JP2001239136A - Treating system and operating method therefor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide treating systems which can obtain treated water of stable quality and the operating method therefor. SOLUTION: The treating systems 500-508 are provided with various devices 200-208 as pretreating devices and spiral membrane modules 100 at the latter stages of the preheating devices 100. The modules 100 are provided with spiral membrane elements capable of washing by backward flow under a backward pressure of 0.05-0.3 MPa. When the treating systems 500-508 are operated, plural kinds of raw water are pretreated by the respective devices 200-208, and the plural kinds of pretreated water obtained from the respective devices 200-208 are fed to the spiral membrane modules 100 through feed systems 300 and further separated by the membranes.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

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

[0002]

2. Description of the Related Art Conventionally, when performing pretreatment in seawater desalination, etc., purification of process liquid, production of various types of water, collection of wastewater and reuse treatment, etc., filtration using sand, anthracite, etc. Adsorption treatment using activated carbon, zeolite, etc., biological treatment using activated sludge or biofilm filtration, etc.
Alternatively, separation processes such as centrifugation, ion exchange, pressure flotation, coagulation separation, sedimentation separation, and the like are performed. By such treatment, contaminants, impurities and the like in the water to be treated are removed. Further, sterilization treatment of the water to be treated by ozone oxidation treatment, strong acid water treatment, ultraviolet treatment, sodium hypochlorite treatment and the like is also performed. These various processes are performed alone or in combination. The treated water obtained by the above treatment is used for various uses, or supplied to a subsequent system for further treatment.

[0003]

In the above-mentioned separation treatments such as the filtration treatment, the adsorption treatment, the biological treatment, and the centrifugal separation, the quality of the obtained treated water varies depending on the quality of the supplied treated water. For this reason, it is difficult to obtain treated water of stable water quality.

On the other hand, the above-mentioned filtration treatment, adsorption treatment,
2. Description of the Related Art In a processing apparatus that performs biological treatment and separation processing such as centrifugation, it is necessary to periodically perform cleaning in order to maintain the processing capacity of the apparatus. When washing such a processing apparatus, backwashing or normal washing is performed using a large amount of washing water.
A large amount of washing water used during washing is discharged out of the system as wastewater each time washing is performed.

Further, since the properties of the treated water obtained from the treatment apparatus are not stable immediately after washing, the treated water may not be collected until the properties are stabilized, and the treated water during this time must be discharged to the outside of the system. is there.

As described above, the above-mentioned filtration treatment, adsorption treatment,
In a processing apparatus that performs a biological treatment and a separation treatment such as a centrifugal separation, a large amount of wastewater is generated by washing. Therefore, effective use of the washed wastewater is desired.

An object of the present invention is to provide a treatment system capable of obtaining treated water of stable water quality and a method of operating the treatment system.

[0008] Another object of the present invention is to provide a processing system and a method of operating the same that can effectively use the cleaning wastewater discharged by cleaning the processing apparatus.

[0009]

Means for Solving the Problems and Effects of the Invention A processing system according to a first aspect of the present invention includes one or a plurality of pre-processing apparatuses for performing a predetermined pre-processing, and a pre-processing apparatus having a pressure higher than 0.05 MPa.
A spiral-type membrane module in which one or more spiral-type membrane elements capable of backwashing with a back pressure of 3 MPa or less are housed in a pressure vessel having a stock solution inlet, And a supply system for guiding the solution into the pressure vessel through the undiluted solution inlet.

[0010] In the processing system according to the present invention, the pretreatment liquid treated by the pretreatment device is introduced into the pressure vessel of the spiral membrane module via the supply system and supplied to the spiral membrane element. In the spiral membrane element, the pretreatment liquid is further subjected to membrane separation. Therefore, in the processing system according to the present invention, it is possible to obtain a processing liquid having good liquid quality.

Since the above-mentioned processing system has a spiral type membrane module, it is possible to obtain a processing liquid having a stable quality even when the properties of the liquid supplied to the processing system change.

Further, since the spiral membrane element of the spiral membrane module can be backwashed with a high back pressure of 0.05 to 0.3 MPa, a required amount of washing liquid can be flowed in a short time. Thereby, the contaminants deposited on the separation membrane of the spiral membrane element can be effectively removed.

As described above, in the above-mentioned processing system, it is possible to obtain a processing liquid having a stable liquid quality in a stable operation while maintaining a high permeation flux.

The pretreatment devices include a filtration treatment device, an adsorption treatment device, a biological treatment device, an ion exchange device, a centrifugal separation device, a membrane separation device, a pressure flotation treatment device, a coagulation separation treatment device, a sedimentation separation treatment device, and ozone oxidation. The apparatus may include at least one of an apparatus, a strongly acidic water treatment apparatus, an ultraviolet sterilization apparatus, and a sodium hypochlorite sterilization apparatus. In this case, a pretreatment liquid from which contaminants have been removed or sterilized by the pretreatment device is supplied to the spiral-wound membrane module.

[0015] A processing system according to a second aspect of the present invention comprises:
A spiral-type membrane module in which one or a plurality of spiral-type elements capable of backwashing at a back pressure of 0.3 MPa or less and higher than 0.3 MPa are housed in a pressure vessel having an undiluted solution inlet; And a supply system for guiding the discharged cleaning liquid through the stock solution inlet of the spiral type membrane module to the inside of the pressure vessel.

In the processing system according to the present invention, the cleaning liquid discharged from the processing apparatus at the time of cleaning the processing apparatus is introduced into the pressure vessel of the spiral type membrane module via the supply system. This washing waste liquid is supplied to the spiral type membrane element and is subjected to membrane separation to remove contaminants. Therefore, in the processing system according to the present invention, it is possible to collect the cleaning waste liquid of the processing apparatus as a reusable liquid, and it is possible to reduce the amount of drain liquid.

The spiral-type membrane module of the above-mentioned processing system has a spiral-type membrane element of 0.05 to 0.1.
Backwashing is possible with a high back pressure of 3 MPa.
For this reason, a required amount of cleaning liquid can be flowed in a short time,
Contaminants deposited on the separation membrane of the spiral membrane element can be effectively removed. Therefore, in the spiral-wound membrane module, it is possible to stably treat the cleaning wastewater containing a large amount of contaminants separated from the processing apparatus while maintaining a high permeation flux.

The pretreatment device may include at least one of a filtration device, an adsorption device, a biological treatment device, a membrane separation device, and a centrifugal separation device. The processing liquid obtained from such a processing apparatus is used for various purposes, or is further supplied to a subsequent system for processing.

According to a third aspect of the present invention, there is provided an operating method of a processing system, wherein one or a plurality of pre-processing devices for performing a predetermined pre-processing are provided and 0.3 MPa higher than 0.05 MPa.
A spiral-type membrane module in which one or more spiral-type membrane elements capable of backwashing with the following back pressure are accommodated in a pressure vessel having a stock solution inlet is provided. It is supplied to the inside of the pressure vessel through the undiluted solution inlet.

In the method of operating the treatment system according to the present invention, the pretreatment liquid treated by the pretreatment device is further subjected to membrane separation in the spiral membrane module. Therefore, it is possible to obtain a processing liquid having good liquid quality.

In this case, since the spiral membrane module is provided in the processing system, a stable processing liquid can be obtained even when the properties of the liquid supplied to the processing system change.

Further, since the spiral type membrane element of the spiral type membrane module can be backwashed with a high back pressure of 0.05 to 0.3 MPa, a required amount of washing liquid can be flowed in a short time. Thereby, the contaminants deposited on the separation membrane of the spiral membrane element can be effectively removed.

As described above, according to the above-described method of operating the processing system, it is possible to obtain a processing liquid having good liquid quality in a stable operation while maintaining a high permeation flux.

The pretreatment devices include a filtration treatment device, an adsorption treatment device, a biological treatment device, an ion exchange device, a centrifugal separation device, a membrane separation device, a pressure flotation treatment device, a coagulation separation treatment device, a sedimentation separation treatment device, an ozone oxidation. The apparatus may include at least one of an apparatus, a strongly acidic water treatment apparatus, an ultraviolet sterilization apparatus, and a sodium hypochlorite sterilization apparatus. In this case, a pretreatment liquid from which contaminants have been removed or sterilized by the pretreatment device is supplied to the spiral-wound membrane module.

According to a fourth aspect of the present invention, there is provided an operating method of a processing system, wherein one or a plurality of processing apparatuses for performing a predetermined processing are provided, and backflow cleaning can be performed with a back pressure higher than 0.05 MPa and 0.3 MPa or less. A spiral-type membrane module in which one or more spiral-type membrane elements are housed in a pressure vessel having a stock solution inlet is provided, and a cleaning liquid discharged from the processing apparatus when the processing apparatus is washed is subjected to pressure through the stock solution inlet of the spiral-type membrane module. It is supplied inside the container.

In the operation method of the processing system according to the present invention, the cleaning liquid discharged from the processing apparatus when cleaning the processing apparatus is subjected to membrane separation in the spiral membrane module.
Therefore, it is possible to remove the contaminants in the washing wastewater by the spiral membrane module and collect them as a reusable liquid. This makes it possible to reduce the amount of drainage.

Further, the spiral membrane element of the above-mentioned processing system has a spiral membrane element of 0.05%.
Backwashing is possible with a high back pressure of 0.3 MPa. Therefore, a required amount of cleaning liquid can be flowed in a short time, and contaminants deposited on the separation membrane of the spiral membrane element can be effectively removed. Therefore,
In the spiral-wound membrane module, it is possible to stably treat the cleaning wastewater containing a large amount of contaminants separated from the processing apparatus while maintaining a high permeation flux.

[0028] The treatment apparatus may include at least one of a filtration treatment apparatus, an adsorption treatment apparatus, a biological treatment apparatus, a membrane separation apparatus, and a centrifugal separation apparatus. The processing liquid obtained from such a processing apparatus is used for various purposes, or is further supplied to a subsequent system for processing.

[0029]

1 and 2 are schematic diagrams showing a processing system according to first to thirteenth embodiments of the first invention.

As shown in FIGS. 1A to 2M, in the processing systems 500 to 512 of the first to thirteenth embodiments, spiral type membrane modules 100 are provided. During the operation of each of the treatment systems 500 to 512, the pretreatment water obtained from the pretreatment device is supplied to the spiral membrane module 100. Hereinafter, details of the processing systems 500 to 512 will be described.

As shown in FIG. 1A, a processing system 500 according to the first embodiment includes, as a pretreatment device, a filtration process other than membrane filtration, for example, a centrifugal filtration using a filter cloth or a sand filtration. An apparatus 200 is provided. Processing system 500
In, the contaminants in the raw water are removed by the filtration device 200.

As shown in FIG. 1 (b), the treatment system 501 in the second embodiment includes, as a pretreatment device, an adsorption treatment device 201 containing an adsorbent such as bone charcoal, activated carbon and zeolite. In the treatment system 501, the contaminants in the raw water are adsorbed and removed by the adsorbent in the adsorption treatment device 201.

As shown in FIG. 1C, the treatment system 502 in the third embodiment has a biological treatment device 202 such as an activated sludge tank as a pretreatment device. In the treatment system 502, contaminants in raw water are decomposed and removed by microorganisms in the biological treatment device 202.

As shown in FIG. 1D, the processing system 503 according to the fourth embodiment includes a centrifugal separator 203 as a pretreatment device. In the processing system 503, the contaminants in the raw water are settled by the centrifugal separator 203, and the settled contaminants are removed.

As shown in FIG. 1E, the processing system 504 according to the fifth embodiment includes a membrane separation device 204 as a pretreatment device. In the processing system 504,
The contaminants in the raw water are removed by the membrane separation device 204.

As shown in FIG. 1 (f), the processing system 505 in the sixth embodiment includes a pressure flotation processing device 205 as a preprocessing device. In the processing system 505,
Air bubbling of raw water is performed by using compressed air in the pressurized flotation apparatus 205 to float contaminants in the raw water and remove the contaminated substances that have floated.

As shown in FIG. 1 (g), the processing system 506 in the seventh embodiment includes a coagulation / separation processing device 206 as a pre-processing device. In the treatment system 506, the contaminants in the raw water are aggregated by the aggregation and separation processing device 206, and the settled contaminants are removed.

As shown in FIG. 1 (h), the processing system 507 in the eighth embodiment includes a settling / separation processing device 207 as a pretreatment device. In the treatment system 507, the contaminants in the raw water are settled by the sedimentation separation treatment device 207 to remove the contaminants.

As shown in FIG. 1 (i), the processing system 508 in the ninth embodiment includes an ion exchange device 208 containing an ion exchange resin as a pretreatment device. In the treatment system 508, the raw water is ion-exchanged by the ion exchange device 208, and the electric conductivity of the raw water increases to the pure water level. Note that the ion exchange device 208 cannot remove fine particles such as contaminants in raw water.

As shown in FIG. 2 (j), the processing system 509 in the tenth embodiment includes an ozone oxidizing device 209 as a pre-processing device. In the treatment system 509, the raw water is sterilized by the ozone oxidizing device 209, and propagation of various bacteria in the raw water is suppressed.

As shown in FIG. 2 (k), the treatment system 510 in the eleventh embodiment has a strong acid water treatment device 210 containing strongly acidic ionic water as a pretreatment device.
In the treatment system 510, the strong acid water treatment device 21
0 sterilizes the raw water and suppresses the growth of various bacteria in the raw water. It should be noted that the strongly acidic ionic water is acidic water having a pH of about 2.5 obtained by electrolyzing several percent of a saline solution.

As shown in FIG. 2 (l), the processing system 511 in the twelfth embodiment includes an ultraviolet (UV) sterilization processing device 211 as a preprocessing device. In the processing system 511, an ultraviolet (UV) sterilization processing device 211
Sterilizes the raw water and suppresses the growth of various bacteria in the raw water.

As shown in FIG. 2 (m), the processing system 512 in the thirteenth embodiment includes a sodium hypochlorite sterilizing apparatus 212 as a pre-processing apparatus. In the treatment system 512, the sodium hypochlorite sterilization treatment device 2
12 sterilizes the raw water and suppresses the propagation of various bacteria in the raw water. The preferred free chlorine concentration is 0.1 ppm
１０００1000 ppm.

In the above treatment systems 500 to 512, the pretreated water treated by each of the devices 200 to 212 is supplied to the subsequent spiral membrane module 100 through the supply system 300.

FIG. 4 is a partially cutaway perspective view showing an example of a spiral membrane element used in the spiral membrane module of FIG.

In the spiral membrane element 1 shown in FIG. 4, an envelope membrane (bag-like membrane) 4 is formed by superimposing separation membranes 2 on both sides of a permeated water spacer 3 made of a synthetic resin net and bonding three sides. It is formed by attaching the opening of the envelope-shaped membrane 4 to the water collecting pipe 5 and spirally winding the outer peripheral surface of the water collecting pipe 5 together with the raw water spacer 6 made of a synthetic resin net. The separation membrane 2 may be an ultrafiltration membrane or a microfiltration membrane. The outer peripheral surface of the spiral-type membrane element 1 is covered with an exterior material.

As shown in FIGS. 5 to 9, the spiral membrane module 100 has a spiral membrane element 1 housed in a pressure vessel 10. The details of the structure and operation method of the spiral membrane module 100 will be described later.

In the spiral-type membrane element 1 shown in FIG. 4, backflow cleaning can be performed at a back pressure of 0.05 to 0.3 MPa by using a separation membrane 2 having a structure described later.

At the time of filtration, raw water 7 is supplied from one end face of the spiral membrane element 1. In this example, the pretreated water obtained from each of the devices 200 to 212 corresponds to the raw water 7. The raw water 7 flows linearly in a direction parallel to the water collecting pipe 5 along the raw water spacer 6, and is discharged as concentrated water 9 from the other end surface side of the spiral membrane element 1.

While the raw water 7 flows along the raw water spacer 6, a part of the raw water 7 permeates the separation membrane 2 due to the pressure difference between the raw water side and the permeated water side, and the permeated water 8 flows along the permeated water spacer 3. The water flows into the water collecting pipe 5 and is taken out of the spiral membrane module 100 from the end of the water collecting pipe 5 as treated water. As shown in FIGS. 1A to 2M, the permeated water 8 (treated water) taken out of the spiral-wound membrane module 100 is used for various purposes, or is supplied to a further system. Is processed.

As described above, the processing systems 500 to 50
8, the filtration device 200 and the adsorption device 20
1. Biological treatment device 202, centrifugal separator 203, membrane separator 204, pressure flotation device 205, coagulation separator 20
6. Pretreatment water pretreated by the sedimentation separation device 207 and the ion exchange device 208 is subjected to membrane separation by the subsequent spiral type membrane module 100, and contaminants are further removed. Thereby, in the treatment systems 500 to 508, it is possible to obtain treated water having good water quality.

In the treatment system 508, fine particles in the raw water cannot be removed by the treatment using only the ion exchange device 208, but the pretreated water obtained from the ion exchange device 205 is further processed by the spiral membrane module 100. By performing the treatment, the fine particles in the raw water can be removed. Thereby, the purity of the treated water can be further increased.

Here, each of the devices 200 to 20 for performing the pre-processing
In 8, the property of the treated water obtained changes in accordance with the property of the supply water. On the other hand, in the spiral-type membrane module 100, even if the property of the supply water changes, the property of the treated water is hard to change, and it is possible to obtain the treated water having a stable property. Therefore, the processing system 5
In 00 to 508, the treated water of each of the devices 200 to 208 is further treated by the spiral membrane module 100, so that treated water of a more stable water quality can be obtained as compared to the case where the treatment is performed only by each of the devices 200 to 208. It is possible to obtain.

In the treatment systems 509 to 512, the pretreated water sterilized by the ozone oxidizer 209, the strong acid water processor 210, the UV sterilizer 211 and the sodium hypochlorite sterilizer 212 is converted into a spiral type in the latter stage. The contaminants are removed by membrane separation by the membrane module 100. Therefore, in the treatment systems 509 to 512, it is possible to obtain treated water having good water quality.

Here, as described above, in the spiral-type membrane module 100, even if the property of the supplied water changes, treated water with stable properties can be obtained. Therefore, in the treatment systems 509 to 512, it is possible to obtain treated water of stable water quality irrespective of changes in the properties of raw water.

In the treatment systems 500 to 512 described above, the pre-treated water pretreated by the devices 200 to 212 is supplied to the spiral membrane module 100, so that the load on the spiral membrane element 1 during filtration is reduced. Is done.

Further, the spiral membrane module 100
In the above, 0.05 to 0.3 M
Since the spiral-type membrane element 1 can be backwashed with a high back pressure of Pa, a necessary amount of washing water can be flowed in a short time. Thereby, the contaminants deposited on the membrane surface of the spiral membrane element 1 during the filtration can be effectively removed, and the performance can be recovered. Therefore, in the spiral membrane module 100, it is possible to stably perform filtration without causing a decrease in permeation flux over a long period of time.

From the above, the above processing system 50
In the case of 0 to 512, it is possible to perform a stable treatment with a high permeation flux while maintaining a stable quality of the treated water.

For example, each of the above processing systems 500 to 5
In the case where wastewater is collected and reused using the wastewater 12, the wastewater is supplied to each of the devices 200 to 212 and subjected to various pretreatments. The pretreated water obtained from each device is supplied to the supply system 30
0 and supplied to the spiral type membrane module 100 for membrane separation. Thus, the processing systems 500 to 5
12, the suspended solids and colloidal substances in the wastewater are reduced. In this case, even if the properties of the wastewater supplied to the treatment systems 500 to 512 change, treated water with stable water quality can be obtained. The treated water obtained from the treatment systems 500 to 512 may be used for various purposes as reused water, or may be supplied to a subsequent system for treatment.

The above processing systems 500 to 512
In the above, one pre-processing device is provided in a stage preceding the spiral membrane module 100, but a processing system having a plurality of pre-processing devices may be used. For example, a processing system may be used in which a pretreatment is performed by combining the above apparatuses 200 to 212, and the pretreatment water is further processed by the spiral membrane module 100.

FIG. 3 is a schematic diagram showing a processing system according to the first to fifth embodiments of the second invention.

As shown in FIGS. 3 (a) to 3 (e),
The processing systems 700 to 704 according to the fifth embodiment include the spiral membrane module 100 including the spiral membrane element 1 (FIG. 4), similarly to the processing systems 500 to 512 according to the first embodiment of the present invention. Processing system 700-7
04, the washing wastewater discharged at the time of washing the various devices 200 to 204 is supplied to the spiral membrane module 100.
And recover reusable treated water. Hereinafter, details of the processing systems 700 to 704 will be described.

As shown in FIG. 3A, the processing system 7
At 00, the raw water is treated by the filtration treatment device 200, and contaminants in the raw water are removed. Filtration device 2
The treated water No. 00 is used for various purposes, or is supplied as a water to be treated to a system provided at the subsequent stage of the filtration treatment device 200, for example, a reverse osmosis membrane separation device. When the treated water of the filtration treatment device 200 is supplied to a subsequent system, the filtration treatment device 200 corresponds to a pretreatment device.

In the processing system 700, after the operation of the filtration apparatus 200 has been performed for a predetermined time, the filtration apparatus 2
00 is performed. In the cleaning of the filtration device 200, backflow cleaning or normal cleaning is performed using a large amount of cleaning water.
The washing water used for washing the filtration treatment device 200 is taken out of the filtration treatment device 200 and then supplied to the supply system 31.
0 to the spiral-type membrane module 100.

As shown in FIG. 3B, the processing system 7
In 01, raw water is treated by the adsorption treatment apparatus 201, and contaminants in the raw water are adsorbed and removed. The treated water of the adsorption treatment device 201 is used for various purposes, or is supplied as a treatment target water to a system provided at a subsequent stage of the adsorption treatment device 201, such as a reverse osmosis membrane separation device. When the treated water of the adsorption processing device 201 is supplied to a subsequent system, the adsorption processing device 201 corresponds to a pretreatment device.

In the processing system 701, after the operation of the adsorption processing apparatus 201 has been performed for a predetermined time,
01 is performed. In the cleaning of the adsorption treatment apparatus 201, backwashing or normal cleaning is performed using a large amount of washing water.
The cleaning water used for cleaning the adsorption treatment device 201 is taken out of the adsorption treatment device 201 to the outside, and then supplied to the supply system 31.
0 to the spiral-type membrane module 100.

As shown in FIG. 3C, the processing system 7
In 02, raw water is treated by the biological treatment device 202, and pollutants in the raw water are decomposed and removed. The treated water of the biological treatment apparatus 202 is used for various purposes, or supplied as a water to be treated to a system provided downstream of the biological treatment apparatus 202, for example, a reverse osmosis membrane separation apparatus. When the treated water of the biological treatment device 202 is supplied to a subsequent system, the biological treatment device 202 corresponds to a pretreatment device.

In the treatment system 702, after the biological treatment device 202 has been operated for a predetermined time, the biological treatment device 2
02 is performed. In cleaning the biological treatment device 202, backwashing or normal cleaning is performed using a large amount of washing water.
Wash water used for washing the biological treatment device 202 is taken out of the biological treatment device 202 to the outside, and then supplied to the supply system 31.
0 to the spiral-type membrane module 100.

As shown in FIG. 3D, the processing system 7
In 03, the raw water is treated by the centrifugal separator 203, and contaminants in the raw water are removed. Centrifuge 2
The treated water 03 is used for various purposes, or is supplied as a water to be treated to a system provided downstream of the centrifugal separator 203, for example, a reverse osmosis membrane separator. When the treated water of the centrifugal separator 203 is supplied to the subsequent system, the centrifugal separator 203 corresponds to a pretreatment device.

In the processing system 703, after the centrifuge 203 is operated for a predetermined time, the centrifuge 203 is washed. For washing the centrifuge 203,
Backwashing or forward washing is performed using a large amount of washing water. The washing water used for washing the centrifuge 203 is
After being taken out of the centrifugal separator 203, it is supplied to the spiral membrane module 100 via the supply system 310.

As shown in FIG. 3E, the processing system 7
In 04, the raw water is treated by the membrane separation device 204, and contaminants in the raw water are removed. Membrane separation device 204
The treated water is used for various purposes, or supplied as a water to be treated to a system provided downstream of the membrane separation device 204, for example, a reverse osmosis membrane separation device. Membrane separation device 204
When the treated water is supplied to the subsequent system, the membrane separation device 204 corresponds to a pretreatment device.

In the processing system 704, after the operation of the membrane separation device 204 has been performed for a predetermined time,
Is washed. In cleaning the membrane separation device 204, backwashing or normal cleaning is performed using a large amount of washing water. The washing water used for washing the membrane separation device 204 is supplied to the membrane separation device 2
After being extracted from the outside to the outside, it is supplied to the spiral membrane module 100 via the supply system 310.

As described above, the processing systems 700 to 70
In 4, the washing wastewater from each of the devices 200 to 204 is introduced into the pressure vessel 10 (FIGS. 5 to 9) of the spiral membrane module 100 via the supply system 310, and the spiral membrane element 1 (FIG. 4) Supplied to In the spiral type membrane element 1, the method shown in FIG.
The washing wastewater is separated into permeated water 8 and concentrated water 9. In addition,
In this example, the cleaning wastewater of each of the devices 200 to 204 corresponds to the raw water 7. The permeated water 8 of the spiral-wound membrane module 100 thus obtained is used as a treatment water for washing water, cooling water, etc., and is reused. On the other hand, concentrated water 9
Is discharged out of the system.

As described above, the processing systems 700 to 70
In No. 4, the cleaning wastewater of each of the devices 200 to 204 is treated by the spiral membrane module 100 to remove contaminants and recover reusable treated water (permeated water). For this reason, it is possible to effectively reuse the washing wastewater of each of the devices 200 to 204 and reduce the amount of wastewater.

In this case, the cleaning wastewater discharged from each of the devices 200 to 204 contains a large amount of contaminants removed from each of the devices 200 to 204. Therefore, when the washing wastewater is filtered using the spiral membrane module 100, contaminants are deposited on the membrane surface of the separation membrane 2 of the spiral membrane element 1 (FIG. 4) of the spiral membrane module 100. Therefore, after filtering the washing wastewater for a predetermined time using the spiral membrane module 100, the spiral membrane module 100 is washed.

Here, as described above, the back flow cleaning of the spiral type membrane element 1 can be performed at a high back pressure of 0.05 to 0.3 MPa when cleaning the spiral type membrane module 100. The required amount of washing water. Thereby, the contaminants deposited on the membrane surface of the spiral membrane element 1 during the filtration can be effectively removed, and the performance can be recovered. Therefore, in the spiral membrane module 100, filtration can be performed stably without causing a decrease in permeation flux over a long period of time.

From the above, the above processing system 70
In the case of 0 to 704, stable treatment is performed with a high permeation flux, and the washing wastewater discharged from each of the devices 200 to 204 can be effectively used.

The above processing systems 700 to 704
In the above, the case where the washing water used for the backflow washing or the normal washing at the time of washing of each of the devices 200 to 204 is treated by the spiral membrane module 100 has been described. The wastewater may be treated by the spiral membrane module 100.

For example, immediately after the cleaning of each of the devices 200 to 204, the properties of the treated water obtained from each of the devices 200 to 204 are not stable. Water may be discharged as wastewater. In such a case, the treated water discharged from each of the devices 200 to 204 may be treated by the spiral membrane module 100. Also in this case, the treated water discharged as wastewater can be effectively reused, and the amount of wastewater can be reduced.

Further, the above processing systems 700 to 70
4, one device 200 to 204 is provided, but a plurality of devices 200 to 204 are provided.
A processing system that performs a process by combining 00 to 204 may be used.

Subsequently, the processing systems 500 to 512 shown in FIGS. 1 and 2 and the processing system 700 shown in FIG.
Spiral type membrane module 100 used in
The driving method will be described.

FIG. 5 is a sectional view showing an example of an operation method of a spiral type membrane module used in the processing system shown in FIGS. 1 to 3, (a) shows an operation method at the time of filtration,
(B) shows an operation method at the time of backwashing.

As shown in FIG. 5, a pressure vessel (pressure vessel)
10 is a cylindrical case 11 and a pair of end plates 12a, 12
b. One end plate 12a has raw water inlet 1
3 and a concentrated 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 structure of the pressure vessel is not limited to the structure shown in FIG. 5, and a pressure vessel having a side entry shape in which a raw water inlet and a concentrated water outlet are provided in a cylindrical case may be used.

The spiral-type membrane element 1 with the packing 17 attached near one end of the outer peripheral surface is attached to the cylindrical case 1.
1 and both open ends of the cylindrical case 11 are sealed with end plates 12a and 12b, respectively. One open end of the water collecting pipe 5 is fitted to the permeated water outlet 14 of the end plate 12b, and an end cap 16 is attached to the other open end. The inner space of the pressure vessel 10 is filled with a first liquid chamber 18 by a packing 17.
And the second liquid chamber 19. Thus, the spiral type membrane module 100 is configured.

At the time of filtration, as shown in FIG. 5A, the raw water 7 is introduced from the raw water inlet 13 into the first liquid chamber 18 of the pressure vessel 10 via the supply systems 300 and 310 (FIGS. 1 to 3). Then, the spiral membrane element 1 is supplied from one end to the inside. In the treatment systems 500 to 512, the pretreated water obtained from each of the devices 200 to 212 corresponds to the raw water 7. In the processing systems 700 to 704, the cleaning wastewater discharged from each of the devices 200 to 204 corresponds to the raw water 7.

The concentrated water 9 is discharged from the other end of the spiral membrane element 1 to the second liquid chamber 19, and the concentrated water outlet 15
Through the pressure vessel 10. Further, the permeated water 8 is discharged from the opening end of the water collecting pipe 5 and the permeated water outlet 1
4 to the outside of the pressure vessel 10. In this process, suspended substances, colloidal substances or dissolved substances contained in the raw water 7 are deposited as pollutants on the membrane surface of the separation membrane of the spiral membrane element 1.

At the time of backwashing of the spiral membrane module 100, as shown in FIG. 5B, washing water 21 is introduced from the end of the water collecting pipe 5 through the permeated water outlet 14. As the washing water 21, for example, permeated water is used. Wash water 21
Is led out of the outer peripheral surface of the water collecting pipe 5 into the inside of the separation membrane, and permeates the separation membrane in a direction opposite to that at the time of filtration. At this time, contaminants deposited on the surface of the separation membrane are separated from the separation membrane. Since the outer peripheral surface of the spiral membrane element 1 is covered with the exterior material, the washing water 21 that has passed through the separation membrane flows in the axial direction inside the spiral membrane element 1 along the raw water spacer, and the spiral membrane element 1 Are discharged into the first liquid chamber 18 and the second liquid chamber 19 from both ends of the raw water inlet 13.
And through the concentrated water outlet 15 respectively.

Wash water 21 taken out from raw water inlet 13
Is discharged out of the system as wastewater. Alternatively, a part of the washing water 21 is discharged as wastewater to the outside of the system, and a part thereof is reused as raw water, for example, the supply systems 300 and 310.
(FIGS. 1 to 3).

The washing water 2 taken out from the concentrated water outlet 15
In the case of 1, the entire amount is discharged outside the system as wastewater. Or
A part of the washing water 21 is discharged out of the system as wastewater, and a part is reused as raw water, for example, in the supply systems 300 and 310.
(FIGS. 1 to 3).

In this case, 0.05 to 0.3 MP is applied to the separation membrane.
The pressure on the permeated water outlet 14 side, the pressure on the raw water inlet 13 side, and the pressure on the concentrated water outlet 15 side are set so as to apply the back pressure a. Thus, a required amount of the washing water 21 can be flowed in a short time, and contaminants deposited on the surface of the separation membrane can be effectively removed. Therefore, in the spiral membrane module 100, a stable filtration operation can be performed without causing a decrease in the permeation flux over a long period of time.

In the example of FIG. 5, the washing water 21 is discharged from both ends of the spiral membrane element 1 at the time of backwashing, and is taken out from the raw water inlet 13 and the concentrated water outlet 15, respectively. The pressure at the permeated water outlet 14 and the pressure at the raw water inlet 13 are set so that the water 21 is discharged from one end of the spiral membrane element 1 to the first liquid chamber 18 and taken out from the raw water inlet 13 to the outside. Is also good. In this case, the concentrate outlet 15 is closed. Alternatively, the pressure on the permeated water outlet 14 side and the concentrated water outlet 15 side such that the washing water 21 is discharged from the other end of the spiral membrane element 1 to the second liquid chamber 19 and taken out from the concentrated water outlet 15 to the outside. May be set. In this case, the raw water inlet 13 is closed.

FIG. 6 is a sectional view showing another example of the method of operating the spiral type membrane module used in the processing system shown in FIGS. FIG. 6 shows an operation method during backwashing. The operation method at the time of filtration is the same as the operation method shown in FIG.

At the time of backwashing, as shown in FIG. 6, washing water 21 is introduced from the end of the water collecting pipe 5 through the permeated water outlet 14. The washing water 21 led out from the outer peripheral surface of the water collecting pipe 5 to the inside of the separation membrane permeates the separation membrane. At this time, contaminants deposited on the surface of the separation membrane are separated from the separation membrane.

In this case, the separation membrane has a thickness of 0.05 to 0.3 MP.
The pressure on the permeated water outlet 14 side, the pressure on the raw water inlet 13 side, and the pressure on the concentrated water outlet 15 side are set so as to apply the back pressure a. Thus, a required amount of the washing water 21 can be flowed in a short time, and contaminants deposited on the surface of the separation membrane can be effectively removed.

At the same time, raw water 31 is introduced from the raw water inlet 13 into the first liquid chamber 18 of the pressure vessel 10. In the processing systems 500 to 512, each of the devices 200 to 212
The pre-treated water obtained from corresponds to the raw water 31. In the processing systems 700 to 704, each of the devices 200 to
The washing wastewater discharged from 204 corresponds to the raw water 31.
The raw water 31 is supplied from one end of the spiral membrane element 1 and flows in the spiral membrane element 1 in the axial direction toward the other end. As a result, the contaminants separated from the separation membrane are washed away from one end of the spiral membrane element 1 by the raw water 31 to the other end, and together with the washing water 21, from the other end of the spiral membrane element 1 to the second liquid chamber 19. To the pressure vessel 1 through the concentrated water outlet 15
0 is taken out.

The washing water 2 taken out from the concentrated water outlet 15
In the case of 1, the entire amount is discharged outside the system as wastewater. Or
A part of the washing water 21 is discharged out of the system as wastewater, and a part of the water is reused as raw water.
(FIGS. 1 to 3).

As described above, the raw water 7 at the time of filtration during the backwashing is used.
By flowing the raw water 31 in the same direction as the supply direction, contaminants separated from the separation membrane in the spiral membrane element 1 can be quickly discharged out of the system. Thereby,
Contaminants separated from the separation membrane are prevented from attaching to the separation membrane again. Therefore, a stable filtration operation can be performed over a long period of time without causing a decrease in the permeation flux.

FIG. 7 is a sectional view showing still another example of the operation method of the spiral membrane module used in the processing system shown in FIGS. FIG. 7 shows an operation method during backwashing. The operation method at the time of filtration is the same as the operation method shown in FIG.

At the time of backwashing, as shown in FIG. 7, washing water 21 is introduced from the end of the water collecting pipe 5 through the permeated water outlet 14. The washing water 21 led out from the outer peripheral surface of the water collecting pipe 5 to the inside of the separation membrane permeates the separation membrane. At this time, contaminants deposited on the surface of the separation membrane are separated from the separation membrane.

In this case, the separation membrane has a thickness of 0.05 to 0.3 MP.
The pressure on the permeated water outlet 14 side, the pressure on the raw water inlet 13 side, and the pressure on the concentrated water outlet 15 side are set so as to apply the back pressure a. Thus, a required amount of the washing water 21 can be flowed in a short time, and contaminants deposited on the surface of the separation membrane can be effectively removed.

At the same time, the raw water 41 is introduced from the concentrated water outlet 15 into the second liquid chamber 19 of the pressure vessel 10. In the processing systems 500 to 512, each of the devices 200 to 21
The pre-treated water obtained from 2 corresponds to the raw water 41. Also,
In the processing systems 700 to 704, each device 200
The washing wastewater discharged from to 204 corresponds to the raw water 41. Raw water 41 is supplied from the other end of the spiral membrane element 1 and flows in the spiral membrane element 1 in the axial direction toward the one end. As a result, the contaminants separated from the separation membrane are flushed from the other end of the spiral membrane element 1 to the one end by the raw water 41, and the washing water 21 is removed.
And from the one end of the spiral membrane element 1
Of the pressure vessel 10 through the raw water inlet 13.
Taken out of the

Wash water 21 taken out from raw water inlet 13
Is discharged out of the system as wastewater. Alternatively, a part of the washing water 21 is discharged as wastewater to the outside of the system, and a part thereof is reused as raw water, for example, the supply systems 300 and 310.
(FIGS. 1 to 3).

As described above, the raw water 7 at the time of filtration during backwashing is used.
By flowing the raw water 41 in the direction opposite to the supply direction, the contaminants deposited on the side of the spiral membrane element 1 near the first liquid chamber 18 can be easily removed and discharged. Thus, the contaminants separated from the separation membrane are prevented from attaching to the separation membrane again. Therefore, a stable filtration operation can be performed over a long period of time without causing a decrease in the permeation flux.

The operation method shown in FIG. 6 and the operation method shown in FIG. 7 may be performed in order. Thereby, the contaminants distributed throughout the spiral membrane element 1 can be uniformly removed and discharged.

FIG. 8 is a cross-sectional view showing still another example of the operation method of the spiral type membrane module used in the processing system of FIGS. 1 to 3, and FIG. (B) shows an operation method after backwashing. The operation method at the time of filtration is the same as the operation method shown in FIG.

At the time of backwashing the spiral membrane module 100, as shown in FIG. 8A, washing water 21 is introduced from the end of the water collecting pipe 5 through the permeated water outlet 14. Wash water 21 led out from the outer peripheral surface of the water collecting pipe 5 to the inside of the separation membrane
Permeates through the separation membrane. At this time, contaminants deposited on the surface of the separation membrane are separated from the separation membrane.

In this case, the separation membrane has a thickness of 0.05 to 0.3 MP.
The pressure on the permeated water outlet 14 side, the pressure on the raw water inlet 13 side, and the pressure on the concentrated water outlet 15 side are set so as to apply the back pressure a. Thus, a required amount of the washing water 21 can be flowed in a short time, and contaminants deposited on the surface of the separation membrane can be effectively removed. The washing water 21 is discharged from the other end of the spiral membrane element 1 to the second liquid chamber 19, and is taken out of the pressure vessel 10 through the raw water inlet 13 and the concentrated water outlet 15.

Washing water 2 taken out from the concentrated water outlet 15
In the case of 1, the entire amount is discharged outside the system as wastewater. Or
A part of the washing water 21 is discharged out of the system as wastewater, and a part is reused as raw water, for example, in the supply systems 300 and 310.
(FIGS. 1 to 3).

After the backwashing, as shown in FIG.
Raw water 51 is introduced from the raw water inlet 13 into the first liquid chamber 18 of the pressure vessel 10. In the treatment systems 500 to 512, the pretreated water obtained from each of the devices 200 to 212 corresponds to the raw water 51. Also, the processing systems 700 to 7
In 04, the cleaning wastewater discharged from each of the devices 200 to 204 corresponds to the raw water 51. The raw water 51 is supplied from one end of the spiral membrane element 1 and flows in the spiral membrane element 1 in the axial direction toward the other end. As a result, the contaminants separated from the separation membrane are removed from the raw water 5
The water is flushed from one end of the spiral-type membrane element 1 to the other end thereof, and is discharged from the other end of the spiral-type membrane element 1 to the second liquid chamber 19 together with the cleaning water remaining inside the spiral-type membrane element 1. , Concentrated water outlet 15
Through the pressure vessel 10.

Raw water 51 extracted from the concentrated water outlet 15
Is discharged out of the system as wastewater. Alternatively, a part of the raw water 51 may be discharged out of the system as wastewater, and a part may be returned to, for example, the supply systems 300 and 310 (FIGS. 1 to 3) for reuse as raw water.

As described above, the raw water 7 at the time of filtration after backwashing was used.
By flowing the raw water 51 in the same direction as the supply direction, the contaminants separated from the separation membrane in the spiral membrane element 1 can be quickly discharged out of the system. Thereby,
Contaminants separated from the separation membrane are prevented from attaching to the separation membrane again. Therefore, a stable filtration operation can be performed over a long period of time without causing a decrease in the permeation flux.

During the backwashing, the washing water 21 may be discharged from one end of the spiral membrane element 1 to the first liquid chamber 18 and taken out of the pressure vessel 10 through the raw water inlet 13, or the backwashing may be performed. Occasionally, the washing water 21 is discharged from one end and the other end of the spiral membrane element to the first liquid chamber 18 and the second liquid chamber 19, and then to the outside of the pressure vessel 10 through the raw water inlet 13 and the concentrated water outlet 15, respectively. You may take it out.

FIG. 9 is a cross-sectional view showing still another example of the operation method of the spiral membrane module used in the processing system shown in FIGS. 1 to 3, and FIG. 9A shows the operation method during backwashing. (B) shows an operation method after backwashing. The operation method at the time of filtration is the same as the operation method shown in FIG.

At the time of backwashing, as shown in FIG. 9A, washing water 21 is introduced from the end of the water collecting pipe 5 through the permeated water outlet 14. The washing water 21 led from the outer peripheral surface of the water collecting pipe 5 to the inside of the separation membrane permeates the separation membrane. At this time,
Contaminants deposited on the surface of the separation membrane are separated from the separation membrane.

In this case, the separation membrane has a thickness of 0.05 to 0.3 MP.
The pressure on the permeated water outlet 14 side, the pressure on the raw water inlet 13 side, and the pressure on the concentrated water outlet 15 side are set so as to apply the back pressure a. Thus, a required amount of the washing water 21 can be flowed in a short time, and contaminants deposited on the surface of the separation membrane can be effectively removed. The washing water 21 is discharged from the one end and the other end of the spiral membrane element 1 to the first liquid chamber 18 and the second liquid chamber 19, and goes out of the pressure vessel 10 through the raw water inlet 13 and the concentrated water outlet 15, respectively. Taken out.

The washing water 21 taken out from the raw water inlet 13
Is discharged out of the system as wastewater. Alternatively, a part of the washing water 21 is discharged as wastewater to the outside of the system, and a part thereof is reused as raw water, for example, the supply systems 300 and 310.
(FIGS. 1 to 3).

Wash water 2 taken out from the concentrated water outlet 15
In the case of 1, the entire amount is discharged outside the system as wastewater. Or
A part of the washing water 21 is discharged out of the system as wastewater, and a part is reused as raw water, for example, in the supply systems 300 and 310.
(FIGS. 1 to 3).

After the backwashing, as shown in FIG.
Raw water 61 is introduced from the concentrated water outlet 15 into the second liquid chamber 19 of the pressure vessel 10. Note that the processing systems 500 to 512
In, the pretreated water obtained from each of the devices 200 to 212 corresponds to the raw water 61. Also, the processing system 700 to
In 704, the cleaning wastewater discharged from each of the devices 200 to 204 corresponds to the raw water 61. The raw water 61 is supplied from the other end of the spiral membrane element 1 and flows in the spiral membrane element 1 in the axial direction toward the one end. As a result, the contaminants separated from the separation membrane are washed away from the other end of the spiral membrane element 1 by the raw water 61 to one end, and together with the washing water remaining inside the spiral membrane element 1, the spiral membrane element 1 is removed.
Is discharged into the second liquid chamber 19 from one end of the raw water inlet 13.
Through the pressure vessel 10.

Raw water 61 extracted from the raw water inlet 13
Is discharged out of the system as wastewater. Alternatively, a part of the raw water 61 may be discharged as wastewater to the outside of the system, and a part of the raw water 61 may be returned to, for example, the supply systems 300 and 310 (FIGS. 1 to 3) for reuse as raw water.

As described above, the raw water 7 at the time of filtration after the backwashing was used.
By flowing the raw water 61 in the direction opposite to the supply direction, the contaminants deposited on the side of the spiral membrane element 1 near the first liquid chamber 18 can be easily removed and discharged. Thus, the contaminants separated from the separation membrane are prevented from attaching to the separation membrane again. Therefore, a stable filtration operation can be performed over a long period of time without causing a decrease in the permeation flux.

The washing water 21 may be discharged from one end of the spiral membrane element 1 to the first liquid chamber 18 at the time of backwashing, and may be taken out of the pressure vessel 10 through the raw water inlet 13 or may be washed at the time of backwashing. The washing water 21 may be discharged from the other end of the spiral membrane element 1 to the second liquid chamber 19 and taken out of the pressure vessel 10 through the concentrated water outlet 15.

After the backwashing shown in FIG. 8A or 9A, the operation method shown in FIG. 8B and the operation method shown in FIG. 9B may be performed in order. Thereby, the contaminants distributed throughout the spiral membrane element 1 can be uniformly removed and discharged.

Although FIGS. 5 to 9 show the case where the spiral membrane module 100 includes one spiral membrane element 1, the spiral membrane module including a plurality of spiral membrane elements 1 is described. May be used for the processing systems 500 to 512 and 700 to 704. In a spiral membrane module in which a plurality of spiral membrane elements 1 are housed in a pressure vessel, operation is performed by a method similar to the method described with reference to FIGS.

Next, the separation membrane 2 of the spiral membrane element 1 provided in the spiral membrane module 100 will be described.

FIG. 10 is a sectional view of a separation membrane used in the spiral membrane element of FIG. The separation membrane 2 is formed by tightly integrating a permeable membrane 2b having a substantial separation function on the surface of a porous reinforcing sheet (porous sheet material) 2a.

The permeable membrane 2b may be made of one kind of polysulfone-based resin or a mixture of two or more kinds of polysulfone-based resins, or a copolymer of a polysulfone-based resin with a polymer such as polyimide or fluorine-containing polyimide resin, or Formed from a mixture.

[0127] The porous reinforcing sheet 2a is made of polyester,
It is formed of a woven fabric, a nonwoven fabric, a mesh net, a foamed sintered sheet, or the like made of polypropylene, polyethylene, polyamide, or the like, and a nonwoven fabric is preferable from the viewpoint of film forming properties and cost.

The porous reinforcing sheet 2a and the permeable membrane 2
b is an anchored state in which a part of the resin component constituting the permeable membrane 2b is filled in the inside of the hole of the porous reinforcing sheet 2a.

The back pressure strength of the separation membrane 2 lined with the porous reinforcing sheet 2a exceeds 0.2 MPa, and is 0.4 to 0.1 MPa.
It improved to about 5 MPa. The method of defining the back pressure strength will be described later.

In order to obtain a back pressure strength of 0.2 MPa or more using a nonwoven fabric as the porous reinforcing sheet 2a, the thickness of the nonwoven fabric is 0.08 to 0.15 mm and the density is 0.
It is preferably from ⁵ to 0.8 g / cm ³ . When the thickness is less than 0.08 mm or when the density is 0.5 g / cm
If it is smaller than ³ , the strength as a reinforcing sheet cannot be obtained, and it is difficult to secure the back pressure strength of the separation membrane 2 of 0.2 MPa or more. On the other hand, when the thickness is greater than 0.15 mm or the density is greater than 0.8 g / cm ³ ,
The filtration resistance of the porous reinforcing sheet 2a is increased, and the anchoring effect on the nonwoven fabric (porous reinforcing sheet 2a) is reduced, so that peeling easily occurs at the interface between the permeable membrane 2b and the nonwoven fabric.

Next, a method for manufacturing the separation membrane 2 will be described. First, a solvent, a non-solvent, and a swelling agent are added to polysulfone and dissolved by heating to prepare a uniform film forming solution.
Here, the polysulfone-based resin has the following structural formula (Formula 1)
As shown in the figure, at least one (-SO
There is no particular limitation as long as it has a _2- ) site.

[0132]

Embedded image

Here, R represents a divalent aromatic, alicyclic or aliphatic hydrocarbon group, or a divalent organic group in which these hydrocarbon groups are bonded by a divalent organic bonding group.

Preferably, polysulfones represented by the following structural formulas (Formula 2) to (Formula 4) are used.

[0135]

Embedded image

[0136]

Embedded image

[0137]

Embedded image

As the solvent for polysulfone, N-
It is preferable to use methyl-2-pyrrolidone, dimethylformamide, dimethylacetamide, dimethylsulfoxide and the like. Further, as the non-solvent, aliphatic polyhydric alcohols such as ethylene glycol, diethylene glycol, propylene glycol, polyethylene glycol, and glycerin, lower aliphatic alcohols such as methanol, ethanol, and isopropyl alcohol, and lower aliphatic ketones such as methyl ethyl ketone are used. Is preferred.

The content of the non-solvent in the mixed solvent of the solvent and the non-solvent is not particularly limited as long as the obtained mixed solvent is uniform, but is usually 5 to 50% by weight, preferably 20 to 45% by weight.

Examples of the swelling agent used to promote or control the formation of the porous structure include metal salts such as lithium chloride, sodium chloride and lithium nitrate, polyethylene glycol, polyvinyl alcohol, polyvinylpyrrolidone, polyacrylic acid and the like. Or a metal salt thereof, formamide or the like. The content of the swelling agent in the mixed solvent is not particularly limited as long as the film forming solution is uniform, but is usually 1 to 50% by weight.

The concentration of the polysulfone in the membrane forming solution is usually preferably from 10 to 30% by weight. When it exceeds 30% by weight, the water permeability of the obtained porous separation membrane becomes poor in practicality. When it is less than 10% by weight, the mechanical strength of the obtained porous separation membrane becomes poor and sufficient back pressure is obtained. Can't get strength.

Next, the above-mentioned film forming solution is formed on a nonwoven fabric support. That is, using a continuous film forming apparatus, a support sheet such as a non-woven fabric is sequentially sent out, and a film forming solution is applied to the surface thereof. As a coating method, a film forming solution is coated on a nonwoven fabric support using a gap coater such as a knife coater or a roll coater. For example, when a roll coater is used, a film-forming solution is stored between two rolls, the film-forming solution is applied on a nonwoven fabric support, and at the same time, the inside of the nonwoven fabric is sufficiently impregnated. In addition, a slight amount of water in the atmosphere is absorbed by the surface of the liquid film applied on the nonwoven fabric, and microphase separation is caused on the surface layer of the liquid film. Thereafter, the liquid film is immersed in a coagulation water bath to phase-separate and coagulate the entire liquid film, and the solvent is washed and removed in a water washing bath. Thereby, the separation film 2 is formed.

As described above, since the separation membrane 2 has a high back pressure strength, even when the back flow cleaning is performed at a back pressure of 0.05 to 0.3 MPa when the separation membrane 2 is used for the spiral membrane element 1 of FIG. The occurrence of breakage of the separation membrane 2 is prevented.

[Brief description of the drawings]

FIG. 1 is a schematic diagram showing a processing system according to first to ninth embodiments of the first invention.

FIG. 2 is a schematic diagram showing a processing system according to tenth to thirteenth embodiments of the first invention.

FIG. 3 is a schematic diagram showing a processing system according to first to fifth embodiments of the second invention.

FIG. 4 is a partially cutaway perspective view showing an example of a spiral membrane element used in the spiral membrane module of FIGS. 1 to 3;

FIG. 5 is a cross-sectional view showing an example of an operation method of a spiral membrane module used in the processing system of FIGS.

FIG. 6 is a cross-sectional view showing another example of an operation method of the spiral membrane module used in the processing systems of FIGS.

FIG. 7 is a cross-sectional view showing still another example of an operation method of the spiral membrane module used in the processing systems of FIGS.

FIG. 8 is a cross-sectional view showing still another example of a method of operating a spiral type membrane module used in the processing systems of FIGS.

FIG. 9 is a cross-sectional view showing still another example of the operation method of the spiral membrane module used in the processing systems of FIGS.

FIG. 10 is a sectional view of a separation membrane used for the spiral-wound membrane element of FIG.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Spiral type membrane element 2 Separation membrane 3 Permeated water spacer 4 Envelope membrane 5 Water collecting pipe 6 Raw water spacer 7 Raw water 8 Permeated water 9 Concentrated water 10 Pressure vessel 13 Raw water inlet 14 Permeated water outlet 15 Concentrated water outlet 21 Wash water 31, 41 , 51,61 Raw water 100 Spiral membrane module 300,310 Supply system 500-512,700-704 Treatment system

 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D006 GA06 GA07 HA61 JA03B JA03C KA02 KA03 KA63 KB04 KB11 KB12 KB13 KB14 KB20 KB21 KB30 KC03 KC13 KD09 KD12 KD19 KD21 KD24 KE06R MA03 MB16 MC58 MC62 NA05 NA10 NA13 PA01 P08 P08

Claims (8)

[Claims] A pressure vessel having one or more pretreatment devices for performing a predetermined pretreatment and a spiral type membrane element capable of backwashing with a back pressure higher than 0.05 MPa and 0.3 MPa or less having a stock solution inlet. One or more spiral-type membrane modules housed therein, and a supply system for introducing the treatment liquid of the pretreatment device into the pressure vessel through the stock solution inlet of the spiral-type membrane module. Characteristic processing system. 2. The pretreatment device includes a filtration treatment device, an adsorption treatment device, a biological treatment device, an ion exchange device, a centrifugal separation device, a membrane separation device, a pressure flotation treatment device, a coagulation separation treatment device, and a sedimentation separation treatment device. 2. The treatment system according to claim 1, further comprising at least one of an ozone oxidizer, a strongly acidic water treatment device, an ultraviolet sterilization treatment device, and a sodium hypochlorite sterilization treatment device. 3. A pressure vessel having a stock solution inlet and one or more processing devices for performing a predetermined process and a spiral type element capable of backwashing with a back pressure higher than 0.05 MPa and lower than 0.3 MPa are provided. Alternatively, a spiral membrane module containing a plurality of spiral membrane modules, and a supply system for guiding a cleaning liquid discharged from the processing apparatus during cleaning of the processing apparatus to the inside of the pressure vessel through the undiluted liquid inlet of the spiral membrane module are provided. A processing system characterized by being performed. 4. The processing system according to claim 3, wherein the pretreatment device includes at least one of a filtration device, an adsorption device, a biological treatment device, a membrane separation device, and a centrifugal separation device. 5. A spiral membrane element having one or more pretreatment devices for performing a predetermined pretreatment and capable of backwashing with a back pressure higher than 0.05 MPa and 0.3 MPa or less has a stock solution inlet. One or more spiral-type membrane modules housed in a pressure vessel are provided, and the processing liquid of the pretreatment device is supplied to the inside of the pressure vessel through the raw solution inlet of the spiral-type membrane module. How to operate the processing system. 6. The pretreatment device includes a filtration treatment device, an adsorption treatment device, a biological treatment device, an ion exchange device, a centrifugal separation device, a membrane separation device, a pressure flotation treatment device, a coagulation separation treatment device, and a sedimentation separation treatment device. The method for operating a treatment system according to claim 5, further comprising at least one of an ozone oxidizer, a strongly acidic water treatment device, an ultraviolet sterilization treatment device, and a sodium hypochlorite sterilization treatment device. 7. One or a plurality of processing devices for performing a predetermined process are provided, and 0.3 MPa or more higher than 0.05 MPa.
A spiral-type membrane module in which one or more spiral-type membrane elements capable of backwashing with a back pressure of not more than MPa are housed in a pressure vessel having a stock solution inlet is provided, and is discharged from the processing apparatus when the processing apparatus is washed. The method of operating a processing system, wherein the cleaning liquid to be supplied is supplied to the inside of the pressure vessel through the undiluted solution inlet of the spiral membrane module. 8. The method according to claim 7, wherein the processing apparatus includes at least one of a filtration processing apparatus, an adsorption processing apparatus, a biological processing apparatus, a membrane separation apparatus, and a centrifugal separation apparatus. .