JP6212435B2 - Water treatment apparatus and water treatment method - Google Patents

Description

The present invention relates to a water treatment apparatus and a water treatment method, and more particularly, to a water treatment apparatus and a water treatment method capable of easily washing a membrane module even if the membrane module is hardly contaminated.

Conventionally, raw water is purified by a water treatment apparatus provided with a polymer water treatment membrane. Examples of the purification of raw water include turbidity of river water and groundwater, clarification of industrial water, treatment of drainage and sewage, pretreatment for desalination of seawater, and the like. The polymer water treatment membrane is often a hollow fiber-like porous membrane (hereinafter also referred to as “hollow fiber membrane”) made of a polymer material. This is because the hollow fiber membrane easily separates various components contained in the raw water.

In order to separate raw water, the membrane separation performance of the hollow fiber membrane is important. As an example of the configuration of the hollow fiber membrane, Japanese Patent Application Laid-Open No. 10-249105 (Patent Document 1) discloses a hollow fiber membrane having a hollow portion with an inner diameter of 200 μm and a three-layer structure. The structure of the hollow fiber membrane of Patent Document 1 is, in order from the inside, a porous layer with a thickness of 25 μm, a non-porous layer with a thickness of 1 μm, and 30 μm.
Three layers of porous layers are laminated.

As another example of the hollow fiber membrane, in Japanese Patent Application Laid-Open No. 09-253631 (Patent Document 2), the hollow fiber membrane is folded back in a U shape at the center, and the tip of the hollow fiber membrane is heated together with the container. Potting with curable resin. In this container, the wedge-shaped protrusion is provided on the inner peripheral portion of the end portion, thereby increasing the adhesive force between the thermosetting resin and the container.

JP-A-10-249105 Japanese Patent Application Laid-Open No. 09-256331

However, since the conventional hollow fiber membrane has an outer diameter of the order of μm, when the container, the hollow fiber membrane and the thermosetting resin are bonded, the thermosetting resin does not spread sufficiently,
Adhesion between the container and the hollow fiber membrane may not be sufficient. Due to such poor adhesion, peeling between the hollow fiber membrane and the container was likely to occur, and the reliability of the membrane module was low. Also,
In some cases, the interfacial separation of the hollow fiber membrane may occur due to the reverse flow of the cleaning liquid during the cleaning of the hollow fiber membrane.

This invention is made | formed in view of the said present condition, The objective provides the water treatment apparatus and water treatment method which can improve the reliability of a membrane module by fixing a hollow fiber membrane reliably. There is.

The present inventor considered the reason why the thermosetting resin does not sufficiently spread on the surface of the hollow fiber membrane. When the outer diameter of the hollow fiber membrane is small and the membrane filling rate is large, the surface tension of the hollow fiber membrane is It was found that the thermosetting resin is difficult to diffuse due to the large thickness. Based on this knowledge, by adjusting the outer diameter and filling rate of the hollow fiber membrane, the space between the hollow fiber membranes can be secured while maintaining the self-supporting property of the membrane itself, and thermosetting The resin was sufficiently distributed between the hollow fiber membranes to complete the present invention described below.
[1] The water treatment device of the present invention is connected to the storage tank that stores the raw water, the membrane module that processes the raw water, the storage tank and the membrane module, and returns the concentrated water processed by the membrane module to the storage tank. The membrane module includes a hollow fiber membrane that solid-liquid separates raw water, a holding member that holds the hollow fiber membrane, and a thermosetting resin that fixes the hollow fiber membrane and the holding member, and is hollow Yarn membrane
The outer diameter is 3 mm or more and 10 mm or less, and the film filling rate is 40% or more and 70% or less.
[2] It is preferable to further include a supply pipe connected to the storage tank and the membrane module and supplying the raw water stored in the storage tank to the membrane module.
[3] The holding member preferably further includes a support for holding the shape of the hollow fiber membrane.
[4] A supply device for supplying raw water to the membrane module is preferably connected.
[5] The water treatment method of the present invention is a water treatment method using the water treatment apparatus according to any one of the above [1] to [4], wherein the flow rate of raw water supplied to the hollow fiber membrane is 0. .05 m / sec to 1 m / sec.

In the water treatment apparatus and the water treatment method of the present invention, since the hollow fiber membrane is securely fixed, the reliability of the membrane module is high, and the leakage of raw water due to poor filling of the thermosetting resin is prevented during the production of the membrane module. be able to.

It is a schematic diagram which shows the water treatment apparatus of Embodiment 1. FIG. It is the schematic diagram and sectional drawing of a membrane module. It is a schematic diagram which shows an example of the form which combined multiple membrane modules. It is a left view of what connected the membrane module of FIG. It is a conceptual diagram which shows the water treatment apparatus of Embodiment 2. It is a conceptual diagram which shows the water treatment apparatus of Embodiment 3.

<Embodiment 1>
(Water treatment equipment)
FIG. 1 is a schematic diagram illustrating an outline of the water treatment apparatus according to the first embodiment. As shown in FIG. 1, the water treatment apparatus according to this embodiment is a “outside tank type” in which the membrane module 2 is disposed outside the storage tank 1. The water treatment apparatus of this embodiment is connected to the storage tank 1 for storing raw water, the membrane module 2 for processing raw water, the storage tank 1 and the membrane module 2, and the concentrated water processed by the membrane module 2 is stored in the storage tank 1.
And a return pipe 4 to be supplied. The water treatment apparatus of the present embodiment further includes a supply pipe 3 that is connected to the storage tank 1 and the membrane module 2 and supplies the raw water stored in the storage tank 1 to the membrane module 2. Moreover, it is preferable to further include a permeated water pipe 6 that supplies permeated water that has passed through the membrane module 2 to the permeated water tank 9. The membrane module which is a characteristic part of the present invention will be described below.

FIG. 2 is a schematic view and a cross-sectional view of the membrane module. Membrane module 2 used in water treatment equipment
As shown in FIG. 2, a hollow fiber membrane 7 for solid-liquid separation of raw water, a holding member 11 for holding the hollow fiber membrane 7, and a thermosetting resin for fixing the hollow fiber membrane 7 and the holding member 11 8 and so on. The hollow fiber membrane 7 has an outer diameter of 3 mm to 10 mm and a membrane filling rate of 40% to 70%. By using the hollow fiber membrane 7 having such an inner diameter and a membrane filling rate, the thermosetting resin 8 can be easily adapted to the surface of the hollow fiber membrane 7.
1 shows an excellent effect that the adhesiveness to 1 is improved and the reliability of the module is improved.

Here, the material constituting the hollow fiber membrane preferably contains a hygroscopic resin. “Hygroscopic resin” means a resin having a weight increase rate (water content) of 0.1% or more and 6% or less after being left for 24 hours at 23 ° C. and 50% relative humidity. The moisture content of the hygroscopic resin is preferably 1% or more and 5% or less, and more preferably 2% or more and 3% or less. In addition, humidity shall evaluate the moisture content in resin by adjusting humidity by the method prescribed | regulated by JISP8111.

Examples of the hygroscopic resin include one or more resins selected from the group consisting of polyvinyl acetate, polyvinyl formal, polyacetal, polyvinyl butyral, and polyvinyl alcohol. By using such a resin, it becomes difficult for the contaminants to adhere to the hollow fiber membrane 7, and even if temporarily attached, the contaminants can be easily removed by a washing process such as backwashing. In addition to the selection of such materials, it is effective to use a hollow fiber membrane having a large diameter such as the inner diameter in the above numerical range, and such a material and a hollow fiber membrane having an outer diameter are used to prevent the adhesion of contaminants. Thus, the flow rate in the membrane can be easily controlled, and an excellent effect of easily removing contaminants attached to the hollow fiber membrane is exhibited.

A water treatment procedure of the water treatment apparatus of the present embodiment will be described with reference to FIG. First, raw water to be treated is stored in the storage tank 1. Then, the raw water in the storage tank 1 is supplied to the membrane module 2 through the supply pipe 3. Raw water is treated by passing the raw water through the membrane module 2. The permeate treated by the membrane module 2 is supplied to the permeate tank 9 through the permeate pipe 6. On the other hand, the concentrated water concentrated in the membrane module 2 is returned to the storage tank 1 via the return pipe 4. A first gas supply device 5 is connected to the return pipe 4. Air is supplied from the first gas supply device 5 to the return pipe 4. This air serves as a power source and the concentrated water is returned to the storage tank 1. Raw water is treated by a series of these flows. Below, each part which comprises the water treatment apparatus of this embodiment is demonstrated.

(Membrane module)
FIG. 2 is a schematic diagram showing the form of the membrane module. The membrane module 2 is provided to separate raw water into permeate and concentrated water. In FIG. 2, raw water is supplied from the supply pipe 3 to the membrane module, and permeated water that has permeated through the hollow fiber membrane 7 in the membrane module is supplied from the permeated water pipe 6 to the permeated water tank. On the other hand, the contaminant collected in the hollow fiber membrane is returned to the storage tank 1 through the return pipe 4 as concentrated water. The separation of the permeated water and the concentrated water is performed by loading the membrane module 2 with a differential pressure between the inner and outer membranes.

As shown in the cross-sectional view of FIG. 2, the membrane module 2 includes a plurality of hollow fiber membranes 7 and a holding member 11 that houses the hollow fiber membranes 7. The outer diameter, length, number, etc. of the hollow fiber membrane 7 can be appropriately adjusted according to the characteristics of the membrane module to be obtained. A predetermined number of hollow fiber membranes 7 may be bundled to form a hollow fiber membrane bundle. The hollow fiber membrane bundle is preferably straight.
The hollow fiber membrane bundle is preferably cut into a predetermined length according to the holding member 11 and inserted into the holding member.

As shown in FIG. 2, the supply pipe 3 is connected to one end side of the tubular membrane module 2,
A return pipe 4 is connected to the other end side of the tubular membrane module 2. In the membrane module of FIG.
The raw water is supplied from the lower supply pipe 3 in the figure, the concentrated water is taken out from the return pipe 4, and the permeated water pipe 6.
Permeate is taken out of the water. That is, the raw water supplied from the supply pipe 3 is membrane-separated by the hollow fiber membrane 7 and supplied to the permeate pipe 6 as permeate before reaching the thermosetting resin 8. on the other hand,
A portion of the raw water that has not permeated through the hollow fiber membrane passes between the thermosetting resins 8 as concentrated water and is discharged to the return pipe 4.

The connection position between the supply pipe 3 and the membrane module 2 is preferably higher than the lowermost part of the membrane module 2. By connecting the supply pipe 3 to such a position, raw water can be supplied even from the side surface side of the membrane module, and the membrane module can be made independent. Furthermore, when the supply pipe 3 is connected to the lower part of the membrane module 2, the height of the entire apparatus is increased by the members necessary for the connection, so that the installation space of the membrane module can be made compact.

The membrane module 2 may be used alone or in combination of two or more. When two or more membrane modules are used, each membrane module may be connected in series, may be connected in parallel, or a combination of series and parallel may be used. FIG. 3 is a schematic diagram showing a form in which ten membrane modules are connected in parallel. By connecting the membrane modules in series,
Since the total length of the membrane module is increased, equivalent permeated water and concentrated water can be obtained with less power. Further, as shown in FIG. 3, the membrane modules 2 may be connected in parallel. This
The flow rate of the raw water supplied to the hollow fiber membrane can be adjusted, and the hollow fiber membrane is not easily clogged.

In FIG. 3, the supply pipe 3 of each membrane module is connected to the supply main pipe 13, the permeate pipe 6 of each membrane module is connected to the permeate main pipe 16, and the return pipe 4 of each membrane module is , Connected to the return main pipe 14. Raw water is supplied from the supply main pipe 13 to each supply pipe 3, treated with water in each membrane module, and permeated water is supplied from the permeate pipe 6 of each membrane module to the permeated water main pipe 16. Concentrated water is supplied from the return pipe 4 to the return main pipe 14.

FIG. 4 is a left side view of the membrane module of FIG. 3 connected. Referring to FIG. 4, when the diameter of the supply water main pipe 13 is N _m , the supply pipe 3 connected to the supply water main pipe 13 is supplied to a position within ½ N _m from the center of the supply water main pipe. Membrane module 2 so that the center of tube 3 is arranged
It is preferable that connected to, more preferably within 1 / 4N _m. By connecting the supply pipe to such a connection position, the installation space of the membrane module can be made compact, and the balance between the arrangement of the supply water main pipe 13 and the supply pipe 3 becomes suitable.

In addition, referring to FIG. 4, the supply pipe 3, the return pipe 4, and the permeate pipe 6 of the membrane module 2 are preferably connected to the same height from the bottom of the membrane module. By connecting each pipe to such a position, the number of membrane modules can be increased or decreased as needed. Further, it is preferable that the main pipe 14 is connected to the upper stage of the membrane module 2, the permeated water main pipe 16 is connected to the middle stage of the membrane module 2, and the supply main pipe 13 is connected to the lower stage of the membrane module 2. The permeated water main pipe 16 is preferably connected to a position that is lower than the connection position of the permeated water pipe 6 by a distance D. By connecting in this way, the permeate pipe 6 and the permeate main pipe 16
And a pipe having a distance D can absorb a strain generated when a lateral force is applied to the membrane module. The membrane module having such a function is not easily destroyed even when a lateral force is applied to the entire membrane module due to an earthquake or the like. On the other hand, when the distance D between the permeated water main pipe 16 and the permeated water pipe 6 is 0, that is, when the permeated water main pipe 16 and the permeated water pipe 6 have the same height, the supply pipe 3 and the return pipe 4 Since the permeated water pipe 6 is connected at three points in parallel, the connection of each membrane module itself is strong, but the resistance when a lateral force is applied due to an earthquake or the like is not necessarily sufficient. . Here, the distance D between the permeated water main pipe 16 and the permeated water pipe 6 is preferably 10% or more and 60% or less of the entire length of the membrane module (the length in the hand direction). Is 20% to 50%, more preferably 25% to 40%.

As shown in FIG. 3, the membrane modules 2 are preferably connected in parallel after standing upright in the vertical direction. By connecting in parallel in this way, the connection piping between the membrane modules can be simplified, and the number of membrane modules can be easily increased or decreased.

When supplying raw water to the membrane module 2, it is preferable that gas is supplied simultaneously with the raw water. When gas is supplied to the membrane module 2, the contaminants attached to the membrane are efficiently peeled off,
This is because the efficiency of water treatment can be improved. Therefore, it is preferable to connect a gas supply device to the supply pipe 3 or the supply water main pipe 13.

When a certain period of time elapses from the start of water treatment, suspended matter or the like accumulates on the membrane module 2, and the separation performance of the membrane module 2 may be reduced. At this time, backwashing is preferably performed. The backwashing is preferably performed by a backwashing pump 10 as shown in FIG. As a result, suspended matter or the like attached to the membrane module 2 can be peeled off, and the processing performance of the membrane module can be regenerated.

In the constant pressure filtration, the backwashing is preferably performed when the decrease in water permeability is 20% or more, and in the quantitative filtration, it is preferably performed when the increase in transmembrane pressure difference is 20% or more. The backwashing is preferably performed with a variation in transmembrane pressure difference within 10%. Thereby, the frequency | count of backwashing by a high voltage | pressure can be reduced, and a hollow fiber membrane can be lengthened.

(Hollow fiber membrane)
In the present embodiment, the hollow fiber membrane may be formed of a single main constituent material, or the shape may be held by a support (not shown) in the holding member 11. When using a support,
What has the intensity | strength which can hold | maintain the shape of a hollow fiber membrane is preferable, and it is preferable to use a ceramic, a nonwoven fabric, etc. By using the support in this manner, the shape of the hollow fiber membrane can be stabilized, and the adhesion between the hollow fiber membrane and the thermosetting resin can be enhanced.

Here, “single main constituent material” means that the main material is a single material.
That is, the material forming the hollow fiber membrane (for example, the resin constituting the membrane) is 50% by mass or more (preferably 60% by mass or more, more preferably 70% by mass or more, more preferably 80% by mass or more), More preferably 85% by mass or more).

The hollow fiber membrane preferably has a self-supporting structure. “Having a self-supporting structure” means that when the hollow fiber membrane is used, the shape thereof has a strength that can maintain a desired shape such as a cylindrical shape. Thus, by forming a hollow fiber membrane having a self-supporting structure with a single main constituent material, a separation function is provided on both the front and back surfaces, preventing contamination during backwashing and avoiding contamination inside the hollow fiber membrane It is also possible to do.

The hollow fiber membrane is characterized by a membrane filling rate of 40% to 70%, preferably
The film filling rate is 45% or more and 65% or less. With such a membrane filling rate, the hollow fiber membrane can be easily fixed by the thermosetting resin 8, and thus the reliability of the membrane module can be improved. Here, the membrane filling rate is expressed by the following relational expression (I) where N is the inner diameter of the holding member, n is the outer diameter of the hollow fiber membrane, and x is the number of hollow fiber membranes held by the holding member. ).
{1-((N ² × π) − (n ² × π) × x) / (N ² × π)} × 100 (I)

The outer diameter of the hollow fiber membrane is preferably 3 mm to 10 mm, more preferably 4 mm to 8 mm, further preferably 4.5 mm to 7 mm, particularly preferably 5 m.
m to 7 mm. Moreover, it is preferable that the film thickness of a hollow fiber membrane is 0.1 mm or more and 1.7 mm or less, More preferably, it is 0.5 mm or more and 1.5 mm or less, More preferably, it is 0.6 mm or more and 1 mm or less. By using a hollow fiber membrane having such an outer diameter, it is difficult for contaminants to adhere, and even if temporarily adhered, contaminants can be easily removed. If the inner diameter of the hollow fiber membrane is thin, the resistance when air passes is large, and the raw water tends to be difficult to circulate. Further, by using the hollow fiber membrane having the above thickness, the bending strength of the hollow fiber membrane itself can be improved, and the adhesion between the thermosetting resin and the hollow fiber membrane can be ensured.

Both ends of the plurality of hollow fiber membranes 7 are sealed with the thermosetting resin 8 in the holding member 11. The thermosetting resin 8 is formed by, for example, potting by centrifugal molding.
The material of the thermosetting resin 8 is preferably a material having a low initial viscosity, a viscosity that increases with time and is cured, and finally is cured to a predetermined hardness. Examples of such a material include an epoxy resin and a urethane resin. Etc. In the present embodiment, by using the above-described large-diameter hollow fiber membrane, an appropriate space is formed between the hollow fiber membranes, and the thermosetting resin 8 can easily go around the hollow fiber membrane. This makes it easier for the thermosetting resin 8 to spread on the surface of the hollow fiber membrane 7, reducing potting failure, reducing the failure of the sealing part during use, and improving the long-term reliability of the membrane module 2. be able to.

The thermosetting resin 8 preferably has an initial viscosity of 100 mPa · s or more and 2500 mPa · s or less from the viewpoint of facilitating wraparound around the hollow fiber membrane.
It is more preferable that it is a m or more and 2000 mPa * s or less, More preferably, it is 500
mPa · s or more and 1500 mPa · s or less. By using a thermosetting resin having such a viscosity, the thermosetting resin easily flows between the hollow fiber membranes.

(Holding member)
The holding member 11 is not particularly limited as long as it can hold the hollow fiber membrane 7. Holding member 1
Metal, plastic, or the like can be used as the material constituting 1, but plastic is preferable from the viewpoint of easy molding and easy mechanical strength. Examples of the plastic include acrylic resin, polystyrene resin, ABS resin, AS resin, polycarbonate resin, and vinyl chloride resin.

(First gas supply device)
The first gas supply device 5 is connected to the supply pipe 3 or the return pipe 4. When the 1st gas supply apparatus 5 is connected to the supply pipe | tube 3, it is used as what wash | cleans the hollow fiber membrane in a membrane module efficiently. When the first gas supply device 5 is connected to the return pipe 4, the first gas supply device 5 is a power source for circulating the raw water in the water treatment device. By providing the first gas supply device 5 at this position, the energy efficiency of the water treatment can be improved, and air can be supplied without any pressure loss in the membrane module. Further, air is less likely to accumulate in the supply pipe 3 and the return pipe 4. For this reason, air can be uniformly distributed and supplied in the membrane module.

Examples of the gas supplied by the first gas supply device 5 include air, compressed air, ozone, nitrogen, carbon dioxide, and the like, but compressed air is preferable. Moreover, it is preferable that gas is supplied with the form of a bubble, More preferably, it is a microbubble about several dozen micrometer-several hundred micrometer. Microbubbles have the advantage of easily circulating the raw water uniformly. As a method for supplying air bubbles, for example, a diffuser tube in which air discharge holes of about 1 mm to several tens of mm are formed in stainless steel, ceramic, plastic, rubber, or the like may be used. Examples of the first gas supply device 5 include a blower, a compressor, and a microbubble generating blower.

(Return pipe)
The return pipe 4 is connected to the storage tank 1 and the membrane module 2 and is provided to supply the concentrated water treated by the membrane module 2 to the storage tank 1. Supply pressure when supplying concentrated water to the return pipe 4 is 2
It is preferably 0 kPa or more and 200 kPa or less, more preferably 20 kPa or more and 1
00 kPa or less. The return pipe 4 may be provided with an air release line for extracting air from the return pipe.

The inner diameter of the return pipe can be arbitrarily set, but is preferably 10 mm or more and 250 mm or less, more preferably 30 mm or more and 400 mm or less, and further preferably 40 mm or more and 200 mm or less. By using such an inner diameter, pressure loss can be reduced and transfer efficiency can be increased.

The timing which the 1st gas supply apparatus 5 supplies gas is not specifically limited, Water treatment, backwashing,
Alternatively, it may be performed during any step of flushing. The time for supplying the gas varies depending on the size of the bubble, but continuously is 1 second or more, 1 minute or more, preferably several seconds to several minutes,
It is more preferable to always supply. The bubbles introduced into the membrane module are preferably supplied in a volume of 0.25 or more and 2.5 or less with respect to the raw water volume (raw water ratio) introduced into the membrane module. Normally, the volume ratio between the amount of gas and the raw water to be circulated is the difference between the water level and the pipe resistance before and after the module,
It depends on the flow resistance in the module and the uniformity of the air flow in the module.

(Supply pipe)
The supply pipe 3 is connected to the storage tank 1 and the membrane module 2 and is provided to supply raw water to the membrane module 2. The supply pressure when supplying raw water to the supply pipe 3 is preferably 20 kPa or more and 100 kPa or less, for example.

(Permeate pipe)
The permeated water pipe 6 is connected to the membrane module 2 and the permeated water tank 9 and is provided to supply permeated water that has permeated through the hollow fiber membrane of the membrane module 2 to the permeated water tank 9. The inner diameter and length of the permeate pipe 6 are not particularly limited.

(Permeate tank)
The permeated water tank 9 is provided for storing permeated water filtered by the membrane module. The permeated water tank 9 includes a backwash pipe connected to the membrane module through a different path from the pipe through which the permeated water from the membrane module 2 passes so that a part of the permeated water can be used for backwashing. Preferably it is. By connecting the backwash pump 10 to the backwash tube, the membrane module can be backwashed using a portion of the permeate stored in the permeate tank.

(Backwash pump)
The backwash pump 10 is a pump used to supply permeated water to the membrane module during backwashing. Examples of the backwash pump 10 include a centrifugal pump, a diffuser pump, a spiral mixed flow pump, a mixed flow pump, a piston pump, a plunger pump, a diaphragm pump,
A gear pump, screw pump, vane pump, cascade pump, jet pump, or the like can be used.

(Reservoir)
The storage tank 1 is a tank for storing raw water. The storage tank 1 is connected to a supply pipe 3 for supplying raw water to the membrane module 2 and a return pipe 4 for returning permeated water from the membrane module 2. The storage tank 1 may be a single unit of about 2 m × 10 m or a connected storage tank, or 5 m × 5.
It may be a water tank of about 0 m or a connected storage tank.

(Raw water)
Raw water includes wastewater containing activated sludge from sewage treatment plants, urban sewage such as household wastewater, industrial wastewater, biological wastewater, seawater, well water, river water, lake water, fruit juice, milk, etc. It may be a liquid food. Suspended solids (SS) of raw water is preferably less than 20000.

(Water treatment method)
The water treatment method using the water treatment apparatus of the present embodiment is preferably a cross flow method. In the cross flow method, the membrane surface of the hollow fiber membrane and the flow direction of the raw water are substantially parallel, and the suspended matter attached to the membrane surface of the hollow fiber membrane can be peeled and circulated. Thereby, clogging of the hollow fiber membrane is suppressed, and the treatment speed of the raw water is stabilized. Note that the water treatment apparatus of this embodiment may be used in a dead-end manner depending on the contamination state of raw water.

The flow rate of the raw water in the pipe is preferably 0.3 m / s or more and 2 m / s or less, and
More preferably, it is 5 m / s or more and 1.5 m / s or less, More preferably, it is 0.7 m / s.
s to 1 m / s. In addition, the value calculated based on the volume of the raw | natural water circulated per unit time shall be employ | adopted for the pipe | tube flow velocity.

The flow rate of the raw water supplied to the hollow fiber membrane is preferably 0.05 m / second or more and 1 m / second or less, more preferably 0.2 m / second or more and 0.6 m / second or less. By supplying raw water to the hollow fiber membrane at such a flow rate, it becomes difficult for contaminants to adhere to the hollow fiber membrane, so that it is possible to continue to treat the raw water efficiently. Here, the flow rate of raw water supplied to the hollow fiber membrane is a value measured by an electromagnetic flow meter for wastewater treatment (manufactured by Endless Hauser).

The raw water is preferably supplied into the hollow fiber membrane by applying a transmembrane pressure difference of 5 kPa to 200 kPa, more preferably a transmembrane pressure of 10 kPa to 100 kPa. With such a transmembrane pressure difference, it is possible to maintain water permeability performance that is practically required, and to prevent contaminants from adhering to the hollow fiber membrane.

The raw water may be treated with an internal pressure type or with an external pressure type. The internal pressure type is a system in which raw water is supplied inside the hollow fiber membrane and permeate is taken out from the outside of the hollow fiber membrane. The external pressure type is a system in which raw water is supplied to the outside of the hollow fiber membrane and permeate is taken out from the inside of the hollow fiber membrane. From the viewpoint that the film surface flow rate can be set higher, it is preferable to perform the treatment with an internal pressure method.

When switching between water treatment and backwashing, flushing or draining may be performed, or water treatment may be temporarily stopped.

Flushing is a process of removing suspended matters attached to the storage tank, each pipe, and the membrane module. A suspended matter or the like larger than the inner diameter of the hollow fiber membrane may block the circulation path of the raw water. This blockage can be prevented by flushing in the direction opposite to the supply direction of the raw water. Flushing is preferably performed at a membrane surface flow rate of 0.1 m / s or higher without pressurizing raw water. The water that has passed through the membrane module 2 by flushing is returned to the storage tank 1 as flushing water.

Draining is a step of discharging suspended matter remaining in the hollow fiber membrane of the membrane module out of the system.
Drain is collected by opening the membrane module with the water treatment device stopped and dropping the concentrate, or backwashing with the membrane module opened, and collecting backwash wastewater. To do. The collected concentrated water or backwash waste water may be stored in a drain water tank provided separately.

Although the water treatment apparatus of this embodiment is not shown in FIG. 1, a biological treatment tank, a flocculant treatment tank, a flocculant injection means, a chemical liquid tank, a chemical liquid injection means, a concentrated water tank, an on-off valve, an ultrasonic generator, A suction device or the like may be provided.

When using the water treatment apparatus of this embodiment as a seawater desalination apparatus, it is preferable to perform turbidity treatment such as sand filtration. By executing the turbidity removal treatment, coarse impurities can be removed. Moreover, since the dissolved oxygen in raw | natural water can be raised by supplying air from a 1st gas supply apparatus, the aeration motive power when using a water treatment apparatus as a biological treatment tank can also be suppressed.

<Embodiment 2>
FIG. 5 is a schematic diagram illustrating an outline of the water treatment apparatus according to the second embodiment. As shown in FIG. 5, the present embodiment is that the permeated water suction device 17 is connected to the first embodiment, the connection position of the first gas supply device 5 is changed, and the supply device 15 is connected. Embodiment 1 is different except that
It is the same water treatment apparatus. The permeated water suction device 17 has a function of sucking permeated water.

The supply device 15 is not particularly limited as long as it exhibits the effect of floating the contaminants attached to the hollow fiber membrane. For example, a centrifugal pump, a diffuser pump, a spiral mixed flow pump, a mixed flow pump, a piston pump, a plunger Pumps, diaphragm pumps, gear pumps, screw pumps, vane pumps, cascade pumps, jet pumps, and the like can be used.

<Embodiment 3>
FIG. 6 is a schematic diagram illustrating an outline of the water treatment apparatus according to the third embodiment. As shown in FIG. 6, this embodiment is the same as the second embodiment except that the suction device 12 is connected to the return pipe 4 instead of the supply device 15. It is. The pressure in the return pipe is reduced by the suction device 12, whereby raw water is supplied to the membrane module. As the suction device 12, the same device as the supply device 15 can be used.

Hereinafter, a water treatment device and a water treatment method of the present invention are explained in detail based on an example. In addition, this invention is not limited only to these Examples.

(Examples 1-4)
In Examples 1 to 4, a membrane module having a membrane filling rate shown in the column of “Membrane filling rate” in Table 1 was prepared using a hollow fiber membrane containing a vinylpyrrolidone-vinyl chloride copolymer. In the production of the membrane module, the hollow fiber membrane was sealed using a urethane resin having the “viscosity” characteristics shown in Table 1 as a thermosetting resin. The membrane filling rate of the hollow fiber membrane is expressed as follows when the inner diameter of the holding member is N, the outer diameter of the hollow fiber membrane is n, and the number of hollow fiber membranes held by the holding member is x. It was calculated by the formula (I).
{1-((N ² × π) − (n ² × π) × x) / (N ² × π)} × 100 (I)

Using the membrane module obtained as described above, a water treatment apparatus having a structure shown in FIG. 1 was produced.

When the raw water of activated sludge suspended matter (MLSS): 8000 to 10000 was supplied to the water treatment apparatus of each example, the flow rate of the raw water flowing through the supply pipe is a value shown in the column of “flow rate” in Table 1. It was. In the water treatment apparatus of each example, there was no defective filling in the initial stage of water treatment, and the sealing part did not peel off when used. From this result, it becomes clear that by treating raw water using a hollow fiber membrane having a predetermined outer diameter and membrane filling rate, water treatment can be performed stably with high reliability.
The effect of the present invention was shown.

The present invention is widely used as a water treatment apparatus used for water purification such as clarification of river water and groundwater, clarification of industrial water, drainage and sewage treatment, pretreatment for seawater desalination, etc. It is possible to carry out economical and efficient water treatment.

DESCRIPTION OF SYMBOLS 1 Storage tank 2 Membrane module 3 Supply pipe 4 Return pipe 5 1st gas supply apparatus 6 Permeate pipe 7 Hollow fiber membrane 8 Thermosetting resin 9 Permeate tank 10 Backwash pump 11 Holding member 12 Suction device 13 Supply main pipe 14 Return book Pipe 15 Supply device 16 Permeated water main pipe 17 Permeated water suction device

Claims (5)

A storage tank for storing raw water;
A membrane module for treating the raw water;
A return pipe connected to the storage tank and the membrane module, and supplying concentrated water treated by the membrane module to the storage tank,
The membrane module includes a hollow fiber membrane for solid-liquid separation of the raw water, a holding member for holding the hollow fiber membrane, and a thermosetting resin for fixing the hollow fiber membrane and the holding member,
The hollow fiber membrane has an outer diameter of 3 mm to 10 mm, the inner diameter of the holding member is N, the outer diameter of the hollow fiber membrane is n, and the number of hollow fiber membranes held by the holding member is when the x, water treatment apparatus, characterized in that the calculated filling factor is 70% or less 40% or more by the following formula (I).
{(N ² × π × x) / (N ² × π)} × 100 (I)   The water treatment apparatus according to claim 1, further comprising a supply pipe connected to the storage tank and the membrane module and configured to supply raw water stored in the storage tank to the membrane module.   The water treatment apparatus according to claim 1, wherein the holding member further includes a support for holding the shape of the hollow fiber membrane.   The water treatment device according to any one of claims 1 to 3, further comprising a supply device for supplying the raw water to the membrane module. A water treatment method using the water treatment apparatus according to any one of claims 1 to 4,
The water treatment method, wherein a flow rate of the raw water supplied to the hollow fiber membrane is 0.05 m / second or more and 1 m / second or less.