KR20190010502A - Seawater desalination apparatus - Google Patents

Abstract

Provided is a seawater desalination device. According to an embodiment of the present invention, the seawater desalination device comprises: a pretreatment unit including an electrocoagulation module for electro-coagulating suspended solids included in incoming seawater and a filter module for filtering aggregates contained in electrocoagulation water introduced from the electrocoagulation module; and an osmotic filtration unit including an osmosis membrane module for desalinating pretreated water introduced from the pretreatment unit. According to the present invention, it is possible to efficiently aggregate foreign matter contained in seawater or brackish water as raw water, treat the aggregated foreign matter at a high rate, and discharge the foreign matter at a high flow rate, thereby increasing the desalinated flow rate and significantly improving the durability for osmosis equipment for desalination. In addition, since foreign matter can be removed without additional chemical additives in a pretreatment process of seawater or brackish water, the present invention is environmentally friendly. It is easy to perform a backwashing process for removing foreign matter collected by the pretreatment. The present invention has an extended use period with high durability and is very economical in operation.

Description

Seawater desalination apparatus

The present invention relates to a seawater desalination apparatus, and more particularly, to a seawater desalination apparatus capable of improving the pretreatment efficiency of seawater as raw water to reduce the damage of the osmosis module for desalination and to increase the fresh water amount To a desalination apparatus.

Seawater desalination is a series of water treatment processes that remove high-purity drinking water, domestic water, and industrial water by removing dissolved substances including salt from living waters and industrial waters, which are difficult to use directly. In other words, seawater desalination refers to the removal of salinity from seawater containing salinity to obtain fresh water.

Such seawater desalination methods include evaporation using water evaporation phenomenon, membrane filtration using membrane differentiation and selective permeability, and the membrane filtration method is divided into reverse osmosis and electrodialysis in detail.

Reverse osmosis (RO) method of seawater desalination, in particular, accounted for 48% of the total desalination market until 2005, but due to problems such as rising energy costs, Is expected to increase. The reverse osmosis system separates the components contained in seawater or sea water into product water (or treated water) and concentrated water by using a polymer membrane (reverse osmosis membrane). The product water is used as water and drinking water by diluting the component concentration The concentrated water is discharged to the sea again. The reverse osmosis membrane used in the reverse osmosis system requires a very fine pore structure to be able to withstand high pressure exceeding about 25 kg / cm 2, which is osmotic pressure of seawater so that reverse osmosis occurs, . In recent years, seawater desalination has been attempted using seawater desalination.

On the other hand, seawater, which is a raw water, contains a large amount of foreign matter such as large-scale obstruction, small-sized algae and suspended substances. When osmosis is carried out in a state that seawater contains such foreign matter, osmosis membrane such as reverse osmosis membrane or osmosis membrane The durability is greatly reduced and frequent pressure correction is required due to the deepening of the fouling phenomenon, so that the foreign matter should be prevented from being injected into the reverse osmosis process at the maximum.

For this purpose, it is desirable to add the seawater to the osmosis process with a large amount of contaminants or foreign substances removed through pretreatment. Therefore, a membrane filtration method using a filter medium such as a hollow fiber membrane as a pretreatment facility has been widely used. However, there is a problem in that the flow rate is insufficient and the time required for the pretreatment is prolonged or the amount of fresh water obtained is very small. Also, there is a problem that the backwashing efficiency for removing various foreign substances adsorbed on the membrane is low and the durability capable of sufficiently performing backwashing is not secured.

Therefore, it is urgently required to develop a seawater desalination apparatus capable of desalinating seawater in an environmentally friendly manner, since a sufficient flow rate is obtained in the pretreatment process, a removal rate of foreign matters is excellent, and no separate chemical treatment is required.

Korean Patent Publication No. 10-1051345

SUMMARY OF THE INVENTION The present invention has been made in view of the above points, and it is an object of the present invention to provide a method and apparatus for effectively flocculating foreign matter contained in raw water or sea water and discharging the flocculated foreign matter at a high flow rate, And a seawater desalination apparatus having the pretreatment apparatus for the seawater desalination apparatus.

In addition, since the present invention can remove foreign substances without any chemical additives in the pretreatment process of seawater or nautical water, it is eco-friendly, and it is easy to perform backwashing process for removing foreign substances collected by pretreatment, Another object of the present invention is to provide a pretreatment apparatus for a seawater desalination apparatus having an extended use period and being very economical in operation and a seawater desalination apparatus having the same.

In order to solve the above-described problems, the present invention provides a pretreatment apparatus comprising a pretreatment unit including an electrocoagulation module for electrocoagulating a foreign substance contained in the seawater, and a filter module for filtering aggregates contained in the electrocoagulated water introduced from the electrocoagulation module, ; And an osmotic membrane module for desalinating the pre-treatment water introduced from the pre-treatment unit.

According to an embodiment of the present invention, the electrocoagulation module electrocoagulates foreign matter contained in seawater through positive ions generated at the sacrificial electrode, and the treatment capacity of the introduced seawater may be 1 m ³ / h or more.

The filter module may include a plurality of filter units having filter media, and the filter media may include an aggregated water having a filtration flow rate of 50 LMH or more and a particle diameter of 0.2 μm or more, The filtration efficiency may be over 99%.

The filter media is a flat membrane having a nanofiber web and a second support laminated in order on both sides of the first support, and a channel through which the filtrate filtered in the nanofiber web flows in the direction of the first support is formed Lt; / RTI >

The first support and the second support may be independently any one of a nonwoven fabric, a woven fabric, and a knitted fabric, and more preferably a nonwoven fabric.

The basis weight of the nanofiber web may be 30 g / m 2 or less, the basis weight of the first support may be 250 g / m 2 or more, and the thickness may be 90% or more of the total thickness of the filter media.

The basis weight of the first support may be 250 to 800 g / m 2, and more preferably 350 to 600 g / m 2. In addition, the thickness of the first support may be 2 to 8 mm, more preferably 2 to 5 mm, and still more preferably 3 to 5 mm.

The basis weight of the second support may be 35 to 100 g / m 2, and the thickness may be 150 to 250 탆.

Also, the nanofiber web may include a fluorine-based compound as a fiber-forming component, and the fluorine-based compound may be at least one selected from the group consisting of polytetrafluoroethylene (PTFE), tetrafluoroethylene-perfluoroalkylvinylether copolymer (PFA) (EPE) based, tetrafluoroethylene-ethylene copolymer (ETFE) based, tetrafluoroethylene-hexafluoropropylene copolymer (FEP) based, tetrafluoroethylene-hexafluoropropylene-perfluoroalkyl vinyl ether copolymer , Polychlorotrifluoroethylene (PCTFE), chlorotrifluoroethylene-ethylene copolymer (ECTFE), polyvinylidene fluoride (PVDF), and the like.

Also, the nanofiber web may have an average pore size of 0.1 to 5 μm and a porosity of 60 to 90%.

In addition, the nanofiber forming the nanofiber web may have an average diameter of 0.05 to 1 mu m.

The basis weight of the nanofiber web may be 0.05 to 20 g / m 2.

The second support includes a second composite fiber including a support component and a low melting point component such that at least a part of the low melting point component is exposed to the outer surface, and the low melting point component of the second composite fiber is The second support body and the nanofiber web may be bonded to each other to be bonded to the nanofiber web.

The first support of the filter media includes a first composite fiber including a support component and a low melting point component such that at least a part of the low melting point component is exposed on the outer surface, Component and the low melting point component of the second composite fiber, the first support and the second support can be bonded.

The filter unit may be a flat filter unit including a support frame for supporting the rim of the filter media, and the support frame may include a flow path for allowing the filtrate filtered out from the filter media to flow out to the outside.

Further, the electrocoagulation module may include: a housing having an upper space opened; And an electrode unit disposed in the inner space, the electrode unit including a sacrificial electrode and a power electrode for agglomerating foreign matter contained in raw water supplied from the outside, wherein the internal space includes a first chamber into which the raw water flows, And a third chamber disposed at an upper side of the first chamber and in which the electrode portion is disposed, and a third chamber in which the electro-coagulation reaction completed electro-coagulation water is temporarily stored in the second chamber.

The present invention also relates to an electrocoagulation module for electrocoagulating a foreign substance contained in an influx of seawater; And a filter module for filtering the agglomerates contained in the electrocoagulation water introduced from the electrocoagulation module. The present invention also provides a pretreatment device for a seawater desalination apparatus.

According to the present invention, it is possible to effectively flocculate foreign matters contained in raw seawater or sea water, treat the flocculated foreign matter at a high speed and discharge it at a high flow rate, thereby increasing the flow rate of desalination and durability to osmosis equipment for desalination Can be improved. In addition, since the foreign matter can be removed without pretreatment of seawater or nose in the pretreatment process, it is eco-friendly, and it is easy to perform the backwashing process for removing the foreign substances collected by the pretreatment. Cycle, and is very economical in operation.

1 is a schematic diagram of a seawater desalination apparatus according to an embodiment of the present invention,
2 is a schematic view showing an electrocoagulation module included in an embodiment of the present invention,
Fig. 3 is a view showing the main configuration of Fig. 2,
Fig. 4 is a partial cutaway view showing the internal structure of the housing in Fig. 3,
5 is a cross-sectional view of Fig. 3,
Fig. 6 is a schematic view showing the case where an air diffusing tube is included in Fig. 3,
Fig. 7 is a sectional view of Fig. 6,
8 is a schematic view showing an inflow pipe applied to an electrocoagulation module included in an embodiment of the present invention,
9 is a schematic view showing an air diffuser applied to an electrocoagulation module included in an embodiment of the present invention,
10 is a view showing a main configuration of an electrocoagulation module included in another embodiment of the present invention,
11 is a view showing the separation of Fig. 10,
Fig. 12 is a bottom view showing the electrode case applied to Fig. 10,
FIG. 13A is a perspective view of a filter unit, and FIG. 13B is a sectional view of a boundary line XX 'in FIG. 13A. FIG. 13A is a plan view of a filter unit included in a filter module included in an embodiment of the present invention. A schematic view showing a filtration flow as a reference,
15 is a cross-sectional view of a filter medium provided in a filter module included in an embodiment of the present invention,
16 is a SEM photograph of a nanofiber web applied to a filter media included in an embodiment of the present invention,
FIG. 17 is a photograph of the swollen filter material after the washing liquid is trapped inside the filter material after the layer separation in the filter material by the backwashing process,
Fig. 18 is a schematic view showing the first support and the nanofiber web being directly joined together as an example of the filter media. Fig.
FIGS. 19A and 19B are views schematically illustrating the filter media according to an embodiment of the present invention. FIG. 19A is a view showing the nanofiber web and the second support are laminated together, FIG. 19B is a cross- And the second support body is disposed on both surfaces of the first support body,
20 to 23 are sectional views of other filter media provided in the filter unit included in an embodiment of the present invention, and
24 is a partially exploded perspective view of an osmotic unit provided in the osmotic filtration part included in an embodiment of the present invention, and Fig.
Fig. 25 is an exploded perspective view of the osmotic unit according to Fig. 24 in which the internal components are removed from which the outer housing is removed. Fig.

Hereinafter, exemplary embodiments of the present invention will be described in detail with reference to the accompanying drawings, which will be readily apparent to those skilled in the art to which the present invention pertains. The present invention may be embodied in many different forms and is not limited to the embodiments described herein. In order to clearly illustrate the present invention, parts not related to the description are omitted, and the same reference numerals are assigned to the same or similar components throughout the specification.

The seawater desalination apparatus according to an embodiment of the present invention includes a pretreatment unit 3200 for filtering foreign substances contained in seawater taken as shown in FIG. 1, and a pretreatment unit 3300 for removing salt and the like contained in seawater And a supply pump 3100 for supplying the collected seawater to the pretreatment unit 3200. [ Although not shown in FIG. 1, a water pump for taking in seawater or sea water, a raw water storage tank for storing the collected seawater, a storage tank for storing pre-treated electrolytic flocculation water in the pretreatment unit 3200, A facility to be provided in a known seawater desalination apparatus such as a post-treatment facility in which the production water is post-treated or a water tank in which post-treatment purified water is stored.

The pretreatment unit 3200 removes various suspended substances such as microorganisms such as algae contained in raw water or sea water, salts formed by combining ions, and colloidal substances, Thereby relieving the filtration burden on the osmotic filtration portion and significantly improving the durability of the osmotic filtration portion.

The pretreatment unit 3200 includes an electrocoagulation module 3210 for electrocoagulation of suspended solids contained in the seawater, a filter for filtering aggregates contained in the electrocoagulation water introduced from the electrocoagulation module 3210, Module 3220. < / RTI >

The electrocoagulation module 3210 may be configured to aggregate foreign substances in the suspension water contained in the raw water or sea water through ions having charges opposite thereto to form an aggregate or to remove foreign substances from the electrochemically generated aggregate To carry out the electrocoagulation process of the foreign substance.

The electrocoagulation module 3210 may be employed without limitation in the case of an electrocoagulation device known to perform such a process. Preferably, the electrocoagulation module 3210 preferably has a treating capacity of at least 1 m ³ / h of the raw water so as to process the raw water of a large capacity in a short period of time.

The electrocoagulation module 3210 includes, for example, a housing having a predetermined hollow space for accommodating raw water to be introduced therein, performing an electrocoagulation reaction of foreign matter, and a sacrificial electrode for generating positive ions. . ≪ / RTI >

The size of the housing, the thickness of the outer wall, the volume / structure of the inner space and the like can be determined by considering the capacity of the raw water to be treated, the kind / content of the foreign substance contained in the raw water, The present invention is not particularly limited thereto since the apparatus can be suitably changed in accordance with the use of the apparatus.

The electrode unit may further include a sacrificial electrode capable of generating a direct electric agglutination reaction with the foreign substance or indirectly generating a cation mediating an electroaggregation reaction, and a power electrode for allowing the sacrificial electrode to generate positive ions And each of the sacrificial electrode and the power electrode may be provided in a suitable shape, size, weight, and number in consideration of processing capacity and processing speed of the raw water.

As a non-limiting example, the sacrificial electrode may be made of a material capable of generating positive ions by a power source to which the sacrificial electrode is applied. Examples of the sacrificial electrode include metals made of aluminum, iron, lyrium, zinc, nickel, . In addition, the power electrode is preferably made of a material insoluble in an external power source, for example, stainless steel.

When a predetermined voltage is applied to the sacrificial electrode of the electrode unit, the sacrificial electrode is dissolved and the metal ions are eluted as raw water. The metal ions aggregate with foreign substances of opposite charge contained in the raw water, or metal hydroxide And the foreign substance is adsorbed on the metal hydroxide, so that the foreign matter can be electrocopherized.

The electrocoagulation module 3210 may have such a structure that the electrocoagulation reaction is efficiently performed and the coagulated foreign matter can be more easily removed.

The electrocoagulation modules 100, 100 ', 200 according to an embodiment of the present invention may include the housings 110, 210 and the electrode unit 120 as shown in FIGS. 2 to 12.

The housings 110 and 210 serve to provide a space for temporarily storing raw water supplied from the outside. For this purpose, it may be in the shape of a shell having an inner space with an open top. That is, the housings 110 and 210 may be formed of an internal space, which is a holding space of the raw water, so that the foreign substances contained in the raw water introduced from the outside are cohered through the electrocoagulation reaction and then the raw water is transferred to the separate processing space side .

The internal space includes a first chamber 111 into which raw water flows, a second chamber 112 in which the electrode unit 120 is disposed, and a second chamber 112 in which the electrocoagulation reaction is completed in the second chamber 112, And a third chamber 113 that is temporarily stored.

The second chamber 112 in which the electrode unit 120 is disposed may be formed on the upper side of the first chamber 111 and the third chamber 113 may be formed on the upper side of the first chamber 111 And the second chamber 112 and the third chamber 113 arranged in parallel to each other can be partitioned from each other by a partition wall 114 projecting at a predetermined height in the inner space have.

Accordingly, the first chamber 111 functions as a buffer space in which the raw water supplied from the outside is retained before moving to the second chamber 112 side where the electro-coagulation reaction is performed, 2 chamber 112 side. The raw water flowing into the second chamber 112 can contact the sacrificial electrode 122 and the power electrode 121 constituting the electrode unit 120 in a uniform area to increase the overall processing speed.

A hollow inflow pipe 130 having a predetermined length and a plurality of injection holes 131 formed along the longitudinal direction is disposed on the first chamber 111 side so that raw water supplied from the outside is injected into the injection holes 131 (Refer to FIGS. 4 and 8), the inflow pipe 130 is arranged in a direction parallel to the arrangement direction of the plurality of electrodes constituting the electrode unit 120 . In addition, a drain discharge hole 118 may be formed on the bottom surface of the first chamber 111 to be connected to the drain pipe 119 so as to discharge the drain to the outside.

As described above, in the electrocoagulation modules 100, 100 ', 200 according to the present invention, raw water injected toward the first chamber 111 through the injection hole 131 of the inflow pipe 130 flows into the first chamber 111 The water level gradually increases to flow into the second chamber 112 where the electrode unit 120 is disposed and the raw water introduced into the second chamber 112 while maintaining an even water level flows into the electrode unit 120 And then flows into the third chamber 113 from the second chamber 112 through the upper end of the partition 114.

At this time, the partition wall 114 may be formed with a sloped surface on one side constituting the wall surface of the third chamber 113. For example, the inclined surface may be inclined downward toward the third chamber 113 from the upper end of the partition 114 toward the lower end (see FIGS. 2 to 4). Accordingly, the process water overflowing through the upper end of the partition 114 can be smoothly moved toward the third chamber 113 along the inclined surface.

At least one discharge hole 118 may be formed in the bottom surface of the third chamber 113. The discharge hole 118 may be connected to a post-treatment device for treating foreign matters agglomerated through an electro-agglomeration reaction through a separate pipe 40 so that the treatment water can be transferred to the post-treatment device.

Meanwhile, the housings 110 and 210 may be formed of an insulator or a non-insulator so as to prevent a short circuit with the electrode unit 120 disposed on the second chamber 112 side when power is applied. For example, the housing 110 and 210 may be made of a material such as plastic, concrete, or plywood, but it is not limited thereto and any known insulator or non-insulator can be used.

In addition, the outer surface of the housings 110 and 210 is coated with a coating layer having at least one of chemical resistance, corrosion resistance, and electrical conductivity, thereby preventing the housings 110 and 210 from being damaged by heavy metals contained in the raw water .

The housing 110 and 210 may be fixed through a separate support frame 160. When the support frame 160 is included, the control unit 140 may be fixed to one side of the support frame 160 have.

The electrode unit 120 may include a plurality of plate-shaped electrodes having a predetermined area, and the plurality of electrode plates may be spaced apart from each other at a predetermined interval in the second chamber 112. For example, the plurality of electrode plates may include a pair of power electrodes 121 to which power is supplied from the outside, and a pair of power electrodes 121 that are parallel to each other so as to face one another with a predetermined gap between the pair of power electrodes 121 And a plurality of sacrifice electrodes 122 spaced apart from one another.

The pair of power electrodes 121 are formed to have a longer length than that of the sacrificial electrode 122 so that power supplied from the outside can be smoothly applied. Therefore, when the power electrode 121 is disposed on the second chamber 112 side, The length of at least part of the surface of the raw water can be exposed to the outside without being completely immersed in the raw water stored in the second chamber 112 (see FIG. 3). On the other hand, the plurality of sacrifice electrodes 122 disposed between the pair of power electrodes 121 are disposed so as to be completely submerged by the raw water stored in the second chamber 112, so that the entire area comes into contact with the raw water, Can be maximized.

The sacrificial electrode 122 and the power electrode 121 constituting the electrode unit 120 may be fixed directly to the housing 110 or may be fixed to a separate member side, The other member may be coupled to the other side.

For example, the electrode unit 120 may be directly fixed to the inner wall of the housing 110 as shown in FIGS. That is, the inner wall of the housing 110 defining the second chamber 112, more specifically the inner wall of the partition wall 114 facing each other and the inner wall of the housing 110 are provided with a plurality of fitting grooves 115 And the plurality of fitting grooves 115 may be formed in a number corresponding to the number of the power electrode 121 and the sacrifice electrode 122 of the electrode unit 120.

Here, the insertion groove 115 has an upper end opened and a lower end closed, thereby limiting the insertion depth of the lower end of the electrode unit 120.

Accordingly, by inserting the electrode unit 120 into the fitting groove 115, each of the neighboring electrodes can be arranged in parallel with one side facing each other with a predetermined gap therebetween.

10 to 12, the electrode unit 120 is fixed to the electrode case 116, and the electrode case 116 is fixed to the second chamber 112 side of the housing 210 Or may be fixed via a combination.

At this time, the electrode case 116 may have a plurality of fitting grooves 117 formed along the height direction on the inner walls facing each other, and may have a shape with a top and a bottom opened. When the electrode unit 120 is inserted into each fitting groove 117 and the electrode case 116 is inserted into the second chamber 112, the first chamber 111 It is possible to smoothly flow the raw water ascending from the water supply pipe (not shown).

Here, the electrode case 116 may be formed of an insulator or a non-insulator so as to prevent a short circuit with the electrode unit 120 inserted into the fitting groove 117 when power is applied. For example, the electrode case 116 may be made of a material such as plastic, concrete, or plywood, but it is not limited thereto, and any known insulator or non-insulator can be used. In addition, since the coating layer having at least one of chemical resistance, corrosion resistance and electric conductivity is applied to the outer surface of the electrode case 116, the electrode case 116 is not damaged by the heavy metal contained in the raw water .

As another example, as shown in FIGS. 13A and 13B, the electrode unit of the electrocoagulation module 200 'is disposed on the outer side of the housing member 123 (120') so as to face each other, The power electrode 121 'as a pair of electrode plates and the conductive lump 122' instead of the electrode plate as the sacrificial electrode 122 described above can be accommodated in the housing member 123. As a result of the sacrifice electrode 122, the metal cation eluted from the conductive mass 122 'provided in place of the plate-shaped electrode plate is electrically neutralized with the charged foreign substance to cause the coagulation reaction and the oxidation and reduction reaction, . The above-described electrocoagulation principle is well known in the art including the above description, and thus a detailed description thereof will be omitted.

In the case of the electrode unit 120 of the type illustrated in FIGS. 1 to 12, a plurality of sacrifice electrodes 122 are disposed apart from each other between the electrode plates as the power electrodes 121 facing each other. A difference in power consumption occurs depending on the relative distance between the power consumption and the power consumption. On the other hand, when the sacrificial electrode is provided with a plurality of conductive masses 122 'as shown in FIGS. 13A and 13B, it is possible to exhibit the same level of electrocoagulation efficiency while significantly reducing the consumption of electric power. Further, it may be more suitable for seawater desalination.

Specifically, the conductive lump 122 'may be received in the receiving member 123, and a pair of electrode plates 121' may be disposed on the outer side of the receiving member 123. The housing member 123 includes at least one first passage hole 123b for introducing raw water from the first chamber 111 to the accommodation space side of the accommodation member and at least one through hole 123b through the first passage hole 123b And at least one second passage hole 123a for moving the introduced raw water toward the two electrode plates 121 'facing each other may be formed.

For example, the accommodating member 123 may be provided in a shape of an open top, and the first through-hole 123b may be formed on the bottom surface, and the second through- May be formed through the side opposite to the electrode 121 '.

The raw water introduced into the housing member 123 through the first passage hole 123b may surround the surface of the conductive masses 122 'filled in the housing member 123, And can also contact the power electrode 121 'through the through hole 123a.

Therefore, when a power is applied to the power electrode 121 ', a plurality of conductive lumps 122' filled in the receiving member 123 are supplied with a constant voltage through the raw water, have.

13A and 13B illustrate that the housing member 123 and the power electrode 121 'can be drawn into the housing 110 through the electrode case 116' It is possible to change the design to be combined with Specifically, the electrode case has a shape in which a lower surface is not opened, so that the conductive mass 122 'can be received in the inner space, and a plurality of holes are formed in the lower surface of the electrode case, 1 through hole can be provided. The power electrode 121 'is electrically connected to the conductive lump 122' so that the pair of power electrodes 121 'provided on both sides of the electrode case face each other and the conductive lump 122' In the inner space of the electrode case so that the raw water flowing into the space inside the electrode case flows through the separating plate and flows toward the two electrode plates, And a second passage hole having a hole formed therethrough. In addition, the separator may be an insulator or an insulator to electrically isolate the power electrode 121 'and the conductive lump 122'. On the other hand, without the electrode case, the housing is provided with a fitting groove or the like so that the power electrode 121 'is directly opposed to each other, and the above-mentioned housing member 123 and the above- The conductive lump 122 'housed in the conductive lump 122' may be disposed.

At least one through hole may be formed through the conductive mass 122 'to increase the contact area with the raw water. For example, the conductive lump 122 'may be in the form of a hollow tube or a porous form having a plurality of through holes penetrating therethrough. Accordingly, even when the conductive masses 122 'are formed in the same size, the contact area with the raw water can be further increased compared to the conductive masses having no through holes, thereby reducing the total number of the conductive masses 122' The same processing efficiency can be obtained.

Meanwhile, the receiving member 123 may be made of an insulator or a non-conductor so as to prevent an electrical short circuit with the power electrode 121 'when power is applied. For example, the housing member 123 may be made of a material such as plastic, concrete, or plywood, but it is not limited thereto and any known insulator or non-insulator can be used. In addition, a coating layer having at least one of chemical resistance, corrosion resistance, and electrical thermal conductivity is applied to the outer surface of the receiving member 123 to prevent the receiving member 123 from being damaged by heavy metals contained in the raw water .

In addition, the gap between the conductive lump 122 'filled in the housing member 123 and the power electrode 121' may have a proper interval so as to prevent electric short-circuiting and to provide a smooth power supply. For example, the interval between any one of the conductive lumps 122 'and the power electrode 121' may be 1 to 10 mm, and the distance between the electrode pads of the power electrode 121 ' May have a thickness of 1 to 10 mm.

It is noted that the number of the plurality of conductive masses 122 'filled in the housing member 123 can be appropriately changed according to the processing capacity of the raw water to be processed. It is also noted that the amount of current applied to the power electrode 121 'can be appropriately changed depending on the correlation with the total surface area of the conductive mass 122' that is filled in the receiving member 123 and brought into contact with the raw water . Also, it is noted that the number of the electrode plates that serve as the power electrode 121 'may be provided in a plurality, and the position of the electrode plate may be appropriately changed.

6 and 7, in the electrocoagulation module 100 'according to the present invention, a diffuser 150 for generating fine bubbles is disposed on the first chamber 111 side where the raw water flows .

That is, the air diffusing pipe 150 is disposed on the first chamber 111 side formed on the lower side of the second chamber 112, so that the fine bubbles generated during the process of blowing air supplied from the outside To pass between the electrode plates of each electrode unit 120 disposed on the chamber 112 side.

As a result, agglomerates such as polymer hydroxides flocs generated in the electrocoagulation reaction adhere to the electrode unit 120 to prevent contamination of each of them, so that a smooth flocculation reaction can be performed. The maintenance time can be increased by reducing the maintenance cost.

The air diffuser 150 may be a hollow tube having a predetermined length and a plurality of discharge holes 151 formed in the longitudinal direction through which the diffuser holes 151 pass, May be disposed in a direction parallel to the inflow pipe (130) disposed in the first chamber (111).

It is noted that the air diffuser 150 may be disposed at the same height as the inflow pipe 130 or may be disposed at the upper or lower side of the inflow pipe 130.

At this time, the air diffuser 150 may include a porous substrate 152 covering the discharge hole 151 so that fine bubbles discharged through the discharge hole 151 have a size of 10 탆 or less , The porous substrate 152 may be formed with micropores having an average pore size of 5 mu m or less.

If the size of the fine bubbles discharged through the discharge hole 151 exceeds 10 mu m, the activation of the metal ions generated in the electrode unit 120 is inhibited for the electrocoagulation reaction upon power application, .

Accordingly, in the present invention, fine bubbles of 10 μm or less are generated by covering the discharge holes 151 through which the bubbles are discharged through the porous substrate 152 having fine pores, so that metal ions are smoothly generated in the electrode unit 120 .

Here, it is noted that the porous substrate 152 may be provided so as to entirely cover the outer surface of the air diffusing pipe 150, or may be partially provided only in a region corresponding to the discharge hole 151.

The electric coagulation modules 100, 100 ', 200, 200' according to the present invention may include a control unit for controlling the overall operation such as the power supply size and the current density applied to the pair of power electrodes 121, 121 ' (140).

At this time, the controller 140 may periodically convert polarities of the power applied to the pair of power electrodes 121 and 121 '. Accordingly, the polarity applied to both surfaces of the power electrodes 121 and 121 'is periodically changed during the electrocoagulation reaction, thereby enabling both surfaces to be used evenly. Accordingly, both sides of the power electrode 121 can be used evenly, so that the replacement period of the power electrode 121 can be increased.

Electrolytic water, which is the raw water that has passed through the electrocoagulation modules 3210, 100, 100 ', 200, 200', flows into the filter module 3220, and various suspended substances including electrocoagulated aggregates are filtered through the filter module 3220 Can be.

To this end, the filter module 3220 may include a plurality of flat filter units 2000 having filter filter media 1000 as shown in FIGS. 14A and 14B. At this time, a plurality of flat plate type filter units 2000 may be formed in a unit block spaced apart from the outer case at predetermined intervals, and at least one unit block may be provided to implement the filter module 3220.

The planar filter unit 2000 further includes a support frame 1100 for supporting a rim of the filter media 1000. The filter media 1000 may be provided on one side of the filter media 1000, A suction port 1110 capable of causing an intermediate pressure difference can be provided. In addition, the support frame 1100 may be provided with a flow path E through which the filtrate filtered out through the filter filter media 1100 can be discharged to the outside.

Specifically, when a suction force of high pressure is applied to the filter unit 2000 through the inlet port 1110, as shown in FIG. 14B, the electrolytic flocculation water P including the agglomerated agglomerated electro- and facing the interior of the media 1000, a filter media 1000, the filtrate was passed through, and filtered (Q ₁₎ has a flow path provided on the rear support frame 1100 is flowed along the flow path formed in the filter media 1000 ( E, and the introduced filtrate Q ₂ may be discharged to the outside through the inlet 1110.

And a filter media 1000 capable of filtering the agglomerated agglomerated matter and other foreign matter in the planar filter unit 2000. The filter material 1000 can be employed without limitation as a known filter material used in the water treatment field. However, it is important to select a filter material having a high water treatment speed in consideration of a treatment capacity of 1 m ³ / h or more of the electrocoagulation module 3210. If the filtration speed for the raw water flowing at a high speed and / or a large amount is slow in the electrocoagulation module having the treating capacity of 1 m ³ / h or more, the filtration efficiency and the durability of the device There is a problem that if the processing speed of the raw water passing through the filter media is increased in order to prevent such problems, the filtration efficiency of the electro-agglomerated foreign substances contained in the raw water may be deteriorated.

Accordingly, the filter medium 1000 provided in the filter module 3220 can have a filtration flow rate of 50 LMH or more with respect to the agglomerated body contained in the introduced electrolytic coagulation water, thereby minimizing an increase in the back pressure applied to the filtration part, The raw water can be quickly supplied to the osmotic filtration unit 3300 in accordance with the processing capacity of the cohesion module 3210 and the cohesion foreign matter contained in the raw water introduced from the electric cohesion module 3210 can be effectively removed. Further, the filter module includes a plurality of filter units each having a filter material 1000, and the filter material 1000 has a filtration flow rate of not less than 50 LMH with respect to the number of flocculated water flowing from the electrocoagulation module 3210 , The filtration efficiency for the agglomerates having a particle diameter of 0.2 탆 or more is 99% or more, so that the number of flocculated electro-agglomerated particles can be quickly treated and the filtration efficiency for the agglomerate is excellent.

In the case of the filter material 1000 having the above-mentioned physical properties, the filter module 3220 of the pretreatment unit 3200 included in the present invention can be employed without limitation, but in terms of durability due to improved backwashing efficiency and high mechanical strength, 15, the filter media 1000 according to an embodiment of the present invention includes a second support body 321, 322 sequentially stacked on both sides of a first support body 330, and a second support body 321, And the filtrate filtered in the nanofiber webs 311 and 312 may have a filtration path that flows in the direction of the first support body 130.

As shown in FIG. 15, a filter media 1000 provided in a filter module according to an embodiment of the present invention includes at least two types of supports 321/322 and 330 having different thicknesses. In this case, the filter media 1000 preferably has a basis weight of the nanofiber webs 311 and 312 of 30 g / m 2 or less, a basis weight of the first support 330 of 250 g / m 2 or more, Or more than 90% of the total thickness of the substrate 1000. The reason why the thickness of the first support body 330 should be thick enough to be 90% or more of the total thickness of the filter media 1000 and the reason why the filter media 1000 Quot;) should be provided in addition to the first support member.

As the water treatment process of the electrocoagulated water is repeated using the filter media, foreign substances such as agglomerates included in the electrocoagulated water adhere to the filter media to form an adherent layer or to be embedded in the filter media, thereby blocking the flow path and deteriorating the filtration function. Whenever the same problem arises, replacing the filter media increases the cost of seawater desalination. Accordingly, in order to extend the service life of the filter media, it is necessary to perform a cleaning process of periodically applying physical stimulus to the filter media to adhere to the filter media or to remove impurities contained in the filter media. BACKGROUND OF THE INVENTION [0003] BACKGROUND OF THE INVENTION [0004] BACKGROUND OF THE INVENTION [0005] BACKGROUND OF THE INVENTION [0005] [Background Art] [0005] Backwashing typically involves washing water in a direction opposite to the filtration direction of filter media, It is necessary to supply washing water or air at a pressure higher than the pressure applied to the filter media in the filtration process.

Accordingly, in order for the filter media to have the backwashing ability, it is important that the filter media have such mechanical strength that the filter media is not deformed or damaged even under high applied pressure, and a support for compensating mechanical strength is usually provided in the filter media . Factors that may affect the mechanical strength of the support include the structure of the support, for example, the diameter of the fibers forming the nonwoven fabric when the support is nonwoven, the length of the fibers, the manner of interfiber bonding, thickness and basis weight, The thicker or larger the basis weight, the greater the mechanical strength of the support. Therefore, for example, a nonwoven fabric having a large thickness or a nonwoven fabric having a very large basis weight may be used as a support for designing a filter medium which is resistant to backwashing.

On the other hand, it is preferable that the support has a large pore size so as not to affect the flow of the filtrate of the filter media. The lowering of the flow rate due to the support provided for compensating the mechanical strength is very undesirable because it deteriorates the main properties of the filter media. For example, when a nonwoven fabric exhibiting sufficient mechanical strength even though it has a small thickness is used as a support, the basis weight of the nonwoven fabric is very large, and thus the diameter and porosity of the pores in the nonwoven fabric are inevitably small. There is a problem in that a desired level of flow can not be ensured according to the flow rate.

Accordingly, the filter material 1000 according to the present invention has nanofiber webs 311 and 312 having a basis weight of 30 g / m 2 or less and a whole of the filter material 1000 in order to ensure the mechanical strength of the filter material 1000, It is preferable to provide the first support 330 having a thickness of 90% or more of the thickness. In the filter media 1000 having a nanofiber web having a basis weight of 30 g / m 2 or less, the thickness of the first support body 330 may account for 90% or more of the total thickness of the filter media 1000, 95% or more, and more preferably 95 to 98% of the total thickness of the substrate (1000). If the first support is less than 90% of the total thickness of the filter media 1000, the filter media 1000 having a basis weight of 30 g / m < 2 > or less may not have sufficient mechanical strength, The replacement cycle of the battery 1000 can be shortened. However, even when the thickness of the first support body satisfies 90% or more of the total thickness of the filter media 1000, there is a problem that sufficient mechanical strength can not be obtained when the basis weight of the first support body is small. Thus, the basis weight of the first support may satisfy 250 g / m 2 or more. If the basis weight of the first support is less than 250 g / m < 2 >, mechanical strength for backwashing can not be developed, and damage to the filter media and durability thereof can be reduced. Adhesion can also be significantly reduced.

Further, securing the mechanical strength of the first support member to such an extent that the first support member is less than 90% of the total thickness of the filter media 1000 and sufficient to withstand backwashing means that the flow of the electrolytically coagulated water due to the first support member, And in this case, the filter module 3220 has a high filtration speed due to the slow filtration speed of the filter medium 1000 for the raw water flowing at a high speed and / or a large amount in the electrocoagulation module having a treatment capacity of 1 m ³ / h or more. Back pressure is applied, which may cause problems in filtration efficiency and durability of the apparatus. Preferably, the first support 330 may have a basis weight of 800 g / m 2 or less. If the basis weight of the first support 330 exceeds 800 g / m 2, the thickness may be less than 90% The flow rate may be significantly reduced.

However, if the binding strength between the nanofiber webs 311, 312 functioning as a filter medium and the first support 330 is weak, the durability of the filter media 1000 due to backwashing may be deteriorated even though the mechanical strength is excellent. That is, the high pressure applied in the backwashing process can accelerate the interfacial separation between the layers forming the filter media 1000, and in this case, as shown in FIG. 17, There is a problem that the function can be remarkably reduced or completely lost as a separation membrane.

Therefore, it has been found that a filter having a certain level of adhesion between a first support having a considerably increased thickness and a nanofiber web as a filter medium has a high pressure applied during backwashing and a filter medium exhibiting sufficient durability against frequent backwashing It has an important meaning.

In general, a method of attaching the support and the nanofiber web may be performed by using a separate adhesive material or by fusing a low melting point component provided on the support to the nanofiber web to bond the two layers together. However, when the two layers are bonded to each other through a separate bonding material, there is a possibility that the bonding material is dissolved by the for-treatment water, thereby causing a problem of contamination of the filtrate and lowering of water permeability. If the binder material is partially backwashed, the backfill of the filter media or the nanofiber web may peel off and the filter media may be completely lost.

Accordingly, a method in which the nanofiber web and the support are bonded via the fusion bonding (A) can be adopted, and heat and / or heat may be applied to both the support 1 and the nanofiber web 2 stacked as shown in Fig. Pressure can be applied to bond them. However, when applying heat and / or pressure, consideration must be given to minimizing the physical and chemical transformation of the nanofiber web 2, which acts as a filter media due to the applied heat and pressure, The physical properties such as the flow rate and the filtration rate of the filter material designed at the beginning can be changed when the nano web is physically and chemically deformed.

On the other hand, when selecting the heat and / or pressure conditions in the attachment process so that there is no physical / chemical deformation of the nanofiber web 2, the material properties of the nanofiber web and support, such as melting point, thermal conductivity, . A low melting point component of the support may be fused to the nanofiber web by applying a temperature or pressure not lower than the melting point or higher than the melting point at the same time and applying a high pressure even if the melting point of the support is slightly lower than the melting point .

However, since the material forming the support or the nanofiber web is a polymer compound, such a polymer compound has a small thermal conductivity and a very large heat capacity. Therefore, even if a predetermined heat (H ₁ , H ₂ ) (H ₁ , H ₂ ) reaches the interface between the nanofiber web 1 and the support 2 to raise the temperature of the low melting point component provided in the support 2 to the melting point, Should be applied. 18, heat (H ₂ ) transmitted from below is transmitted to the vicinity of the interface between the nanofiber web 2 and the support 1, and when the support (1) It may take a longer time to raise the temperature of the melting point component to the melting point and it is necessary to apply a larger amount of heat downward to shorten the time. However, when too large heat is applied from below, melting of the low melting point component may occur first in the lower part of the first support, and the shape and structure of the support may be changed.

In this case, the nanofibrous web 2 may be physically / chemically deformed. In this case, the heat (H1) applied to the nanofibrous web 2 may be increased, There is a problem in that the physical properties of the filter media designed in the present invention can not be fully manifested.

If the thickness of the support 1 is too thick, the diameter of the fibers constituting the support 1 can be very large. As a result, when the support 1 and the nanofiber web 2 are joined together, It is inevitably accompanied by a decrease in the adhesion force, which makes it easy to peel off easily during backwashing or to inflate the nanofiber web 2.

Accordingly, the filter material 1000 according to an embodiment of the present invention does not face the first support 330 and the nanofiber webs 311 and 312 directly but intervenes between the second supports 321 and 322 having a smaller thickness This makes it possible to carry out the interlayer adhesion process more stably and easily, and exhibits remarkably excellent bonding force at the interface between the respective layers, and minimizes delamination and peeling problems even when a high external force is applied due to backwashing or the like.

19a, the second support 3, which occupies less than 10% of the total thickness of the filter media, is different in thickness from the nanofiber web 2 in that the nanofiber web 2 and the first support 1 The heat (H ₁ , H ₂ ) applied above and below the laminated body of the nanofiber web 2 / the second support 3 reaches the interface therebetween, B) is easier than in Fig. 18A, since the amount and time of heat to be applied is more easily controlled than in FIG. 18, it is advantageous to prevent physical / chemical deformation of the nanofiber web 2, ), There is an advantage that the nanofibers can be bonded with excellent adhesive force on the support without changing the physical properties of the nanofiber web 2 designed at the beginning.

The basis weight of the second support bodies 321 and 322 is preferably higher than that of the nanofiber webs 311 and 312 because the second support bodies 321 and 322 simultaneously exhibit excellent adhesion with the first support body 330 and the nanofiber webs 311 and 312, And the basis weight 330 of the first support body may be 8 to 16.5 times the basis weight of the second support bodies 321 and 322. [ If the basis weight of the second support body is set so that any of the basis weights of the first support body and the nano fiber body do not satisfy the above range, there is a fear of detachment during backwashing due to decrease in adhesion force, And / or the flow rate can be significantly reduced.

The first support body 330 supports the filter media 1000 and forms a large flow path to perform the filtration process or the backwash process more smoothly. . Specifically, when a pressure gradient is formed so as to have a lower internal pressure than that of the filter media in the filtration process, the filter media can be squeezed. In this case, since the flow path through which the filtrate flows in the filter media is significantly reduced or blocked There is a problem that a larger differential pressure is applied to the filter filter material and the flow rate is remarkably lowered. In addition, during backwashing, an external force may be applied to expand the filter media toward the outside in both directions. However, the filter media may be damaged due to an external force applied when the mechanical strength is low.

The first support 330 is provided to prevent the above-mentioned problems occurring in the filtration process and / or the backwashing process. The first support 330 may be a known porous member that is used in the water treatment field and has mechanical strength. For example, The first support may be a nonwoven, fabric or fabric.

The fabric means that the fibers included in the fabric have longitudinal and lateral directions, and the specific structure may be plain weave, twill weave, etc., and the density of warp and weft yarn is not particularly limited. Further, the knitted fabric may be a known knit structure, a weft knitted fabric, a knitted fabric, or the like, and may be, for example, a tricot knitted yarn. 15, the first support 330 may be a nonwoven fabric having no directionality in the longitudinal direction of the fibers 330a, and may be a dry nonwoven fabric such as a chemical bonding nonwoven fabric, a thermal bonding nonwoven fabric, an airray nonwoven fabric, a wet nonwoven fabric, a spunless nonwoven fabric , Needle punching nonwoven fabric, or meltblown, may be used.

The first support 330 may be provided to occupy 90% or more of the total thickness of the filter media as described above in order to exhibit sufficient mechanical strength. For example, it may be 2 to 8 mm, more preferably 2 to 5 mm, and even more preferably 3 to 5 mm of the first support 130. If the thickness is less than 2 mm, it may not exhibit sufficient mechanical strength to withstand frequent backwashing. Also, when the thickness exceeds 8 mm, the degree of integration of the filter material per unit volume of the module may be reduced when the filter material is implemented as a filter unit described below and a plurality of filter units are implemented by a limited space filter module.

 Preferably, the first support 330 has a basis weight of 250 to 800 g / m 2, more preferably 350 to 600 g / m 2, while satisfying the thickness condition as described above. If the basis weight is 250 g / m < 2 >, it may be difficult to exhibit sufficient mechanical strength, and adhesion with the second support may decrease. If the basis weight exceeds 800 g / m & And it may be difficult to smoothly back-wash due to an increase in pressure difference.

When the first support 330 is formed of fibers such as nonwoven fabric, the average diameter of the fibers may be 5 to 50 탆, more preferably 20 to 50 탆, still more preferably 25 to 50 탆, In consideration of the diameter of the fibers constituting the second support bodies 121 and 122 to be described later, it is possible to increase the contact area of the first support body and the second support body in the jointing state and thereby to exhibit an increased adhesion force There is an advantage to be able to. For example, the fiber diameter may be 35 micrometers. The first support 330 may have an average pore size of 20 to 200 μm, and preferably 30 to 180 μm. For example, the first support 330 may have an average pore size of 100 μm, May be 50 to 90%, preferably 55 to 85%. For example, the first support 330 may have a porosity of 70%, but is not limited thereto. In the filtration process and / or the backwash process There is no limitation as long as the nanofiber webs 311 and 312 described below are supported to exhibit a desired level of mechanical strength and at the same degree of porosity and pore size so as to smoothly form a flow path at high pressure.

The material of the first support body 330 is not limited if it is used as a filter media support body. By way of non-limiting example, synthetic polymer components selected from the group consisting of polyester based, polyurethane based, polyolefin based and polyamide based; Or a natural polymer component including a cellulose system may be used. However, if the first support has a brittle physical property, it may be difficult to expect a desired level of bonding force in the process of laminating the first support and the second support. This is because the first support has a smooth surface The surface may be macroscopically roughened while forming the porosity, and the surface formed by the fibers, such as nonwoven fabric, may not have a smooth surface depending on the arrangement of the fibers and the fineness of the fibers, to be. If the remaining portions are bonded while the portion not in contact with the interface between the two layers being bonded is present, delamination may be started due to the non-adhered portion. In order to solve this problem, it is necessary to carry out the lapping process while increasing the degree of close contact between the two layers by applying pressure in both layers. If the brittle physical property is strong, The support may be damaged when applying a larger pressure, so that the material of the first support may be flexible, the material of high elongation may be suitable, and preferably the second support 321 and 322 may have excellent adhesion The first support 330 may be a polyolefin-based material.

Meanwhile, the first support body 330 may include a low melting point component to bond with the second support bodies 321 and 322 without a separate adhesive or an adhesive layer. When the first support 330 is a nonwoven fabric, the first composite fiber 330a may have a low melting point. The first composite fiber 330a may include a supporting component and a low melting point component so that at least a part of the low melting point component is exposed on the outer surface. For example, a cis-core type conjugate fiber in which a support component forms a core portion and a low melting point component forms a sheath portion surrounding the core portion, and a side-by-side composite fiber having a low- Lt; / RTI > The low-melting-point component and the support component may be polyolefin-based in view of the flexibility and elongation of the support, as described above. For example, the support component may be polypropylene and the low-melting component may be polyethylene. The melting point of the low melting point component may be 60 to 180 ° C, more preferably 100 to 140 ° C. Through this, it is possible to exhibit an excellent adhesive strength without damaging the nanofiber web and the second support, It is advantageous to achieve.

Next, the second support bodies 321 and 322 arranged on both sides of the above-described first support body 330 will be described. The second supports 321 and 322 support the nanofibrous webs 311 and 312 to be described later and function to increase the bonding strength of the layers provided in the filter media.

The second support bodies 321 and 322 are not particularly limited as long as they generally serve as a support for the filter media. However, the second support bodies 321 and 322 are preferably fabric, knitted or nonwoven fabric. The fabric means that the fibers included in the fabric have longitudinal and lateral directions, and the specific structure may be plain weave, twill weave, etc., and the density of warp and weft yarn is not particularly limited. The knitted fabric may be a known knitted fabric, and may be a knitted fabric, a knitted fabric, or the like, but is not particularly limited thereto. The nonwoven fabric means that the fibers are not oriented in the longitudinal and transverse directions. The nonwoven fabric may be a dry nonwoven fabric such as a chemical bonding nonwoven fabric, a thermal bonding nonwoven fabric, an airlay nonwoven fabric, a wet nonwoven fabric, a spunless nonwoven fabric, a needle punching nonwoven fabric or a meltblown A non-woven fabric manufactured by the above-mentioned method can be used.

The second support bodies 323 and 322 may be nonwoven fabrics. The fibers forming the second support bodies 321 and 322 may have an average diameter of 5 to 30 μm, more preferably 10 to 25 μm, Considering both the diameters of the fibers constituting the first support body 130 and the diameters of the fibers constituting the nanofibrous webs 311 and 312, the area of the first support body and the second support body, There is an advantage that the contact area of the nanofiber web at the time of lapping can be increased and the increased adhesion force can be exhibited. The thickness of the second support bodies 321 and 322 may be 100 to 400 탆, more preferably 150 to 400 탆, still more preferably 150 to 250 탆, for example, 200 탆 . If the thickness of the second support is less than 100 탆, it may be difficult to secure sufficient mechanical strength in backwashing, and in particular, adhesion with the first support and / or the nanofiber web may be deteriorated. Or the basis weight becomes too large, the water permeability is lowered, and peeling may occur during backwashing. Also, if the thickness exceeds 400 탆, thermal bonding may not be easy when joining with the nanofiber web, and peeling may occur during backwashing.

The second support bodies 321 and 322 may have an average pore size of 20 to 100 μm and a porosity of 50 to 90%. However, the present invention is not limited thereto, and it is possible to support the nanofiber webs 311 and 322 to be described later to develop a desired level of mechanical strength, and at the same time, to prevent the flow of the filtrate flowing through the nanofiber webs 311 and 322 Porosity, and pore size.

The basis weight of the second support bodies 321 and 322 may be 35 to 100 g / m 2, more preferably 35 to 75 g / m 2, and may be 40 g / m 2, for example. If the basis weight is less than 35 g / m < 2 >, the amount of fibers forming the second support distributed at the interface formed with the nanofiber webs 311 and 312 described later may be small, A reduction in area may not be able to produce the desired level of cohesion. Further, the nanofibrous web may not exhibit sufficient mechanical strength to support the nanofiber web, and the adhesion with the first support may be reduced. In addition, if the basis weight exceeds 100 g / m 2, it may be difficult to secure a desired level of flow rate, and there may be a problem that smooth backwashing is difficult due to an increase in differential pressure.

When the second support bodies 321 and 322 are used as a support for the filter media, there is no limitation on the material of the second support bodies 321 and 322. By way of non-limiting example, synthetic polymer components selected from the group consisting of polyester based, polyurethane based, polyolefin based and polyamide based; Or a natural polymer component including a cellulose system may be used.

However, the second support bodies 321 and 322 may be polyolefin-based polymer components for enhancing adhesion between the nanofiber webs 311 and 312 described later and the first support body 130 described above. When the second support bodies 321 and 322 are made of the same material as the nonwoven fabric, they may be made of the second composite fiber 321a containing a low melting point component. The second composite fiber 321a may include a supporting component and a low melting point component so that at least a part of the low melting point component is exposed on the outer surface. For example, a cis-core type conjugate fiber in which a support component forms a core portion and a low melting point component forms a sheath portion surrounding the core portion, and a side-by-side composite fiber having a low- Lt; / RTI > The low-melting-point component and the support component may be polyolefin-based in view of the flexibility and elongation of the support, as described above. For example, the support component may be polypropylene and the low-melting component may be polyethylene. The melting point of the low melting point component may be from 60 to 180 ° C, more preferably from 100 to 140 ° C. Thus, it is advantageous to achieve the object of the present invention that the adhesive strength can be expressed with excellent strength without damaging the nanofiber web .

If the first support body 330 is embodied as the first composite fiber 330a having a low melting point component to exhibit a further improved bonding strength with the second support bodies 321 and 322, It is possible to form a more solidly welded portion due to fusion of the low melting point component of the first composite fiber 330a and the low melting point component of the second composite fiber 321a at the interface between the two supports 321. [ At this time, the first composite fiber 330a and the second composite fiber 321a may be made of the same material in terms of compatibility.

Next, the nanofiber webs 311 and 312 arranged above the second support bodies 321 and 322 will be described. The nanofiber webs 311 and 312 may have a three-dimensional network structure in which one strand or multiple strands of nanofibers are randomly and three-dimensionally stacked (see FIG. 16).

The nanofibers forming the nanofiber web may be formed of known fiber forming components. However, in order to exhibit excellent chemical resistance and heat resistance, the fluorine-based compound may be contained as a fiber-forming component. Thus, even if the raw water is seawater, the filtration efficiency / flow rate can be secured to a desired level without changing the properties of the filter media, There is an advantage that it can have a cycle. The fluorine-based compound may be used without limitation in the case of a known fluorine-based compound that can be prepared as a nanofiber. Examples of the fluorine-based compound include polytetrafluoroethylene (PTFE), tetrafluoroethylene-perfluoroalkylvinylether copolymer Tetrafluoroethylene-hexafluoropropylene copolymer (PEP), tetrafluoroethylene-hexafluoropropylene copolymer (FEP), tetrafluoroethylene-hexafluoropropylene-perfluoroalkyl vinyl ether copolymer (EPE) (ETFE), polychlorotrifluoroethylene (PCTFE), chlorotrifluoroethylene-ethylene copolymer (ECTFE), and polyvinylidene fluoride (PVDF) More preferably, the production cost is low and mass production of nanofibers through electrospinning is easy, and the mechanical strength and chemical resistance are excellent In one aspect may be a polyvinylidene fluoride (PVDF). When the nanofiber includes PVDF as a fiber forming component, the PVDF may have a weight average molecular weight of 10,000 to 1,000,000, preferably 300,000 to 600,000, but is not limited thereto.

The nanofibers may have an average diameter of 0.05 to 1 탆, more preferably 50 to 450 nm, and may be 250 nm, for example. If the average diameter of the nanofibers is less than 50 nm, the porosity and the permeability may be lowered, and if the average diameter exceeds 1 탆, the filtration efficiency may be lowered and the tensile strength may be lowered. In addition, the nanofiber may have an aspect ratio of 1,000 to 100,000, but is not limited thereto. For example, the nanofibers provided in the nanofiber webs 311 and 312 may include a first nanofiber group having a diameter of 0.1 to 0.2 μm, a second nanofiber group having a diameter of 0.2 to 0.3 μm and a second nanofiber group having a diameter of 0.3 to 0.4 μm 3 to 30% by weight, and 5 to 15% by weight based on the total weight of the nanofiber web 311, thereby improving adhesion with the second support, It is possible to further improve the mechanical strength upon backwashing due to the increase of the mechanical strength of itself, and it may be more advantageous to achieve the object of the present invention such as filtration efficiency, obtaining excellent flow rate. For example, the first nanofiber group having a diameter of 0.1 to 0.2 μm, the second nanofiber group having a diameter of 0.2 to 0.3 μm and the third nanofiber group having a diameter of 0.3 to 0.4 μm are respectively 35 wt%, 53 wt% 12% by weight.

The thickness of the nanofiber webs 311 and 312 may be 0.5 to 200 μm, more preferably 10 to 50 μm, and may be 20 μm, for example. If the thickness is less than 0.5 占 퐉, it is difficult to withstand backwashing due to mechanical strength deterioration, and there is a possibility that the damage is very likely to occur or the pore size is very small, and the flow rate may be significantly reduced. If the thickness exceeds 200 탆, there is a fear that the flow rate is reduced and swelling or peeling may occur due to backwashing. The porosity of the nanofiber webs 311 and 312 may be 40 to 90%, and more preferably 60 to 90%. In addition, the average pore diameter may be 0.1 to 5 占 퐉, more preferably 0.1 to 3 占 퐉, and may be 0.25 占 퐉, for example. If the average pore diameter of the nanofiber web is less than 0.1 탆, the water permeability against the permeated overpoor can be lowered, and if the average pore size exceeds 5 탆, the filtration efficiency against the pollutant may not be good.

In addition, the nanofiber webs 311 and 312 may be provided in more than one layer in the filter material 1000, and the pore size, pore size, basis weight, and / or thickness of each nanofiber web may be different.

Meanwhile, the nanofibers forming the nanofiber webs 311 and 312 may be modified to increase the hydrophilicity. For example, the hydrophilic coating layer may be further provided on at least a part of the outer surface of the nanofibers. If the nanofibers include a fluorine-based compound as described above, the fluorine-based compound has a very high hydrophobicity, and thus the flow rate is poor when the supernatant is a hydrophilic solution. For example, the hydrophilic coating layer may be formed on the surface of the hydrophobic nanofibers. The hydrophilic coating layer may be formed of a known hydrophilic polymer having a hydroxyl group, or the hydrophilic polymer may be crosslinked through a crosslinking agent . For example, the hydrophilic polymer may be a polyvinyl alcohol (PVA), an ethylenevinyl alcohol (EVOH), a sodium alginate, or the like, and most preferably a polyvinyl alcohol (PVA). The crosslinking agent may be used without limitation in the case of a known crosslinking agent having a functional group capable of crosslinking through a condensation reaction with a hydroxyl group of the hydrophilic polymer. For example, the functional group may be a hydroxyl group, a carboxyl group, or the like.

On the other hand, the hydrophilic coating layer may be formed on part or all of the outer surface of the nanofiber. At this time, the hydrophilic coating layer may be coated with nanofibers such that the hydrophilic coating layer contains 0.1 to 2 g per unit area (m2) of the nanofiber web.

The wetting angle of the surface of the modified nanofiber web 311, 312 to have a hydrophilic coating layer may be 30 degrees or less, more preferably 20 degrees or less, even more preferably 12 degrees or less, and still more preferably 5 degrees or less And thus it is possible to secure an improved flow rate despite the fact that it is a fibrous web embodied by nanofiber which is hydrophobic in material.

The filter material 1000 described above can be manufactured by a manufacturing method described later, but is not limited thereto.

The filter media 1000 may include (1) laminating a nanofiber web and a second support; And (2) arranging and laminating the lapped nanofiber web and the second support on both sides of the first support so that the second support abuts the first support.

First, in step (1), a step of laminating the nanofiber web and the second support may be performed.

The nanofiber web can be used without limitation in the case of a method of forming a fibrous web having a three-dimensional network shape with nanofibers. Preferably, the nanofiber web may be prepared by electrospinning a spinning solution containing a fluorine-based compound on a second support to form a nanofiber web.

The spinning liquid may be a fiber-forming component, for example, a fluorine-based compound and a solvent. The fluorine-based compound may be contained in the spinning solution in an amount of 5 to 30 wt%, preferably 8 to 20 wt%. If the fluorine-based compound is less than 5 wt%, it is difficult to form fibers, Even if the film is formed or spun, a large amount of beads are formed and the volatilization of the solvent is not performed well, so that the pores may be clogged in the calendering process described later. If the amount of the fluorine-based compound exceeds 30% by weight, the viscosity increases and the surface of the solution becomes solidified, which makes it difficult to spin for a long period of time.

The solvent may be any solvent that does not affect the radioactivity of the nanofibers described below without causing a precipitate while dissolving the fluorine-based compound as the fiber-forming component, but is preferably selected from γ-butyrolactone, cyclohexanone, 3 And at least one selected from the group consisting of hexanone, 3-heptanone, 3-octanone, N-methylpyrrolidone, dimethylacetamide, acetone dimethylsulfoxide and dimethylformamide. For example, the solvent may be a solvent for the mixing of dimethylacetamide and acetone.

The prepared spinning solution can be produced by a known electrospinning apparatus and method. For example, the electrospinning device may be an electrospinning device having a single spinning pack with one spinning nozzle or an electrospinning device with a plurality of single spinning packs or a spinning pack with multiple nozzles for mass production Also, Also, in the electrospinning method, wet spinning with dry spinning or external coagulation can be used, and there is no limitation with respect to the method.

The nanofiber web formed of nanofibers can be obtained when a spinning solution stirred in the electrospinning device is injected to electrospray on a collector, for example, paper. As the specific conditions for the electrospinning, the air pressure of the air injection nozzle provided in the nozzle of the spinning pack may be set in the range of 0.01 to 0.2 MPa. If the air pressure is less than 0.01 MPa, it can not contribute to the collection and accumulation. If the air pressure exceeds 0.2 MPa, the cone of the spinning nozzle is hardened to block the needles, and radiation trouble may occur. In addition, when the spinning solution is spinned, the injection rate of the spinning solution per nozzle may be 10 to 30 μl / min. The distance between the tip of the nozzle and the collector may be 10 to 30 cm. However, it is not limited to this, and it can be changed according to purpose.

Alternatively, the nanofiber web may be directly formed on the second support by directly electrospinning the nanofibers on the above-mentioned second support. The nanofibers accumulated / collected on the second support have a three-dimensional network structure, and heat and / or pressure is applied to retain the desired water permeability, filtration efficiency, porosity, pore size, And can be implemented as a nanofiber web having a three-dimensional network structure by being further added to the accumulated / collected nanofibers. As a specific method of applying the heat and / or the pressure, a known method may be adopted. As a non-limiting example, a conventional calendering process may be used, and the temperature of the applied heat may be 70-190 ° C. When the calendering process is carried out, it may be carried out a plurality of times, for example, a drying process for removing a part or all of the solvent and moisture remaining in the nanofibers through primary calendering, Secondary calendering can be performed for control and strength enhancement. At this time, the degree of heat and / or pressure applied in each calendering process may be the same or different.

On the other hand, when the second support is made of the low-melting-point conjugated fiber, the binding through the thermal fusion between the nanofibrous web and the second support can be promoted simultaneously through the calendering process.

Further, another hot melt powder or hot melt web may be further interposed to bind the second support and the nanofiber web. In this case, the applied heat may be 60 to 190 ° C, and the pressure may be 0.1 to 10 kgf / cm 2, but is not limited thereto. However, components such as hot melt powder, which are separately added for binding, are frequently melted in the laminating process between the support and the support and between the support and the nanofiber to frequently open the pores, thereby achieving the initial designed filter media flow rate It can not be done. In addition, it may dissolve in the water treatment process, which may cause environmental negative problems, so that it is preferable to bond the second support and the nanofiber web without preferably including them.

And then forming a hydrophilic coating layer by heat-treating the hydrophilic coating layer-forming composition treated on the nanofiber web. The drying process of the solvent in the hydrophilic coating layer-forming composition can be performed at the same time through the heat treatment. The heat treatment may be performed in a dryer, and the heat applied at this time may be 80-160 ° C., and the treatment time may be 1 minute to 60 minutes, but is not limited thereto.

Next, in step (2), the laminated nanofiber web and the second support are disposed on both sides of the first support so that the second support abuts the first support in the laminated second support and the nanofiber web, .

The step (2) includes: 2-1) laminating a second support and a nanofiber web laminated on both sides of the first support in the step (1) described above; And 2-1) fusing the first support and the second support by applying at least one of heat and pressure.

As a specific method of applying the heat and / or pressure in the step 2-2), a known method may be adopted. As a non-limiting example, a conventional calendering process can be used, and the temperature of the applied heat is 70 To 190 < 0 > C. When the calendering process is carried out, it may be carried out a plurality of times, for example, a first calendering followed by a second calendering. At this time, the degree of heat and / or pressure applied in each calendering process may be the same or different. Through the step 2-2), bonding can be carried out through thermal fusion between the second support and the first support, and an additional adhesive or adhesive layer can be omitted.

Meanwhile, the filter module 3220 included in another embodiment of the present invention is a filter filter material for achieving a further improved water treatment speed. As shown in FIG. 20, the nanofiber webs 411 and 412 are formed on both surfaces of the first support 430 The first support body 430 may include a plurality of filter media 1001 which penetrate the surfaces facing the nanofiber webs 411 and 412 in order to increase the flow path and minimize the water permeation resistance. And may have a hole (Q). The holes Q provided in the first support body 430 greatly reduce the flow resistance of the raw water to be filtered by providing a larger flow path for the filtrate that has passed through the nanofiber webs 411 and 412, Pressure can also be reduced. Therefore, even when a larger filtration pressure and / or a backwashing pressure is applied to the filter medium, the pressure applied to the filter medium can be further reduced, the damage of the filter medium including the nanofiber web can be minimized, And may be easier to remove the electrocoagulated foreign material more quickly in accordance with the raw water flowing at high speed and / or large capacity in the electrocoagulation module.

Alternatively, as shown in FIG. 21, the first support body 430 of the filter media 1002 may be provided with a first support body 430, a second support body 420, And a plurality of holes (Q) passing through the surfaces facing the first and second plates (421, 422).

22 and 23, the filter media 1003 and 1004 have a structure in which one support body 530 includes a plurality of first holes Q passing through a surface opposed to the second support bodies 521 and 522, And a plurality of second holes P passing through the second support bodies 521 and 522 in the same direction as the direction in which the first holes Q are penetrated. At this time, the diameter p of the second hole P may be equal to or smaller than the diameter q of the first hole Q. The second hole P may be positioned to communicate with the first hole Q as shown in FIG. 22, or may be positioned so as not to communicate with the first hole Q as shown in FIG. 23, The flow rate, the bonding strength of the first support body 530 and the second support bodies 521 and 522, and the like.

The diameters of the holes P, Q, the shapes of the cross sections, the pitches between the holes, and the like can be changed according to the purpose, so that they are not particularly limited in the present invention.

Between the electrocoagulation modules 3210, 100, 100 ', 200 and the filter module 3220, a storage tank for temporarily storing the electrocoagulation water treated in the electrocoagulation modules 3210, 100, 100', 200, A feed pump for feeding the filter module 3220, and other control devices.

Next, the osmotic filtration unit 3300 for processing the pretreated water introduced from the above-described pretreatment unit 3200 will be described.

The osmotic filtration unit 3300 includes an osmosis membrane module for desalinating the introduced pretreatment water, and the osmosis membrane module may be a reverse osmosis membrane module or a normal osmosis membrane module. The osmotic membrane module may further include a high-pressure pump for applying pressure higher than osmotic pressure of raw water or sea water to the module if the osmosis membrane module is a reverse osmosis membrane module.

The osmotic module may include a plurality of osmotic units including a known reverse osmosis membrane or a normal osmosis membrane and having unit units formed in a known shape. 24 and 25, the osmotic unit 700 includes a plurality of osmosis membranes 730 wound around a porous permeated water outlet pipe 720 and wound therearound, .

The porous permeate outlet pipe 720 can be used without limitation in the case of an outflow pipe commonly used for a reverse osmosis membrane or a osmosis membrane. The porous permeate outlet pipe 720 includes a plurality of holes 721 through which saline-free treated water can be drained through the osmosis process, and preferably the diameter thereof may be 4 to 8 inches, May be between 30 and 50 inches. However, the present invention is not limited thereto, and the diameter and length of the porous permeated water outlet pipe 720 may vary depending on the purpose.

The osmosis membrane 730 may include a spacer 733 interposed between the first osmosis membrane 731, the second osmosis membrane 732 and the first osmosis membrane 731 and 732. The first osmosis membrane 731 and the second osmosis membrane 732 can be a known reverse osmosis membrane or a normal osmosis membrane and include, for example, a support, a polymer support formed on the support, and an optional separation layer formed on the polymer support Lt; / RTI >

The support is not particularly limited as long as it functions as a supporting member of the membrane, and usually serves as a support of the membrane, and may preferably be a woven fabric or a nonwoven fabric. The fabric means that the fibers forming the fabric have a longitudinal and transverse directionality, and the specific structure may be plain weave, twill weave, etc., and the density of warp and weft yarn is not particularly limited. The support material is preferably a synthetic fiber selected from the group consisting of polyester, polypropylene, nylon and polyethylene; Or a natural fiber including a cellulose system may be used. When the support is a nonwoven fabric layer, the physical properties of the membrane can be controlled according to the porosity and hydrophilicity of the material. When the support is a nonwoven fabric, the average pore diameter may be 1 to 600 탆, preferably 5 to 300 탆, so that smooth permeation of the fluid and water permeability required for the reverse osmosis membrane can be improved. However, the diameter of the pores is not limited. When the nonwoven fabric is used, the thickness is preferably from 20 to 150 mu m, and if it is less than 20 mu m, the strength and supportability of the entire film is insufficient, and if it exceeds 150 mu m, the flow rate may be decreased.

Next, the polymer scaffold formed on the support will be described. The polymer scaffold is not particularly limited as long as it can form a reverse osmosis membrane. However, in consideration of mechanical strength, it is preferable to use a polymer scaffold having a weight average molecular weight in the range of 65,000 to 150,000, and preferred examples thereof include polysulfone or polyethersulfone An olefinic polymer such as a polysulfone polymer, a polyamide polymer, a polyimide polymer, a polyester polymer or a polypropylene, a polybenzimidazole polymer, polyvinylidene fluoride or polyacrylonitrile, etc. Lt; / RTI > The thickness of the polymer scaffold may be from 30 to 300 탆. If it is less than 30 탆, there may be a problem of a decrease in flow rate and durability due to compaction, and if it exceeds 300 탆, . The pore size of the polymer scaffold is preferably 1 to 500 nm. If the pore size exceeds 500 nm, after forming the thin film of the selective separation layer, the thin film may sink into the pore of the polymer support layer, so that it may be difficult to achieve the required flat sheet structure.

Next, the selective separation layer formed on one side of the polymer scaffold may be used without limitation as long as it is a selective separation layer that can be generally used for the reverse osmosis membrane. Preferably, the selective separation layer is formed of a polyamide-, polypiperazine-, polyphenylenediamine-, A phenylene diamine type, and a polybenzidine type, and more preferably, it may be formed of a polyamide-based material. If the thickness of the selective separation layer is less than 0.1 탆, the salt removing ability is deteriorated to fail to serve as a separation layer. If the thickness is more than 1 탆, the thickness of the separation layer is excessively thick, There may be a problem.

The osmosis membrane 730 may be provided in the osmosis unit 700 such that the selective layer of the first osmosis membrane 731 and the second osmosis membrane 732 faces outward and the respective supports abut against each other, A spacer 733 may be provided between the first osmosis membrane 731 and the second osmosis membrane 732 to secure a sufficient channel. The spacer 733 increases the amount of the flow path in the osmosis membrane 730 and the amount of the flow path, thereby improving the inflow of the raw water to be desalinated and generating a uniform filtration flux along the flow path. Further, as the turbulence is promoted along the flow path, the flow rate at the surface of the osmotic membrane is improved, so that the osmotic action can be smoothened, and high-flow fresh water can be obtained. The spacer may be a mesh or a tricot, and is preferably selected from the group consisting of polypropylene, polyethylene, poly-4-methylpentene, crystalline copolymers with propylene-alpha olefins, polyethylene terephthalate, polybutylene terephthalate, Polycarbonate, or a modified polyester (LMP: Low Melting Polyethylene Terephthalate) in which nylon or polypropylene is copolymerized with a polyethylene terephthalate resin. The thickness of the spacer may be 0.01 to 1 mm, but is not limited thereto.

The osmosis membrane 730 may be wound into a plurality of porous permeated water outlet pipes 720 in a spiral shape. The osmosis membrane 730 may include a spacer 740 for smooth flow passage between the plurality of osmosis membranes 730 For example, a mesh sheet.

The osmosis membrane 730 wound around the porous permeated water outlet pipe 720 through the spacer may be provided in an outer housing 710 capable of receiving the osmosis membrane 730 therein and may be embodied as an osmosis unit 700, A plurality of units 700 may be mounted to form an osmosis module.

Although the osmotic unit described above has been described with reference to the osmosis membrane of a flat membrane, the osmosis membrane may be a hollow fiber membrane, or it may be an osmotic unit implemented with a known reverse osmosis or osmosis hollow fiber membrane.

The treated water passing through the osmotic filtration unit 3300 including the osmotic module described above can be further roughened by a known post-treatment facility for sterilization and filtration of the target material. The filtered water after the post-treatment facility is stored in the storage tank, , Industrial water, agricultural water, and the like.

The present invention will now be described more specifically with reference to the following examples. However, the following examples should not be construed as limiting the scope of the present invention, and should be construed to facilitate understanding of the present invention.

≪ Example 1 >

An electrocoagulation module and a filter module were prepared as a pretreatment section. As shown in FIGS. 13A and 13B, the electro-agglomerating module was constructed such that 300 conductive particles of aluminum were disposed between power electrodes facing each other, and the distance between one electrode of the conductive material and one electrode was 10 mm An electrocoagulation module with a capacity of 1 m ³ / h was prepared. In addition, the filter module implemented the filter media prepared as described below as a filter unit of a flat membrane as shown in FIGS. 14A and 14B, and 20 filter units thus implemented were mounted on the filter module. Thereafter, the electrolytic coagulation water treated in the electrocoagulation module is introduced into the filter module, and the filtered water processed in the filter module is connected to the osmotic filtration part. The osmosis filtration unit has a known reverse osmosis module and is constructed according to a known design, thereby implementing a seawater desalination apparatus as shown in Table 1 below.

* Preparation Example - Filter media

First, to prepare a spinning solution, 12 g of polyvinylidene fluoride (Arkema, Kynar 761) as a fiber-forming component was added to 88 g of a mixed solvent of a mixture of dimethylacetamide and acetone at a weight ratio of 70:30 for 6 hours Using a magnetic bar to prepare a mixed solution. The spinning solution was poured into a solution tank of the electrospinning device and discharged at a rate of 15 / / min / hole. At this time, the temperature of the spinning section was kept at 30 ° C, the humidity was maintained at 50%, the distance between the collector and the tip of the spinning nozzle was 20 cm, the polyethylene having the melting point of about 120 ° C as the second support, (NANYANG nonwoven fabric, CCP40) having a thickness of about 200 mu m and a basis weight of 40 g / m < 2 > formed of low melting point second composite fibers having an average diameter of 20 mu m with propylene as the core part was placed. (Spin Nozzle Pack) and an air pressure of 0.03 MPa per spinning nozzle was applied to the surface of the second support to form a laminate having a nanofiber web formed of PVDF nanofibers having an average diameter of 250 nm on one surface of the second support . The fabricated nanofiber web was composed of a first nanofiber group having a diameter of 0.1 to 0.2 μm, a second nanofiber group having a diameter of 0.2 to 0.3 μm and a third nanofiber group having a diameter of 0.3 to 0.4 μm, 53% by weight and 12% by weight, and had an average diameter of 250 nm. The basis weight was 10 g / m 2, the thickness was 13 μm, the average pore diameter was 0.3 μm, and the porosity was about 75%.

Next, the solvent and moisture remaining in the nanofiber web of the laminate were dried, and the calendering process was performed by applying heat and pressure at a temperature of 140 ° C or more and 1 kgf / cm 2 to heat-seal the second support and the nanofiber web . 6, the second support and the nanofiber web were thermally fused together, and the nanofiber web was implemented in a three-dimensional network structure as shown in FIGS. 5A and 5B.

The resulting laminate was immersed in the hydrophilic coating layer forming composition prepared in the following preparation example, and then dried in a dryer at a temperature of 110 ° C for 5 minutes to provide a hydrophilic coating layer on the surface of the nanofibers of the nanofiber web.

Thereafter, the laminate was placed on both sides of the first support so that the second support faced each other in the produced laminate. The first support is a nonwoven fabric having a basis weight of 450 g / m < 2 > formed of low melting point second composite fibers having a thickness of 5 mm, polyethylene having a melting point of about 120 DEG C as an initial portion and a polypropylene core portion having a diameter of about 30 mu m (NANYANG nonwoven fabric, NP 450) was used. Thereafter, heat of 140 ° C and a pressure of 1 kgf / cm 2 were applied to produce filter media

≪ Comparative Example 1 &

A seawater desalination apparatus as shown in Table 1 was implemented in the same manner as in Example 1 except that a pretreatment unit was not provided and only three doses were used.

≪ Comparative Example 2 &

The pretreatment unit was constructed in the pretreatment unit with only the filter module without the electrocoagulation module to implement the seawater desalination apparatus as shown in Table 1 below.

<Experimental Example 1>

The seawater desalination apparatus was operated under the same conditions by introducing seawater at a flow rate of 1 m ³ / h into the pretreatment unit of the seawater desalination apparatus according to Example 1, Comparative Example 1 and Comparative Example 2, The time point of arrival of the replacement cycle of the battery was evaluated. As a result of evaluation, the reverse osmosis membrane replacement cycle arrival time in the other Examples and Comparative Example 2 was expressed as a relative percentage based on the reverse osmosis membrane replacement cycle arrival time in Comparative Example 1 as 100. At this time, the replacement cycle was evaluated by setting the point at which the flow rate decreased by about 30% from the obtained flow rate based on the desalination flow rate obtained during the operation time of the initial 30 hours of the seawater desalination apparatus.

Example 1 Comparative Example 1 Comparative Example 2 The pre- Electrocoagulation module + filter module none Filter module Reverse osmosis membrane backwash timing (%) 560 100 240

As can be seen from Table 1, in the case of Embodiment 1 including both the electrocoagulation module and the filter module as the pretreatment portion before the osmotic filtration portion, it can be confirmed that the replacement time of the osmosis membrane of the osmotic filtration portion can be remarkably extended.

&Lt; Examples 2 to 16 >

The filter media were prepared in the same manner as in Example 1 except that the thickness / weight of the first support, the thickness / weight of the second support, and the basis weight of the nano-island web were changed as shown in Table 2 or Table 3 below, The filter media as shown in Table 3 were fabricated and the seawater desalination system was implemented.

In this case, in Example 12, a support having a specification similar to that of Example 1, the first support and the second support was used, and the initial portion was formed of a low melting point polyester copolymer having a melting point of 142 ° C The first support body and the second support body were changed to each other, and the temperature at the time of laminating was changed to 160 ° C, respectively, to implement the filter media.

<Experimental Example 2>

The following properties of the seawater desalination apparatus employing the respective filter media prepared in the examples were evaluated and shown in Tables 2 and 3 below.

1. Initial water permeability measurement

The operating pressure was applied to the filter module at 50 kPa to measure the water permeability per unit area of 0.5 m 2 and filtration efficiency for one filter unit. In this case, the initial water permeability was calculated as a relative percentage of the water permeability of the filter unit implemented with the filter material according to the other embodiments based on the water permeability of the filter unit implemented in the filter material of Example 1 as 100. [

2. Back wash durability evaluation

After separating one filter unit from the filter module, the separated filter unit was immersed in water, and then the operation pressure was increased to 50 kPa, and backwashing was performed under the condition that 400 LMH of water was pressurized for 2 minutes per 0.5 m 2, The back washing durability was evaluated as? When the appearance abnormality such as swelling occurred in the course of the process, and when the abnormality was not observed, the back washing durability was evaluated.

At this time, only the filter unit in which the appearance abnormality did not occur during the operation under the operating condition of 50 kPa was backwashed by increasing the pressure to 125 kPa, which is the pressurizing condition exceeding the normal backwashing condition, Respectively.

The water permeability of the filter unit was measured in the same manner as in the initial water permeability measurement method when backwashing at an operating pressure of 125 kPa was carried out.

At this time, the water permeability was calculated by the rate of change according to the following equation (1) for the water permeability (B) after backwashing with respect to the initial water permeability (A) of each specimen. The larger the variation ratio, the more damage to the nanofiber webs due to backwashing and the interlayer delamination that is not visible as a result of appearance.

(%) = {(B - A) 100} / A

Example 1 Example 2 Example 3 Example 4 Example 5 Example 6 Example 7 Example 8 Nanofiber web Basis weight (g / ㎡) 10 20 29 25 10 10 10 10 Thickness (㎛) 15 25 40 40 15 15 15 15 The second support Basis weight (g / ㎡) 40 40 40 40 59 62 40 40 Thickness (㎛) 200 200 200 200 250 250 200 200 The first support Basis weight (g / ㎡) 450 450 450 450 450 450 330 650 Thickness (㎛) 5000 5000 5000 5000 5000 5000 5000 5000 Filter media Total thickness (㎛) 5215 5225 5240 5240 5265 5265 5215 5215 The ratio of the first support body thickness in the filter media as a whole (%) 95.9 95.7 95.4 95.0 95.0 95.9 95.9 95.9 Nanofibrous web Basis standard second support weight scale 4 2 1.38 1.60 5.9 6.2 4 4 Second support weight basis first support weight load factor 11.25 11.25 11.25 10.23 7.63 7.26 8.25 16.25 Initial water permeability (%) 100 92 82 88 96 91 100 86 Backwash durability Abnormal
(@ 50kPa) × × × × × × × × Abnormal
(@ 125kPa) × × × × × × × × Water permeability variation (%) 6.8 8.1 21.5 13.6 13.1 28.9 12.2 7.6

Example 9 Example 10 Example 11 Example 12 Example 13 Example 14 Example 15 Example 16 Nanofiber web Basis weight (g / ㎡) 10 10 10 10 10 10 10 32 Thickness (㎛) 15 15 15 15 15 15 15 40 The second support Basis weight (g / ㎡) 40 40 40 41 40 40 0 40 Thickness (㎛) 200 200 200 200 230 230 0 200 The first support Basis weight (g / ㎡) 680 450 270 430 270 230 270 450 Thickness (㎛) 5000 3400 2200 5000 2000 2500 2200 5000 Filter media Total thickness (㎛) 5215 3615 2415 5215 2245 2745 2215 5240 The ratio of the first support body thickness in the filter media as a whole (%) 95.9 94.1 91.1 95.9 89.2 91.1 99.4 95.4 Nanofibrous web Basis standard second support weight scale 4 4 4 4.1 4 4 0 1.25 Second support weight basis first support weight load factor 17 11.25 6.75 10.49 6.75 5.75 - 11.25 Initial water permeability (%) 84 87 80 100 79 87 94 76 Backwash durability Abnormal
(@ 50kPa) × × × × × ○ ○ × Abnormal
(@ 125kPa) × × × × ○ Not performed Not performed ○ Water permeability variation (%) 12.1 13.6 14.0 14.6 Unmeasured Unmeasured Unmeasured Unmeasured

As can be seen in Tables 2 and 3,

In the filter medium of Example 16 having a basis weight of the nanofiber web of 30 g / m &lt; 2 &gt;, there was no apparent abnormality upon backwashing at a pressure of 50 kPa, but when the backwashing pressure was 125 kPa, The swelling phenomenon as shown in Fig. 17 occurred. On the other hand, in the case of Examples 1 to 3, in which the basis weight of the nano-fiber web is 30 g / m 2 or less, no abnormality occurs during backwashing at a pressure of 125 kPa.

In the case of Example 13 in which the thickness of the first support was less than 90% of the total filter media thickness, there was no abnormality in appearance due to backwashing at a pressure of 50 kPa, but when the pressure was increased to 125 kPa, Has occurred. On the contrary, in the case of Example 11 in which the thickness of the first support body is 90% or more as compared with the total thickness of the filter media under the same condition, the pressure is increased to 125 kPa to confirm that the appearance abnormality does not occur even though the backwashing is performed.

In the case of Example 14 in which the basis weight of the first support was less than 250 g / m 2, although the thickness of the first support was 90% or more as compared with the total thickness of the filter media, the appearance abnormality occurred even in the backwashing pressure of 50 kPa It can be confirmed that the durability after backwashing is significantly lower than that of Comparative Example 1 due to the decrease in mechanical strength due to washing.

In addition, in Example 15 in which the second support was not included, it was confirmed that an appearance abnormality occurred even when backwashing was performed at a pressure of 50 kPa. This is expected as a result of the weakening of the adhesion between the first support and the nanofiber web despite the fact that it has a first support capable of withstanding the pressure of backwashing as in Example 11 without the second support.

On the contrary, in the case of Example 11 in which the basis weight of the first support was 250 g / m &lt; 2 &gt; or more, it was confirmed that the appearance abnormality did not occur even under the harsh driving condition of 125 kPa.

On the other hand, in Examples 3 and 6 in which the basis weight of the second support is not in the range of 1.5 to 6 times the basis weight of the nanofiber web among Examples, the water permeability variation As shown in Fig.

In addition, in the case of Example 6, Example 6 in which the basis weight of the first support member does not fall within the range of 8 to 16.5 times based on the second support member, the water permeability variation ratio was significantly larger than that in Example 7, Example 9 shows that the water permeability variation rate was increased compared with Example 8, and the initial water permeability was significantly lowered.

In addition, even when the thickness of the first support is 90% or more of the total thickness of the filter media, it can be seen that Example 1 in which the thickness of the first support is 95% or more of the total thickness of the filter media is significantly lower than that in Example 10 Can be confirmed.

In the case of Example 12 in which the first support and the second support were formed of polyester-based low-melting-point conjugated fibers other than polyolefin-based, the durability after backwashing was lowered when the backwashing pressure was 125 kPa, It was expected that the adhesive force was lowered than that of Example 1 which is a polyolefin type due to a physical property.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed exemplary embodiments, It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

3100: Feed pump 3200: Pretreatment unit
100, 100 ', 200, 200', 3210: electrocoagulation module 3210: filter module
100, 100 ', 200: electrocoagulation device 110, 210: housing
111: first chamber 112: second chamber
113: third chamber 114: partition wall
115: fit-in groove 116, 116 ': electrode case
117: insertion groove 118: exhaust hole
119: drain pipe 120, 120 ': electrode unit
121, 121 ': Power electrode 122:
122 ': conductive lump 123: housing member
123a: second discharge hole 123b: first discharge hole
130: Inflow pipe 131:
140: control unit 150:
151: Discharge ball
1,330, 430, 530:
2,311, 312, 411, 412, 511, 512:
3, 321, 322, 421, 422, 521, 522:
700: osmotic unit 710: outer housing
720: Porous permeate outlet tube 730: Osmosis membrane
740: Spacer
1000, 1001, 1002, 1003, 1004: Filter filter material 1100: Support frame
2000: Plate type filter unit

Claims (15)

A pretreatment unit including an electrocoagulation module for electrocoagulating suspended solids contained in the influent seawater and a filter module for filtering aggregates contained in the electrocoagulated water introduced from the electrocoagulation module; And
And an osmotic filtration unit having an osmosis membrane module for desalinating the pre-treatment water introduced from the pre-treatment unit. The method according to claim 1,
Wherein the electrocoagulation module electrocoagulates foreign matter contained in the seawater through positive ions generated from the sacrificial electrode, and the treatment capacity of the inflowing seawater is not less than 1 m ³ / h. The method according to claim 1,
Wherein the filter module comprises at least one filter unit having a filter medium, wherein the filter medium has a filtration flow rate of not less than 50 LMH for the coagulated water introduced from the electrocoagulation module, Wherein the efficiency is 99% or more. The method of claim 3,
Wherein the filter medium comprises a second support layer and a nanofiber web layer sequentially stacked on both sides of the first support layer, wherein a flow path is formed through which the filtrate filtered in the nanofiber web flows in the direction of the first support Seawater desalination equipment. 5. The method of claim 4,
Wherein the first support has a basis weight of 250 to 800 g / m 2 and a thickness of 2 to 8 mm. 5. The method of claim 4,
Wherein the basis weight of the second support is 35 to 100 g / m 2, and the thickness of the second support is 150 to 250 탆. 5. The method of claim 4,
Wherein the nanofiber web comprises a fluorine-based compound as a fiber-forming component,
The fluorine-based compound may be at least one selected from the group consisting of polytetrafluoroethylene (PTFE), tetrafluoroethylene-perfluoroalkylvinylether copolymer (PFA), tetrafluoroethylene-hexafluoropropylene copolymer (FEP) (EPE) -based, tetrafluoroethylene-ethylene copolymer (ETFE) -based, polychlorotrifluoroethylene (PCTFE) -based, chlorotrifluoroethylene-based, ethylene-hexafluoropropylene-perfluoroalkylvinylether copolymer -Ethylene copolymer (ECTFE) -based and polyvinylidene fluoride (PVDF) -based compounds. 5. The method of claim 4,
Wherein the nanofiber web has an average pore size of 0.1 to 5 占 퐉 and a porosity of 60 to 90%. 5. The method of claim 4,
Wherein the nanofibers forming the nanofiber web have an average diameter of 0.05 to 1 占 퐉. 5. The method of claim 4,
Wherein the basis weight of the nanofiber web is 30 g / m 2 or less, the basis weight of the first support is 250 g / m 2 or more, and the thickness is 90% or more of the total thickness of the filter media. 5. The method of claim 4,
Wherein the basis weight of the second support body is 1.5 to 6 times the basis weight of the nanofiber web and the basis weight of the first support body is 8 to 16.5 times the basis weight of the second support body. 5. The method of claim 4,
Wherein the second support comprises a second composite fiber including a support component and a low melting point component such that at least a portion of the low melting point component is exposed on the outer surface, Respectively,
Wherein the first support comprises a first composite fiber including a support component and a low melting point component such that at least a portion of the low melting point component is exposed on an outer surface, and the low melting point component of the first composite fiber and the second composite Wherein the first support and the second support are joined by fusing between low-melting-point components of the fiber. The method of claim 3,
Wherein the filter unit further comprises a support frame for supporting a rim of the filter media,
Wherein the support frame has a flow path for allowing the filtrate filtered out from the filter media to flow out to the outside. The electrochemical device according to claim 1,
A housing having an inner space with an open top; And
And an electrode unit disposed in the inner space, the electrode unit including a sacrificial electrode and a power electrode for agglomerating foreign matter contained in externally supplied seawater,
The internal space is divided into a first chamber into which the seawater flows, a second chamber which is disposed on the upper side of the first chamber and in which the electrode section is disposed, and a third chamber in which the electrocoagulation reaction completed in the second chamber is temporarily stored. Wherein the seawater desalination apparatus comprises a chamber. An electrocoagulation module for electrocoagulating a foreign substance contained in the seawater; And
And a filter module for filtering the agglomerates contained in the electrolytic flocculation water introduced from the electrocoagulation module.

Images