Device for removing dimethyl isoralin in drinking water production

Abstract

The application belongs to the technical field of 2-MIB removal, and discloses a 2-methylisobornyl alcohol removal device for drinking water production, which comprises a dissolved air pump and a flotation treatment machine. The water delivery pipe and the dissolved air pipe of the dissolved air pump are communicated with the flotation treatment machine, fine air bubbles are dissolved in water and delivered to the flotation treatment machine. The 2-methylisobornyl alcohol removal device further comprises a secondary removal module, which is communicated with the dissolved air pump and is used for further filtering soluble impurities including 2-methylisobornyl alcohol in the water treated by flotation. The cooperation between the stop valve one, the three-way pipe and the stop valve two of the multilayer secondary removal module can switch the parallel treatment mode with relatively fast initial efficiency and the series treatment mode with relatively high removal rate. 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 adsorptions. Compared with the prior art, the removal strategy is variable, and the adaptability to working conditions is strong.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of 2-MIB removal, and particularly relates to a 2-methylisoborneol removal device for drinking water production. BACKGROUND

[0002] 2-methylisoborneol (hereinafter referred to as 2-MIB) is a common harmful substance in drinking water, which can stimulate the eyes and respiratory tract, cause tearing, coughing and even shortness of breath, and is a potential carcinogen, long-term exposure to which can increase the risk of cancer and cause kidney damage. Therefore, it is one of the harmful substances that need to be removed from drinking water.

[0003] The currently used removal device is a continuous treatment device, that is, the drinking water passes through the filter layer of the device, and the 2-MIB in the water is adsorbed and removed by activated carbon. Usually, after continuous treatment for hundreds of hours, the adsorption effect will decrease significantly, and then the filter layer needs to be replaced for continuous removal work, which has relatively low efficiency. Alternatively, the adsorbent is directly mixed with water, and after adsorption is completed, the adsorbent and water are separated by filtration treatment. Compared with the former method, the removal efficiency is relatively high, but the post-treatment speed is relatively slow due to the addition of a filtration process (such as the invention patent disclosed in application No. 202210843678.0). Therefore, the present application provides a 2-methylisoborneol removal device for drinking water production to overcome the above-mentioned defects. SUMMARY

[0004] To solve the problems in the background art, the present application provides a 2-methylisoborneol removal device for drinking water production.

[0005] To achieve the above-mentioned purposes, the present application provides the following technical solution: a 2-methylisoborneol removal device for drinking water production, comprising a dissolved air pump and a flotation treatment machine, wherein the water delivery pipe and the dissolved air pipe of the dissolved air pump are communicated with the flotation treatment machine, fine air bubbles are dissolved in water and delivered to the flotation treatment machine, and the 2-methylisoborneol removal device further comprises a secondary removal module, which is communicated with the flotation treatment machine for further filtering soluble impurities including 2-methylisoborneol in the water treated by the flotation treatment machine.

[0006] An aerator is communicated with the output end of the secondary removal module to perform aeration treatment on the water filtered by the secondary removal module.

[0007] The secondary removal module is provided with at least four layers for continuous treatment or parallel treatment of the drinking water.

[0008] The adjacent two secondary removal modules are communicated through a stop valve one and a three-way pipe, the adjacent two three-way pipes are controlled to be cut off or connected through a stop valve two, and the communication port of the three-way pipe and the secondary removal module is provided with a handwheel valve.

[0009] Preferably, one end of the secondary removal module can serve as an input port for water to be treated, and filtered water enters through one end of the tee joint and is discharged through the other end of the tee joint for parallel processing.

[0010] Preferably, the uppermost secondary removal module can serve as an output port for water to be treated, and filtered water enters through the water inlet at the top end thereof, and after being processed once inside, the water is introduced into other secondary removal modules through the cooperation of the stop valve one and the tee joint or the cooperation between the tee joint and the stop valve two.

[0011] Preferably, the air floatation processor includes three cabins, namely a scum chamber, a residue removal chamber, and a drainage tank, a partition plate is connected to the scum chamber, and water input into the scum chamber enters the residue removal chamber by passing over the top of the partition plate, the residue removal chamber injects water treated by air floatation into the drainage tank through a water pipe arranged at the bottom of the chamber, and the air floatation processor further includes a residue removal line arranged at the top for removing air floatation impurities.

[0012] The water in the drainage tank is pumped into the secondary removal module.

[0013] Preferably, the upper part of the scum chamber is further provided with a baffle, the baffle includes a slope surface and a concave surface, the concave surface and the inner wall of the air floatation processor form a collection chamber, and the hanging plate on the residue removal line cooperates with the slope surface of the baffle to guide the air floatation impurities into the collection chamber.

[0014] The middle part of the residue removal chamber is provided with an activated carbon cotton layer, and the activated carbon cotton layer is located above the water pipe in the residue removal chamber.

[0015] Preferably, the secondary removal module includes a filter module composed of a plurality of filter mechanisms connected end to end, the filter mechanism includes a removal layer and an elastic water-permeable film and a water-permeable support covering the removal layer therebetween, and the adjacent two filter mechanisms are sealed at the joint through a sealing sheet.

[0016] A second sub-coaxial rigid micro-porous filter is arranged inside the filter mechanism for supporting the filter mechanism, and the tee joint is connected to the second sub-coaxial rigid micro-porous filter.

[0017] Preferably, the outer part of the elastic water-permeable film is pressed against the first end and the second end of the filter mechanism through a first end clamp and a second end clamp respectively, and the first end clamp further includes a plurality of pressing rods.

[0018] The first end clamp, the second end clamp, and the water-permeable support cooperate to arrange the removal layer in a sinusoidal shape, and the pressing rods press the elastic water-permeable film against the trough line.

[0019] Preferably, the outer periphery of the head and tail end clamps is further provided with a ring of sub-rigid microporous filter material one, the inner side of which is provided with two ridges to support the head and tail end clamps thereon.

[0020] The outer periphery of the sub-rigid microporous filter material one is the shell, and the inner periphery of the shell is also provided with a ridge to support the sub-rigid microporous filter material one thereon.

[0021] Preferably, the removal layer is composed of a layer of fiber filaments wrapped with adsorbent;

[0022] The removal layer is a three-layer composite, the outermost layer and the innermost layer are between 1.5-2mm in thickness, the outermost layer uses thick fibers, and the innermost layer uses a nanofiber layer;

[0023] The middle layer is an adsorbent-loaded fiber layer with a thickness of 6-8mm, the fiber diameter of the middle layer is between 0.1-0.15mm, and the diameter of each fiber filament bundle does not have to be the same.

[0024] Preferably, the adsorbent is a mixture of 200-mesh modified activated carbon and nano-iron oxide in a ratio of 4:1, and the mass ratio of adsorbent to fiber filament bundle is 0.8:1-1.5:1, to maintain the pressure drop and prevent excessive loss during backwashing.

[0025] Compared with the prior art, the beneficial effects of the present application are as follows:

[0026] The present application sets up a multi-layer secondary removal module, guides the water after air floatation treatment into the multi-layer secondary removal module, and through the cooperation between the stop valve one, three-way pipe and stop valve two of the multi-layer secondary removal module, the parallel processing mode with faster initial efficiency and the series processing mode with higher removal rate can be switched, and the parallel processing method can be used in the first 100 hours of treatment according to the working condition. When the adsorption efficiency decreases, the series processing method is used to further improve the removal rate of 2-MIB through at least two adsorptions. Compared with the prior art, the removal strategy is variable and has strong adaptability to working conditions.

[0027] The application directly transports water treated by air dissolving into a scum chamber through a pipeline, the liquid level of the water is raised to pass over the top of the partition plate into the scum removal chamber, at this time, the bubbles dissolved in the water are released in this process to wrap the large particle impurities in the water and float on the water surface, and flow into the scum removal chamber with the liquid level. The scraper on the scum removal line slowly pushes away the bubbles and impurities for unified collection, and an activated carbon cotton layer is arranged in the scum removal chamber for preliminary removal treatment of the water body to reduce the concentration of 2-MIB. The application sets an adsorption layer as a mixed coating layer of fiber filaments and adsorbents, and constructs a three-dimensional adsorption network. The traditional technology is relatively dependent on the random accumulation of adsorbent particles, and the porosity is relatively low, but in the application, the complex interlayer channel is constructed by directional arrangement of fibers, and the porosity is greatly increased, about 62-68%. And the loading rate of activated carbon in the general filter carrier is greatly improved, and the 2-MIB removal rate is also significantly improved. And it is arranged in a sinusoidal wave shape to increase the water surface and improve the removal efficiency. BRIEF DESCRIPTION OF DRAWINGS

[0028] Figure 1 It is a structural schematic diagram of the application;

[0029] Figure 2 It is a front view of the application;

[0030] Figure 3 It is an internal schematic diagram of the air floatation treatment machine of the application;

[0031] Figure 4 It is a partial sectional view of the secondary removal module of the application;

[0032] Figure 5 It is a structural sectional view of the filter mechanism of the application;

[0033] Figure 6 It is an enlarged schematic diagram of part A of the application; Figure 5

[0034] Figure 7 It is a structural exploded view of the secondary removal module of the application;

[0035] Figure 8 ​This is a schematic diagram of the longitudinal arrangement of the fiber filaments of the present invention. In the diagram: 100, dissolved air pump; 101, water supply pipe; 200, air flotation treatment machine; 202, scum chamber; 203, scum removal chamber; 204, drainage tank; 205, collection chamber; 206, scum conveying line; 207, baffle; 208, activated carbon cotton layer; 300, aerator; 400, secondary removal module; 401, stop valve one; 402, tee pipe; 403, stop valve two; 404, filtration mechanism; 4041, removal layer; 4042, elastic permeable membrane; 4043, permeable support; 4044, sealing sheet; 405, head clamp; 4051, pressure rod; 406, tail clamp; 407, outer shell; 408, subrigid microporous filter material one; 409, subrigid microporous filter material two. Detailed Implementation

[0036] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0037] like Figures 1 to 8 As shown, the present invention provides a dimethyl isoborneol removal device for drinking water production, including a dissolved air pump 100 and an air flotation treatment machine 200. The water supply pipe 101 and the dissolved air pipe of the dissolved air pump 100 are connected to the air flotation treatment machine 200 to dissolve microbubbles in water and transport them to the dissolved air pump 100. The dimethyl isoborneol removal device also includes a secondary removal module 400, which is connected to the air flotation treatment machine 200 for further filtering soluble impurities, including dimethyl isoborneol, from the water treated by air flotation.

[0038] Aerator 300 is connected to the output of secondary removal module 400 to aerate the filtered water.

[0039] The secondary removal module 400 has at least four layers for continuous or parallel treatment of drinking water;

[0040] Two adjacent secondary removal modules 400 are connected by a stop valve 401 and a three-way pipe 402. Two adjacent three-way pipes 402 are controlled to be cut off or connected by a stop valve 403. A handwheel valve is provided at the connection port between the three-way pipe 402 and the secondary removal module 400.

[0041] The drinking water is injected through the water pipe 101, and is gathered to the dissolved air pipe. The gas is dissolved in the flowing water through the dissolved air pump 100, and is injected into the air float treatment machine 200 to perform air float treatment, so as to remove the insoluble particulate impurities therein. The treated water is pumped into the secondary removal module 400 to perform 2-MIB removal treatment. The secondary removal module 400 is provided with multiple layers, and the treatment mode can be switched between continuous treatment and parallel treatment through the cut-off valve one 401, the three-way pipe 402, the cut-off valve two 403, and the hand wheel valve arranged at the communication port. The parallel treatment method is adopted in the initial treatment to improve the treatment efficiency, and the series treatment method is adopted to perform superimposed treatment when the removal rate is reduced. After the 2-MIB treatment, the water is input into the aerator 300 to perform aeration treatment.

[0042] As shown in Figure 2 , one end of the secondary removal module 400 can be used as an input port of the water to be treated. The filtered water enters through one end of the three-way pipe 402, and is discharged through the other end of the three-way pipe 402 to perform parallel treatment.

[0043] In this embodiment, the parallel treatment method is adopted. The water after the air float treatment machine 200 treatment is introduced into the three-way pipe 402 side inlet, and the water inlet directly connected with the secondary removal module 400 is closed by the hand wheel valve. The water enters into each layer of the secondary removal module 400 to perform 2-MIB removal treatment. The treated water flows out from the other end of the secondary removal module 400, and finally enters the aerator 300 to perform aeration treatment. The parallel treatment method can accelerate the synchronous water treatment flow and improve the treatment efficiency. When the removal rate of the filter material in the secondary removal module 400 for 2-MIB is reduced, the hand wheel valve is opened, the water inlet is switched to the top layer of the secondary removal module 400, and the water flows into other secondary removal modules 400 from top to bottom through the three-way pipe 402 and the cut-off valve one 401, so as to perform multiple superimposed treatments to further remove 2-MIB in the water.

[0044] As shown in Figure 2 and Figure 3 , the uppermost layer of the secondary removal module 400 can be used as an output port of the water to be treated. The filtered water is input through the water inlet at the top end thereof, and is introduced into other secondary removal modules 400 after being treated once in the internal thereof through the cooperation of the cut-off valve one 401 and the three-way pipe 402 or the cooperation between the three-way pipe 402 and the cut-off valve two 403.

[0045] In the embodiment, the water after the air floatation treatment is guided to the uppermost secondary removal module 400 for the first filtration treatment. Then the treated water is guided into other secondary removal modules 400 for further treatment through the cooperation of the stop valve one 401 and the three-way pipe 402 or the cooperation between the three-way pipe 402 and the stop valve two 403. Or when some of the secondary removal modules 400 are overworked, the cooperation between the three-way pipe 402 and the stop valve two 403 changes the guiding object to switch into other normal secondary removal modules 400 for further filtration treatment.

[0046] As shown in Figure 3 The air floatation treatment machine 200 includes three cabins of the scum chamber 202, the deslag chamber 203 and the drainage tank 204 arranged inside, the baffle is communicated with the scum chamber 202, the water input into the scum chamber 202 enters the deslag chamber 203 by crossing the top of the baffle, the deslag chamber 203 injects the water after the air floatation treatment into the drainage tank 204 through the water pipe arranged at the bottom of the chamber body, and the air floatation treatment machine 200 further includes the deslag conveying line 206 arranged at the top for removing the air floatation impurities.

[0047] The water in the drainage tank 204 is pumped into the secondary removal module 400.

[0048] The water after the air floatation treatment is directly conveyed into the scum chamber 202 through the pipeline, the liquid level of the water crosses the top of the baffle to enter the deslag chamber 203 as the liquid level is increased, at this time, the bubbles dissolved in the water are released in the process to wrap the large-particle impurities on the water surface and flow into the deslag chamber 203 together with the liquid level. The scraper on the deslag conveying line 206 slowly pushes away the bubbles and the impurities for unified collection. The pipeline communicated between the deslag chamber 203 and the drainage tank 204 is further arranged below the deslag chamber 203, the pipeline extends into the drainage tank 204 at a height lower than the liquid level in the scum chamber 202 and the deslag chamber 203. And the drainage flow in the drainage tank 204 and the water inflow in the scum chamber 202 are intelligently controlled through the water supply system to keep the liquid level of the scum chamber 202 and the deslag chamber 203 above the baffle, thereby ensuring the normal treatment of the air floatation impurities by the baffle.

[0049] As shown in Figure 3 The upper part of the scum chamber 202 is further provided with the baffle 207, the baffle 207 includes a slope surface and a concave surface, the concave surface and the inner wall of the air floatation treatment machine 200 form the collection chamber 205, and the hanging plate on the deslag conveying line 206 cooperates with the slope surface of the baffle 207 to guide the air floatation impurities into the collection chamber 205.

[0050] The middle part of the slag removal cavity 203 is provided with an activated carbon layer 208, and the activated carbon layer 208 is located above the water pipe in the slag removal cavity 203.

[0051] The row trajectory of the scraper on the slag conveying line 206 is attached to the slope surface of the baffle 207. During the operation of the slag conveying line 206, the gas floating impurities on the liquid surface of the slag removal cavity 203 are pushed to the collecting cavity 205, fall on the slope surface of the baffle 207, and finally fall into the collecting cavity 205 for unified collection and treatment.

[0052] The activated carbon layer 208 is arranged in the middle part of the slag removal cavity 203 for treating the drinking water permeating downward, and preliminarily adsorbing 2-MIB to reduce the initial concentration of 2-MIB in the drinking water. The activated carbon layer 208 is arranged in a quick-release structure, and can normally perform the preliminary adsorption work in a treatment process of the quantitative drinking water. After the treatment of the quantitative water is completed, the activated carbon layer 208 is disassembled and replaced with a new activated carbon layer 208.

[0053] As shown in Figure 5 and 6 , the secondary removal module 400 includes a filter module composed of a plurality of filter mechanisms 404 connected end to end. The filter mechanism 404 includes a removal layer 4041 and an elastic water-permeable film 4042 and a water-permeable support 4043 covering the removal layer 4041. The sealing sheet 4044 is used for sealing the joint between the two adjacent filter mechanisms 404.

[0054] The inside of the filter mechanism 404 is coaxially provided with a sub-rigid microporous filter material two 409 for supporting it. The three-way pipe 402 is connected to the sub-rigid microporous filter material two 409.

[0055] Each filter mechanism 404 has a length of about 35 cm, and the two filter mechanisms 404 are connected end to end. The sealing sheet 4044 is used for sealing the joint between the two adjacent filter mechanisms 404. The end of the sub-rigid microporous filter material two 409 is pressed on the sealing sheet 4044. The sub-rigid microporous filter material two 409 in the two adjacent filter mechanisms 404 is connected. The inlet of the three-way pipe 402 arranged at the end of the secondary removal module 400 is connected to the inside of the sub-rigid microporous filter material two 409. The sub-rigid microporous filter material two 409 at the two ends is sealed with the end cover.

[0056] The sub-rigid microporous filter material one 408 mainly isolates the remaining insoluble impurities from the incomplete gas floating treatment. The pore size of the sub-rigid microporous filter material two 409 is larger than that of the sub-rigid microporous filter material one 408, which is used to balance the water pressure, and mainly plays a role of internal support.

[0057] After initial flotation treatment, the 2-MIB in the drinking water enters the inner side of the subrigid microporous filter media 409 via the filtration mechanism 404, where it removes the 2-MIB from the drinking water. The treated water then flows through the three-way pipe 402 into other processes.

[0058] like Figures 5-7 As shown, the outer surface of the elastic permeable membrane 4042 is pressed against the first and last ends of the filter mechanism 404 by the first end clamp 405 and the last end clamp 406 respectively. The first end clamp 405 also includes several pressure rods 4051.

[0059] The head clamp 405, tail clamp 406 and permeable support 4043 work together to lay the removal layer 4041 in a sinusoidal wave pattern, and the pressure bar 4051 presses the elastic permeable membrane 4042 onto the trough line.

[0060] The head clamp 405 and tail clamp 406 directly press the elastic permeable membrane 4042 onto the removal layer 4041, making it adhere to the removal layer 4041. Laying the removal layer 4041 in a sine wave pattern helps to expand the filtration area and can extend the water flow path by 1.5-1.7 times.

[0061] The first end clamp 405 and the last end clamp 406 have the same specifications. The pressure rod 4051 is set on the trough of the first end clamp 405. The pressure rod 4051 extends along the axis of the filter mechanism 404 and presses directly on the trough line of the filter mechanism 404, so that the elastic permeable membrane 4042 is firmly attached.

[0062] like Figure 5 As shown, a ring of subrigid microporous filter material 408 is also provided around the front end clamp 405 and the rear end clamp 406. Two protruding ribs are provided on the inner side of the subrigid microporous filter material 408 to support the front end clamp 405 and the rear end clamp 406 above it.

[0063] The outer periphery of the subrigid microporous filter material 408 is the outer shell 407, and the inner circumference of the outer shell 407 is also provided with protruding ridges to support the subrigid microporous filter material 408 on top.

[0064] The aforementioned protrusions can be hollow to allow water flow, and the protrusions themselves serve a positioning and supporting function. During installation, they can be directly pushed into the outer casing 407 along the protrusions, or they can be directly pulled out during disassembly.

[0065] like Figure 8 As shown, the removal layer 4041 is composed of a layer of fibers coated with adsorbent;

[0066] The 4041 removal layer is a three-layer composite layer. The outermost and innermost layers are between 1.5-2mm thick. The outermost layer uses coarse fibers, and the innermost layer uses nanofibers.

[0067] The intermediate layer is an adsorbent-loaded fiber layer with a thickness of 6-8 mm, the fiber diameter of the intermediate layer is between 0.1-0.15 mm, and the diameter of each fiber bundle does not have to be the same.

[0068] The adsorbent and the fiber layer can be coated by electrospinning, and a three-layer composite laying means is used to intercept larger particle impurities and flocculent impurities, balance the water flow resistance, and control the loss of adsorbent.

[0069] The diameter of each fiber bundle does not have to be different, which is used to improve the complexity of the pores in the fiber layer.

[0070] The adsorbent is mixed by 200 mesh modified activated carbon and nano iron oxide in a ratio of 4:1, and the mass ratio of adsorbent to fiber bundle is 0.8:1-1.5:1, which is used to maintain the pressure drop and prevent excessive loss of backwashing.

[0071] Under the accelerated life test results:

[0072] After continuous operation for 120 h at a high flow rate of 10 m / h, the 2-MIB removal rate decreases from 82% to 76% (12 kPa / m) when the mass ratio of adsorbent to fiber bundle is 1:2;

[0073] The 2-MIB removal rate decreases from 91% to 85% (18 kPa / m) when the mass ratio of adsorbent to fiber bundle is 1:1.5;

[0074] The 2-MIB removal rate decreases from 96% to 88% (27 kPa / m) when the mass ratio of adsorbent to fiber bundle is 1:1.2, and the amount of carbon powder loss is less than 0.3 mg / L.

[0075] However, when the mass ratio of adsorbent to fiber bundle is higher than 1:0.8, the fiber voids will be blocked (pressure grouting > 50 kPa / m);

[0076] When the mass ratio of adsorbent to fiber bundle is lower than 1:1.5, the adsorption capacity is obviously insufficient.

[0077] Therefore, the preferred embodiment is around 1:1.2.

[0078] Of course, the intermediate layer of the composite layer mentioned above can still use a gradient loading structure, and the front end layer (water inlet side), the middle layer and the end layer are set respectively, and the mass ratio between the layers is different to optimize the strategy.

[0079] The mass ratio of adsorbent to fiber bundle in the front end layer is 1:1.2, which is used to correspond to the initial high concentration of 2-MIB (> 100 ng / L) by high adsorption capacity;

[0080] The middle layer adsorbent and fiber bundle mass ratio is 1:1.5, to balance adsorption and water flow resistance;

[0081] The end layer adsorbent and fiber bundle mass ratio is 1:0.9, to set a dense layer to intercept carbon powder loss.

[0082] The working principle and use process of the present application are as follows:

[0083] Drinking water is injected through the water pipe 101, converged to the dissolved gas pipe, the gas is dissolved in the water by the dissolved gas pump 100, and then injected into the air floatation treatment machine 200 for air floatation treatment to remove insoluble particulate impurities. The treated water is pumped into the secondary removal module 400 for 2-MIB removal treatment.

[0084] The secondary removal module 400 is provided with multiple layers, and the treatment mode can be switched by the stop valve one 401, the three-way pipe 402, the stop valve two 403 and the hand wheel valve arranged at the communication port, to switch between continuous treatment and parallel treatment according to the working condition. The parallel treatment method is used for initial treatment to improve the treatment efficiency, and the series treatment method is used for superimposed treatment when the removal rate decreases.

[0085] After 2-MIB treatment, the water is input into the aerator 300 for aeration treatment.

[0086] It should be noted that, in the present text, relational terms such as first and second and the like can only be used to distinguish one entity or action from another entity or action, without necessarily requiring or implying any such actual relationship or order between these entities or actions. Moreover, the terms "comprises", "comprising", or any other variant thereof are intended to cover non-exclusive inclusions, so that a process, method, article, or apparatus that comprises a list of elements does not only include those elements, but also other elements not explicitly listed, or other elements inherent to such a process, method, article, or apparatus. Although embodiments of the present application have been shown and described, it will be understood by those of ordinary skill in the art that various changes, modifications, substitutions and alterations can be made thereto without departing from the principles and spirit of the present application, the scope of which is defined by the appended claims and their equivalents.

Claims

1. A device for removing dimethyl isobornyl alcohol in drinking water production, comprising a dissolved air pump (100) and a flotation treatment machine (200), the water delivery pipe (101) and the dissolved air pipe of the dissolved air pump (100) are communicated with the flotation treatment machine (200), the micro-bubbles are dissolved in water and delivered to the flotation treatment machine (200), the drinking water is injected through the water delivery pipe (101), the water is gathered to the dissolved air pipe, the air is dissolved in the water by the dissolved air pump (100), and then the water is injected into the flotation treatment machine (200) for flotation treatment, characterized in that: The dimethyl isobornyl alcohol removal device further comprises a secondary removal module (400) in communication with the air floatation processor (200) for further filtering soluble impurities including dimethyl isobornyl alcohol in the air floatation processed water; ​ An aerator (300) in communication with the output end of the secondary removal module (400) for aerating the filtered water; The secondary removal module (400) is provided with at least four layers for continuous or parallel processing of the drinking water; Two adjacent secondary removal modules (400) are in communication through a stop valve I (401) and a three-way pipe (402), and two adjacent three-way pipes (402) are in communication or cut off through a stop valve II (403), and the communication port of the three-way pipe (402) and the secondary removal module (400) is provided with a hand wheel valve; The secondary removal module (400) comprises a filter module composed of a plurality of filter mechanisms (404) connected end to end, the filter mechanism (404) comprises a removal layer (4041) and an elastic water-permeable film (4042) and a water-permeable support (4043) wrapping the removal layer (4041), and the adjacent two filter mechanisms (404) are sealed at the joint through a sealing sheet (4044); The outer part of the elastic water-permeable film (4042) is pressed at the first end and the tail end of the filter mechanism (404) through a first end hoop (405) and a tail end hoop (406), and the first end hoop (405) further comprises a plurality of pressing rods (4051); The first end hoop (405), the tail end hoop (406) and the water-permeable support (4043) cooperate to arrange the removal layer (4041) in a sinusoidal shape, and the pressing rods (4051) press the elastic water-permeable film (4042) on the valley line; The removal layer (4041) is composed of a fiber filament layer wrapped with an adsorbent; The removal layer (4041) is a three-layer composite, the outermost layer and the innermost layer have a thickness of 1.5-2 mm, the outermost layer uses coarse fibers, and the innermost layer uses a nanometer fiber 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 0.1-0.15 mm, the adsorbent is a mixture of 200 mesh modified activated carbon and nano iron oxide in a ratio of 4:1, and the mass ratio of the adsorbent to the fiber filament bundle is 0.8:1-1.5:

1.

2. The device for removing dimethyl isosorbide from drinking water according to claim 1, characterized in that: One end of the secondary removal module (400) can serve as an input port for the water to be processed, and the filtered water enters one end of the three-way pipe (402) and is discharged from the other end of the three-way pipe (402) for parallel processing.

3. The device for removing dimethyl isosorbide from drinking water according to claim 1, characterized in that: The uppermost secondary removal module (400) can serve as an output port for the water to be processed, and the filtered water is input into the water inlet at the top end, and after being processed once, the water is introduced into other secondary removal modules (400) through the cooperation of the stop valve I (401) and the three-way pipe (402) or the cooperation between the three-way pipe (402) and the stop valve II (403).

4. A device for removing dimethyl isosorbide from drinking water according to claim 2 or 3, characterized in that: The air floatation treatment machine (200) comprises three cabins of a scum chamber (202), a deslag chamber (203) and a drainage tank (204) arranged inside the air floatation treatment machine (200), a partition plate is communicated with the scum chamber (202), water input into the scum chamber (202) enters into the deslag chamber (203) by crossing the top of the partition plate, the deslag chamber (203) injects water treated by air floatation into the drainage tank (204) through a water pipe arranged at the bottom of the chamber, and the air floatation treatment machine (200) further comprises a deslag conveying line (206) arranged at the top for removing air floatation impurities. Water in the drainage tank (204) is pumped into the secondary removal module (400).

5. A device for removing dimethyl isosorbide from drinking water according to claim 4, characterized in that: The scum chamber (202) is further provided with a baffle (207) above the scum chamber (202), the baffle (207) comprises a slope surface and a concave surface, the concave surface and the inner wall of the air floatation treatment machine (200) form a collecting chamber (205), and the hanging plate on the deslag conveying line (206) cooperates with the slope surface of the baffle (207) to guide air floatation impurities into the collecting chamber (205). The middle part of the deslag chamber (203) is provided with an activated carbon cotton layer (208), and the activated carbon cotton layer (208) is located above the water pipe in the deslag chamber (203).

6. A device for removing dimethyl isosorbide from drinking water according to claim 5, characterized in that: The inside of the filter mechanism (404) is coaxially provided with a second sub-rigid microporous filter material (409) for supporting the filter mechanism (404), and the three-way pipe (402) is communicated into the second sub-rigid microporous filter material (409).

7. The device for removing dimethyl isosorbide from drinking water according to claim 1, characterized in that: The periphery of the first end hoop (405) and the tail end hoop (406) is further provided with a ring of first sub-rigid microporous filter material (408), and the inner side of the first sub-rigid microporous filter material (408) is provided with two convex edges to support the first end hoop (405) and the tail end hoop (406) above the first sub-rigid microporous filter material (408). The periphery of the first sub-rigid microporous filter material (408) is the shell (407), and the inner periphery of the shell (407) is also provided with a convex edge to support the first sub-rigid microporous filter material (408) above the first sub-rigid microporous filter material (408).

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