CN113301977B - Water treatment filter and method for manufacturing same - Google Patents
Water treatment filter and method for manufacturing same Download PDFInfo
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- CN113301977B CN113301977B CN201980088634.8A CN201980088634A CN113301977B CN 113301977 B CN113301977 B CN 113301977B CN 201980088634 A CN201980088634 A CN 201980088634A CN 113301977 B CN113301977 B CN 113301977B
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Abstract
The present invention relates to a water treatment filter and a method for manufacturing the same. More particularly, the present invention relates to a water treatment filter and a method of manufacturing the same, the method comprising the steps of: mixing a positive charge additive, glass fibers, binder fibers, cellulose, zeolite powder, and water; and molding the resulting mixture.
Description
Technical Field
The present invention relates to a water treatment filter and a method of manufacturing the same, and more particularly, to a water treatment filter including a positive charge additive, glass fibers, binder fibers, cellulose, and zeolite to effectively remove hardness substances and various contaminants in water, and a method of manufacturing the same.
Background
Water treatment filters are used to remove various contaminants contained in water. In the primary removal mechanism, contaminants are removed by a sieving effect, in which material having a size larger than the pore size in the filter does not pass through the filter and material having a size smaller than the pore size passes through the filter.
Generally, water treatment filters are applied to air purifiers used in water purification plants, sewage treatment plants, various industrial sites, and offices or homes.
The filter can be mainly divided into a reverse osmosis membrane, a nanofiltration membrane, an ultrafiltration membrane and a microfiltration membrane. Since the pore size of each of the ultrafiltration membrane and the microfiltration membrane is relatively large, the permeation performance of each of the ultrafiltration membrane and the microfiltration membrane is excellent and it is difficult to remove fine particles. Both reverse osmosis membranes and nanofiltration membranes are capable of removing very small particles. However, the permeation performance of each of the reverse osmosis membrane and the nanofiltration membrane is relatively low, and water needs to be supplied at high pressure. As a result, maintenance expenses such as power ratio and installation cost are high.
Meanwhile, hardness-inducing materials represented by calcium and magnesium are contained in water in a dissolved state. In particular, a large amount of such hard materials is dissolved in groundwater. Since high hardness water forms scale in pipes, high hardness water is not suitable for industrial water as well as drinking water in many cases.
Chemicals may be injected, adsorption using ion exchange resins may be performed, or filtration using a reverse osmosis membrane or a nanofiltration membrane may be performed as a hardness removal method. However, as described above, the maintenance cost of the reverse osmosis membrane or the nanofiltration membrane is high, and chemicals or ion exchange resins require additional equipment. Therefore, there is a limitation in application to small-scale water treatment products such as water purifiers.
(Prior art documents)
(patent document 1) Korean patent application publication No. 2005-0126143
(patent document 2) Korean registered patent publication No. 1470620
Disclosure of Invention
Technical problem
The present invention has been made in view of the above problems, and it is an object of the present invention to provide a method of manufacturing a water treatment filter capable of effectively removing hardness-inducing material and contaminants contained in water.
It is another object of the present invention to provide a filter capable of simultaneously removing contaminants and hardness-inducing materials contained in water.
Technical scheme
In order to achieve the above object, a method of manufacturing a water treatment filter according to the present invention includes: a step of mixing the positive charge additive, the glass fiber, the binder fiber, the cellulose, the zeolite powder, and water with each other; and a shaping step.
The step of mixing the positive charge additive, the glass fiber, the binder fiber, the cellulose, the zeolite powder and the water with each other may include the steps of: i) A step of mixing a positive charge additive and water with each other to prepare a first mixture; ii) a step of mixing glass fibers, water and binder fibers with each other to prepare a second mixture; iii) A step of mixing water and cellulose with each other to prepare a third mixture; iv) a step of mixing the first mixture prepared in step i) with the third mixture prepared in step iii) to prepare a fourth mixture; v) a step of mixing the fourth mixture prepared in step iv) with the second mixture prepared in step ii) to prepare a fifth mixture; and vi) a step of mixing the fifth mixture prepared in step v) with a zeolite powder to prepare a raw material slurry mixture, and the forming step may include: vii) a step of laminating the raw material slurry mixture prepared in step vi) on a mesh belt; and viii) a step of dehydrating the raw material slurry mixture laminated on the mesh belt.
The method may further comprise the steps of: after step viii), ix) a step of pressing the dewatered raw material slurry mixture using a press roll; and x) a drying step using hot air.
Step viii) may comprise the steps of: a primary dewatering step of depressurizing the raw material slurry mixture while laminating the raw material slurry mixture on the web in step vii); and performing a secondary dehydration step after the primary dehydration step.
The positive charge additive may be at least one selected from the group consisting of polyvinylamine, vinylamine copolymer, vinylamine terpolymer, and vinylamine homopolymer, the glass fiber may have a diameter of 0.1 μm to 0.6 μm, and the binder fiber may be at least one selected from the group consisting of polyethylene, polypropylene, and polyethylene terephthalate; and the zeolite may have a diameter of 2 to 10 μm.
The vacuum pressure in the primary dewatering step of step viii) may be 50 to 80cmHg and the vacuum pressure in the secondary dewatering step may be 10 to 40cmHg.
In the pressing step of the step ix), the pressing may be performed at a pressure of 3 to 7atm, and the drying step using hot air of the step x) may be performed at a temperature of 100 to 150 ℃.
15L to 40L of the positive charge additive and 400L to 600L of water may be mixed with each other in step i), 1800g to 3000g of glass fibers, 400L to 600L of water and 300g to 600g of binder fibers may be mixed with each other in step ii), 400L to 600L of water and 4000g to 6000g of cellulose may be mixed with each other in step iii), and 2400g to 6000g of zeolite powder may be mixed in step vi).
Further, the water treatment filter according to the present invention comprises: 15L to 40L of at least one positively charged additive selected from the group consisting of polyvinylamine, vinylamine copolymers, vinylamine terpolymers, and vinylamine homopolymers; 1800 to 3000g of glass fibers having a diameter of 0.1 to 0.6 μm; 300g to 600g of at least one binder fiber selected from the group consisting of polyethylene, polypropylene and polyethylene terephthalate; 4000g to 6000g cellulose; and 2400g to 6000g of zeolite powder having a diameter of 2 μm to 10 μm.
Advantageous effects
The water treatment filter according to the present invention having the above-described structure has an effect of including a positive charge additive, cellulose, and zeolite, whereby various contaminants including hardness-inducing materials in water can be effectively removed.
Further, the method of manufacturing a water treatment filter according to the present invention is advantageous in that the positively charged additive and cellulose are first mixed and stirred with each other, and then the step of mixing and stirring the binder fiber is performed, whereby the positive charge is sufficiently formed on the surface of the cellulose, and thus the contaminant removal efficiency can be improved.
Further, the method of manufacturing a water treatment filter according to the present invention is advantageous in that primary reduced-pressure dewatering is performed while laminating the raw material slurry mixture on the mesh belt, whereby the magnitude of load applied to the mesh belt can be reduced and bonding between fibers is achieved, whereby a filter having a uniform thickness can be manufactured.
Drawings
Fig. 1 is a flow chart illustrating a method of manufacturing a water treatment filter according to an embodiment of the present invention.
Fig. 2 is a view showing the configuration of an apparatus for manufacturing a water treatment filter according to an embodiment of the present invention.
Figure 3 is a photograph of a water treatment filter according to one embodiment of the present invention.
Detailed Description
Hereinafter, the present invention will be described in more detail with reference to preferred embodiments thereof and the accompanying drawings. It is intended that the embodiments be described in detail to the extent that those skilled in the art to which the present invention pertains can easily carry out the present invention without limiting the technical spirit and scope of the present invention.
Unless otherwise defined, all terms (including technical and scientific terms) have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs. Terms commonly used, such as those defined in a typical dictionary, should be construed as consistent with the contextual meaning of the related art, and should not be construed in an idealized or overly formal sense unless expressly so defined to the contrary.
Fig. 1 is a flow chart illustrating a method of manufacturing a water treatment filter according to an embodiment of the present invention. As shown in fig. 1, the method for manufacturing a water treatment filter according to the present invention includes a step of mixing a positive charge additive, glass fiber, binder fiber, cellulose, zeolite powder and water with each other and a forming step.
The step of mixing the positively charged additive, the glass fibers, the binder fibers, the cellulose, the zeolite powder and the water with each other comprises: i) A step of mixing a positive charge additive and water with each other to prepare a first mixture; ii) a step of mixing glass fibers, water and binder fibers with each other to prepare a second mixture; iii) A step of mixing water and cellulose with each other to prepare a third mixture; iv) a step of mixing the first mixture prepared in step i) with the third mixture prepared in step iii) to prepare a fourth mixture; v) a step of mixing the fourth mixture prepared in step iv) with the second mixture prepared in step ii) to prepare a fifth mixture; and vi) a step of mixing the fifth mixture prepared in step v) with zeolite powder to prepare a raw material slurry mixture.
The forming step comprises: vii) a step of laminating the raw material slurry mixture prepared in step vi) on a mesh belt; viii) a step of dewatering the raw material slurry mixture laminated on the mesh belt; ix) a step of pressing the dehydrated raw material slurry mixture using a press roll; and x) a drying step using hot air.
The above steps will be described in more detail. Step i) is a step of mixing the positively charged additive and water with each other to prepare a first mixture. At this time, the positive charge additive is preferably mixed so that 15L to 40L based on 600L of water is occupied. In the case where the amount of the positive charge additive mixed therein is less than 15L, the amount of positive charges formed on the fiber surface is insufficient, whereby the contaminant removal ability is lowered. On the other hand, in the case where the amount of the positive charge additive mixed is more than 40L, the coupling force between the fibers is too strong, so that dehydration cannot be properly performed. Therefore, it is preferable to mix the positive charge additive to have the above percentage.
Here, as the positive charge additive, at least one may be selected from the group consisting of polyvinylamine, vinylamine copolymer, vinylamine terpolymer, and vinylamine homopolymer.
The first mixture having the mixing ratio defined as described above is stirred in the stirrer at a speed of 1300RPM to 1800RPM for 45 minutes to 75 minutes.
Step ii) is a step of mixing glass fibers, water and binder fibers with each other to prepare a second mixture.
At this time, it is preferable that the glass fiber is mixed so as to occupy 1800g to 3000g based on 600L of water, and the binder fiber is mixed so as to occupy 300g to 600g based on 600L of water.
In the case where the amount of glass fiber mixed therein is less than 1800g, the pores of the filter which has been manufactured are too large and the retention of zeolite is low. On the other hand, in the case where the amount of glass fibers mixed therein is more than 3000g, the amount of fibers increases, whereby it is difficult to control the basis weight and the pores when manufacturing the filter. Therefore, it is preferable to mix the glass fiber to have the above percentage. Here, it is preferable that the glass fiber has a diameter of 0.1 μm to 0.6 μm and a length of 5 μm to 50 μm.
Further, at least one selected from the group consisting of polyethylene, polypropylene and polyethylene terephthalate may be used as the binder fiber. In the case where the amount of the binder fiber mixed is less than 300g, the fibers are not entangled, and thus the paper strength is low, thereby making it difficult to move into a drying oven. On the other hand, in the case where the amount of the binder fiber mixed is more than 600g, the contents of the glass fiber and the cellulose are relatively small, thereby not sufficiently exhibiting the function as a filter. Therefore, it is preferable to mix the binder fiber to have the above percentage.
The second mixture having the mixing ratio defined as described above is stirred in the stirrer at a speed of 1300RPM to 1800RPM for 100 to 140 minutes.
Step iii) is a step of mixing water and cellulose with each other to prepare a third mixture.
At this time, the cellulose is preferably mixed so that 4000g to 6000g are occupied based on 600L of water.
In the case where the amount of cellulose mixed therein is less than 4000g, the retention of zeolite is low. On the other hand, in the case where the amount of cellulose mixed therein is more than 6000g, it is difficult to manufacture the filter due to pore control and a reduction in dehydration force. Therefore, it is preferable to mix the cellulose to have the above percentage. Here, the cellulose may be obtained from various herbaceous plants or woody plants. For example, the wood fibers can be obtained by mechanical methods using a grinder, a high-pressure homogenizer, or a microfluidizer.
Preferably, the cellulose has a diameter of 0.1 μm to 0.6 μm and a length of 3 μm to 10 μm.
The third mixture having the mixing ratio defined as described above is stirred in the stirrer at a speed of 1300RPM to 1800RPM for 100 to 140 minutes.
Step iv) is a step of mixing the first mixture prepared in step i) with the third mixture prepared in step iii) to prepare a fourth mixture. Preferably, the stirring is carried out under the same conditions as in step iii).
Step v) is a step of mixing the fourth mixture prepared in step iv) with the second mixture prepared in step ii) to prepare a fifth mixture. Preferably, the stirring is carried out under the same conditions as in step i).
The first mixture, the second mixture and the third mixture prepared in steps i) to iii) are not mixed with each other at the same time but the first mixture and the third mixture are first mixed with each other to prepare a fourth mixture and then the fourth mixture is mixed with the second mixture to prepare a fifth mixture in step iv), because positive charges must be maximally formed on the surface of cellulose. That is, in the case where the first mixture containing the positively charged additive and the third mixture containing the cellulose are mixed with each other and first stirred, a positive charge is formed on the surface of the cellulose. However, in the case where the first mixture, the second mixture, and the third mixture are simultaneously mixed with each other or in the case where the first mixture, the second mixture, and the third mixture are sequentially mixed with each other, a sufficient amount of positive charge is not formed on the surface of the cellulose due to the binder fibers in the second mixture.
Step vi) is a step of mixing the fifth mixture prepared in step v) with zeolite powder to prepare a raw material slurry mixture.
At this time, the zeolite powder is preferably mixed with the prepared fifth mixture to occupy 2400g to 6000g. The raw material slurry mixture is stirred at a speed of 1300RPM to 1800RPM for 20 minutes to 40 minutes.
In the case where the amount of zeolite powder mixed therein is less than 2400g, the ability to remove the hardness material is reduced. On the other hand, in the case where the amount of zeolite powder mixed therein is greater than 6000g, the basis weight and thickness of the filter are unnecessarily increased. Therefore, it is preferable to mix the zeolite to have the above percentage. Here, it is preferred that the zeolite has a diameter of 2 μm to 10 μm. In the case where the diameter of the zeolite is less than 2 μm, the diameter of the zeolite is too small, whereby the pores of the filter become too small. On the other hand, in the case where the diameter of the zeolite is larger than 10 μm, the diameter of the zeolite is too large, and thus the hard material cannot be sufficiently removed. Accordingly, the zeolite preferably has the above diameter range.
The reason for the final mixing of the zeolite powder in the preparation of the raw material slurry mixture is that it is necessary to prevent the zeolite surface from clogging due to the binding fibers.
Step vii) is a step of laminating the raw material slurry mixture prepared in step vi) on a mesh belt. As an example, the manufacturing apparatus shown in fig. 2 may be used.
Specifically, the raw material slurry mixture prepared in step vi) is transferred into the hopper 100 by a pump (not shown), and the nozzle 110 connected to one side of the hopper 100 sprays the raw material slurry mixture onto the mesh belt 200 moving at a predetermined speed.
Here, it is preferable that the nozzle 110 of the hopper 100 is located in the headbox 300 isolated from the outside so as to form a separate space.
Step viii) is a step of dewatering the raw material slurry mixture laminated on the mesh belt 200, and may include a primary dewatering step and a secondary dewatering step.
Specifically, the primary dewatering step may be performed by the first reduced-pressure dewatering device 310 located at the lower surface of the mesh belt 200, which is the surface opposite to the surface on which the raw material slurry mixture is laminated at the time when the raw material slurry mixture is laminated on the mesh belt 200 in step vii). In this case, the vacuum pressure is preferably 50 to 80cmHg.
As described above, in the case where the primary decompression dewatering is performed at the time when the raw material slurry mixture is laminated on the mesh belt 200, the magnitude of the load applied to the mesh belt 200 can be reduced, whereby the equipment maintenance cost can be reduced. In particular, since the bonding between the fibers is achieved by the primary dewatering, the laminated raw material slurry mixture remains unchanged even if the mesh belt 200 moves in a slightly inclined state, whereby a filter having a uniform thickness can be obtained.
The secondary dewatering step, which is a step of further reducing the amount of moisture in the raw material pulp mixture of the primary dewatering and simultaneously causing denser bonding between fibers, may be performed by the second reduced-pressure dewatering device 400 located at the rear of the first reduced-pressure dewatering device 310. Vacuum dewatering is preferably carried out using a vacuum pressure of 10 to 40cmHg, although natural gravity methods are also possible.
Step ix) is a step of pressing the dehydrated raw material slurry mixture. The dewatered raw material slurry mixture on the mesh belt 200 is transferred to a pair of press rolls 500 spaced apart from each other by a predetermined distance to be pressed.
Step x) is a drying step using hot air. This step is a step of completely removing residual moisture after the dehydration step to obtain a filter. The hot air drying is preferably performed using the drying apparatus 600 maintained at a temperature of 100 to 150 ℃.
Subsequently, winding may be performed using the winding device 700 as needed. Further, at least one of the following steps may be repeatedly performed: further laminating the raw material slurry mixture on a mesh belt; a dehydration step; a pressing step; and a drying step using hot air.
Hereinafter, a method of manufacturing a water treatment filter according to the present invention will be described in more detail by way of specific examples.
< example >
600L of water and 15L to 40L of polyvinylamine were mixed with each other and stirred to prepare a first mixture, and 600L of water, 2000g to 3000g of glass fiber, and 300g to 600g of polyethylene were mixed with each other and stirred to prepare a second mixture. In addition, 600L of water and 4000g to 5500g of cellulose are mixed with each other and stirred to prepare a third mixture, and the first mixture and the third mixture are mixed with each other and stirred to prepare a fourth mixture.
Subsequently, the fourth mixture and the second mixture are mixed with each other and stirred to prepare a fifth mixture, and the fifth mixture is mixed with 3000g to 6000g of zeolite powder to prepare a raw material slurry mixture.
The prepared raw material slurry mixture was injected to a mesh belt, dehydrated, pressed, and subjected to hot air drying using the apparatus of fig. 2 to manufacture a filter.
[ Table 1]
< examples of experiments >
The flow rate, zeta potential, particle removal rate and hardness removal rate of the filter manufactured under the conditions of the embodiment shown in table 1 above were measured to evaluate the performance of the filter. The results are shown in Table 2.
[ Table 2]
In the case where the amount of raw material used in manufacturing the filter having the basis weight is large and the zeolite content is high, the performance of each filter is high, and in the case where the amount of zeolite added is large, the thickness of each filter is small.
The pores of the filters according to examples 4 to 6 were 0.81 to 0.84 μm, which is the smallest pore, and the zeta potential of the filters according to examples 4 to 6 was 15.9 to 18.5mV, which is relatively high.
The flow rate of the filters according to examples 7 to 12 was 2.23LPM to 2.45LPM, which is a relatively large amount of water transfer. However, the 1 μm-sized particle removal capacity of the filters according to examples 7 to 12 was lower than that of the filters according to examples 1 to 6, and the thickness of the filters according to examples 7 to 12 was too large. In particular, the filters according to examples 4 to 6 had a hardness removal rate of 53% to 55%, which was high, whereas the filters manufactured under the conditions of examples 7 to 9 had a hardness removal rate of less than 30%.
Meanwhile, fig. 3 is a picture of a filter manufactured under the condition of example 5 of the present invention.
The present invention has been described above based on the preferred embodiments thereof. It will be understood by those skilled in the art that the present invention may be embodied in modified forms without departing from the inherent characteristics of the invention. Accordingly, the disclosed embodiments must be considered from an illustrative point of view, and not from a restrictive point of view. It is intended that the scope of the invention be defined by the appended claims rather than by the foregoing description, and that the invention include equivalents thereto.
(description of reference numerals)
100: hopper
110: nozzle with a nozzle body
200: mesh belt
300: head box
310: first decompression dewatering device
400: second decompression dehydration device
500: press roller
600: drying device
700: winding device
Claims (7)
1. A method of manufacturing a water treatment filter, the method comprising the steps of:
a step of mixing the positive charge additive, the glass fiber, the binder fiber, the cellulose, the zeolite powder, and water with each other; and
a step of forming the composite material,
wherein the step of mixing the positively charged additive, the glass fiber, the binder fiber, the cellulose, the zeolite powder and water with each other comprises:
i) A step of mixing a positive charge additive and water with each other to prepare a first mixture;
ii) a step of mixing glass fibers, water and binder fibers with each other to prepare a second mixture;
iii) A step of mixing water and cellulose with each other to prepare a third mixture;
iv) a step of mixing the first mixture prepared in step i) with the third mixture prepared in step iii) to prepare a fourth mixture;
v) a step of mixing the fourth mixture prepared in step iv) with the second mixture prepared in step ii) to prepare a fifth mixture; and
vi) a step of mixing the fifth mixture prepared in step v) with a zeolite powder to prepare a raw material slurry mixture,
the forming step includes:
vii) a step of laminating the raw material slurry mixture prepared in step vi) on a mesh belt; and
viii) a step of dewatering the raw material slurry mixture laminated on the mesh belt,
wherein the positive charge additive is at least one selected from the group consisting of polyvinylamine, vinylamine copolymer, vinylamine terpolymer and vinylamine homopolymer, the glass fiber has a diameter of 0.1 μm to 0.6 μm, the binder fiber is at least one selected from the group consisting of polyethylene, polypropylene and polyethylene terephthalate, and the zeolite has a diameter of 2 μm to 10 μm.
2. The method of claim 1, further comprising the steps of:
after step viii) of the method according to the invention,
ix) a step of pressing the dehydrated raw material slurry mixture using a press roll; and
x) a drying step using hot air.
3. The method according to claim 1, wherein step viii) comprises the steps of:
a primary dewatering step of depressurizing the raw material slurry mixture while laminating the raw material slurry mixture on the mesh belt in step vii); and
a secondary dewatering step is performed after the primary dewatering step.
4. The method of claim 3, wherein,
the vacuum pressure in the primary dewatering step of step viii) is 50 to 80cmHg, and
the vacuum pressure in the secondary dehydration step is 10 to 40cmHg.
5. The method of claim 2, wherein,
in the pressing step of the step ix), the pressing is performed at a pressure of 3atm to 7atm, and
the drying step using hot air of step x) is carried out at a temperature of 100 ℃ to 150 ℃.
6. The method of claim 1, wherein
In step i) 15L to 40L of a positive charge additive and 400L to 600L of water are mixed with one another,
mixing 1800g to 3000g of glass fibers, 400L to 600L of water and 300g to 600g of binder fibers with one another in step ii),
400L to 600L of water and 4000g to 6000g of cellulose are mixed with one another in step iii), and
2400g to 6000g of zeolite powder are mixed in step vi).
7. A water treatment filter made by the method of any one of claims 1 to 6, comprising:
15L to 40L of at least one positively charged additive selected from the group consisting of polyvinylamine, vinylamine copolymers, vinylamine terpolymers, and vinylamine homopolymers;
1800 to 3000g of glass fibers having a diameter of 0.1 to 0.6 μm;
from 300g to 600g of at least one binder fiber selected from the group consisting of polyethylene, polypropylene and polyethylene terephthalate;
4000g to 6000g cellulose; and
2400g to 6000g of zeolite powder with a diameter of 2 μm to 10 μm.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/KR2019/000622 WO2020149429A1 (en) | 2019-01-16 | 2019-01-16 | Water treatment filter and method for manufacturing same |
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| CN113301977A CN113301977A (en) | 2021-08-24 |
| CN113301977B true CN113301977B (en) | 2022-12-16 |
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| CN (1) | CN113301977B (en) |
| MY (1) | MY194639A (en) |
| WO (1) | WO2020149429A1 (en) |
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| KR20180023395A (en) * | 2016-08-25 | 2018-03-07 | 주식회사 엔바이오니아 | Method of making pore filter media having iron oxide nano particles, and making apparatus thereof |
| KR101962675B1 (en) * | 2017-11-01 | 2019-03-27 | 주식회사 엔바이오니아 | Filter for water treatment and preparation method thereof |
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2019
- 2019-01-16 MY MYPI2021003966A patent/MY194639A/en unknown
- 2019-01-16 CN CN201980088634.8A patent/CN113301977B/en active Active
- 2019-01-16 WO PCT/KR2019/000622 patent/WO2020149429A1/en active Application Filing
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| Publication number | Publication date |
|---|---|
| CN113301977A (en) | 2021-08-24 |
| WO2020149429A1 (en) | 2020-07-23 |
| MY194639A (en) | 2022-12-08 |
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