranged at the top for removing air flotation impurities.

[0013] The water in the drainage tank is pumped into the secondary removal module.

[0014] Preferably, a baffle is further arranged above the scum chamber. The baffle includes a slope surface and a concave surface. The concave surface and the inner wall of the air flotation processor enclose a collection chamber. The hanging plate on the slag conveying line cooperates with the slope surface of the baffle to guide the air flotation impurities into the collection chamber.

[0015] An activated carbon cotton layer is arranged in the middle of the slag removal chamber, and the activated carbon cotton layer is located above the water pipe in the slag removal chamber.

[0016] Preferably, the secondary removal module includes a filtration module formed by splicing a number of filtration mechanisms end to end. The filtration mechanism includes a removal layer, an elastic water-permeable membrane, and a water-permeable support that wraps the removal layer therebetween. The joints between adjacent two filtration mechanisms are sealed by a sealing sheet.

[0017] A sub-rigid microporous filter material II is coaxially arranged inside the filtration mechanism for supporting it, and the tee pipe is connected to the sub-rigid microporous filter material II.

[0018] Preferably, the outside of the elastic water-permeable membrane is respectively pressed at the head and tail ends of the filtration mechanism by a head end hoop and a tail end hoop. The head end hoop further includes a number of pressure rods.

[0019] The head end clamp, the tail end clamp and the permeable support cooperate to lay the removal layer in a sine wave shape, and the pressure rod presses the elastic permeable membrane on the wave trough line.

[0020] Preferably, a circle of semi-rigid microporous filter material I is further arranged on the periphery of the head end clamp and the tail end clamp, and two convex ribs are arranged on the inner side of the semi-rigid microporous filter material I to support the head end clamp and the tail end clamp above it;

[0021] The periphery of the semi-rigid microporous filter material I is the outer shell, and convex ribs are also arranged on the inner circumference of the outer shell to support the semi-rigid microporous filter material I above it.

[0022] Preferably, the removal layer is composed of a fiber filament layer wrapped with an adsorbent;

[0023] The removal layer is laid in a three-layer composite manner. The outermost layer and the innermost layer have a thickness between 1.5-2 mm. The outermost layer uses coarse fibers, and the innermost layer uses a nanofiber layer;

[0024] The middle layer is an adsorbent-loaded fiber layer with a thickness of 6-8 mm. The fiber diameter of the middle layer is between 0.1-0.15 mm, and the diameter of each fiber filament bundle does not have to be the same.

[0025] Preferably, the adsorbent is composed of 200-mesh modified activated carbon and nano-ferric oxide mixed in a ratio of 4:1. The mass ratio of the adsorbent to the fiber filament bundle is 0.8:1-1.5:1, so as to maintain the pressure drop and prevent excessive loss during backwashing.

[0026] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0027] By setting up a multi-layer secondary removal module, the present invention guides the water after air flotation treatment into the multi-layer secondary removal module. Through the cooperation between the stop valve I, the three-way pipe and the stop valve II of the multi-layer secondary removal module, it is possible to switch between the parallel treatment method with a relatively fast initial efficiency and the series treatment method with a relatively high removal rate, and it is possible to, according to the working conditions, adopt the parallel treatment method during the first 100 hours of treatment. When the adsorption efficiency decreases, the series treatment method is adopted, and the removal rate of 2-MIB is further improved through at least two-stage adsorption. Compared with the prior art, the removal strategy is variable and the adaptability to working conditions is strong.

[0028] In the present invention, the water after dissolved air treatment is directly transported to the scum chamber through a pipeline. As the water level rises, it will cross over the baffle and enter the slag removal chamber. At this time, the bubbles dissolved in the water are released during this process, wrapping the large particulate impurities in the water and floating them on the water surface, and flowing into the slag removal chamber together with the water level. The scraper on the slag conveying line slowly pushes away the bubble impurities for unified collection, and an activated carbon cotton layer is also arranged in the slag removal chamber for preliminary removal treatment of the water body to reduce the concentration of 2-MIB in it.

[0029] In the present invention, by setting the adsorption layer as a mixed coating layer of fiber filaments and adsorbent, a three-dimensional adsorption network is constructed. Traditional technologies rely relatively more on the random packing of adsorbent particles, with relatively low porosity. However, in this application, through the directional arrangement of fibers, complex interlayer channels are constructed, and the porosity is greatly increased, approximately 62 - 68%. Moreover, the loading rate of activated carbon in general filter media carriers is greatly improved, and the resulting 2-MIB removal rate is also significantly increased. And it is arranged in a sine wave shape to increase its water flow surface and improve the removal efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 is a schematic structural diagram of the present invention;

[0031] Figure 2 is a front view of the present invention;

[0032] Figure 3 is an internal schematic diagram of the air flotation processor of the present invention;

[0033] Figure 4 is a partial cross-sectional view of the secondary removal module of the present invention;

[0034] Figure 5 is a structural cross-sectional view of the filtering mechanism of the present invention;

[0035] Figure 6 is the present invention Figure 5 magnified schematic view of part A;

[0036] Figure 7 is a schematic diagram of the structural disassembly of the secondary removal module of the present invention;

[0037] Figure 8 is a schematic diagram of the longitudinal arrangement of the fiber filaments of the present invention.

[0038] In the figure: 100, dissolved air pump; 101, water delivery pipe; 102, dissolved air pipe; 200, air flotation processor; 201, partition; 202, scum chamber; 203, slag removal chamber; 204, drainage tank; 205, collection chamber; 206, slag transportation line; 207, baffle; 208, activated carbon cotton layer; 300, aerator; 400, secondary removal module; 401, stop valve one; 402, tee; 403, stop valve two; 404, filtering mechanism; 4041, removal layer; 4042, elastic water-permeable film; 4043, water-permeable support; 4044, sealing piece; 405, head end hoop; 4051, pressure bar; 406, tail end hoop; 407, outer shell; 408, sub-rigid microporous filter material one; 409, sub-rigid microporous filter material two. DETAILED DESCRIPTION OF THE INVENTION

[0039] Next, the technical solutions in the embodiments of the present invention will be clearly and completely described in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention without creative efforts shall fall within the protection scope of the present invention.

[0040] As Figures 1 to 8 shown, the present invention provides a device for removing 2-methylisoborneol from drinking water production, including a dissolved air pump 100 and an air flotation processor 200. The water delivery pipe 101 of the dissolved air pump 100 is communicated with the partition plate 201 of the air flotation processor 200 to dissolve fine air bubbles in water and transport it to the dissolved air pump 100. The 2-methylisoborneol removal device further includes a secondary removal module 400, and the secondary removal module 400 is communicated with the dissolved air pump 100 for further filtering soluble impurities including 2-methylisoborneol in the water treated by air flotation;

[0041] An aerator 300, which is communicated with the output end of the secondary removal module 400 to perform aeration treatment on the filtered water;

[0042] The secondary removal module 400 is provided with at least four layers for continuously or parallelly treating drinking water;

[0043] Adjacent two secondary removal modules 400 are communicated between a stop valve 401 and a tee pipe 402, and the communication between adjacent two tee pipes 402 is controlled to be cut off or connected by a stop valve 403. A handwheel valve is arranged at the communication port between the tee pipe 402 and the secondary removal module 400.

[0044] Drinking water is injected through the water delivery pipe 101, converges to the dissolved air pipe 102, and the dissolved air pump 100 dissolves gas in the flowing water, and then injects it into the air flotation processor 200 for air flotation treatment to remove insoluble particulate impurities therein. The treated water is pumped into the secondary removal module 400 for 2-MIB removal treatment. The secondary removal module 400 is provided with multiple layers, and the treatment mode can be switched through the stop valve 401, the tee pipe 402, the stop valve 403 and the handwheel valve arranged at the communication port, and it can be switched between continuous treatment and parallel treatment according to the working conditions. The parallel treatment method is adopted at the initial treatment to improve the treatment efficiency, and when the removal rate decreases, the series treatment method is adopted for superimposed treatment of the removal rate. After 2-MIB treatment, it is input into the aerator 300 for aeration treatment.

[0045] As Figure 2 shown, one end of the secondary removal module 400 can be used as the input port of the water to be treated, and the filtered water enters through the tee pipe 402 at one end and is discharged through the tee pipe 402 at the other end for parallel treatment.

[0046] In the parallel processing method adopted in this embodiment, the water after being treated by the air flotation processor 200 is led to the side water inlet of the tee pipe 402, and the water inlet directly communicated with the secondary removal module 400 is closed by a handwheel valve. The water simultaneously enters each layer of the secondary removal module 400 for the removal treatment of 2-MIB. The water after the removal treatment flows out from the other end of the secondary removal module 400 and finally enters the aerator 300 for aeration treatment. The parallel processing method can accelerate the synchronous water treatment flow rate and improve the treatment efficiency. When the removal rate of the filter material in the secondary removal module 400 for 2-MIB decreases, the handwheel valve is opened, and the water inlet is turned to the topmost secondary removal module 400, and the water flows into the other secondary removal modules 400 through the tee pipe 402 and the first stop valve 401 from top to bottom for multiple superimposed treatments to further remove 2-MIB in the water.

[0047] As Figure 2 and Figure 3 shown, the secondary removal module 400 located at the topmost layer can serve as the output port of the water to be treated. The filtered water is input from the water inlet at its top, and after being processed once inside, the water is introduced into the other secondary removal modules 400 through the cooperation of the first stop valve 401 and the tee pipe 402 or the cooperation between the tee pipe 402 and the second stop valve 403.

[0048] In this embodiment, a series processing method is adopted, that is, the water after air flotation treatment is guided to the secondary removal module 400 located at the topmost layer, and the water is subjected to the first filtration treatment by this secondary removal module 400. Subsequently, the treated water is guided into the other secondary removal modules 400 through the cooperation of the first stop valve 401 and the tee pipe 402 or the cooperation between the tee pipe 402 and the second stop valve 403 for further treatment. Or after a certain secondary removal module 400 is over-fatigued, the guiding object is changed through the cooperation of the tee pipe 402 and the second stop valve 403, so that it switches to the other normal working secondary removal modules 400 to continue the filtration treatment.

[0049] As Figure 3 shown, the air flotation processor 200 includes three chambers, namely a scum chamber 202, a slag removal chamber 203, and a drainage tank 204, which are arranged inside it. The partition 201 communicates with the scum chamber 202, and the water input into the scum chamber 202 enters the slag removal chamber 203 by crossing the top of the partition. The slag removal chamber 203 injects the water after air flotation treatment into the drainage tank 204 through a water pipe arranged at the bottom of the chamber. The air flotation processor 200 also includes a slag conveying line 206 arranged at the top for removing air flotation impurities.

[0050] The water in the drainage tank 204 is pumped into the secondary removal module 400.

[0051] The water after dissolved air treatment is directly transported to the scum chamber 202 through a pipeline. As the water level rises, it will pass over the partition and enter the slag removal chamber 203. At this time, the bubbles dissolved in the water are released during this process, wrapping the large particulate impurities in the water and floating them on the water surface, and flowing into the slag removal chamber 203 together with the water level. The scraper on the slag conveying line 206 slowly pushes away the bubble impurities for unified collection. There is also a pipeline connecting the lower part of the slag removal chamber 203 to the drainage tank 204, and the height of this pipeline extending into the drainage tank 204 is lower than the liquid levels in the scum chamber 202 and the slag removal chamber 203. And the drainage flow rate into the drainage tank 204 through this pipeline and the water inflow rate in the scum chamber 202 are intelligently regulated through the water supply system to keep the liquid levels in the scum chamber 202 and the slag removal chamber 203 always above the partition, so as to ensure the normal treatment of air-floated impurities by the plate.

[0052] As Figure 3 shown, a baffle 207 is also provided above the scum chamber 202. The baffle 207 includes a slope surface and a concave surface. The concave surface and the inner wall of the dissolved air treatment machine 200 enclose a collection chamber 205. The hanging plate on the slag conveying line 206 cooperates with the slope surface of the baffle 207 to guide the air-floated impurities to the collection chamber 205;

[0053] An activated carbon cotton layer 208 is provided in the middle of the slag removal chamber 203, and the activated carbon cotton layer 208 is located above the water pipe in the slag removal chamber 203.

[0054] The running track of the scraper on the slag conveying line 206 fits the slope surface of the baffle 207. During the operation of the slag conveying line 206, the air-floated impurities on the liquid surface of the slag removal chamber 203 are pushed towards the collection chamber 205, pushed onto the slope surface of the baffle 207, and finally fall into the collection chamber 205 for unified collection and treatment.

[0055] The activated carbon cotton layer 208 is provided in the middle of the slag removal chamber 203 to treat the drinking water seeping down from above, and to perform a preliminary adsorption treatment on 2-MIB in it to reduce the initial concentration of 2-MIB in the drinking water. The activated carbon cotton layer 208 is set as a quick-disassembly structure to ensure its normal preliminary adsorption work during a treatment process of a fixed amount of drinking water. After completing the treatment work of timed or quantitative water, it is disassembled and a new activated carbon cotton layer 208 is replaced.

[0056] As Figure 5 and 6 shown, the secondary removal module 400 includes a filter module formed by splicing a number of filter mechanisms 404 end to end. The filter mechanism 404 includes a removal layer 4041, an elastic water-permeable membrane 4042 and a water-permeable support 4043 that wrap the removal layer 4041 therebetween. The joints between adjacent two filter mechanisms 404 are sealed by a sealing piece 4044;

[0057] Inside the filtering mechanism 404, a sub-rigid microporous filter material II 409 is coaxially arranged to support it, and the tee 402 communicates with the sub-rigid microporous filter material II 409.

[0058] Each section is about 35 cm in length, and they are joined end to end in pairs. The splicing gap between adjacent filtering mechanisms 404 is sealed by a sealing sheet 4044, and the end of the sub-rigid microporous filter material II 409 is pressed on the sealing sheet 4044. The sub-rigid microporous filter materials II 409 inside adjacent filtering mechanisms 404 are connected. The inlet of the tee 402 provided at the end of the secondary removal module 400 communicates with the inside of the sub-rigid microporous filter material II 409. The sub-rigid microporous filter materials II 409 at both ends are hermetically connected to the end caps.

[0059] The sub-rigid microporous filter material I 408 mainly isolates the remaining insoluble impurities that are not completely treated by air flotation again. The aperture of the sub-rigid microporous filter material II 409 is larger than that of the sub-rigid microporous filter material I 408 to balance the water pressure, and it mainly plays an internal support role.

[0060] After preliminary air flotation treatment, 2-MIB in the drinking water penetrates through the filtering mechanism 404 and enters the inner side of the sub-rigid microporous filter material II 409, and the filtering mechanism 404 removes 2-MIB in the drinking water. The treated water enters other processes through the tee 402.

[0061] As Figures 5 to 7 shown, the outside of the elastic water-permeable membrane 4042 is pressed on the head and tail ends of the filtering mechanism 404 by a head end hoop 405 and a tail end hoop 406 respectively. The head end hoop 405 also includes a number of pressure rods 4051;

[0062] The head end hoop 405, the tail end hoop 406 and the water-permeable support 4043 cooperate to lay the removal layer 4041 in a sine wave shape, and the pressure rods 4051 press the elastic water-permeable membrane 4042 on the wave trough line.

[0063] The head end hoop 405 and the tail end hoop 406 directly press the elastic water-permeable membrane 4042 on the removal layer 4041 to make it fit on the removal layer 4041. Laying the removal layer 4041 in a sine wave shape helps to expand the filtering area and can extend the water flow path by 1.5 - 1.7 times.

[0064] The head end hoop 405 and the tail end hoop 406 have the same specifications. The pressure rods 4051 are arranged on the wave troughs of the head end hoop 405. The pressure rods 4051 extend along the axis direction of the filtering mechanism 404 and directly press on the wave trough line of the filtering mechanism 404 to make the elastic water-permeable membrane 4042 fit firmly.

[0065] As Figure 5As shown, a ring of first sub-rigid microporous filter material 408 is also provided on the outer periphery of the head end hoop 405 and the tail end hoop 406. Two convex ribs are provided inside the first sub-rigid microporous filter material 408 to support the head end hoop 405 and the tail end hoop 406 above it.

[0066] The outer periphery of the first sub-rigid microporous filter material 408 is the outer shell 407. Convex ribs are also provided on the inner circumference of the outer shell 407 to support the first sub-rigid microporous filter material 408 above it.

[0067] The above convex ribs can be hollow to allow water flow through, and the convex ribs themselves play the role of positioning and support. During installation, it can be directly pushed into the outer shell 407 along the convex ribs, or pulled out directly during disassembly.

[0068] As Figure 8 shown, the removal layer 4041 is composed of a fiber filament layer wrapped with an adsorbent.

[0069] The removal layer 4041 is laid in a three-layer composite manner. The outermost layer and the innermost layer have a thickness between 1.5 - 2 mm. The outermost layer uses coarse fibers, and the innermost layer uses a nanofiber layer.

[0070] The middle layer is an adsorbent-loaded fiber layer with a thickness of 6 - 8 mm. The fiber diameter of the middle layer is between 0.1 - 0.15 mm, and the diameter of each fiber filament bundle does not have to be the same.

[0071] Electrospinning coating can be used between the adsorbent and the fiber filament layer. By using the three-layer composite laying method, it can intercept larger particle impurities and flocculent impurities, balance the water flow resistance, and control the loss of the adsorbent.

[0072] The diameter of each fiber filament bundle does not have to be different, which is used to increase the complexity of the pores in the fiber filament layer.

[0073] The adsorbent is composed of 200-mesh modified activated carbon and nano-iron oxide mixed in a ratio of 4:1. The mass ratio of the adsorbent to the fiber filament bundle is 0.8:1 - 1.5:1, which is used to maintain the pressure drop and prevent excessive loss during backwashing.

[0074] Under the accelerated life test results:

[0075] After continuously operating at a high flow rate of 10 m / h for 120 h, when the mass ratio of the adsorbent to the fiber filament bundle is 1:2, the 2-MIB removal rate drops from 82% to 76% (12 kPa / m).

[0076] When the mass ratio of the adsorbent to the fiber filament bundle is 1:1.5, the 2-MIB removal rate drops from 91% to 85% (18 kPa / m).

[0077] When the mass ratio of the adsorbent to the fiber bundle is 1:1.2, the removal rate of 2-MIB decreases from 96% to 88% (27 kPa / m), and the loss of carbon powder is <0.3 mg / L.

[0078] However, when the mass ratio of the adsorbent to the fiber bundle is higher than 1:0.8, it will cause blockage of the fiber voids (pressure grouting > 50 kPa / m);

[0079] When the mass ratio of the adsorbent to the fiber bundle is lower than 1:1.5, the adsorption capacity is significantly insufficient.

[0080] Therefore, the preferred embodiment should be around 1:1.2.

[0081] Of course, the intermediate interlayer of the composite layer mentioned above can still adopt a gradient loading structure, and the front layer (water inlet side), the middle layer, and the end layer are respectively set, and there are certain differences in the mass ratio between each layer to optimize the strategy.

[0082] The mass ratio of the adsorbent to the fiber bundle in the front layer is 1:1.2, so as to correspond to the initial high concentration of 2-MIB (>100 ng / L) through a high adsorption capacity;

[0083] The mass ratio of the adsorbent to the fiber bundle in the middle layer is 1:1.5, so as to balance adsorption and water flow resistance;

[0084] The mass ratio of the adsorbent to the fiber bundle in the end layer is 1:0.9, so as to set a dense layer to intercept the loss of carbon powder.

[0085] The working principle and usage process of the present invention:

[0086] Drinking water is injected through the water delivery pipe 101, converges to the air dissolving pipe 102, and the gas is dissolved in the flowing water through the air dissolving pump 100, and then injected into the air flotation processor 200 for air flotation treatment to remove the insoluble particulate impurities therein. The treated water is pumped into the secondary removal module 400 for 2-MIB removal treatment.

[0087] The secondary removal module 400 is provided with multiple layers, and the treatment method can be switched through the stop valve I 401, the three-way pipe 402, the stop valve II 403, and the handwheel valve arranged at the communication port, and it can be switched between continuous treatment and parallel treatment according to the working conditions. The parallel treatment method is adopted at the initial treatment to improve the treatment efficiency, and when the removal rate decreases, the series treatment method is adopted for superimposed treatment of the removal rate.

[0088] After the 2-MIB treatment, it is input into the aerator 300 for aeration treatment.

[0089] It should be noted that in this text, relational terms such as first and second are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply any actual relationship or order between these entities or operations. Moreover, the term "comprising", "including" or any other variant thereof is intended to cover non-exclusive inclusion, such that a process, method, article or device comprising a series of elements not only includes those elements but also includes other elements not expressly listed, or elements inherent to such process, method, article or device.

[0090] Although the embodiments of the present invention have been shown and described, those of ordinary skill in the art can understand that various changes, modifications, substitutions and variations can be made to these embodiments without departing from the principles and spirit of the present invention. The scope of the present invention is defined by the appended claims and their equivalents.

Claims

1. A device for removing dimethyl isoborneol from drinking water, comprising an air dissolving pump (100) and an air flotation treatment machine (200), wherein a water delivery pipe (101) and an air dissolving pipe (102) of the air dissolving pump (100) are connected to the air flotation treatment machine (200), and fine bubbles are dissolved in water and transported to the air flotation treatment machine (200), characterized in that: The dimethyl isoborneol removal device further comprises a secondary removal module (400), wherein the secondary removal module (400) is connected to the air dissolving pump (100) and is used for further filtering soluble impurities including dimethyl isoborneol in the air flotation treated water; an aerator (300) connected to the output end of the secondary removal module (400) to perform aeration treatment on the filtered water; The secondary removal module (400) is provided with at least four layers for continuously or in parallel treating drinking water; Two adjacent secondary removal modules (400) are connected via a stop valve 1 (401) and a three-way pipe (402), and two adjacent three-way pipes (402) are controlled to be cut off or connected via a stop valve 2 (403), and a handwheel valve is provided at the connection port between the three-way pipe (402) and the secondary removal module (400).

2. A dimethyl isoborneol removal device for drinking water production according to claim 1, characterized in that: One end of the secondary removal module (400) can serve as an input port for water to be treated, and the filtered water enters through the three-way pipe (402) at one end and is discharged through the three-way pipe (402) at the other end for parallel treatment.

3. A dimethyl isoborneol removal device for drinking water production according to claim 1, characterized in that: The secondary removal module (400) located at the top layer can serve as an output port for water to be treated. The filtered water is input into the water inlet at its top. After being treated once inside, the water is introduced into other secondary removal modules (400) through the cooperation between the stop valve 1 (401) and the three-way pipe (402) or the cooperation between the three-way pipe (402) and the stop valve 2 (403).

4. A dimethyl isoborneol removal device for drinking water production according to claim 2 or 3, characterized in that: The flotation treatment machine (200) comprises three chambers arranged therein, namely a slag chamber (202), a slag removal chamber (203) and a drainage box (204); the partition (201) is connected to the slag chamber (202); water input into the slag chamber 2 (02) enters the slag removal chamber (203) by passing over the top of the partition; the slag removal chamber 2 (03) injects the water subjected to the flotation treatment into the drainage box (204) through a water pipe arranged at the bottom of the chamber; the flotation treatment machine (200) further comprises a slag transport line (206) arranged at the top for removing flotation impurities; The water in the drainage tank (204) is pumped into the secondary removal module (400).

5. A device for removing dimethyl isoborneol from drinking water according to claim 4, characterized in that: A baffle (207) is also provided above the slag chamber (202), the baffle (207) comprising a slope surface and a concave surface, the concave surface and the inner wall of the air flotation treatment machine (200) together form a collection chamber (205), and the hanging plate on the slag transport line (206) cooperates with the slope surface of the baffle (207) to guide the air flotation impurities into the collection chamber (205); An activated carbon cotton layer (208) is provided in the middle of the slag removal chamber (203), and the activated carbon cotton layer (208) is located above the water pipe in the slag removal chamber (203).

6. A device for removing dimethyl isoborneol from drinking water according to claim 5, characterized in that: The secondary removal module (400) comprises a filter module formed by connecting a plurality of filter mechanisms (404) end to end, wherein the filter mechanism (404) comprises a removal layer (4041), an elastic water-permeable membrane (4042) and a water-permeable support (4043) covering the removal layer (4041), and a sealing sheet (4044) is used to seal the joints between two adjacent filter mechanisms (404); A second sub-rigid microporous filter material (409) is coaxially arranged inside the filtering mechanism (404) for supporting it, and the three-way pipe (402) is connected to the second sub-rigid microporous filter material (409).

7. A device for removing dimethyl isoborneol from drinking water according to claim 6, characterized in that: The outside of the elastic water-permeable membrane (4042) is pressed against the front and rear ends of the filter mechanism (404) through a front end clamp (405) and a rear end clamp (406), respectively, and the front end clamp (405) also includes a plurality of pressure rods (4051); The head end clamp (405), the tail end clamp (406) and the water-permeable support (4043) cooperate to lay out the removal layer (4041) in a sinusoidal wave shape, and the pressure rod (4051) presses the elastic water-permeable membrane (4042) onto the trough line.

8. The device for removing dimethyl isoborneol from drinking water according to claim 7, characterized in that: A circle of sub-rigid microporous filter material 1 (408) is also arranged on the periphery of the head end clamp (405) and the tail end clamp (406), and two convex ridges are arranged on the inner side of the sub-rigid microporous filter material 1 (408) to support the head end clamp (405) and the tail end clamp (406) above them; The outer periphery of the sub-rigid microporous filter material 1 (408) is the outer shell (407), and the inner periphery of the outer shell (407) is also provided with ridges to support the sub-rigid microporous filter material 1 (408) upward.

9. The device for removing dimethyl isoborneol from drinking water according to claim 8, characterized in that: The removal layer (4041) is composed of a fiber layer wrapped with an adsorbent; The removal layer (4041) is laid in a three-layer composite manner, the outermost layer and the innermost layer have a thickness between 1.5 and 2 mm, the outermost layer is made of coarse fiber, and the innermost layer is made of nanofiber layer; The middle layer is an adsorbent-loaded fiber layer with a thickness of 6-8 mm. The fiber diameter of the middle layer is between 0.1-0.15 mm, and the diameter of each fiber bundle does not have to be the same.

10. The device for removing dimethyl isoborneol from drinking water according to claim 9, characterized in that: The adsorbent is made of 200-mesh modified activated carbon and nano-iron oxide in a 4:1 ratio, and the mass ratio of the adsorbent to the fiber bundle is 0.8:1-1.5:1, which is used to maintain the pressure drop and prevent excessive loss during backwashing.

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