JPH10230140A - Spiral membrane element - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a spiral membrane element which can be manufactured at a low cost and cleaned easily and further, is of high reliability. SOLUTION: Independent or continuous envelope-like membranes 3 are wound around the outer peripheral face of a water collecting pipe 2, and at the same time, an untreated water spacer 4 is introduced into a gap between the membranes 3 to form a spiral membrane element 1a. The untreated water spacer 4 is 0.1-0.5mm thick. In addition, the outer peripheral face of the spiral membrane element 1a is wrapped with a material 5 for a flow path on the outer peripheral part. The untreated water is supplied from at least, the outer peripheral part side of the spiral membrane element 1a to obtained the delivery of a penetrating water from the opening end of the water collecting pipe 2.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a spiral type membrane element used for a low pressure reverse osmosis membrane separation device, an ultrafiltration device, a microfiltration device and the like.

[0002]

2. Description of the Related Art In recent years, a membrane separation technique has been applied to a water purification technique, and a membrane separation technique has been applied as a pretreatment of a reverse osmosis membrane separation system used for seawater desalination and the like.
As a type of membrane used for such membrane separation, a microfiltration membrane or an ultrafiltration membrane capable of obtaining a high amount of permeated water is widely used, but recently, an ultra-low pressure of 10 kgf / cm ² or less has been used. Reverse osmosis membranes that provide a permeate volume have also been developed.

As a form of the membrane element used for the membrane separation, a hollow fiber membrane element is often used in view of a membrane area per unit volume (volume efficiency). However, the hollow fiber membrane element has a disadvantage that the membrane is easily broken, and if the membrane is broken, the raw water mixes with the permeated water and the separation performance is reduced.

On the other hand, there is a spiral type membrane element as a form of a membrane element capable of increasing a membrane area. This spiral type membrane element has an advantage that separation performance can be maintained and reliability is high as compared with a hollow fiber membrane element.

FIG. 10 is a partially cutaway perspective view of a conventional spiral membrane element, and FIG. 11 is an external perspective view of the conventional spiral membrane element.

[0006] As shown in FIG. 10, a spiral membrane element 21 has separation membranes 26 on both surfaces of a permeated water spacer 25.
Are overlapped and three sides are adhered to each other to form an envelope-like film (bag-like film) 23. The opening of the envelope-like film 23 is attached to a water collecting pipe 22 formed of a perforated hollow tube, and the net-like (net-like) ) Is wound around the outer peripheral surface of the water collecting pipe 22 in a spiral shape together with the raw water spacer 24).

The raw water spacer 24 is provided for forming a flow path through which raw water passes between the envelope membranes 23. If the thickness of the raw water spacer 24 is small, the filling efficiency of the separation membrane 26 is increased, but clogging with the suspended substance occurs. Therefore, usually, the thickness of the raw water spacer 24 is about 0.7 mm to 3.0 m.
m.

A spiral membrane element using a zigzag corrugated raw water spacer (so-called corrugated spacer) for treating raw water containing a large amount of suspended substances, such as river water, has already been known.

As shown in FIG. 11, the outer peripheral surface of the spiral-type membrane element 21 is covered with an exterior material 27 made of FRP (fiber reinforced plastic), a shrink tube, or the like.
Packing holders 28 called anti-telescopes are respectively attached to both ends.

FIG. 12 is a sectional view showing an example of a conventional method of operating a spiral type membrane element. As shown in FIG. 12, the pressure vessel (pressure-resistant vessel) 30 is composed of a cylindrical case 31 and a pair of end plates 32a and 32b. A raw water inlet 33 is formed on one end plate 32a, and a concentrated water outlet 35 is formed on the other end plate 32b. A permeated water outlet 34 is provided at the center of the other end plate 32b.

A spiral type membrane element 21 having a packing 37 attached near one end of the outer peripheral surface is mounted in a cylindrical case 31, and both open ends of the cylindrical case 31 are sealed with end plates 32a and 32b, respectively. I do. One open end of the water collecting pipe 22 is fitted to the permeated water outlet 34 of the end plate 32b, and an end cap 36 is attached to the other open end.

During the operation of the spiral type membrane element 21, the raw water 51 is introduced into the first liquid chamber 38 from the raw water inlet 33 of the pressure vessel 30. As shown in FIG.
Is supplied from one end face side of the spiral membrane element 21. The raw water 51 flows in the axial direction along the raw water spacer 24, and is discharged as concentrated water 53 from the other end surface side of the spiral membrane element 21. As the raw water 51 flows along the raw water spacer 24, the permeated water 52 that has passed through the separation membrane 26 is collected along the permeated water spacer 25 by the water collecting pipe 2.
2 and discharged from the end of the water collecting pipe 22.

The permeated water 52 is supplied to the pressure vessel 30 shown in FIG.
Is taken out from the permeated water outlet 34 to the outside. Further, the concentrated water 53 is taken out of the second liquid chamber 39 in the pressure vessel 30 through the concentrated water outlet 35 to the outside.

[0014]

When the membrane element is operated, the clogging of the membrane is caused by suspended substances in the raw water, and the permeation flux is reduced. For this reason, clogging is removed by performing chemical cleaning or the like to recover the permeation flux, but the labor and cost required for chemical cleaning poses a problem. Therefore, in order to prevent clogging, for example, in a hollow fiber membrane element,
Backwashing with permeate or air is performed periodically.

However, in the conventional spiral membrane element 21, the outer peripheral surface of the envelope membrane 23 wound around the water collecting pipe 22 is covered with the exterior material 27. There is a problem that contaminants such as turbid substances causing clogging are easily captured by the raw water spacer 24 before being discharged from the end of the membrane element 21 and are not sufficiently removed.

Further, a gap existing between the inner peripheral surface of the cylindrical case 31 of the pressure vessel 30 and the spiral membrane element 21 becomes a dead space S, and stagnation of the fluid (liquid pool) occurs. When the spiral type membrane element 21 is used for a long time, the fluid staying in the dead space is denatured. In particular, when the fluid is a liquid containing an organic substance, germs such as microorganisms propagate, and the germs may decompose the organic substance to generate a bad smell or decompose the separation membrane. Leads to a decrease in

Further, in the conventional spiral membrane element 21, raw water is supplied from one end of the spiral membrane element 21 and discharged from the other end.
A packing holder 28 is required to prevent the envelope-shaped film 23 wound in 2 from being deformed into a bamboo shoot shape.
Further, a pressure difference occurs between the raw water inflow side and the concentrated water outlet side due to the pressure loss due to the raw water spacer 24 and the pressure loss due to clogging, and the spiral membrane element 21 is deformed. In order to prevent this deformation, the outer peripheral surface of the envelope-like film 23 wound around the water collecting pipe 22 is covered with an exterior material 27 such as an FRP or a shrinkable tube. These increase component costs and manufacturing costs.

Further, it is necessary to obtain a sufficient film surface linear velocity in order to prevent the formation of cake due to contaminants in raw water, and for this purpose, a sufficient concentration-side flow rate is required. If the flow rate on the concentration side is increased, the recovery rate per membrane element will be low, and the pump for supplying raw water will be large, and the system cost will be very large.

An object of the present invention is to provide a highly reliable spiral-type membrane element which can be reduced in cost and is easy to clean.

[0020]

Means for Solving the Problems and Effects of the Invention In the spiral membrane element according to the first invention, a plurality of envelope-like membranes, which are independent or continuous on the outer peripheral surface of a perforated hollow tube, are arranged via a stock solution flow path material. To form a spiral membrane element,
The thickness of the undiluted liquid channel material is 0.1 mm or more and 0.5 mm or less, and undiluted liquid is supplied from the outer peripheral side and both ends of the spiral membrane element, and the permeated liquid is supplied from at least one open end of the perforated hollow tube. Is derived.

In the spiral membrane element according to the present invention, since the outer peripheral surface and both end surfaces of the spiral membrane element are open without being covered with the exterior material, the undiluted solution is supplied to the outer peripheral portion and both ends of the membrane element. Supply from the department side,
Full volume filtration can be performed.

As described above, since the undiluted solution is supplied from the outer peripheral side and both ends of the membrane element, contaminants are captured at the outer peripheral section and both ends of the membrane element. After filtering for a certain period of time, backflow washing with a permeate is performed from the permeate side. During backwashing, the permeated liquid that has been back-filtered from the perforated hollow tube flows toward the outer peripheral portion and both end portions along the raw liquid flow path material. As a result, the contaminants trapped on the outer peripheral portion and both ends of the membrane element are easily separated. Therefore, the contaminants can be uniformly removed by backwashing.

In particular, since the thickness of the stock solution channel material is as small as 0.1 mm or more and 0.5 mm or less, it is possible to prevent contaminants from entering between the envelope membranes while securing the stock solution flow channel. Therefore, it is possible to easily remove the contaminants captured at the outer peripheral portion and both ends of the membrane element by the backwashing operation. In addition, since the stock solution channel material is thin, the efficiency of filling the separation membrane increases. In addition, a cake layer is formed by the contaminants trapped on the outer periphery and both ends of the membrane element, and cake filtration is performed by the cake layer on the outer periphery and both ends of the membrane element, and a separation membrane is formed inside the membrane element. Membrane filtration is performed.

Further, according to the structure of the present invention, since dead space S is not formed in the gap between the membrane element and the pressure vessel due to the total filtration, the flow of the fluid in the gap between the membrane element and the pressure vessel is prevented. No stagnation occurs. Therefore, even when used for separating a fluid containing an organic substance, problems such as propagation of various germs such as microorganisms, generation of offensive odor due to decomposition of the organic substance, and decomposition of the separation membrane do not occur, and high reliability can be obtained.

Further, the undiluted solution is supplied from the outer peripheral side and both ends of the membrane element, and pressure is applied to the membrane element from all directions and no pressure that causes displacement in the axial direction is applied. The envelope-shaped film wound around the sheet does not deform into a bamboo shoot. This eliminates the need for a packing holder and an exterior material, thereby reducing parts costs and manufacturing costs. In addition, since the whole amount is filtered, a high recovery rate can be obtained without using a large pump for supplying the stock solution. Thereby, the system cost is reduced.

Further, since pressure is applied to the membrane element from all directions, the membrane element does not deform even if the supply pressure of the stock solution is increased. Therefore, high pressure resistance can be obtained.

In the spiral membrane element according to the second invention, a plurality of independent or continuous envelope membranes are wound around the outer peripheral surface of the perforated hollow tube via a stock solution flow path material to form a spiral membrane element. Formed, the thickness of the stock solution flow path material is 0.1 mm or more and 0.5 mm or less, one end of the spiral membrane element is sealed, and the stock solution is supplied from the outer peripheral side and the other end side of the spiral membrane element. The permeated liquid is led out from at least one open end of the perforated hollow tube.

In the spiral membrane element according to the present invention, since the outer peripheral surface and one end surface of the spiral membrane element are open without being covered with the exterior material, the undiluted solution is supplied to the outer peripheral portion and one end of the membrane element. Supply from the department side,
Full volume filtration can be performed.

As described above, since the undiluted solution is supplied from the outer peripheral side and one end side of the membrane element, contaminants are captured at the outer peripheral side and one end of the membrane element. After filtering for a certain period of time, backflow washing with a permeate is performed from the permeate side. During backwashing, the permeated liquid that has been back-filtered from the perforated hollow tube flows toward the outer peripheral side and one end side along the raw liquid flow path material. Thereby, the contaminants trapped on the outer peripheral portion and one end portion of the membrane element are easily peeled off. Therefore, the contaminants can be uniformly removed by backwashing.

In particular, since the thickness of the stock solution channel material is as small as 0.1 mm or more and 0.5 mm or less, it is possible to prevent contaminants from entering between the envelope-shaped membranes while securing the stock solution flow channel. Therefore, it is possible to easily remove the contaminants trapped on the outer peripheral portion and one end portion of the membrane element by the backwashing operation. In addition, since the stock solution channel material is thin, the efficiency of filling the separation membrane increases. In addition, a cake layer is formed by the contaminants trapped on the outer periphery and one end of the membrane element, and cake filtration is performed by the cake layer on the outer periphery and one end of the membrane element, and a separation membrane is formed inside the membrane element. Membrane filtration is performed.

In particular, since there is no need to provide a space for supplying the undiluted solution to the sealed end of the membrane element, the pressure vessel for accommodating the membrane element can be downsized. Further, by disposing the sealed end of the membrane element on the side of the undiluted solution inlet of the pressure vessel, it is possible to prevent dirt from being attached to the end face of the spiral membrane element due to the dynamic pressure of the undiluted solution during undiluted solution introduction. it can.

Also, in the structure of the present invention, dead space S is not formed in the gap between the membrane element and the pressure vessel by the total filtration, so that germs such as microorganisms propagate, and odors are generated due to decomposition of organic substances. Problems such as decomposition of the separation membrane do not occur, and high reliability can be obtained.

Furthermore, since pressure is applied from all directions of the membrane element and does not apply a pressure that causes displacement in the axial direction, the envelope-shaped membrane wound around the perforated hollow tube is deformed into a bamboo shoot. There is no. This eliminates the need for a packing holder and an exterior material, thereby reducing parts costs and manufacturing costs. In addition, since the whole amount is filtered, a high recovery rate can be obtained without using a large pump for supplying the stock solution. Thereby, the system cost is reduced.

Further, since pressure is applied to the membrane element from all directions, the membrane element does not deform even if the supply pressure of the stock solution is increased. Therefore, high pressure resistance can be obtained.

In the spiral type membrane element according to the third aspect of the present invention, a plurality of independent or continuous envelope-shaped membranes are wound around the outer peripheral surface of the perforated hollow tube via a stock solution flow path material to form a spiral-shaped membrane element. Formed, the thickness of the stock solution flow path material is 0.1 mm or more and 0.5 mm or less, both ends of the spiral membrane element are sealed, and the stock solution is supplied from the outer peripheral side of the spiral membrane element. The permeated liquid is led out from at least one open end of the empty tube.

In the spiral membrane element according to the present invention, since the outer peripheral surface of the spiral membrane element is open without being covered with the exterior material, the undiluted solution is supplied from the outer peripheral side of the membrane element. Filtration can be performed.

As described above, since the undiluted solution is supplied from the outer peripheral side of the membrane element, contaminants are captured at the outer peripheral section of the membrane element. After filtering for a certain period of time, backflow washing with a permeate is performed from the permeate side. At the time of backwashing, the permeated liquid that has been back-filtered from the perforated hollow tube flows toward the outer peripheral side along the stock solution flow path material. Thereby, the contaminants trapped on the outer peripheral portion of the membrane element are easily peeled off. Therefore, the contaminants can be uniformly removed by backwashing.

In particular, since the thickness of the stock solution channel material is as small as 0.1 mm or more and 0.5 mm or less, it is possible to prevent contaminants from entering between the envelope-shaped membranes while securing the stock solution flow channel. Therefore, it is possible to easily remove the contaminants captured on the outer peripheral portion of the membrane element by the backwashing operation. In addition, since the stock solution channel material is thin, the efficiency of filling the separation membrane increases. In addition, a cake layer is formed by the contaminants trapped on the outer periphery of the membrane element, and cake filtration is performed by the cake layer on the outer periphery of the membrane element, and membrane filtration is performed by a separation membrane inside the membrane element.

In particular, since a space for supplying the undiluted solution is not required on both ends of the sealed membrane element, the pressure vessel for accommodating the membrane element can be downsized. Further, by disposing one of the sealed both ends of the membrane element on the side of the undiluted liquid inlet of the pressure vessel, it is possible to prevent dirt from adhering to the end face of the spiral membrane element due to the dynamic pressure of the undiluted liquid when introducing undiluted liquid. be able to.

Also in the structure of the present invention, dead space S is not formed in the gap between the membrane element and the pressure vessel due to the total amount filtration, so that germs such as microorganisms can propagate, and the generation of offensive odors due to decomposition of organic substances can be prevented. Problems such as decomposition of the separation membrane do not occur, and high reliability can be obtained.

Furthermore, since pressure is applied from all directions of the membrane element and no pressure causing displacement in the axial direction is applied, the envelope-shaped membrane wound around the perforated hollow tube is deformed into a bamboo shoot. There is no. This eliminates the need for a packing holder and an exterior material, thereby reducing parts costs and manufacturing costs. In addition, since the whole amount is filtered, a high recovery rate can be obtained without using a large pump for supplying the stock solution. Thereby, the system cost is reduced.

Further, since pressure is applied to the membrane element from all directions, no deformation of the membrane element occurs even when the supply pressure of the stock solution is increased. Therefore, high pressure resistance can be obtained.

In the spiral membrane element according to the first, second or third aspect of the present invention, the porosity in the thickness direction of the stock solution channel material is preferably 10% or more and 80% or less. Thus, it is possible to sufficiently secure the flow path of the undiluted solution while preventing intrusion of contaminants between the envelope-shaped membranes. Therefore, the contaminants can be reliably captured at least at the outer peripheral portion of the membrane element, and the stock solution can be sufficiently supplied between the envelope-shaped membranes.

The mesh pitch of the stock solution flow path material is 0.5
It is preferably from 10 mm to 10 mm. Thereby, it is possible to prevent the envelope membranes from coming into contact with each other and to reduce the flow path of the stock solution while reducing the pressure loss.

[0045]

FIG. 1 is a partially cutaway perspective view of a spiral membrane element according to an embodiment of the present invention.
FIG. 2 is a cross-sectional view showing an example of the envelope-shaped membrane of the spiral membrane element shown in FIG. 1, and FIG. 3 is a cross-sectional view showing another example of the envelope-shaped membrane of the spiral membrane element shown in FIG. is there.

The spiral membrane element 1 shown in FIG.
Includes a spiral-shaped membrane element 1a formed by winding a plurality of independent envelope-shaped membranes 3 or a plurality of continuous envelope-shaped membranes 3 on the outer peripheral surface of a water collecting pipe 2 composed of a perforated hollow pipe. . A raw water spacer (raw liquid flow path material) 4 is inserted between the envelope films 3 in order to prevent the envelope films 3 from adhering to each other and to reduce the film area, and to form a flow path for raw water. Have been. Spiral membrane element 1
The outer peripheral surface of a is covered with an outer peripheral channel material 5 made of a net formed of plastic, metal, rubber, fiber, or the like such as polypropylene, polyethylene, or polystyrene.

As shown in FIG. 2 and FIG.
Is formed by superposing two separation membranes 7 on both sides of a permeated water spacer (permeated liquid flow path material) 6 and bonding three sides thereof, and the opening of the envelope-shaped membrane 3 is formed on the outer periphery of the water collecting pipe 2. Attached to the surface. 10 kgf / c for the separation membrane 7
Low pressure reverse osmosis membranes, ultrafiltration membranes, microfiltration membranes, etc., operated at m ² or less are used.

In the example of FIG. 2, a plurality of envelope-shaped membranes 3 are formed by independent separation membranes 7, respectively. In the example of FIG.
A plurality of envelope membranes 3 are formed by folding a continuous separation membrane 7.

FIG. 4 shows the spiral type membrane element 1 shown in FIG.
FIG. 5 is a perspective view of the raw water spacer 4 used in FIG.

As shown in FIG. 4, the raw water spacer 4 is formed in a lattice shape such that a plurality of wires 41 and 42 made of a synthetic resin such as polypropylene and polyethylene cross each other at right angles.

As shown in FIG. 5, the thickness of the wire 41 is set larger than the thickness of the wire 42. Thereby,
The raw water 51 easily flows between the wires 41 in a straight line parallel to the wires 41.

FIG. 6 is a sectional view showing another example of the raw water spacer 4. In the raw water spacer 4 of FIG. 6, the wire 42 intersects the wire 41 at the center in the thickness direction. Also in this case, the thickness of the wire 41 is set to be larger than the thickness of the wire 42. Therefore, the raw water easily flows between the wires 41 in a straight line in parallel with the wires 41.

If the thickness t of the raw water spacer 4 is larger than 0.5 mm, it becomes difficult to capture contaminants in the raw water at least at the outer peripheral portion of the membrane element 1. On the other hand, if the thickness t of the raw water spacer 4 is smaller than 0.1 mm, the envelope-shaped membranes 3 are likely to come into contact with each other, and the membrane area is reduced. Therefore, the thickness of the raw water spacer 4 is 0.1 mm or more and 0.5 m or more.
m or less.

If the porosity in the thickness direction of the raw water spacer 4 is smaller than 10%, it is not possible to sufficiently secure the flow path of the raw water. On the other hand, if the porosity in the thickness direction of the raw water spacer 4 is larger than 80%,
Contaminants can easily enter the gap. Therefore, the porosity in the thickness direction of the raw water spacer 4 is 10% or more and 80% or more.
The following is preferred.

Further, when the mesh pitch of the raw water spacer 4 is smaller than 0.5 mm, the pressure loss increases. On the other hand, when the mesh pitch of the raw water spacers 4 is larger than 10 mm, the envelope membranes 3 come into contact with each other and the flow path of the raw water becomes small. Therefore, the mesh pitch of the raw water spacer 4 is preferably 0.5 mm or more and 10 mm or less.

FIG. 7 is a longitudinal sectional view of the spiral membrane element of FIG. As shown in FIG. 7, in the spiral membrane element 1 of the present embodiment, the raw water spacer 4 is such that the wire 41 is perpendicular to the axial direction of the water collecting pipe 2 and the wire 42 is parallel to the axial direction of the water collecting pipe 2. Are arranged as follows.
Thereby, the raw water easily flows in a direction perpendicular to the axial direction of the water collecting pipe 2.

When the thickness of the outer peripheral channel member 5 is larger than 30 mm, the volumetric efficiency of the membrane element 1 with respect to the pressure vessel storing the membrane element 1 is reduced. On the other hand, if the thickness of the outer peripheral channel member 5 is smaller than 0.6 mm, the flow rate of the raw water for discharging contaminants attached to at least the outer peripheral portion of the membrane element 1 during backflow cleaning of the permeated water is small. Therefore, it may be difficult to discharge the attached contaminants out of the system. Therefore, the thickness of the outer peripheral channel material 5 is 0.6
It is preferable that it is not less than mm and not more than 30 mm.

FIG. 8 is a sectional view showing an example of a method of operating the spiral type membrane element of this embodiment. As shown in FIG. 8, the pressure vessel (pressure-resistant vessel) 10 includes a cylindrical case 11 and a pair of end plates 12a and 12b. A raw water inlet 13 is formed on one end plate 12a, and a raw water outlet 15 is formed on the other end plate 12b. A permeated water outlet 14 is provided at the center of the other end plate 12b.

The spiral type membrane element 1 is housed in a cylindrical case 11, and both open ends of the cylindrical case 11 are sealed by end plates 12a and 12b, respectively. One end of the water collecting pipe 2 is fitted to the permeated water outlet 14 of the end plate 12b, and an end cap 16 is attached to the other end. End plate 1
A pipe 17 and a valve 18 are connected to the raw water outlet 15 of 2b.

During the operation of the spiral membrane element 1, the raw water 51 is introduced into the pressure vessel 10 from the raw water inlet 13 of the pressure vessel 10. The raw water 51 is supplied from at least the outer peripheral side of the spiral membrane element 1 to the raw water spacer 4.
Along the space between the envelope-shaped membranes 3. In the example of FIG. 8, raw water 51 enters between the envelope-shaped membranes 3 from the outer peripheral side and both end sides of the spiral membrane element 1. The permeated water that has passed through the separation membrane 7 flows into the water collecting pipe 2 along the permeated water spacer 6. Thereby, the permeated water outlet 14 of the pressure vessel 10
The permeated water 52 is taken out from the tank. In this way, total filtration is performed.

In this case, since the thickness of the raw water spacer 4 is so thin that contaminants such as turbid substances are trapped at least at the outer peripheral portion (the outer peripheral portion and both ends in the example of FIG. 8) of the membrane element 1, A cake layer of a contaminant is formed on at least the outer peripheral portion of the device. At least the outer periphery of the membrane element 1 is subjected to cake filtration by the cake layer, and the inside of the membrane element 1 is subjected to membrane filtration by the separation membrane 7.

The raw water may be partially taken out from the raw water outlet 15 by opening the valve 18. In this case, a flow of raw water can be formed at the outer peripheral portion of the membrane element 1. Thereby, a part of the contaminants can be discharged to the outside of the pressure vessel 10 while the sedimentation of the contaminants in the raw water is suppressed.

After filtration for a certain period of time, backwashing with permeated water is performed from the permeation side. During backwashing, the permeated water back-filtered from the water collection pipe 2 flows along the raw water spacer 4 at least toward the outer peripheral portion. Thereby, the contaminants captured at least at the outer peripheral portion of the membrane element 1 are easily peeled off. In particular, since the raw water spacers 4 are arranged as shown in FIG. 7, the permeated water discharged from the water collecting pipe 2 easily flows straight toward the outer peripheral portion. Therefore,
The resistance that the permeated water receives from the raw water spacer 4 is reduced,
Increases peeling power of contaminants.

At this time, when the valve 18 is opened while supplying the raw water from the raw water inlet 13, the separated contaminants are discharged out of the system. As a result, the permeation flux is remarkably recovered as compared with before the backwashing.

As described above, in the spiral membrane element 1 of the present embodiment, the filling efficiency of the separation membrane 7 is increased because the thickness of the raw water spacer 4 is small. Further, since the raw water flow path is narrowed and the contaminants are captured at least at the outer peripheral portion of the membrane element 1, it is possible to easily discharge the contaminants out of the system during backwashing.

Further, since the dead space S is not formed in the gap between the membrane element 1 and the pressure vessel 10 by the above-described filtration mode, the propagation of various germs such as microorganisms and the generation and separation of offensive odors due to the decomposition of organic substances. Problems such as decomposition of the film do not occur, and high reliability can be obtained.

Further, since pressure is applied to the membrane element 1 from all directions, the problem of deformation of the membrane element 1 does not occur, and the packing holder and the exterior material become unnecessary. Thereby,
Component and manufacturing costs are reduced.

Since the whole amount is filtered, it is not necessary to use a large pump for supplying raw water. Thereby, the system cost is reduced.

FIG. 9 is a front view of a spiral membrane element according to another embodiment of the present invention. In FIG. 9, the illustration of the outer peripheral channel material is omitted.

The spiral type membrane element 1 shown in FIG.
In, both end portions of the spiral membrane element 1a are sealed with a resin layer 19. In the spiral membrane element 1 shown in FIG. 9B, one end of the spiral membrane element 1 a is sealed with a resin layer 19.

In the spiral type membrane element 1 shown in FIGS. 9 (a) and 9 (b), the number of working steps at the time of manufacturing increases, but a space for supplying raw water to both ends or one end of the membrane element 1 becomes unnecessary. Therefore, the pressure vessel can be reduced in size, and the spiral membrane module in which the membrane element 1 is housed in the pressure vessel can be reduced in size.

Further, by arranging the end portion of the membrane element 1 sealed with the resin layer 19 on the side of the raw water inlet of the pressure vessel, dirt adheres to the end face of the membrane element 1 due to the dynamic pressure of the raw water when the raw water is introduced. Can be prevented.

[Brief description of the drawings]

FIG. 1 is a partially cutaway perspective view of a spiral membrane element according to an embodiment of the present invention.

FIG. 2 is a cross-sectional view showing an example of an envelope-shaped membrane of the spiral membrane element shown in FIG.

FIG. 3 is a cross-sectional view showing another example of the envelope-shaped membrane of the spiral membrane element shown in FIG.

FIG. 4 is a perspective view of a raw water spacer used in the spiral membrane element of FIG. 1;

FIG. 5 is a sectional view taken along line XX of the raw water spacer of FIG. 4;

FIG. 6 is a sectional view showing another example of the raw water spacer.

FIG. 7 is a longitudinal sectional view of the spiral membrane element of FIG. 1;

FIG. 8 is a sectional view showing an example of an operation method of the spiral membrane element of FIG.

FIG. 9 is a front view of a spiral-type membrane element according to another embodiment of the present invention.

FIG. 10 is a partially cutaway perspective view of a conventional spiral-type membrane element.

FIG. 11 is an external perspective view of a conventional spiral-type membrane element.

FIG. 12 is a cross-sectional view showing an example of a conventional method of operating a spiral-type membrane element.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Spiral type membrane element 1a Spiral type membrane element 2 Water collecting pipe 3 Envelope type membrane 4 Raw water spacer 5 Peripheral flow path material 6 Permeated water spacer 7 Separation membrane 10 Pressure vessel 13 Raw water inlet 14 Permeated water outlet 41,42 Wire rod 51 Raw water 52 Permeated water

Claims (5)

[Claims] 1. A spiral membrane element is formed by winding a plurality of independent or continuous envelope-shaped membranes on the outer peripheral surface of a perforated hollow tube via a raw liquid flow path material, and the thickness of the raw liquid flow path material is formed. Is 0.1 mm or more and 0.5 mm or less, a stock solution is supplied from the outer peripheral side and both ends of the spiral membrane element, and a permeated liquid is led out from at least one open end of the perforated hollow tube. A spiral type membrane element characterized by the above-mentioned. 2. A spiral membrane element is formed by winding a plurality of independent or continuous envelope-shaped membranes on the outer peripheral surface of a perforated hollow tube via a raw liquid flow path material, and the thickness of the raw liquid flow path material is formed. Is not less than 0.1 mm and not more than 0.5 mm, one end of the spiral membrane element is sealed, a stock solution is supplied from the outer peripheral side and the other end side of the spiral membrane element, and the perforated hollow A spiral-type membrane element wherein a permeate is discharged from at least one open end of a tube. 3. A spiral membrane element is formed by winding a plurality of independent or continuous envelope-shaped membranes on the outer peripheral surface of a perforated hollow tube via a raw liquid flow path material, and the thickness of the raw liquid flow path material is formed. Is 0.1 mm or more and 0.5 mm or less, both ends of the spiral membrane element are sealed, a stock solution is supplied from the outer peripheral side of the spiral membrane element, and at least one of the perforated hollow tubes is provided. A spiral type membrane element wherein a permeate is discharged from an open end. 4. The spiral membrane element according to claim 1, wherein a porosity in a thickness direction of the stock solution flow path material is 10% or more and 80% or less. 5. The mesh pitch of the stock solution channel material is 0.5.
2. The thickness is not less than 10 mm and not more than 10 mm.
The spiral-type membrane element according to any one of Items 1 to 4, wherein