JP2001029756A - Treatment system using spiral membrane module and operation method thereof - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a treatment system equipped with a spiral membrane module possible to reduce cost, easy to wash and high in reliability and an operation method thereof. SOLUTION: A treatment system is constituted by parallelly connecting units 151, 152 equipped with spiral membrane modules 100 and each of the spiral membrane modules 100 is constituted by packing a pressure container with spiral membrane elements. Each spiral membrane element is constituted by winding a plurality of independent or continuous envelope-shaped membranes around the outer peripheral surface of a water gathering pipe through a raw water spacer successively covering the same with separation membranes and an outer peripheral flow channel material. In this treatment system, the filtering operation of the unit 151 is performed at a time of the washing of the unit 152 and the filtering operation of the unit 152 is performed at a time of the washing of the unit 151. At a time of washing, backwashing and chemical soln. dipping are performed.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a processing system using a spiral type membrane module and a method of operating the same.

[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.

[0003] As a form of a membrane element used for 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. 15 is a partially cutaway perspective view of a conventional spiral membrane element, and FIG. 16 is an external perspective view of a conventional spiral membrane element.

As shown in FIG. 15, a spiral membrane element 21 is composed of an envelope-shaped membrane (bag) by superposing separation membranes 26 on both surfaces of a permeated water spacer (permeate liquid flow path material) 25 and bonding three sides thereof. Film) 23, and the envelope-shaped film 2
3 is attached to the water collecting pipe 22 formed of a perforated hollow pipe, and is wound spirally around the outer peripheral surface of the water collecting pipe 22 together with the net-shaped (net-shaped) raw water spacer 24 (raw water liquid passage material). Is done.

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. 16, 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 shrinkable tube or the like.
Packing holders 28 called anti-telescopes are respectively attached to both ends.

FIG. 17 is a sectional view showing an example of a conventional method of operating a spiral type membrane element. As shown in FIG. 17, the pressure vessel (pressure-resistant vessel) 30 is constituted by 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 spiral type membrane element is operated, the membrane is clogged by the suspended matter in the raw water, and the membrane flux is reduced. Therefore, although clogging is removed by performing chemical cleaning or the like to recover the membrane flux, 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 permeated water or air is periodically performed.

However, in the conventional spiral-type membrane element 21, the following problems occur when backwashing is performed.

FIG. 18 is a partially cutaway perspective view showing a backwashing operation in a conventional spiral membrane element.
As shown in FIG. 18, permeated water 52 is introduced from the end of the water collecting pipe 22. Since the outer peripheral surface of the envelope film 23 wound around the water collecting pipe 22 is covered with the exterior material 27, the water collecting pipe 22
The permeated water 52 derived from the outer peripheral surface of the spiral membrane element 21 passes through the envelope-shaped membrane 23, flows in the axial direction inside the spiral membrane element 21 along the raw water spacer 24, and is discharged from the end of the spiral membrane element 21. You. Therefore, even if the backwashing is performed, contaminants such as turbid substances causing clogging of the membrane are easily captured by the raw water spacer 24 before being discharged from the end of the spiral membrane element 21. There is a problem that it is not sufficiently removed.

Further, a gap existing between the inner peripheral surface of the cylindrical case 31 of the pressure vessel 30 of FIG. 17 and the spiral-type membrane element 21 becomes a dead space S, and a fluid accumulation (liquid accumulation) occurs. Spiral type membrane element 21
When used for a long period of time, the fluid remaining in the dead space undergoes metamorphosis. 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 type membrane element 21, raw water is supplied from one end of the spiral type 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.
In addition, 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 that purpose, a sufficient flow rate on the concentration side is required. When the flow rate on the concentration side is increased, the recovery rate per spiral type membrane element is reduced, and the pump for supplying the raw water is large, and the system cost is very large.

An object of the present invention is to provide a processing system using a spiral-type membrane module which can be reduced in cost, is easy to clean, and has high reliability, and an operation method thereof.

[0021]

Means for Solving the Problems and Effects of the Invention A method for operating a processing system according to the first invention is a method for operating a processing system in which a plurality of spiral type membrane modules are connected in parallel. Type membrane module
One or a plurality of spiral membrane elements are housed in a pressure vessel having a stock solution inlet. The spiral membrane element has a plurality of independent or continuous envelope membranes on the outer peripheral surface of a perforated hollow tube. A spiral membrane element wound around a material is provided, and during the filtration operation, the undiluted solution is supplied from at least the outer peripheral side of the spiral membrane element through the undiluted liquid inlet of the pressure vessel of each spiral membrane module, and The permeated liquid is taken out of the pressure vessel from at least one of the open ends of the empty tube, and at least one of the spiral-type membrane modules is subjected to a filtration operation when washing any one of the spiral-type membrane modules. Things.

In the method for operating the processing system according to the present invention, when washing any one of the plurality of spiral membrane modules, the filtration operation of at least one other spiral membrane module is performed. This makes it possible to perform the filtration operation in an effective manner. Thereby, efficient and highly productive operation can be performed. In addition, since the spiral membrane elements of the plurality of spiral membrane modules can be sequentially washed, the filtration operation can be performed using the spiral membrane elements whose membrane functions have been restored. As a result, reliable and stable operation can be performed for a long period of time.

The filtering operation here includes a backwashing that is periodically performed. Therefore, at the time of backflow washing during the filtration operation of one spiral membrane module, there is a possibility that the other spiral membrane module will be washed. However, the continuity of the filtration operation in the processing system is hardly affected because the backwash time performed during the filtration operation is short.

From the above, an extremely practical and useful processing system is realized. In the above processing system, during the filtration operation of the spiral-wound membrane module, the stock solution is supplied from at least the outer peripheral side of the spiral-wound membrane element, and the whole amount is filtered. In this case, contaminants are trapped at least at the outer periphery of the spiral-wound membrane element. Thereby, the load on the envelope-shaped membrane is reduced.

Further, since dead space is not formed in the gap between the spiral membrane element and the pressure vessel due to the total filtration, no fluid remains in the gap between the spiral membrane element and the pressure vessel. . 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 stock solution is supplied from at least the outer peripheral side of the spiral type membrane element, and pressure is applied to the spiral type membrane element from all directions and no pressure which causes displacement in the axial direction is applied. The envelope-shaped membrane wound around the empty tube 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 spiral membrane element from all directions, the spiral membrane element does not deform even if the supply pressure of the stock solution is increased. Therefore, high pressure resistance can be obtained.

From the above, long-term stable operation is possible. During the filtration operation of the spiral-wound membrane module, a part of the undiluted solution may always or periodically flow in the axial direction along the outer periphery of the spiral-wound membrane element. Thereby, the contaminants in the stock solution can be prevented from adhering to at least the outer peripheral portion of the spiral membrane element, and more stable operation can be performed.

In the cleaning, a cleaning liquid is introduced from at least one open end of the perforated hollow tube of the spiral type membrane module,
The method may include discharging the cleaning liquid derived from the outer peripheral surface of the perforated hollow tube from at least the outer peripheral side of the spiral membrane element.

When the cleaning liquid is introduced from at least one open end of the perforated hollow tube, the cleaning liquid derived from the outer peripheral surface of the perforated hollow tube flows through the envelope-like membrane and flows along the raw liquid flow path material. Is discharged from at least the outer peripheral portion of the spiral membrane element. Thereby, the contaminants trapped at least at the outer peripheral portion of the spiral membrane element are separated from the spiral membrane element. The separated contaminants are discharged out of the system together with the cleaning liquid. Therefore, it is possible to uniformly remove at least the contaminants trapped on at least the outer peripheral portion of the spiral membrane element, and it is possible to always maintain a constant amount of permeate during the filtration operation.

Further, the cleaning may include maintaining the pressure vessel of the spiral type membrane module filled with the cleaning liquid for a predetermined time.

In this case, since at least the outer peripheral portion of the spiral membrane element is open without being covered with the exterior material, a cleaning liquid is filled in the pressure vessel and the spiral membrane element is immersed in the cleaning liquid. By holding for a predetermined time, the contaminants attached to the membrane surface and at least the outer peripheral portion of the spiral membrane element are separated,
It is possible to recover the membrane function of the spiral membrane element more effectively by washing. Thereby, a stable operation can be performed for a long time in the spiral membrane element.

The cleaning liquid may be a permeate or water equivalent to the permeate. Alternatively, the cleaning liquid may include a chemical having a contaminant stripping or sterilizing action. By immersing the spiral membrane element in such a cleaning liquid, it becomes possible to remove contaminants attached to the membrane surface and at least the outer peripheral portion of the spiral membrane element. In particular, by immersing the spiral-type membrane element in a cleaning solution containing a chemical having a stripping action or a sterilizing action of contaminants, the spiral-type membrane element can be more effectively cleaned, and microorganisms on the membrane surface can be effectively removed. , Etc., can be more effectively suppressed.

The washing liquid may be introduced into the pressure vessel through the undiluted liquid inlet. Alternatively, the cleaning liquid may be introduced into the pressure vessel from at least one open end of the perforated hollow tube. As described above, the cleaning liquid is introduced from the stock solution supply side or the permeate extraction side of the spiral membrane module, and the pressure vessel is filled with the cleaning liquid.

A raw liquid supply pipe and a cleaning liquid pipe are connected to a raw liquid inlet of each spiral type membrane module, and a permeated liquid extraction pipe and a cleaning liquid supply pipe are connected to at least one open end of the perforated hollow pipe. First
, A second valve is inserted in the cleaning liquid discharge pipe, a third valve is inserted in the permeate extraction pipe, a fourth valve is inserted in the cleaning liquid supply pipe, and the first, second, and third valves are inserted. The filtration operation and the washing of each spiral type membrane module may be switched by opening and closing the third and fourth valves. This makes it possible to perform a filtration operation on at least one other spiral-type membrane module when washing any one of the spiral-type membrane modules.

A processing system according to a second aspect of the present invention is a processing system in which a plurality of spiral membrane modules are connected in parallel.
Alternatively, a plurality of spiral-type membrane elements are housed in a pressure vessel having a stock solution inlet, and the spiral-type membrane element comprises a plurality of envelope-like membranes that are independent or continuous on the outer peripheral surface of a perforated hollow tube. The raw liquid is supplied from at least the outer peripheral side of the spiral-type membrane element through the raw-liquid inlet of the pressure vessel of each spiral-type membrane module during the filtration operation. The permeate is taken out of the pressure vessel from at least one open end of the tube, and at least one of the spiral-type membrane modules is subjected to a filtration operation when washing any one of the spiral-type membrane modules. Thus, the flow path switching means capable of switching the flow path is provided.

In the processing system according to the present invention, when one of the plurality of spiral membrane modules is washed, the filtration operation is performed on at least one other spiral membrane module by the flow path switching means. As a result, the filtration operation can be continuously performed. Thereby, efficient and highly productive operation can be performed. In addition, since the spiral membrane elements of the plurality of spiral membrane modules can be sequentially washed, the spiral membrane elements whose membrane functions have been restored can always be used for the filtration operation. As a result, reliable and stable operation can be performed for a long period of time.

From the above, an extremely practical and useful system is realized. In the above processing system, during the filtration operation of the spiral-wound membrane module, the stock solution is supplied from at least the outer peripheral side of the spiral-wound membrane element, and the whole amount is filtered. In this case, contaminants are trapped at least at the outer periphery of the spiral-wound membrane element. Thereby, the load on the envelope-shaped membrane is reduced.

Further, since dead space is not formed in the gap between the spiral membrane element and the pressure vessel due to the total filtration, no fluid remains in the gap between the spiral membrane element and the pressure vessel. . 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, a stock solution is supplied from at least the outer peripheral side of the spiral membrane element, and pressure is applied to the spiral membrane element from all directions, and no pressure that causes displacement in the axial direction is applied. The envelope-shaped membrane wound around the empty tube 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 spiral membrane element from all directions, the spiral membrane element does not deform even if the supply pressure of the stock solution is increased. Therefore, high pressure resistance can be obtained.

From the above, long-term stable operation is possible. During the filtration operation of the spiral-wound membrane module, a part of the undiluted solution may always or periodically flow in the axial direction along the outer periphery of the spiral-wound membrane element. Thereby, the contaminants in the stock solution can be prevented from adhering to at least the outer peripheral portion of the spiral membrane element, and more stable operation can be performed.

The flow path switching means includes a raw liquid supply pipe and a cleaning liquid discharge pipe connected to a raw liquid inlet of each spiral membrane module, a permeated liquid extraction pipe connected to at least one open end of the perforated hollow pipe, and a cleaning liquid. Supply piping,
Including a first valve inserted in the undiluted liquid supply pipe, a second valve inserted in the cleaning liquid discharge pipe, a third valve inserted in the permeated liquid take-out pipe, and a fourth valve inserted in the cleaning liquid supply pipe May be. This makes it possible to perform a filtration operation on at least one other spiral-type membrane module when washing any one of the spiral-type membrane modules.

Each of the first to fourth valves is an automatic valve, and control means for controlling the opening and closing operation of each of the first to fourth automatic valves may be provided. In this case, it is possible to automatically switch the flow path by automatically opening and closing the first to fourth valves using the control means.

The control means may control the opening and closing operation of each of the first to fourth automatic valves based on the time setting. This makes it possible to automatically switch the flow path based on the time setting, and to switch between the filtering operation and the washing at predetermined time intervals.

The control means may control the opening and closing operations of the first to fourth automatic valves in accordance with the supply pressure or supply flow rate of the stock solution during the filtration operation of the spiral type membrane module. Alternatively, the control means may control the opening / closing operation of each of the first to fourth automatic valves according to the pressure in the permeate extraction pipe or the flow rate of the permeate during the filtration operation of the spiral membrane module. Further, the control means is configured to perform the first operation in accordance with the pressure difference between the undiluted solution supply side and the permeated liquid take-out side during the filtration operation of the spiral membrane module.
The opening and closing operations of each of the fourth to fourth automatic valves may be controlled. In these cases, the flow path is automatically switched according to the state of contamination of the spiral membrane element in the spiral membrane module, and it is possible to switch between the filtration operation and the washing.

[0047]

FIG. 1 is a partially cutaway perspective view showing an example of a spiral type membrane element used in a processing system according to 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 type 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. . Raw water spacers (raw liquid flow path material) between the envelope films 3 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.
4 has been inserted.

The outer peripheral surface of the spiral membrane element 1a is covered with a separation membrane 9 which is a liquid permeable material. As the separation membrane 9, a microfiltration membrane or an ultrafiltration membrane is used.

As the microfiltration membrane, a polymer organic membrane such as polyolefin, polysulfone, polypropylene, polyethylene, polystyrene, polyacrylonitrile, and cellulose acetate can be used. As the ultrafiltration membrane, polysulfone, polypropylene, polystyrene,
A high molecular organic film such as polyacrylonitrile, cellulose acetate, or polyethylene can be used.

The outer peripheral surface of the separation membrane 9 is covered with an outer peripheral channel material 5 made of a net. As the material of the net,
Polymer materials such as polyolefin, polysulfone, polypropylene, polyethylene, polystyrene, polyacrylonitrile, and cellulose acetate; inorganic materials such as ceramic;
Metal, synthetic rubber, fiber, or the like can be used.

The pore size of the microfiltration membrane is 0.01 μm or more and 1
It is preferably 0 μm or less. The pore size of the ultrafiltration membrane is preferably from 20,000 to 0.01 μm. Further, it is preferable that the net used as the outer peripheral channel material 5 has a mesh size of 4 mesh or more and 100 mesh or less.

The pore diameter of the microfiltration membrane or the ultrafiltration membrane used as the separation membrane 9 and the number of meshes of the net used as the outer peripheral passage material 5 are selected according to the quality of the raw water.

In the spiral type membrane element 1 shown in FIG. 1, a microfiltration membrane having a pore diameter of 0.4 μm made of polyolefin such as ethylene vinyl alcohol is used as the separation membrane 9. Further, an ultrafiltration membrane made of polysulfone may be used as the separation membrane 9. Further, a 50 mesh net made of PET (polyethylene terephthalate) is used as the outer peripheral channel material 5.

The end face of the spiral membrane element 1a may be covered with the separation membrane 9 in addition to the outer peripheral face of the spiral membrane element 1a.

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.

If the thickness 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 spiral membrane element 1. On the other hand, when the thickness of the raw water spacer 4 is smaller than 0.1 mm, the envelope films 3 are likely to come into contact with each other, and the film area is reduced.
Therefore, the thickness of the raw water spacer 4 is preferably 0.1 mm or more and 0.5 mm or less.

As shown in FIG. 1, the outer peripheral channel material 5 is formed in a lattice shape so that a plurality of wires 61 and 62 intersect each other at right angles. The thickness of the wire 61 is set to be larger than the thickness of the wire 62. This makes it easier for the raw water 51 to flow between the wires 61 almost linearly in a direction parallel to the wires 61.

Further, as shown in FIG.
Are arranged such that the wire 61 is parallel to the axial direction of the water collecting pipe 2. Therefore, the raw water is the spiral membrane element 1
It becomes easy to flow in the axial direction at the outer peripheral portion of a.

When the thickness t of the outer peripheral flow path member 5 is larger than 30 mm, the volume efficiency of the spiral membrane element 1 with respect to the pressure vessel storing the spiral membrane element 1 becomes small. On the other hand, the thickness t of the outer peripheral channel material 5 is 0.6 m.
If it is smaller than m, the flow rate of raw water for discharging contaminants attached to at least the outer peripheral portion of the spiral membrane element 1 during backflow cleaning of permeated water is reduced. Therefore, the thickness of the outer peripheral channel material 5 is 0.6 mm or more and 30 m or more.
m or less.

The porosity in the thickness direction of the outer peripheral flow path member 5 is set to, for example, 20% or more and 60% or less. Thereby, sufficient strength of the outer peripheral channel member 5 can be secured while reducing the resistance of the raw water that moves the contaminant in the axial direction during the backwashing. The vertical and horizontal pitches of the mesh of the outer peripheral channel member 5 are, for example, 3 mm or more and 30 mm or less.
Thus, the raw water can be sufficiently supplied between the envelope-shaped membranes 3 while preventing the outer peripheral surface of the spiral membrane element 1a from contacting the pressure vessel and narrowing the flow path of the raw water.

Incidentally, the whole of the outer peripheral separation membrane 9 may be covered with the outer peripheral channel material 5, or a part of the region may be covered with the outer peripheral channel material 5.

FIG. 4 is a sectional view showing an example of a method of operating a spiral type membrane module used in the processing system according to the present invention. As shown in FIG. 4, a pressure vessel (pressure-resistant vessel) 1
0 denotes a cylindrical case 11 and a pair of end plates 12a, 12b.
It consists of. One end plate 12a has a raw water inlet 13
Are formed, and a raw water outlet 15 is formed in 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 shown in FIG. 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. In this way, a spiral membrane module 100 in which the spiral membrane element 1 is loaded in the pressure vessel 10 is configured. In the raw water inlet 13 of the end plate 12a,
A pipe 19 is connected, and the pipe 19 is further connected to a pipe 2.
0 is connected. The pipes 19 and 20 are provided with valves 18a and 18b, respectively. End plate 1
A pipe 17 is connected to the raw water outlet 15 of 2b. The pipe 17 is provided with a valve 18c. End plate 1
A pipe 21 is connected to the permeated water outlet 14 of 2b, and a pipe 22 is further connected to the pipe 21. The pipes 21 and 22 have valves 18d and 1 respectively.
8e are provided.

During the filtration operation of the spiral membrane module 100, the valve 18a of the pipe 19 and the valve 18d of the pipe 21 are opened, and the valve 18b of the pipe 20 and the pipe 22 are opened.
And the valve 18c of the pipe 17 are closed. Raw water 51 is introduced into the pressure vessel 10 from the raw water inlet 13 of the pressure vessel 10 through the pipe 19. Raw water 51
Flows along the outer peripheral channel member 5 and permeates the separation membrane 9 from at least the outer peripheral side of the spiral membrane element 1,
It penetrates between the envelope membranes 3 along the raw water spacers 4. FIG.
In the example, 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 52 a is taken out from the permeated water outlet 14 of the pressure vessel 10 through the pipe 21. In this way, total filtration is performed.

In this case, since the outer peripheral surface of the spiral membrane element 1 a is covered with the separation membrane 9, contaminants such as turbid substances larger than the pore diameter of the separation membrane 9 are removed from at least the outer periphery of the spiral membrane element 1. Caught in the department. That is,
Only contaminants smaller than the pore size of the separation membrane 9
Break in. Therefore, the load on the separation membrane 7 constituting the envelope-shaped membrane 3 is reduced.

The raw water 51a may be partially taken out from the raw water outlet 15 by opening the valve 18c of the pipe 17. In this case, the flow of raw water can be formed at the outer peripheral portion of the spiral 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 51 is suppressed. Further, at least a part of the extracted raw water 51a may be circulated and returned to the supply side.

Also, the supplied raw water 51 may contain a chemical having a stripping action or a bactericidal action of pollutants. For example, raw water 51 containing sodium hypochlorite at a concentration of 1 to 10000 ppm, raw water 51 containing chloramine at a concentration of 0.1 to 10 ppm, raw water 51 containing hydrogen peroxide at a concentration of 10 to 10000 ppm, and pH 1 to 3 containing sulfuric acid. Raw water 5
1. Raw water 51 of pH 1 to 3 containing hydrochloric acid, raw water 51 of pH 10 to 13 containing sodium hydroxide, concentration of 10 to 100
Raw water 51 containing 00 ppm peracetic acid, concentration 0.1-50
Raw water 51% isopropyl alcohol, concentration 0.
Raw water 51 containing 2 to 2% citric acid or a concentration of 0.2 to 2%
Raw water 51 containing 2% oxalic acid is supplied to the spiral-wound membrane module 100. In this case, the contaminants adhered to the outer peripheral portion of the spiral-wound membrane element 1 are peeled off, whereby the accumulation of the contaminants can be suppressed, and the growth of microorganisms on the film surface can be suppressed. Thereby, stable performance can be obtained in the spiral membrane module 100 for a long time.

After performing the above-mentioned filtration operation for a predetermined time, backwashing is performed by introducing washing water from the permeation side. In the backwashing in this case, the permeated water 52b is used as the washing water.

FIG. 5 shows the spiral type membrane element 1 shown in FIG.
It is a partially notched perspective view which shows the backwash operation | movement in FIG.
During backwashing, the valve 18a of the pipe 19, the valve 18d of the pipe 21, and the valve 18c of the pipe 17 are closed, and the valve 18b of the pipe 20 and the valve 18e of the pipe 22 are opened. The permeated water 52 b is introduced into the water collection pipe 2. The permeated water 52b at the time of backwashing penetrates the envelope-shaped membrane 3 from the water collection pipe 2, peels off the contaminants on the membrane surface from the membrane surface, and flows along the raw water spacer 4 at least toward the outer peripheral portion. In addition, the contaminants trapped on at least the outer peripheral portion of the spiral-wound membrane element 1 are easily separated by the permeated water 52b. The separated contaminants are discharged to the outside through the pipe 20 together with the permeated water 52b. Then, raw water 51b
Flushing. That is, the valve 18a of the pipe 19 is opened, and the valve 18b of the pipe 20 and the pipe 2
In a state where the second valve 18e is closed, the raw water 51 is supplied from the raw water inlet 13 (FIG.
Is opened. As a result, the raw water 51b flows linearly in the axial direction along the outer peripheral flow path material 5, and the separated contaminants are discharged to the outside from the raw water outlet 15 (FIG. 4) via the pipe 17, and the spiral type water is discharged. Contaminants remaining on the outer peripheral portion of the membrane element 1 are peeled off. As a result, the membrane flux is remarkably recovered compared to before the backwashing. The permeated water 52b discharged from the pipe 20 and the pipe 1
Alternatively, at least a part of the raw water 51b discharged from 7 may be circulated and returned to the supply side again.

According to the above-described cleaning method, the contaminants adhering to the outer peripheral portion of the spiral membrane element 1, particularly the separation membrane 9, can be easily and reliably discharged to the outside along the outer peripheral channel member 5. Therefore, an increase in resistance of the separation film 9 can be suppressed. Thereby, a stable amount of permeated water can always be maintained. Further, since the outer peripheral portion of the spiral membrane element 1 is covered with the outer peripheral channel material 5, handling (handling) is improved.

Further, since the dead space such as the dead space S shown in FIG. 17 is not formed in the space between the spiral membrane element 1 and the pressure vessel 10 by the above-mentioned filtration mode, various bacteria such as microorganisms can be formed. There is no problem of odor propagation, generation of offensive odor due to decomposition of organic matter, decomposition of separation membrane, etc., and high reliability can be obtained.

Since pressure is applied to the spiral membrane element 1 from all directions, the spiral membrane element 1
No deformation problem occurs, and the packing holder and the exterior material become unnecessary. Thereby, component costs and manufacturing costs are reduced.

Further, since the whole amount is filtered, the raw water 51
It is not necessary to use a large pump for supplying oil. Thereby, the system cost is reduced.

At the time of the above-mentioned backwashing, first, the permeated water 52b is introduced into the water collecting pipe 2, and the permeated water 52b drawn out from the outer peripheral surface of the water collecting pipe 2 causes the membrane surface and the outer peripheral portion of the spiral type membrane element 1 to be introduced. Although the flushing with the raw water 51b is performed after the contaminants trapped in the water are stripped off, the flushing with the raw water 51b may be performed first, and then the permeated water 52b may be introduced into the water collecting pipe 2. According to this cleaning method, most of the contaminants trapped on the outer peripheral portion of the spiral-type membrane element 1 are removed by flushing, and the permeated water 52b is further introduced, whereby
Contaminants remaining on the membrane surface and the outer peripheral portion of the spiral membrane element 1 can be removed. Therefore, also in this case, the same effect as the above-described backwashing can be obtained.

Alternatively, flushing with the raw water 51b may be performed in parallel with the introduction of the permeated water 52b into the water collecting pipe 2. In this case, the same effect as the above-described cleaning method can be obtained.

In the backwashing described above, the permeated water 52b is used as the washing water. In addition to the permeated water 52b, water from which contaminants have been removed to the same extent or more than the permeated water 52b (hereinafter referred to as permeated water) Equivalent water) may be used as washing water. For example, pure water, purified water, ion-exchanged water, tap water, or other permeated water equivalent water can be used as the wash water.

Further, permeated water 52b used as washing water
Alternatively, the water equivalent to the permeated water may contain a chemical having a stripping action or a bactericidal action of a contaminant. For example, at the time of backflow washing, the permeated water 52b containing sodium hypochlorite having a concentration of 1 to 10000 ppm or water equivalent to permeated water, the permeated water 52b containing chloramine having a concentration of 0.1 to 10 ppm or water equivalent to permeated water, having a concentration of 1 to 1 ppm Permeated water 52b or permeated water equivalent water containing 10,000 ppm of hydrogen peroxide, permeated water 52b or permeated water equivalent to pH 1 to 3 containing sulfuric acid, permeated water 52b or permeated water equivalent to pH 1 to 3 containing hydrochloric acid,
Permeated water 52b having a pH of 10 to 13 containing sodium hydroxide
Or permeated water equivalent water, permeated water 52b containing peracetic acid having a concentration of 10 to 10000 ppm or permeated water equivalent water, having a concentration of 0.1%.
Permeated water 52 containing 1 to 50% isopropyl alcohol 52
b or water equivalent to permeated water, permeated water 52b containing 0.2 to 2% citric acid or water equivalent to permeated water or a concentration of 0.2
Permeated water 52b containing ２2% oxalic acid or water equivalent to permeated water is used as washing water. In this case, it is possible to effectively remove the contaminants attached to the membrane surface and at least the outer peripheral portion of the spiral membrane element 1, and to suppress the growth of microorganisms on the membrane surface.

Further, as a cleaning method other than the backwashing,
The permeated water 52b or the above-mentioned permeated water equivalent water is sealed in the pressure vessel 10 as washing water, and the spiral membrane element 1
May be immersed in permeated water 52b or permeated water equivalent water (permeated water immersion). In this case, the valve 18a of the pipe 19,
The valve 18 b of the pipe 20, the valve 18 c of the pipe 17, and the valve 18 d of the pipe 21 are closed and the valve 18 e of the pipe 22 is opened, and the permeated water 52 b or permeated water equivalent water is supplied from the permeated water side to the inside of the collection pipe 2 through the pipe 22. Supply. Alternatively, the valve 18 a of the pipe 19 is opened and the valve 18 b of the pipe 20, the valve 18 c of the pipe 17, the valve 18 d of the pipe 21, and the valve 18 e of the pipe 22 are closed, and the permeated water enters the pressure vessel 10 from the raw water side through the pipe 19. 52b or water equivalent to permeated water is supplied. Thus, the permeated water 52b or the permeated water equivalent is supplied from the permeated water side or the raw water side, and the raw water 51 in the pressure vessel 10 is replaced with the permeated water 52b or the permeated water equivalent water. Thereafter, the permeated water 52b or permeated water equivalent water is sealed in the pressure vessel 10 for a predetermined time.

In the spiral membrane module 100 in which the permeated water 52b or the water equivalent to the permeated water is sealed, the pressure on the raw water side and the pressure on the permeated water side of the separation membrane of the spiral membrane element 1 are maintained at substantially atmospheric pressure. Therefore, no liquid flow is formed on the raw water side and the permeated water side. By enclosing the permeated water 52b or the water equivalent to the permeated water, it is possible to effectively remove the contaminants attached to the membrane surface of the spiral membrane element 1 and at least the outer peripheral portion.

In addition to the above-described immersion in the permeated water, the permeated water 52b or the permeated water equivalent containing the above-mentioned chemical having a stripping action or a sterilization action of the contaminants as the washing water is applied to the pressure vessel 10 from the permeated water side or the raw water side. And the spiral-type membrane element 1 may be immersed therein (chemical solution immersion). In this case, permeated water 52b containing chemicals or permeated water equivalent water is supplied from the permeated water side or raw water side by the same method as in the case of permeated water immersion, and the inside of pressure vessel 10 is permeated water 52b containing chemicals or permeated water. Replace with equivalent water. Thereafter, the permeated water 52b containing the chemical or permeated water equivalent water is sealed in the pressure vessel 10 and held for a predetermined time. Such chemical immersion makes it possible to more effectively remove contaminants adhering to the membrane surface and the outer peripheral portion of the spiral membrane element 1, and more effectively suppresses the growth of microorganisms on the membrane surface. It is possible to do.

In particular, when the raw water 51 having a high turbidity containing a large amount of contaminants is entirely filtered, a large amount of turbid components (contaminants) in the raw water 51 are captured on the outer peripheral surface of the spiral membrane element 1. accumulate. In addition, contaminants not captured on the outer peripheral surface are deposited on the separation membrane 7. For this reason, it is difficult to completely remove contaminants by backwashing using permeated water 52b or water equivalent to permeated water as cleaning water without containing a chemical. In such a case, by performing the above-described chemical liquid immersion, the deposited contaminants are easily peeled off, and cleaning can be performed effectively.

The spiral type membrane module 100 described above is used for the processing system described below.

FIG. 6 is a schematic configuration diagram showing a processing system according to an embodiment of the present invention. The processing system shown in FIG. 6 uses the spiral type membrane module 10 shown in FIG.
0, pipes 17, 19-22 and valves 18a-18e
Are connected in parallel. Spiral type membrane module 1 of unit 151
A pipe 19 connected to the raw water inlet 13 of FIG.
The pipe 19 connected to the raw water inlet 13 (FIG. 4) of the spiral type membrane module 100 of the unit 152 is connected on the upstream side of the valve 18a, and further connected to the raw water pressurizing pump 101. Further, a chemical injection device 105 having a chemical injection pump and a chemical storage tank is provided downstream of the raw water pressurizing pump 101 in the pipe 19. Further, a pipe 21 connected to the permeated water outlet 14 (FIG. 4) of the spiral type membrane module of the unit 151
And the spiral type membrane module 100 of the unit 152
The pipe 21 connected to the permeated water outlet 14 (FIG. 4)
It is connected downstream of the valve 18d. A pipe 23 is further connected to the connected pipe 21, and the pipe 23 is connected to a permeate tank 104 for washing.
The washing permeated water tank 104 is connected to the washing water pressurizing pump 102 through the pipe 22. A chemical injection device 103 having a chemical injection pump and a chemical storage tank is provided in the pipe 22.
Is provided, and the piping 2 of each unit 151, 152 is further provided.
The first valve 18d is connected to the pipe 21 on the upstream side.

Each valve 18 of each unit 151, 152
a to 18e are automatic valves. Valves 18a to 18e
Each of the opening and closing operations is controlled by a timer (not shown), and is set to open for a predetermined time at predetermined time intervals.

In the chemical storage tanks of the chemical injection devices 103 and 105, chemicals having an action of peeling or sterilizing contaminants, for example, sodium hypochlorite, chloramine, hydrogen peroxide, sulfuric acid, hydrochloric acid, sodium hydroxide, sodium hydroxide, Acetic acid, isopropyl alcohol, citric acid, oxalic acid, etc. are stored.

In the above processing system, the filtering operation of the unit 151 is performed when the unit 152 is washed, and the filtering operation of the unit 152 is performed when the unit 151 is washed.

Hereinafter, a method of operating the processing system will be described. During operation of the processing system, first, the valve 18a of the pipe 19 of the unit 151 and the valve 18d of the pipe 21 are opened, and the valve 18 of the pipe 20 is opened.
b, valve 18c of pipe 17 and valve 1 of pipe 22
8e is closed. Thus, the raw water 51 pressurized by the raw water pressurizing pump 101 is supplied to the unit 1 through the pipe 19.
It is supplied to the spiral type membrane module 100 of 51, and the whole amount is filtered. The spiral type membrane module 1
Details of the filtration operation method of 00 are as described above with reference to FIG. In this case, a part of the obtained permeated water 52a is led out to the permeated water tank 104 for cleaning through the pipe 23 and stored therein. On the other hand, the remaining permeated water 52a
Is taken out through a pipe 21.

In the above-mentioned filtration operation, in the process of the raw water 51 flowing through the pipe 19, a chemical having an action of stripping or sterilizing contaminants is injected into the raw water 51 by the chemical injection device 105. In this case, for example, the raw water 51 containing the chemicals described above in FIG. 4 is supplied to the spiral membrane module 100. Thereby, the contaminant adhered to the outer peripheral portion of the spiral-type membrane element 1 is peeled off, and the deposition of the contaminant can be suppressed. It is also possible to suppress the growth of microorganisms on the membrane surface. Therefore, in the spiral membrane element 1, more stable performance can be obtained over a long period.

During the filtration operation of the unit 151, the valve 18a of the pipe 19 of the unit 152 and the pipe 2
1 and the valve 18c of the pipe 17 are closed, and the valve 18b of the pipe 20 and the valve 1 of the pipe 22 are closed.
8e is opened. Thereby, the permeated water 52b taken from the permeated water tank 104 for cleaning and pressurized by the cleaning water pressurizing pump 102 is supplied as cleaning water to the spiral membrane module 100 of the unit 152 through the pipe 22.
Backwashing is performed. After backwashing, valve 1 of pipe 20
8d and the valve 18e of the pipe 22 are closed, the valve 18a of the pipe 19 and the valve 18c of the pipe 17 are opened, and the raw water 51b is supplied to the spiral membrane module 100 of the unit 152 through the pipe 19 to perform flushing. The details of the backwashing and flushing are as described above with reference to FIG.

[0092] The permeated water 52b used for backwashing is used.
Then, a chemical having a stripping action or a bactericidal action of contaminants may be injected. In this case, the chemical is injected by the chemical injection device 103 while the permeated water 52b flows through the pipe 22, and for example, the permeated water 52b containing the chemical described above with reference to FIG.
Supplied to This makes it possible to more effectively clean the spiral-type membrane element 1 during backwashing.

After the above flushing, the unit 152
18a of the pipe 19 and the valve 18 of the pipe 17
While closing c, the valve 18e of the pipe 22 is opened, and the permeated water 52b is again supplied to the spiral membrane module 100 through the pipe 22. At this time, in the process in which the permeated water 52b flows through the pipe 22, the chemical injecting device 103 injects a chemical having a stripping action or a sterilizing action of the contaminant into the permeated water 52b. In this case, as the washing water, for example, the permeated water 52b containing the chemicals described above in FIG. 4 is supplied to the spiral membrane module 100 from the permeated water side. Thereafter, the valve 18e of the pipe 22 is closed, the permeated water 52b containing a chemical is sealed in the spiral membrane module 100, and the spiral membrane element 1 is immersed in a chemical solution. The details of the chemical solution immersion are as described above with reference to FIG.

By the above-described backwashing and immersion in the chemical solution, the spiral type membrane module 100 of the unit 152 is formed.
In, the membrane function of the spiral membrane element 1, which has been reduced by the adhesion of the contaminants, is restored.

After performing the filtering operation of the unit 151 and the washing of the unit 152 for a predetermined time, the unit 15
The valve 18a of the pipe 19 and the valve 1 of the pipe 21
8d, the valve 18b of the pipe 20 and the valve 18e of the pipe 22 are opened, and the pipe 19 of the unit 152 is opened.
And the valve 18d of the pipe 21 are opened.
As a result, the permeated water 52b is taken from the permeated water tank 104 for cleaning and pressurized by the cleaning water pressurizing pump 102.
Is supplied to the spiral membrane module 100 of the unit 151 through the pipe 22 as washing water. On the other hand, the raw water 51 which is pressurized by the raw water pressurizing pump 101 and in which the chemical is injected by the chemical injection device 105 is supplied to the pipe 1
9 and supplied to the spiral membrane module 100 of the unit 152. Therefore, contrary to the above-described case where the filtering operation is performed in the unit 151 and the washing is performed in the unit 152, the unit 151
, And a filtration operation is performed in the unit 152. At the time of cleaning the unit 151 in this case, backflow cleaning, flushing, and immersion in a chemical solution are performed by a method similar to the method of cleaning the unit 152 described above. Thus, in the unit 151, the membrane function of the spiral membrane element 1, which has been reduced due to the attachment of the contaminant, is restored.

After the cleaning of the unit 151 and the filtering operation of the unit 152 are performed as described above, the filtering operation of the unit 151 and the cleaning of the unit 152 are performed again by the above-described method.

In the above processing system, the valves 18a to 18e of the units 151 and 152 are controlled by a timer.
The opening / closing operation of the unit is controlled, the piping for supplying the raw water 51 and the permeated water 52b is switched at predetermined time intervals, and the filtering operation of the other unit is performed when one unit is washed. In such a processing system, it is possible to continuously perform a filtration operation, and thus it is possible to perform an operation with high efficiency and high productivity. In addition, each unit 151, 1
The spiral-type membrane element 1 of which 52 can be sequentially washed, and the membrane function has been restored by the washing
, It is possible to always perform a filtration operation, so that a highly reliable and stable operation can be performed. Therefore, an extremely practical and useful system is realized.

In the above-described cleaning, the backwashing and the immersion in the chemical solution are performed in order, but the order of the combination of the backwashing and the immersion in the chemical solution is not limited to this.
Further, the number of times of the backwashing and the immersion in the chemical solution is not limited to this. For example, at the time of cleaning, the chemical solution immersion and the backflow cleaning may be performed in this order, the backflow cleaning may be performed before and after the chemical solution immersion, or only the chemical solution immersion may be performed.

Further, instead of immersion in a chemical solution, immersion in permeated water described above with reference to FIG. 4 may be performed. In this case, permeated water 52b is supplied to the spiral membrane module 100 from the permeated water side through the pipe 22 as washing water,
The spiral-type membrane element 1 is immersed by enclosing the spiral-type membrane element 1 in the spiral-type membrane module 100. This makes it possible to effectively remove contaminants adhering to the membrane surface of the spiral membrane element 1 and at least the outer peripheral portion.

In the above-described chemical immersion and permeate immersion, the permeate outlet 14 of the spiral type membrane module 100 is used.
Wash water is supplied from the permeated water side through a pipe 22 connected to (FIG. 4).
Wash water may be supplied from the raw water side through a pipe 19 connected to the raw water inlet 13 (FIG. 4). In the case where the cleaning solution is supplied from the raw water side and the chemical solution is immersed, the chemical injection may be performed using the chemical injection device 105.

In the above treatment system, the time for performing the filtration operation is preferably 3 minutes or more. If the filtration operation time is shorter than 3 minutes, the frequency of backwashing or the like increases, and the filtration efficiency decreases.

It is preferable that the time for performing the backwashing be 10 seconds or more and a maximum of 5 minutes. If the backwash time is shorter than 10 seconds, the spiral membrane element 1
The contaminants adhered to the film surface or the like cannot be sufficiently removed. Generally, the backwash time is 2-3 minutes.

The time for immersion in the chemical solution is preferably 10 minutes or more. When the chemical solution immersion time is shorter than 10 minutes, it is difficult to sufficiently remove contaminants adhered to the film surface or the like of the spiral type membrane element 1 and it is difficult to sufficiently suppress the propagation of microorganisms or the like on the film surface or the like. It is.

The time for immersion in permeated water is preferably 3 minutes or more. When the permeated water immersion time is shorter than 3 minutes, it is difficult to sufficiently remove contaminants attached to the membrane surface of the spiral membrane element 1 and the like.

Therefore, the time of the timer is set so as to satisfy the above conditions, and the opening and closing operations of the valves 18a to 18e of the units 151 and 152 are controlled.

In the above processing system, when the permeated water 52b containing a chemical is supplied to the spiral membrane module 100 at the time of cleaning, the chemical is injected into the permeated water 52b using the chemical injection device 103. A chemical may be directly injected into the permeated water 52b in the permeated water tank 104 for use, and cleaning water containing a predetermined concentration of the chemical may be prepared in advance. In this case, the chemical concentration of the cleaning water can be accurately controlled.

In the above-described backwashing, immersion in a chemical solution, and immersion in permeated water, the permeated water 52b is used as the washing water, but water equivalent to permeated water such as pure water, purified water, ion exchange water, or tap water is used. It may be used instead of the permeated water 52b.

The permeated water is stored in the washing water tank,
The permeated water equivalent water taken from the washing water tank is
May be supplied from the permeated water side of the spiral-wound membrane module 100 or may be supplied from the raw water side of the spiral-wound membrane module 100 through the pipe 19.
Alternatively, a chemical may be directly injected into permeated water equivalent water stored in the cleaning water tank, and cleaning water containing a predetermined concentration of the chemical may be prepared in advance.

In the processing system described above, apart from the backwashing at the time of washing, backflow washing is periodically performed by a timer or the like during the filtration operation of each unit 151, 152. In this case, during the backwashing or immersion of the spiral membrane module of one unit during the washing, the backflow washing of the spiral membrane module of the other unit during the filtration operation may be performed. However, the backwashing during the filtration operation has a short time as described above, and thus has little effect on the continuity of the filtration operation in the treatment system.

In the processing system described above, the filtering operation and the washing are alternately performed in the unit 151 and the unit 152. However, except for the washing of one of the units 151 and 152, the units 151 and 152 are not used. The filtration operation of 152 may be performed in parallel. In this case, the time of the timer is set so that the filtration operation is performed in at least one of the units. Note that both units 1
In the case where the filtration operations are performed in parallel in 51 and 152, settings are made so that backwashing during the filtration operation is not performed simultaneously.

In the above processing system, the units 151 and 152 are provided with the common raw water pressurizing pump 101, the washing water pressurizing pump 102 and the chemical injection devices 103 and 105. A pressurizing pump 101, a washing water pressurizing pump 102, and chemical injection devices 103 and 105 may be provided.

In the above description, the opening and closing operations of the valves 18a to 18e of the units 151 and 152 are controlled by the timer to switch between the filtering operation and the washing at predetermined time intervals. Spiral type membrane element 1 of spiral type membrane module 100
Each valve 18a-18e according to the state of contamination (FIG. 4)
May be controlled by controlling the opening and closing operations of the pipes and switching the pipes.

For example, the spiral type membrane module 100
Each unit according to the supply flow rate of the raw water 51, the supply pressure of the raw water 51, the flow rate of the permeated water 52a, the pressure in the pipe 21 on the permeated water side, or the pressure difference between the raw water supply side and the permeated water take-out side during the filtration operation. 151, 152 each valve 18a-1
8e is controlled to switch from the filtering operation to the washing operation.

In the spiral membrane module 100, contaminants in the raw water 51 accumulate on the membrane surface of the spiral membrane element 1 and at least on the outer periphery thereof along with the filtration operation. During the filtration operation, the backwash is periodically performed as described above, but the contaminants gradually accumulate in the continuous operation. For this reason, it becomes difficult to remove contaminants by backwashing during the filtration operation. When the contamination of the spiral membrane element 1 proceeds, the spiral membrane module 10
0, the supply flow rate of the raw water 51 during the filtration operation,
Supply pressure, flow rate of permeated water 52a, pipe 21 on the permeated water side
The internal pressure or the pressure difference between the raw water supply side and the permeate discharge side changes. Accordingly, the opening and closing operation of each of the valves 18a to 18e is controlled in accordance with such a change, and switching from the filtering operation to the cleaning operation enables efficient cleaning. Thereby, a stable processing system with high filtration efficiency and high reliability is realized.

In the above description, two units 15
Although the processing system including the processing units 1 and 152 has been described, the processing system may include three or more units. In a processing system including three or more units, a filtration operation is performed in at least one unit, and cleaning is performed in the remaining units. At the time of washing, any of backflow washing, chemical solution immersion and permeated water immersion may be performed. Backwashing, immersion in a chemical solution, and immersion in permeated water may be performed alone or in any combination thereof. The details of the filtration operation, backwashing, chemical liquid immersion, and permeated water immersion in each unit are as described above in the processing system shown in FIG.

In the above, the case where the spiral membrane module 100 used in the processing system includes the spiral membrane element 1 shown in FIG. 1 has been described, but the structure of the spiral membrane element is not limited to this. . In the processing system according to the present invention, the following spiral type membrane element can be used.

FIG. 7 is a front view showing another example of the spiral membrane element used in the processing system according to the present invention. In FIG. 7, the illustration of the outer peripheral channel material is omitted.

The spiral type membrane element 1 shown in FIG.
In, both ends of the spiral membrane element 1a are sealed with a resin layer 40. In the spiral membrane element 1 shown in FIG. 7B, one end of the spiral membrane element 1 a is sealed with a resin layer 40.

In the spiral-type membrane element 1 shown in FIGS. 7A and 7B, the number of working steps at the time of manufacturing is increased, but a space for supplying raw water to both ends or one end of the spiral-type membrane element 1 is unnecessary. Become. Therefore, the pressure vessel can be miniaturized, and the spiral membrane module in which the spiral membrane element 1 is housed in the pressure vessel can be miniaturized.

Further, by disposing the end of the spiral membrane element 1 sealed with the resin layer 40 on the raw water inlet side of the pressure vessel, the end face of the spiral membrane element 1 is moved by the dynamic pressure of the raw water when the raw water is introduced. Dirt can be prevented from adhering.

FIG. 8 is a partially cutaway perspective view showing still another example of the spiral membrane element used in the processing system according to the present invention. 9 is a cross-sectional view showing an example of the envelope-shaped membrane of the spiral membrane element shown in FIG. 8, and FIG. 10 is a cross-sectional view showing another example of the envelope-shaped membrane of the spiral membrane element shown in FIG. is there. FIG. 11 is a partially cutaway front view of the spiral membrane element of FIG.

Spiral type 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. . Raw water spacers (raw liquid flow path material) between the envelope films 3 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.
4 has been inserted.

As shown in FIGS. 9 and 10, the envelope-shaped membrane 3 is formed by superposing two separation membranes 7 on both sides of a permeated water spacer (permeated liquid channel material) 6 and bonding three sides thereof. The opening of the envelope-shaped membrane 3 is formed and attached to the outer peripheral surface of the water collecting pipe 2. 10 kgf /
A low pressure reverse osmosis membrane, an ultrafiltration membrane, a microfiltration membrane, or the like, operated at a density of less than ² cm ² is used.

In the example of FIG. 9, a plurality of envelope-shaped membranes 3 are formed by independent separation membranes 7, respectively. In the example of FIG. 10, a plurality of envelope-shaped membranes 3 are formed by folding a continuous separation membrane 7.

The outer peripheral surface of the spiral membrane element 1a is covered with a net 8 which is a liquid permeable material. As a material of the net 8, a synthetic resin such as polyolefin, polysulfone, polypropylene, polyester, polyethylene, polystyrene, polyacrylonitrile, or polyamide, or a metal such as stainless steel or iron can be used.

It is preferable that the net 8 has a size of 3 mesh or more and 200 mesh or less. Thereby, the swelling of the spiral membrane element 1a due to the back pressure at the time of backwashing can be reliably suppressed, and the raw water can be sufficiently supplied into the spiral membrane element 1a from the outer peripheral side during operation.

In the spiral type separation membrane element 1 shown in FIG. 8, the net 8 is made of tricot cloth impregnated with epoxy resin. The net 8 is 50 mesh, the pitch of the warp and the weft is 0.5 mm, and the diameter of the warp and the weft is 0.15 mm.

The end face of the spiral membrane element 1a may be covered with the net 8 in addition to the outer peripheral face of the spiral membrane element 1a.

As shown in FIG. 11, three portions of the net 8 covering the outer peripheral surface of the spiral membrane element 1a are coated with resin 81 along the circumferential direction at equal intervals, whereby the net 8 is formed. It is fixed to the outer peripheral surface of 1a at three places. The number of locations where the resin 81 is applied is not particularly limited because it depends on the back pressure generated during backwashing. However, if the number of locations where the resin 81 is applied is greater than 3 places, contamination of the outer peripheral portion of the spiral membrane element 1a during backflow cleaning will occur. Substances are less likely to be removed. Therefore, for example, in a spiral membrane element 1a having a length of 944 cm, it is preferable to fix about three places with the resin 5a.

The outer peripheral surface of the net 8 is covered with the outer peripheral channel material 5. The material and dimensions of the outer peripheral channel member 5 are the same as those of the outer peripheral channel member 5 shown in FIG.

The entire outer peripheral net 8 may be covered with the outer peripheral flow path member 5, or a part of the area may be covered with the outer peripheral flow path member 5.

The spiral type membrane module provided with the spiral type membrane element 1 shown in FIG. 8 is the same as the spiral type membrane module 100 provided with the spiral type membrane element 1 shown in FIG. It is driven by the driving method.

In this case, since the outer peripheral surface of the spiral membrane element 1a is covered with the net 8, contaminants such as turbid substances larger than the pore diameter of the net 8 are removed during the filtration operation. 1 is captured at least at the outer periphery. That is, only contaminants smaller than the pore diameter of the net 8 enter between the envelope-shaped membranes 3. Therefore, the load on the separation membrane 7 constituting the envelope-shaped membrane 3 is reduced.

After performing the above-mentioned filtration operation for a certain period of time, FIG.
Backwashing is performed by the same method as the method for washing a spiral-type membrane module shown in (1). FIG. 12 shows the operation at the time of backwashing in this case. The permeated water 52b at the time of backwashing penetrates the envelope-shaped membrane 3 from the water collection pipe 2, peels off the contaminants on the membrane surface from the membrane surface, and flows along the raw water spacer 4 at least toward the outer peripheral portion. In addition, the contaminants trapped on at least the outer peripheral portion of the spiral-wound membrane element 1 are easily separated by the permeated water 52b. After performing the backwash in this way, flushing with the raw water 51b is performed. Due to the flushing, the contaminants separated from the raw water outlet 15
From FIG. 4, the contaminants are discharged to the outside via the pipe 17 and the contaminants remaining on the outer peripheral portion of the spiral membrane element 1 are separated from the spiral membrane element 1. As a result, the membrane flux is remarkably recovered compared to before the backwashing.

According to the above-described cleaning method, the contaminants adhering to the outer peripheral portion of the spiral membrane element 1, particularly the net 8, can be easily and reliably discharged to the outside along the outer peripheral flow path member 5. Therefore, it is possible to suppress an increase in the resistance of the net 8. Thereby, a stable amount of permeated water can always be maintained. Further, since the outer peripheral portion of the spiral membrane element 1 is covered with the outer peripheral channel material 5, handling (handling) performance is improved.

In the spiral membrane element 1 shown in FIG. 8, since the outer peripheral surface of the spiral membrane element 1a is covered with the net 8, the spiral membrane element 1a
Even if the back pressure generated during backwashing by the contaminants trapped in the outer peripheral portion of the outer peripheral portion increases, the spiral-shaped membrane element 1a is prevented from bulging by the outer peripheral net 8, and the interval between the envelope-shaped membranes 3 does not increase. Therefore, damage to the membrane due to the bulging of the envelope membrane 3 is prevented, and contaminants in the raw water 51 do not leak into the permeated water 52a.

In particular, since the net 8 is fixed to the outer peripheral portion of the spiral membrane element 1a at a plurality of locations, the spiral membrane element 1a is reliably prevented from bulging even when the back pressure during backwashing is high. .

In the spiral type membrane module provided with the spiral type membrane element 1 shown in FIG. 8, as described above with reference to FIG. 4, even if the supplied raw water 51 contains a chemical having an action of stripping or sterilizing contaminants. Good.
Further, the permeated water 52b containing a chemical having a stripping action or a bactericidal action of the contaminant may be used as the washing water in the backwash. Further, at the time of cleaning, the permeated water 52b may be supplied as cleaning water from the permeated water side or the raw water side into the pressure vessel 10 (FIG. 4) and sealed, and the spiral membrane element 1 may be immersed (permeated water immersion). . Alternatively, the permeated water 52b into which a chemical having a stripping or sterilizing action of contaminants is injected from the permeated water side or the raw water side is supplied as washing water into the pressure vessel 10 (FIG. 4) and sealed therein, and the spiral membrane element is provided. 1 may be immersed (chemical solution immersion). further,
Pure water, purified water, ion-exchanged water, tap water, or the like may be used in place of the permeated water 52b in backwashing, immersion in a chemical solution, or immersion in permeated water. In this case, the same effect as the effect described above with reference to FIG. 4 can be obtained.

In the spiral membrane module provided with the spiral membrane element 1 described above, no dead space is formed in the space between the spiral membrane element 1 and the pressure vessel. No problems such as generation of offensive odor and decomposition of the separation membrane due to the decomposition of the polymer can be obtained, and high reliability can be obtained.

Further, since pressure is applied to the spiral membrane element 1 from all directions, the spiral membrane element 1
No deformation problem occurs, and the packing holder and the exterior material become unnecessary. Thereby, component costs and manufacturing costs are reduced.

Since the whole amount is filtered, the raw water 51
It is not necessary to use a large pump for supplying oil. Thereby, the system cost is reduced.

Further, the spiral membrane module used in the treatment system according to the present invention may include a spiral membrane element 1 using a part of the permeated water spacer 6 as a net as shown in FIG. In such a spiral membrane element 1, the permeated water spacer 6 inserted into one envelope-shaped membrane 3 is extended so as to protrude to the outside from the outer peripheral side of the envelope-shaped membrane 3. The extended portion of the spacer 6 is wound as a net 8 on the outer peripheral surface of the spiral membrane element 1a. The space between the permeate spacer 6 projecting from the outer peripheral side of the envelope-shaped membrane 3 to the outside and the envelope-shaped membrane 3 is sealed with a resin 6a. In this case, the swelling of the spiral membrane element 1a due to the back pressure at the time of backwashing can be prevented by the extended permeated water spacer 6 while suppressing the additional component cost due to the separate provision of the net 8.

The spiral membrane element 1 shown in FIGS. 1, 7, 8 and 13 is a spiral membrane element 1a.
Has a so-called double structure in which the outer peripheral surface is covered with a separation membrane 9, a net 8, or a permeated water spacer 6, and the outer peripheral surface side is covered with an outer peripheral passage material 5. In the above, a spiral-type membrane module provided with a spiral-type membrane element having a so-called single-layer structure in which the outer peripheral surface of the spiral-shaped membrane element 1a is directly covered with the outer peripheral channel material 5 may be used. Also in this case, contaminants are trapped at least at the outer peripheral portion of the spiral membrane element during the filtration operation. Contaminants attached to the spiral-wound membrane element are removed by the backwashing described above.

When the spiral type membrane module provided with the spiral type membrane element other than that shown in FIG. 1 is used in the processing system shown in FIG. 6, the same effects as those described above with reference to FIG. 6 can be obtained. Can be

Further, the processing system according to the present invention may use a spiral-type membrane module in which a plurality of spiral-type membrane elements are loaded in a pressure vessel.

FIG. 14 is a schematic sectional view showing another example of the spiral membrane module used in the processing system according to the present invention.

As shown in FIG. 14, the pressure vessel 510
Cylindrical case 511 and a pair of end plates 520a, 520b
It consists of. A raw water inlet 530 is formed at the bottom of the cylindrical case 511, and a raw water outlet 535 is formed at the top. The raw water outlet 535 is also used for venting air. Further, a permeated water outlet 540 is provided at the center of the end plates 520a and 520b.

A plurality of spiral membrane elements 1 in which the water collecting pipes 2 are connected in series by the interconnector 516 are housed in a cylindrical case 511, and both open ends of the cylindrical case 511 are respectively connected to end plates 520a and 520b. Sealed. In this case, the spiral type membrane element 1 shown in FIG. 1 is used. One end of the water collecting pipe 2 of the spiral type membrane element 1 at both ends is connected to the permeated water outlet 5 of the end plates 520a and 520b via an adapter 515, respectively.
40 is fitted. In this way, a spiral membrane module 500 in which the plurality of spiral membrane elements 1 are loaded in the pressure vessel 510 is configured.

The pipe 19 is connected to the raw water inlet 530 of the cylindrical case 511, and the pipe 19 is further connected to the pipe 20.
Is connected. The pipes 19 and 20 are provided with valves 18a and 18b, respectively. The pipe 17 is connected to the raw water outlet 535 of the cylindrical case 511, and the pipe 17 is provided with a valve 18c.
The pipe 2 is connected to the permeated water outlet 540 of the end plates 520a and 520b.
1 are connected to each other, and a pipe 22 is further connected to the pipe 21. The pipes 21 and 22 are provided with valves 18d and 18e, respectively.

Spiral type membrane module 5 shown in FIG.
00, the valve 18a of the pipe 19 and the valve 18d of the pipe 20 are opened, and the other pipes 20,
The valves 18b, 18e and 18c of the valves 22 and 17 are closed.
The raw water 51 is introduced into the pressure vessel 510 from the raw water inlet 530 of the pressure vessel 510 through the pipe 19. The raw water 51 flows along the outer peripheral channel material 5 of each spiral membrane element 1.

In each spiral type membrane element 1,
The raw water 51 permeates the separation membrane 9 at least from the outer peripheral side,
It penetrates between the envelope membranes 3 along the raw water spacers 4. The permeated water that has passed through the separation membrane 7 flows into the water collecting pipe 2 along the permeated water spacer 6, and the permeated water 52 a is taken out from the permeated water outlets 540 at both ends of the pressure vessel 510. In this way, total filtration is performed. In this case, as in the case of the spiral-type membrane module 100 shown in FIG.
You may take out some raw water from. Thereby, the same effect as the above-described effect can be obtained.

After performing the above-mentioned filtration operation for a certain period of time, as in the case of the spiral-wound membrane module 100, backflow washing with the permeated water 52b is performed from the permeation side. During backwashing,
The valve 18a of the pipe 19, the valve 18d of the pipe 21, and the valve 18c of the pipe 17 are closed, and the valve 1 of the pipe 22 is closed.
8e and the valve 18b of the pipe 20 are opened. Permeated water 52
b is introduced into the water collecting pipe 2 from the permeated water outlet 540 of the spiral membrane module through the pipe 21. In addition,
In the spiral membrane module 500, the end plate 52
0a and 520b from both the permeate outlets 540
2b is introduced.

In each spiral type membrane element 1,
The permeated water 52b permeates the envelope-shaped membrane 3 from the water collecting pipe 2 to separate contaminants on the membrane surface from the membrane surface, and flows along the raw water spacer 4 at least toward the outer periphery. Further, the contaminants trapped on at least the outer peripheral portion of each spiral membrane element 1 are easily separated by the permeated water 52b. Thereafter, the valve 18d of the pipe 21 and the valve 18b of the pipe 20 are closed, the valve 18a of the pipe 19 and the valve 18c of the pipe 17 are opened, and the raw water 51b is supplied to perform flushing. Thereby, the same effect as the flushing effect described above with reference to FIG. 5 can be obtained. Note that, in this case, as described above with reference to FIG. 5, flushing may be performed before backflow cleaning.
Alternatively, flushing may be performed in parallel with backwashing.

In the spiral type membrane module 500, the spiral type membrane module 10 shown in FIG.
As in the case of 0, the supplied raw water 51 or the permeated water 52b used as washing water at the time of backwashing may contain a chemical having an action of stripping or sterilizing contaminants. At the time of washing, the permeated water 52 b
May be supplied into the pressure vessel 510 as cleaning water and sealed, and each spiral membrane element 1 may be immersed (immersion in permeated water). Alternatively, the permeated water 52b containing a chemical from the permeated water side or the raw water side is used as the washing water as the pressure vessel 510.
The spiral-type membrane element 1 may be supplied and sealed therein, and each spiral-type membrane element 1 may be immersed (chemical solution immersion). Further, in backwashing, immersion in a chemical solution or immersion in permeated water, the permeated water 52b
Instead, pure water, purified water, ion-exchanged water, tap water, or the like may be used. In this case, the same effect as the effect described above with reference to FIG. 4 can be obtained.

The spiral type membrane module 5 as described above
In the case of 00, as in the case of the spiral membrane module 100, at the time of the filtration operation, the raw water 51 is supplied from at least the outer peripheral side of each spiral membrane element 1, and the total amount of filtration is performed in each spiral membrane element 1. In this case, in each spiral membrane element 1, contaminants are captured at least at the outer peripheral portion. Therefore, the load on the separation membrane 7 constituting the envelope-shaped membrane 3 is reduced.

Further, at the time of washing, the contaminants adhering to the separation membrane 7 and the outer peripheral portion of each spiral type membrane element 1 can be easily discharged to the outside along the outer peripheral flow path member 5, so that stable permeation can be achieved. Water volume can be maintained.

In addition, a plurality of spiral membrane elements 1
Loaded, the spiral type membrane module 500
Has a large processing capacity and can efficiently obtain the permeated water 52a.

[0158] Further, a dead space is not formed in the gap between each spiral-type membrane element 1 and the pressure vessel 510 by the above-mentioned filtration mode, so that germs such as microorganisms can propagate and malodor due to decomposition of organic substances can be reduced. No problems such as generation and decomposition of the separation membrane occur, and high reliability can be obtained.

Further, since pressure is applied to all the spiral membrane elements 1 from all directions, the problem of deformation of the spiral membrane elements 1 does not occur, and the packing holder and the exterior material are not required. Thereby, component costs and manufacturing costs are reduced.

[0160] Since the whole amount is filtered, the raw water 51
It is not necessary to use a large pump for supplying oil. Thereby, the system cost is reduced.

The configuration of the treatment system using the above spiral membrane module 500 is shown in FIG. 6 except that the pipe 21 for extracting the permeated water 52a is also provided at the permeated water outlet 540 on the raw water inlet side. The configuration is the same as that of the processing system. That is, a plurality of units including the spiral membrane module 500 shown in FIG. 14 are connected in parallel to form a processing system. In such a processing system, as in the processing system of FIG. 6, when at least one unit is washed, the remaining units are filtered. Thereby, the filtration operation can be continuously performed, and the module 500 having the spiral-type membrane element 1 whose membrane function has been recovered by washing can be always used for the filtration operation. Therefore, an extremely practical and useful system is realized.

[Brief description of the drawings]

FIG. 1 is a partially cutaway perspective view showing an example of a spiral membrane element used in a processing system according to 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 cross-sectional view showing an example of a method of operating a spiral membrane module provided with the spiral membrane element of FIG.

FIG. 5 is a partially cutaway perspective view showing a backwashing operation in the spiral membrane element of FIG. 1;

FIG. 6 is a schematic configuration diagram showing a processing system according to an embodiment of the present invention.

FIG. 7 is a front view showing another example of the spiral membrane element used in the processing system according to the present invention.

FIG. 8 is a partially cutaway perspective view showing still another example of the spiral membrane element used in the processing system according to the present invention.

FIG. 9 is a cross-sectional view showing an example of an envelope-shaped membrane of the spiral membrane element of FIG.

FIG. 10 is a cross-sectional view showing another example of the envelope-shaped membrane of the spiral membrane element of FIG.

FIG. 11 is a partially cutaway front view of the spiral membrane element of FIG. 8;

FIG. 12 is a partially cutaway perspective view showing a backwash operation in the spiral membrane element of FIG. 8;

FIG. 13 is a cross-sectional view showing an example in which a permeated water spacer is used as a net.

FIG. 14 is a schematic cross-sectional view showing another example of the spiral membrane module used in the processing system according to the present invention.

FIG. 15 is a partially cutaway perspective view of a conventional spiral-type membrane element.

FIG. 16 is an external perspective view of a conventional spiral-type membrane element.

FIG. 17 is a cross-sectional view illustrating an example of a conventional method of operating a spiral-type membrane element.

FIG. 18 is a partially cutaway perspective view showing a backflow cleaning operation in a conventional spiral 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 8 Net 9 Separation membrane 10, 100 Pressure vessel 13, 130 Raw water inlet 14, 140 Permeated water outlet 51 Raw water 52 Permeated water 61, 62 Wire rod 81 Resin

Continued on the front page F term (reference) 4D006 GA05 GA06 GA07 HA61 HA62 HA65 HA95 JA39Z JA55Z JA63Z KA16 KA52 KA61 KA67 KC02 KC03 KC12 KC13 KC16 KD01 KD06 KD15 KD16 KD24 KE02P KE03P KE06Q KE24Q

Claims (15)

[Claims] 1. A method for operating a processing system comprising a plurality of spiral membrane modules connected in parallel, wherein each spiral membrane module is provided in a pressure vessel having one or more spiral membrane elements having a stock solution inlet. The spiral membrane element includes a spiral membrane element in which a plurality of independent or continuous envelope membranes are wound around the outer peripheral surface of a perforated hollow tube via a stock solution flow path material. During the filtration operation, a raw liquid is supplied from at least the outer peripheral side of the spiral membrane element through the raw liquid inlet of the pressure vessel of each spiral membrane module, and the raw liquid is supplied from at least one open end of the perforated hollow tube. Take out the permeated liquid to the outside of the pressure vessel, when washing any of the spiral-type membrane modules of the plurality of spiral-type membrane modules The method of operating a processing system, characterized by the filtration operation at least one spiral wound membrane module. 2. In the cleaning, a cleaning liquid is introduced from at least one opening end of the perforated hollow tube of the spiral membrane module, and the cleaning liquid derived from the outer peripheral surface of the perforated hollow tube is supplied to the spiral membrane module by the spiral. The method according to claim 1, further comprising discharging the mold element from at least an outer peripheral side of the mold element. 3. The method according to claim 1, wherein the cleaning includes maintaining the pressure vessel of the spiral membrane module filled with a cleaning liquid for a predetermined time. 4. The method according to claim 3, wherein the cleaning liquid is a permeate or water equivalent to the permeate. 5. The cleaning liquid according to claim 3, wherein the cleaning liquid contains a chemical having a stripping action or a bactericidal action of contaminants.
Or the operation method of the processing system according to 4. 6. The method according to claim 3, wherein the cleaning solution is introduced into the pressure vessel through the stock solution inlet. 7. The method according to claim 3, wherein the cleaning liquid is introduced into the pressure vessel from at least one open end of the perforated hollow tube. 8. A raw liquid supply pipe and a cleaning liquid discharge pipe are connected to the raw liquid inlet of each spiral type membrane module, and a permeate extraction pipe and a cleaning liquid supply pipe are connected to at least one open end of the perforated hollow pipe. Then, a first valve is inserted into the stock solution supply pipe, a second valve is inserted into the cleaning liquid discharge pipe, a third valve is inserted into the permeate extraction pipe, and a fourth valve is inserted into the cleaning liquid supply pipe. 8. The filter operation and the washing of each spiral type membrane module are switched by opening and closing the first, second, third and fourth valves through a valve. An operation method of the processing system according to any one of the above. 9. A processing system in which a plurality of spiral membrane modules are connected in parallel, wherein each spiral membrane module is housed in a pressure vessel having one or more spiral membrane elements having a stock solution inlet. The spiral membrane element includes a spiral membrane element in which a plurality of independent or continuous envelope membranes are wound around the outer peripheral surface of a perforated hollow tube via a stock solution flow path material, and a filtration operation is performed. At the time, a stock solution is supplied from at least the outer peripheral portion side of the spiral membrane element through the stock solution inlet of the pressure vessel of each spiral membrane module, and the pressure vessel is opened from at least one open end of the perforated hollow tube. The permeated liquid is taken out to the outside, and when washing any one of the plurality of spiral membrane modules, a small amount of the other is removed. A processing system comprising a flow path switching means capable of switching a flow path so that at least one spiral type membrane module performs a filtration operation. 10. The flow passage switching means includes a stock solution supply pipe and a washing solution discharge pipe connected to the stock solution inlet of each spiral membrane module, and a permeation connected to at least one open end of the perforated hollow pipe. A liquid extraction pipe and a cleaning liquid supply pipe, a first valve inserted into the raw liquid supply pipe, a second valve inserted into the cleaning liquid discharge pipe, a third valve inserted into the permeate extraction pipe, and the cleaning liquid The processing system according to claim 9, further comprising a fourth valve interposed in the supply pipe. 11. Each of the first to fourth valves is an automatic valve, and control means for controlling the opening and closing operation of each of the first to fourth automatic valves is provided. Item 11. The processing system according to Item 10. 12. The processing system according to claim 11, wherein said control means controls opening and closing operations of each of said first to fourth automatic valves based on a time setting. 13. The control means controls the opening and closing operation of each of the first to fourth automatic valves according to the supply pressure or supply flow rate of the stock solution during the filtration operation of the spiral membrane module. Claim 11
The processing system as described. 14. The opening / closing operation of each of the first to fourth automatic valves according to the pressure in the permeate extraction pipe or the flow rate of the permeate during the filtration operation of the spiral membrane module. The processing system according to claim 11, wherein 15. The opening / closing operation of each of the first to fourth automatic valves according to a pressure difference between a stock solution supply side and a permeate removal side during the filtration operation of the spiral membrane module. The processing system according to claim 11, wherein