TW200404601A - Operating method of separation membrane module and separation membrane apparatus - Google Patents

Abstract

A method for operating a separation membrane module comprising a spiral membrane element of the type in which an enveloped separation membrane and a feed water spacer are wound around the external circumference of a permeate water collecting pipe, the method comprising regularly or irregularly reversing the flow direction of feed water in the separation membrane module. A series of flushing operations are carried out each time the feed water flow direction is reversed, wherein a first flushing operation is carried out in the direction reverse to the direction of feed water immediately before the flushing operation.

Description

200404601 发明 Description of the invention: [Technical field to which the invention belongs] The present invention relates to a separation membrane module and a method for operating the separation membrane module, which can effectively remove the turbidity accumulated on the raw water separator wound around the spiral membrane element. quality. [Prior art] Conventionally, as a method for obtaining seawater desalination, ultrapure water, and various manufacturing process waters, it has been known to use a reverse osmosis membrane (R 0 membrane) and a nanofiltration membrane (NF membrane) as a permeable membrane. A spiral-type membrane element that separates ionic or low-molecular components from raw water. In addition, spiral-type membrane elements are also used in the out-of-limit filtration method that separates low-molecular and high-molecular components, or only the high-molecular components in low-molecular and high-molecular components, and the precise filtration method that separates fine particles. As shown in FIG. 8, an example of a spiral-type membrane element used in the past is to form a bag-shaped membrane 83 by bonding three sides to each other by overlapping the reverse osmosis membrane 81 on both sides of the water-permeable spacer 8 2. The opening of the bag-shaped film 83 is attached to the permeate water collecting pipe 84, and is formed by spirally winding around the outer peripheral surface of the permeate water collecting pipe 84 together with the net-shaped raw water separator 85. Next, raw water 86 is supplied from the end surface side 8 9 a of one end of the spiral type membrane element 80, flows along the raw water separator 85, and is concentrated from the end surface side 8 9 b of the other end of the spiral type membrane element 80. Water 8 8 is drained. The raw water 86 passes through the reverse osmosis membrane 81 and becomes permeate water 87 while flowing along the raw water separator 85. The permeated water 8 7 flows into the permeated water collection pipe 8 4 along the permeated water separator 8 2 and is discharged from the end of the permeated water collection pipe 8 4. In this way, the raw water path is formed by the raw water separator 85 arranged between the rolled bag-shaped films 83. 5 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 In addition, in the past, a separation membrane module equipped with the above-mentioned spiral membrane element was arranged in parallel in each section to be arranged as one or more separation membranes. The device group is connected to a multi-stage separation membrane device with more than two stages to improve the water recovery rate and the water treatment capacity. For example, in the multi-stage separation membrane device 90 of FIG. 9, the raw water supplied by the water pump 91 passes through the raw water supply main pipe 9 2 and the raw water supply branch pipes 9 3 a and 9 3 b. Segment separation membrane modules 9 4 a and 9 4 b are processed, and permeate water is obtained by permeating water outflow pipes 9 6 a and 9 6 b, and concentrated water is obtained by outflowing pipes 9 5 a and 9 5 b. water. The concentrated water flowing out of the separation membrane modules 9 4 a and 9 4 b is collected by concentrated water collecting pipes 9 7 a and 9 7 b, and the concentrated water is supplied to the main pipe from the middle (the raw water supply main pipe in the later stage). ) 9 8 and water is passed through the separation membrane module 9 9 in the second stage. Then, permeate water can be obtained from the permeate water outflow pipe 1 0 1, and concentrated water can be obtained from the concentrated water outflow pipe 100. As described above, the intermediate concentrated water obtained in the previous stage is used as the supply water of the separation membrane module in the subsequent stage to improve the water recovery rate. In addition, a plurality of separation membrane modules are arranged in parallel at each stage. To increase the amount of water treated. In the case of a reverse osmosis membrane spiral-type membrane element having such a structure, to obtain desalination of sea water, ultrapure water, and water for various manufacturing processes, pretreatment is usually performed for the purpose of removing turbidity of raw water. This kind of pretreatment is performed for the purpose of continuously ensuring the raw water flow path and increasing the contact area with the reverse osmosis membrane. Generally, the thickness of the raw water separator of the spiral membrane element of the reverse osmosis membrane is set. The film thickness is less than 1 mm, so turbidity is accumulated on the raw water separator on the raw water flow path, and it becomes easy to block the structure of the raw water flow path. 6 312 / Instruction Manual (Supplement) / 92-11 / 92122684 200404601 For this reason, it is necessary to remove the turbidity in the raw water in advance to avoid the increase of the water pressure difference caused by the accumulation of turbidity and the decrease in the permeate volume and permeate quality, and to maintain stable operation for a long period of time. Such a pretreatment device for the purpose of removing turbidity, for example, includes various devices including agglomerated sludge treatment, filtration treatment, and membrane treatment. These installations not only increase installation costs and operating costs, but also require Large installation area, etc. However, if the pretreatment device for the separation membrane module equipped with a spiral membrane element can be omitted, industrial water or tap water can be supplied to the reverse osmosis membrane module without pretreatment, so that the system can be simplified, The reduction of installation area and cost reduction can greatly increase the industrial use value. Based on this, it is extremely useful to develop a raw water separator with a structure that does not easily accumulate turbidity, or a method that can remove turbidity even if the turbidity is accumulated on the raw water separator by changing the operation method or washing. Technology. In particular, a method for removing turbidity by changing the operation method or rinsing is an optimal choice because it can be directly used in a conventional spiral type membrane element. Japanese Unexamined Patent Publication No. 1 1-1 0 4 6 3 6 discloses that a pressurized laminar gas-liquid laminar flow is supplied in a reverse direction opposite to a normal raw water flow in order to reversely flush reverse osmosis. Membrane module method. However, this reverse washing only removes the turbidity adhered to the hollow fiber membrane surface of the hollow-fiber reverse osmosis membrane module, but cannot remove the turbidity adhered to the raw water separator of the spiral-type reverse osmosis membrane module. Therefore, the purpose of the present invention is to provide a separation membrane module and a method for operating the separation membrane module 7 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601, which can effectively remove the accumulated in the spiral-type membrane Turbidity on raw water separator on element. [Summary of the Invention] In the above-mentioned actual situation, as a result of deliberate review, the inventor found that a spiral-shaped membrane element formed by winding a bag-shaped separation membrane and a raw water separator together is installed on the outer peripheral surface of the water collecting pipe. In the separation membrane module, the turbidity in the raw water accumulates at the point of intersection with the wires of the raw water separator. During the operation of the separation membrane module, the raw water is changed periodically or irregularly in the opposite direction. When running in the direction of flow, the phenomenon of turbidity accumulated on the raw water separator can be easily removed; when the flow direction of the raw water is changed, multiple rinsing (f 1 ushing) can be used to increase the turbidity removal effect. In the operation method of the separation membrane module, when the flushing is suitable, the flushing performed in the initial stage of each flushing is in a direction opposite to the flow direction of the raw water flowing immediately before the flushing starts. By doing so, the phenomenon of turbidity removal and the like can be further increased, which further contributes to the present invention. That is, the present invention provides a method for operating a separation membrane module, which is a separation membrane that is equipped with a spiral membrane element that is formed by winding a bag-shaped separation membrane and a raw water separator around the outer peripheral surface of a water-collecting pipe. Module operation method (hereinafter, also referred to as operation method of separation membrane module (I)), or a front separation membrane mold in which spiral-shaped membrane elements arranged in parallel arranged in one or two or more The middle water of a group or a separation membrane module group is sequentially supplied to a two-stage or more multi-segment separation of a rear separation membrane module or a separation membrane module group equipped with a spiral-type membrane element arranged in parallel in one or two or more. Membrane 8 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 Module operation method (hereinafter, also referred to as the operation method of the separation membrane module (π), and also referred to as the operation of the above-mentioned separation membrane module Method (I) or the operation method of the separation membrane module (Π) is the operation method of the separation membrane module (I) or (Π)), which periodically or irregularly changes the raw water of the separation membrane module in the opposite direction. Flow direction. By adopting the above-mentioned constitution method, it is possible to easily peel off and remove the turbidity accumulated at the intersection portion of the raw water separator. In addition, the present invention provides a method (I) or (Π) of the operation of the separation membrane module, which is performed by alternately rinsing from two directions when the flow direction of the raw water is changed. By adopting the above-mentioned configuration method, the turbidity accumulated at the intersection portion of the raw water separator can be reliably removed. In addition, the present invention provides a method (I) or (Π) for operating a separation membrane module. The flushing performed in the initial stage of each flushing is in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. Direction. By adopting the above-mentioned constitution method, the initial rinsing effectively peels off, and the turbidity accumulated on the intersection portion of the raw water separator is easily removed. In addition, the present invention provides a method (I) or (Π) for operating a separation membrane module, which is a spiral type formed by mounting a bag-shaped separation membrane and a raw water separator around a peripheral surface of a permeate water collecting pipe. A method for operating a separation membrane module of a membrane element. The operation method includes one or more rinsings on the way. The rinsing in the first stage of the rinsing is in the direction of the flow of raw water flowing before the rinsing. Go in the opposite direction. By adopting the above-mentioned constitution method, the same effects as those of the above-mentioned invention can be obtained. In addition, the present invention provides a method (I) or (Π) for operating a separation membrane module, which closes all the valves on the water side during flushing. If you open the valve that passes through the water side of 9 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601, in the case of a high-pressure separation membrane module, the raw water that belongs to the flushing liquid does not pass through during flushing, but at low pressure or super The low-pressure group passed through the raw water, which resulted in a decrease in the flushing flow and the problem of water quality transmission. In addition, there is an effect of floating the pollutants deposited on the film surface immediately after the valve on the permeate side is closed, and the effect can be flushed. In addition, the present invention provides a method (π) for operating a separation membrane module, in which the raw water supply side is removed before the flushing is performed, so that the pressure against the raw water supply side can be used to release the pressing force against the membrane force. It makes the membrane float slightly, and the turbidity accumulated in the membrane sheet can float. In addition, the present invention provides a method (π) for operating a separation membrane module, which divides the above-mentioned multi-stage separation membrane module washing into one separation membrane module or each separation module group. With the constitution method, the spiral-type membrane element at the rear stage can be prevented from being peeled from the spiral-type membrane element at the front stage, and contamination can be prevented. In addition, the present invention provides a separation membrane mold device including a first pipe connected to a raw water supply pump and a first valve; a raw water pipeline connected to the first valve and a separation membrane module; The permeate water side conversion pipe connected to the separation membrane module has a concentrated water outflow first branch pipe valve connecting the raw water supply first pipe and the concentrated water outflow side of the module; and a concentrated water outflow second branch pipe From the raw water supply No. 312 / Invention Specification (Supplements) / 92-11 / 92122684, the degree of pressure of the separation membrane die reduces the aquatic back pressure in one step increase (I) or pressure. Due to the surface pressure and the raw water partition (I) or each section, the above-mentioned turbidity flow is used to supply raw water to the second group; permeate; the separation membrane of the flowing side and the second 2 piping enter the 200404601 line, and the outflow and raw water flow The case where the direction becomes the opposite direction shrinks. By adopting the above-mentioned constituent device, the operation method (I) of the separation membrane module can be confirmed by a simple device. In addition, the present invention provides a multi-segment separation membrane mold device, which is the middle concentrated water obtained by the separation membrane device of the preceding stage or the separation membrane module of the separation membrane device group, and sequentially supplies the separation membrane device of the subsequent stage or the separation membrane installed in the separation membrane. A multi-stage separation membrane module device of two or more modules of the module, a separation membrane device constituting a separation membrane device or a separation membrane device group, includes a first pipe for raw water, which is connected to the first valve; The valve and the separation membrane module; the separation membrane module; the permeate water outflow system is connected to the permeate water side of the separation membrane module; the flow direction conversion pipe is connected to the raw water supply first pipe and the separation membrane module. The concentrated outlet side is provided with a second valve; the concentrated water flows out of the first pipe and is connected to the direction changing pipe and a third valve is provided; and the concentrated water flows out of the pipe and diverges from the raw water supply to the second pipe , And has a < By adopting the above-mentioned constituent device, a simple device can surely implement the operation method (Π) of the release membrane module. [Embodiment] Hereinafter, a method of operating a divided module according to a first embodiment of the present invention will be described with reference to Fig. 1. Fig. 1 is a flowchart showing a permeation membrane device for implementing the operation method of this example. In FIG. 1, the reverse osmosis membrane device 10 includes: a first piping supply 12 which is connected to a raw water supply pump 11 and a first valve water supply / supply second piping 13 which is connected to a first valve a and a reverse osmosis membrane; Module The reverse osmosis membrane module 1 0 A; the water flowing out of the piping 14 is a thick implementation connected to 312 / Invention Specification (Supplement) / 92-11 / 92122684, which will form the supply connection pipe from the obtained set. The distribution water flows through the second valve. The separation membrane reverse osmosis raw water i; original 10 A; the reverse 11 200404601 osmosis membrane module 10 A permeate water side; flow direction switching pipe 15 having a connection between the raw water supply first pipe 12 and the reverse osmosis The concentrated water flowing out of the concentrated water outflow side of the membrane module 1 0 A flows out of the first branch pipe 1 51 and the second valve b; and the concentrated water flows out of the second branch pipe 1 2 1 and diverges from the raw water supply to the second pipe 1 3. Concentrated water in the case where the flow direction of the raw water flows in the opposite direction. In addition, a valve c is attached to the concentrated water flowing out of the first branch pipe 1 51. In the reverse osmosis membrane device 10, first, the second valve b and the valve d are closed to form the inside of the module to a predetermined pressure. To adjust the valve c, open the first valve a and the valve e. The raw water is supplied to the reverse osmosis membrane module 1 0 A by a raw water supply pump 11. The raw water is processed through the reverse osmosis membrane module 10A, and the concentrated water flows out of the first branch pipe 1 51 from the concentrated water to obtain concentrated water. At the same time, the permeated water is obtained from the permeated water outflow pipe 14. In this case, although it depends on the turbidity of the raw water, as the operating time elapses, the raw water separator such as raw water gradually accumulates on the raw water separator wound around the element. When turbidity in raw water accumulates on the raw water separator, the difference in water pressure will increase. In this case, the flow direction of the raw water is changed to the opposite direction. That is, the first valve a and the valve c are closed, the valve d is adjusted so that the inside of the module is formed to a predetermined pressure, and the second valve b is opened. In this way, the raw water system flows in from the concentrated water outflow side of the reverse osmosis membrane module 1 〇 A, and is processed through the reverse osmosis membrane module 10 OA, and the concentrated water flows out of the second branch pipe 1 2 1 to obtain concentrated water. The permeated water outflow pipe 14 obtains permeated water. By changing the flow direction of such raw water to the opposite direction, it is possible to easily peel off and remove the turbidity accumulated on the intersection portion of the raw water separator. Then, with the passage of time 12 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601, suspended matter such as turbidity in the water is re-stored on the raw water separator mounted on the element, and therefore, again Change the flow of raw water to the opposite direction. In the future, this operation is repeated. The direction of changing the direction of the raw water is regular or irregular. Therefore, the interval for changing the direction of the original water can be from 1 hour to 24 hours, preferably 1 hour. If it is less than 1 hour, the number of switching times of the switching valve increases, and the life of the switching valve decreases. If it exceeds 24 hours, the turbidity is not easily removed. In addition, the period of change in the direction of flow of raw water can also be changed, for example, at the point of time when the pressure difference between the flowing water is specified. In this case, frequent changing operations can also remove accumulated turbidity. Therefore, it can also be combined at a specified time. The reverse osmosis membrane device 10 according to this example, which changes the flow direction after a lapse of time and changes the time point when it becomes a specified water pressure difference, because the flow of raw water is reversed to suppress the accumulation of turbidity, so The installation of pretreatment devices such as agglomerated sludge treatment, treatment, and membrane treatment for the purpose of removing turbidity in raw water can be omitted. Therefore, effects are achieved in terms of simplification, reduction in installation area, and cost reduction. Next, a method of operating a module according to a second embodiment of the present invention will be described with reference to FIG. The second embodiment example is based on the method of operating the osmotic membrane module of the first embodiment. The flow direction of the raw water is changed and the two directions are alternately washed several times, thereby being reliably removed at the intersection of the raw water separator. Servings of turbidity. As a method of performing multiple washings alternately from two directions of reverse osmosis, 312 / Invention Specification (Supplement) / 92-11 / 92122684 can be used when the flow of flowing water in the original direction is accumulated ~ 1 2 The above is not ideal. Method, both. Directional technology When the expected separation membrane state of the system is reversed, the de-accumulation membrane module is used to make the most washing at the beginning of 200404601 in a direction opposite to the direction of the flow flowing immediately before the washing. Method (hereinafter, also referred to as reverse side washing); and a method in which the raw water flows in the direction immediately before the rinsing, and the reverse rinsing can be effectively peeled by the rinsing performed in the first stage. It is ideal to accumulate turbidity at the intersection of raw water separators. If the washing direction in the initial stage is the same as that of the raw water flowing just before the start of washing, a part of the turbidity will be removed, but the turbidity accumulated on the remaining part of the raw water separator will also be resisted. As time passes, the accumulated turbidity is washed in the direction of the turbidity. First, the first valve a and the valve c are closed, and the valve b and the valve d are opened. Then, about 3 volumes of raw water supplied through the treated raw water are rapidly supplied to the reverse osmosis membrane module from the concentrated water outflow side, and the raw water from the raw water inflow side is supplied to the second pipe 13 and the concentrated water outflow / branching pipe 1 2 1 can be discharged. After the reverse flushing is completed, the flushing in the opposite direction to the flushing direction in the reverse flushing is subsequently performed. That is, the second valve b and the valve d are closed, and the first valve a and the valve c are opened. Raw water at the same flow rate as the reverse-side wash is rapidly supplied from the raw water inflow side into the reverse osmosis membrane mold, and is discharged through the first branch pipe through the concentrated water outflow side of the concentrated water outflow side. Then, the washing is performed in the opposite direction to the washing direction, and the same operation is repeated afterwards, and the washing can be staggered several times from both directions. When the flushing performed at the initial stage is in the same direction as the flow direction of the raw water flowing immediately before the flushing starts, it is the second operation in the case of performing the above reverse flushing first. In this way, by staggering 312 / Invention Specification (Supplement) / 92-11 / 92122684 from the two directions, the rush on the same section of the raw water rush can stagnate, reverse the second flow, and use% 2 to say, 14 200404601 was washed several times in the direction of the punching group 151, and the turbidity accumulated on the raw water separator was peeled off and excluded from the element. In the case of performing such flushing, in FIG. 1, the pressure release is performed by the pressure adjustment valve c or valve d on the outflow side of the concentrated water. However, the method of pressure release is not limited to this. Alternatively, a valve for pressure release may be provided. In this case, in order to obtain a larger discharge volume of the concentrated water outflow pipe, it is preferable to set the pipe diameter to be larger than that of a wide pipe for pressure adjustment. In addition, an air chamber (not shown) may be disposed in the concentrated water outflow first branch pipe 1 51 and the concentrated water outflow second branch pipe 1 2 1, and the accumulated water may be used for washing by operation. The air chamber referred to here is a device that pressurizes the air stored in the chamber by the pressure of the pressure of the concentrated water. When the flow direction of the raw water is changed, multiple flushes are performed alternately from two directions. Before the above flushing is performed, the pressure on the supply side of the raw water is removed, because the pressure that has been pressed against the membrane surface so far is removed, so that It floats slightly. Therefore, it is ideal to remove the pressure on the raw water supply side because the turbidity accumulated on the membrane surface and the raw water separator can float. As a method for depressurizing the raw water supply side, a raw water supply first pipe 12 on the discharge side of the raw water supply pump 11 may be provided with a discharge pipe (not shown), and a valve (not shown) may be provided in the middle of the discharge pipe. ) And a method of opening the valve, or a method of opening the valve d attached to the concentrated water flowing out of the second branch pipe 1 2 1 while the first valve a, the valve c, and the valve e are opened. There is no particular restriction on the opening speed of the valve, but it is better to open the valve instantaneously, preferably within 1 second. The method of instantaneous decompression makes it easier to float the membrane, and the effect of removing turbidity due to water hammering can also be expected. In addition, in this case, it is better to open the valve 15 of the permeate side 15 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601. This is because the pressure difference between the membranes disappears when the valve e is closed, and the external force against the membranes disappears. For example, even if the pressure on the supply side of the raw water is removed, the membranes do not float. In addition, it is preferable to close all the valves e attached to the permeated water outflow pipe 14 during flushing. If the valve e attached to the permeate water outflow pipe 14 is opened, in the case of a high-pressure reverse osmosis membrane module, raw water that does not belong to the rinsing liquid will pass through at the pressure of the flushing, but the reverse osmosis membrane module is used at a low pressure or an ultra-low pressure. However, there is a problem of permeating through the raw water, which results in a decrease in the flushing flow rate and a decrease in water quality. In addition, there is an effect of floating back the pollutants deposited on the membrane surface by the back pressure generated immediately after the valve attached to the permeate side is closed, which can further increase the flushing effect. The above-mentioned rinsing is preferably performed in two or more staggered rinsings in two directions. When the number of rinses is one time, the rinse only occurs in one direction. Therefore, the cleaning effect is insufficient, and turbidity may accumulate over time. On the other hand, if it exceeds 5 times, the discharged water increases and the recovery rate is lowered. In addition, the time for each flushing is not particularly limited, but it is preferably 30 seconds to 120 seconds. If it is less than 30 seconds, the cleaning effect is insufficient, and if it is more than 120 seconds, the discharge time will increase, resulting in a significant reduction in the recovery rate. It is also possible to supply compressed air to raw water during flushing. By mixing compressed air into the raw water, the washing efficiency can be further improved. The supply amount of compressed air is not particularly limited, but the volume ratio of raw water to air is preferably 2: 1 to 1: 2. After rinsing for a specified time, the raw water is treated again. In this case, the flow direction of the raw water is opposite to the flow direction of the raw water just before the start of the flushing performed in the initial stage. 16 312 / Instruction Manual (Supplement) / 92-11 / 92122684 200404601. That is, the first valve a and the valve c are closed, and the valve is adjusted to form a predetermined pressure in the module. d, and the second valve b and the valve e are opened, and the raw water system is processed through the reverse osmosis membrane module 10 A. In this way, the raw water treatment—rinsing—raw water treatment—rinsing is repeated in sequence. The raw water treatment time may be from 1 hour to 24 hours, and preferably from 1 hour to 12 hours. If the raw water treatment time is less than 1 hour, the number of switching times of the switching valve will increase, which will reduce the life of the switching valve and reduce the recovery rate. If it exceeds 24 hours, the effect of removing accumulated turbidity is reduced. In addition, as a form of conversion from raw water treatment to rinsing, a method of changing a flow direction after the same time elapses, a method of changing a point when a specified water pressure difference is reached, and a combination thereof Change method. A method of operating a separation membrane module according to a third embodiment of the present invention will be described with reference to Fig. 1. The operation method of the separation membrane module in this example is the operation method of the separation membrane module with a spiral membrane element installed. The operation method includes flushing in the middle, and the flushing performed in the initial stage of the flushing, The method is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. That is, in the third embodiment, after the flushing, the flow direction of the raw water may be formed in the same direction as the flow direction of the raw water flowing just before the flushing, or may be formed in the opposite direction. Otherwise, it is the same as the second embodiment. The embodiment examples are the same. Thereby, the optimal form of the raw water during raw water treatment, the operation form of the valves during flushing, and the optimal form of the flushing method are all the same as those of the second embodiment. In the third embodiment, the turbidity can be sufficiently removed by using the flow in the reverse direction at the time of rinsing. Therefore, the same effect as that of the second embodiment can be obtained in 17 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601. . A method of operating a separation membrane module according to a fourth embodiment of the present invention will be described with reference to Fig. 2. In FIG. 2, the same constituent elements as those in FIG. 1 are assigned the same reference numerals, and descriptions thereof are omitted. The following description mainly focuses on the differences. That is, in FIG. 2, the difference from FIG. 1 is that the reverse osmosis membrane module 1 0 B in the rear stage and the reverse osmosis membrane module 1 0 A in the front stage are provided on the downstream side of the reverse osmosis membrane module 10 A. The reverse osmosis membrane module 1 0 B at the rear stage is connected to the primary permeate water outflow pipe 14 supplied with the permeated water of the reverse osmosis membrane module 10 A at the front stage as the treated water of the rear stage device. The permeate water outflow pipe 16 and the return pipe 18 before returning the concentrated water to the original water supply water pump are discharged from the reverse osmosis membrane module 10 B at the rear stage. In addition, the reverse osmosis membrane module 10 B at the rear stage is provided with a concentrated water outflow pipe 17. The reverse osmosis membrane module 10 A at the front stage uses the reverse osmosis membrane device of the present invention, and the reverse osmosis membrane module 10 B at the rear stage uses a conventional reverse osmosis membrane device. That is, in the reverse osmosis' membrane device 10a, raw water is supplied to the reverse osmosis membrane module 10A in the previous stage by a raw water supply water pump 11. The raw water is processed by the reverse osmosis membrane module 10 A at the front stage, and the concentrated water flows out of the pipe 15 to obtain a concentrated shrinkage, and the permeated water flows out of the pipe 14 to obtain a once-permeated water. Next, the primary permeate water is processed through the reverse osmosis membrane module 10 B at the rear stage, and secondary permeate water is obtained from the permeate water outflow pipe 16 while the secondary concentrated water is returned from the return pipe 18 to the original water supply water pump. This secondary concentrated water system is the permeated water that has been degassed by the reverse osmosis membrane module 10 A in the previous stage and then concentrated through the reverse osmosis membrane module 10 B in the subsequent stage, which has a lower conductivity than the raw water. . Therefore, it is possible to circulate the entire amount of the secondary concentrated water, and the recovery rate of water 18 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 can be improved. Thus, in the reverse osmosis membrane device 10a, the part to which the present invention is applicable is the reverse osmosis membrane module 100A of the previous stage. The reverse osmosis membrane device 10a can also replace a pretreatment device used only for turbidity removal in a conventional device, and a reverse osmosis membrane module capable of implementing the operation method of the present invention is used in the previous stage. A reverse osmosis membrane can be used in substantially two stages. Of course, the pre-treatment device of the conventional device has no dechlorination function. Therefore, the reverse osmosis membrane device 10 a is more excellent in the quality of water permeated than the conventional reverse osmosis membrane device. A method of operating a separation membrane module according to a fifth embodiment of the present invention will be described with reference to Fig. 3. Fig. 3 is a flowchart of a multi-stage separation membrane device for implementing the operation method of this example. The multi-stage separation membrane device 2 8 is for supplying the intermediate concentrated water obtained from each separation membrane module 3 0 a, 3 0 b of the previous separation membrane device group 2 9 a to the separation membrane device group 2 9 b at the later stage. Separation membrane module 4 8 2-stage multi-stage separation membrane device. That is, the separation membrane device 3 1 a provided with the separation membrane module 3 0 a and the separation membrane device 3 1 b provided with the separation membrane module 3 0 b are arranged in parallel to form a front-stage separation membrane device group 2 9 a. The separation membrane device group 2 9 b is arranged at the subsequent stage to constitute a two-stage separation membrane device. In FIG. 3, the separation membrane device 31a includes: a raw water supply first pipe 3 2a, which is connected to the valve a1; a raw water supply second pipe 33a, which connects the valve a1 and the separation membrane module 30a; The separation membrane module 3 0 a; the permeate water outflow pipe 3 4 a has a valve e 1 connected to the water-permeable side of the separation membrane module 30 a; the flow direction switching pipe 3 5 a is connected to the raw water The concentrated water supplied to the first pipe 3 2 a and the separation membrane module 30 a has a valve b 1; the concentrated water flows out of the first branch pipe 3 6 a and is connected to the flow direction switching pipe 3 5 a. A valve c 1 is attached, and the concentrated water flows out of the second branch pipe 3 7 a. The raw water 19 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 is supplied to the second pipe 3 3 a for branching. The valve d 1 of the condensed water in the case of the opposite direction. In addition, 3 1 b and 3 1 c use the same separation membrane device group 2 9 a as the separation membrane device 3 1 a. The raw water supply main pipe 38 is provided, and the raw water outflow first pipe valve f is provided. The supply branch pipes 40 a and 40 b are supplied from the raw water to the main distribution, and the raw water supplies 32 a and 32 b connected to the separation membrane devices 3 1 a and 3 1 b; and the separation membrane devices 31 a and 31 b. In addition, the membrane device group 2 9 b includes: the first concentrated water supply main pipe to the main pipe in the latter stage) 4 1 is a raw water outflow pipe valve attached to the raw water outflow stage in the middle of the connection) m raw water outflow second pipe) 4 7 ; And a separation membrane device 3 1 c. The front section of the separation membrane device group 2 9 a, 2 9 b of the multi-stage separation membrane installation section further includes a water collection and collection pipe 5 1, and a first main pipe (a raw water supply main pipe) 4 from the separation membrane device group 2 9 b. 1 diverges, and is connected to the 2 9 a concentrated water flowing out of the first pipes 3 6 a, 3 6 b and the concentration pipes 3 7 a, 3 7 b. In the multi-stage separation membrane device 28, first, the valves d2, f, h, j, and m are closed to form a predetermined opening adjustment valve c 1, c 2 and i in the module, and the valve a 1, a 2, k. Raw water is supplied to the fruit 50 by the raw water and separated by 3 b. The raw water is processed through the separation membrane modules 30 a and 30 b, and the first pipes 3 6 a and 3 6 b obtain the first concentrated water, and the pipes 3 4 a and 3 4 b obtain the permeated water. From the separation membrane module 3 0 31W invention specification (Supplement) / 92_ 11/92122684 Water flow direction, the separation membrane device is completed. In addition, piping 39 is attached during the connection of the system; raw water pipe 38 is divided into the first piping, and the separation-piping (raw water supply; 2 piping valve (rear water outflow configuration 2 8) is in front. 50; and concentrated 1 concentrated water is supplied to the separation membrane device group. The water flows out of the second distribution bl, b2, dl, and pressure to el, e 2, g, and the membrane module 3 0a, and the concentrated water flows out from the permeated water. a and 3 0 b obtain the first concentrated water (intermediate concentrated water, the same below) of 20 200404601, which is collected by the concentrated water collecting pipe 51 and is supplied to the separation membrane module 48 at the subsequent stage. Then, the second concentrated water is obtained by flowing out of the first pipe 45 from the concentrated water, and the permeated water is obtained by flowing out of the pipe 4 3 through the permeate water. In this case, although it depends on the turbidity of the raw water, as the operation time elapses, turbid matter such as turbidity in the raw water is gradually accumulated on the raw water separator wound around the element. When turbidity in raw water accumulates on the raw water separator, the difference in water pressure will increase. In this case, the flow direction of the raw water is changed to the opposite direction. In other words, the valves a1, a2, c1, c2, g, and i are closed, the adjustment valves d1, d2, and j are opened to form a predetermined pressure in the module, and the valve b is opened 1, b 2 and h. As a result, raw water flows in from the concentrated water outflow sides of the separation membrane modules 30a and 30b, flows through the separation membrane modules 30a and 30b, and flows out of the concentrated water through the second pipes 37a and 3. 7 b obtains the first concentrated water, and at the same time, permeate water is obtained from the permeate water outflow pipes 3 4 a and 3 4 b. The first concentrated water obtained from each separation membrane module is collected by the concentrated water collecting pipe 51, and flows into and is processed from the concentrated water outflow side of the separation membrane module 48 in the subsequent stage. Then, the second concentrated water flows out from the concentrated water flowing out of the second pipe 46, and at the same time, the permeated water is obtained from the permeated water flowing out pipe 43. By changing the flow direction of such raw water to the opposite direction, it is possible to easily peel off and remove the turbidity accumulated at the intersection portion of the raw water separator. Then, as the running time elapsed, the floating material such as turbidity in the raw water was accumulated again on the raw water separator mounted on the element, so the flow direction of the raw water was changed to the opposite direction again. In the future, this operation is repeated. The period of change in the direction of flow of raw water is regular or irregular. Therefore, as an interval to change the direction of flow of raw water, 21 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 is 1 hour to 24 hours, preferably It is 1 to 12 hours. If it is less than 1 hour, the switching times of the switching valve will increase, which will reduce the life of the switching valve. In addition, if it exceeds 24 hours, it is difficult to remove the accumulated turbidity. In addition, in addition to the above, the timing of changing the flow direction of the raw water can also be changed at a time when it becomes a specified pressure difference in water flow. In this case, it is not necessary to frequently change the operation, and the accumulated turbidity can be removed, which is ideal. . It is also possible to combine a method of changing the flow direction after a specified time has elapsed, and a method of changing the method at a point when a specified water pressure difference is reached. According to the multi-stage reverse osmosis membrane device 28 of this example, since the flow direction of the raw water is reversed to suppress the accumulation of turbidity, it is possible to omit agglomerated pollution for the purpose of removing turbidity in the raw water in the conventional technology. Installation of pre-treatment equipment such as sludge treatment, filtration treatment and membrane treatment. Therefore, expected results can be achieved in terms of system simplification, reduction in installation area, and cost reduction. A method of operating a separation membrane module according to a sixth embodiment of the present invention will be described with reference to Fig. 3. The sixth embodiment is based on the operation method of the separation membrane module of the fifth embodiment. When the flow direction of the raw water is changed, a plurality of flushes are performed alternately from two directions, thereby reliably removing the accumulated water in the raw water barrier. Turbidity on the intersection part of the sheet. As a method of performing multiple flushes alternately from two directions of the separation membrane module, a method in which the flushing performed at the initial stage is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing is started ( Hereinafter, it is also referred to as reverse flushing); and a method performed in the same direction as the flow direction of the raw water flowing immediately before the flushing, wherein the reverse flushing uses the initial stage 22 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 is ideal because it can effectively remove the turbidity accumulated at the intersection of the raw water separator. If the flushing performed in the initial stage is the same direction as the flow direction of the raw water flowing just before the flushing, although a part of the turbidity can be removed, it will also oppose the remaining part of the raw water separator. The turbidity on the surface becomes accumulated turbidity over time. The flushing is performed in the reverse direction. First, the valves a 1, a 2, c 1, c 2, f, g, i, and m are closed, and the valves b 1, b 2, d 1, d 2, h, and j are opened. Then, the raw water having a flow rate of approximately three times the supplied raw water permeate is rapidly supplied from the concentrated water outflow side to the separation membrane modules 3 0 a and 3 0 b, and the raw water is supplied to the second pipe 3 3 through the raw water inflow side. a and 3 3 b and concentrated water flow out of the second pipes 3 7 a and 3 7 b and are discharged. The raw water discharged from the separation membrane modules 3 0 a and 3 0 b passes through the concentrated water collecting pipe 51 and is supplied from the concentrated water outflow side into the separation membrane module 4 8 in the subsequent stage, and the raw water is supplied from the raw water inflow side to the first 2 pipes 4 2 and concentrated water flow out of the second pipe 46 and discharged. After the reverse flushing is completed, the flushing in the opposite direction to that in the reverse flushing is then performed. That is, the valves bl, b2, dl, d2, f, h, j, and m are closed, and the valves al, a2, cl, c2, g, and i are opened. Then, raw water with the same flow rate as the reverse direction is flushed from the raw water inflow side to the separation membrane modules 3 0 a and 3 0 b, and the concentrated water from the concentrated water outflow side flows out of the first pipes 3 6 a and 3 6. b drain. The raw water discharged from the separation membrane modules 3 0 a and 3 0 b passes through the concentrated water collecting pipe 51 and is supplied to the separation membrane module 4 8 from the raw water inflow side again, and the concentrated water from the concentrated water outflow side flows out of the first 1 pipe 4 5 discharge. Then, the flushing is performed in a direction opposite to the flushing direction at the time of the flushing. After that, the same operation is repeatedly performed, that is, the flushing may be repeated several times from both directions. 23 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 In the above flushing, it is best to perform the flushing operation method for each separation membrane module group divided into sections. For example, in the above-mentioned reverse flushing, the valve m which was originally closed and the valves h and j which were originally open are closed. First, the previous separation membrane modules 3 a and 30 b are rinsed, so that the raw water is removed from The raw water flows out of the second pipe 47, and after a certain period of time, the valves d1, d2, and m are closed, and c1, c2, h, and j are opened, and the separation membrane module 48 in the subsequent stage is flushed in the reverse direction. According to this method, the turbidity peeled from the raw water separators of the separation membrane modules 30a and 30b in the previous stage will not flow into the separation membrane module 48 in the later stage, and will not pollute the separation membrane module 4 in the later stage. 8 for quick flushing. When the flushing in the opposite direction to the flushing in the reverse direction is performed again, for example, the valves a 1, a 2, and m are opened, and the valves b 1, b 2, h, and j are closed. First, the preceding stage separation is performed. The flushing of the membrane modules 3 a and 30 b causes the raw water to flow from the raw water to the second pipe 4 7. After a certain period of time, the valves c 1, c 2, and m are closed, and d 1, d 2, g, and i. The separation membrane module 48 of the subsequent stage is rinsed. In this way, each separation membrane module group of each stage is rinsed, which is ideal. Even in the case of a multi-segment separation membrane device composed of a separation membrane module group of three or more stages, it is preferable to perform flushing for each separation membrane module group divided into stages. When the flushing performed at the initial stage is in the same direction as the flow direction of the raw water flowing immediately before the flushing starts, it is the second operation in the case where the flushing in the reverse direction is performed first. In this way, by rinsing a plurality of times alternately from both directions, the turbidity accumulated on the raw water separator is peeled off and is surely excluded from the device. In the case of performing such flushing, in FIG. 3, the pressure adjustment valves c 1, c 2, d 1, d 2, and i 24 312 / Invention Specification (Supplement) / 92 -11 / 92122684 200404601 and j to perform pressure release, but the pressure release is not limited to this, and a valve for pressure release may be provided separately. In this case, in order to obtain a larger discharge amount, it is preferable that the piping provided as a valve for force adjustment has a larger diameter. In addition, air chambers are also shrunk out of the first piping 3 6 a, 3 6 b, 4 5 and concentrated water outflow 37a, 37b, and 46 (they are not flushed with the accumulated water during operation). The so-called air here refers to the device that is pressurized by the pressure of concentrated water to accumulate in the outflow of the chamber. When the flow direction of the raw water is changed, the flushing is performed alternately from two directions. Before proceeding, the raw water supply pressure is pumped, because the pressure that has been pressed against the membrane surface so far is caused to float, so the pressure on the raw water supply side is pumped, because the turbid density of the storage surface and the raw water separator can be relaxed The method of pumping off the pressure on the supply side includes a method of turning on the raw water supply water pump 50 and connecting the raw water supply main pipe 38 to the raw water flowing out of the first piping. The raw water flowing out of the first piping valve f Or, in the operation of opening 1 a 2, c 1, c 2, e 1, e 2, g, i, and k, the method of opening d2 and m. There is no particular limitation on the opening speed of the valve It is best to open the valve instantaneously, preferably within 1 second. Instant Intermittent decompression is easier to slow down the membrane, and turbidity caused by water hammer is also expected. In this case, it is best to open the water-permeable valves e 1 and e 2 2 because the valves e 1 and e 2 are closed. At k and k, the pressure difference between the membranes disappears, and the external force against the pressure also disappears. Therefore, for example, even if the pressure 312 / Invention Specification (Supplement) / 92-11 / 92122684 method of the raw water supply side is removed, the pressure can be reduced. In the thick 2 piping diagram), the membrane on the water supply side of the air chamber system slightly accumulates the drainage of the raw water supply of the membrane 39. Valve a 1, valve dl, attached, but the method excludes the effect L k 〇 This is The force of the membrane is still closed at 25 4 a, 3 4 b through the outflow pipe. If you open the attached permeate flow e2 and k, the high-pressure reverse osmosis membrane will not pass through the raw water, which is a flushing solution, but the module will pass through the raw water, so that the produced water will pass through. In addition, the back pressure generated by the valve on the other side for the effect can further increase the flushing for more than 2 times and less than 5 times. The flushing can only be performed in a single direction, and it will accumulate more than 5 times over time. At each time, the amount of discharged water increases every time. If the time is less than 30 seconds, the cleaning effect will increase, and the recovery time will increase, so that the recovery rate will be large. Supply compressed air to the raw water. Can further improve the cleaning efficiency. Pressure, but it is best to treat the raw water and air again. The flushing performed at this stage is just before the start. That is, the closing valves a1, a2, 200404601 are unable to slow down the diaphragm. In addition, during flushing, it is best to close all valves el, e2, and k attached to 43 out of the valves el, modules of the pipes 34a, 34b, and 43. In the case of flushing pressure, but at low or ultra-low pressure, reverse osmosis membranes are used. The raw flushing flow is reduced, and the water quality is reduced by floating the pollutants deposited on the membrane surface that are attached to the permeated water just after closing. The above flushing is preferably staggered from two directions. The number of rinses is time-varying once, so the cleaning effect is not sufficient, and there are some cases of turbidity. On the other hand, if this reduces the recovery rate. In addition, the flushing is limited, but it is preferably 30 seconds to 120 seconds, which is insufficient, and if it exceeds 120 seconds, the displacement decreases. In addition, it is also possible to mix compressed air into raw water during flushing, and the supply ratio of the compressed air is not particularly limited to a ratio of 2: 1 to 1: 2. After rinsing for a specified period of time, the flow direction of the raw water is opposite to the original water flow direction 312 / Invention Specification (Supplement) / 92-11 / 92122684 26 200404601 c 1, c 2, f, g, i And m, opening the adjustment valves d 1, d 2 and j so as to form the inside of the module to a specified pressure, and open the valves b 1, b 2, e 1, e 2 and k, and the raw water system passes through the separation membrane Modules 30a, 30b, and 48 are processed. In this way, the raw water treatment-rinsing-raw water treatment-rinsing is repeated in sequence. The raw water treatment time may be from 1 hour to 24 hours, preferably from 1 hour to 12 hours. If the raw water treatment time is less than 1 hour, the number of switching times of the switching valve will increase, which will reduce the life of the switching valve and reduce the recovery rate. If it exceeds 24 hours, the effect of removing accumulated turbidity is reduced. In addition, as a form of conversion from raw water treatment to rinsing, a method of changing the flow direction after the same time has elapsed, a method of changing the point when a specified water pressure difference is reached, and a combination thereof Change method. A method of operating a separation membrane module according to a seventh embodiment of the present invention will be described with reference to Fig. 3. The operation method of the separation membrane module of this example is a method of operating a multi-segment separation membrane module equipped with a spiral membrane element. The operation method includes a flushing in the middle, and the initial stage of the flushing is performed. The flushing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing starts. That is, in the seventh embodiment, after the flushing, the flow direction of the raw water may be the same as the flow direction of the raw water flowing immediately before the flushing, or may be the opposite direction. Otherwise, it is the same as the sixth The embodiment examples are the same. Thereby, the optimal form of raw water during raw water treatment, the operation form of valves during flushing, and the optimal form of flushing methods are all the same as those of the sixth embodiment. In the seventh embodiment, the turbidity can be sufficiently removed by using the flow in the opposite direction during flushing. Therefore, 27 312 / Inventory Note) / 92-11 / 92122684 200404601 can obtain the same effect as the sixth embodiment. . Examples of the raw water directly supplied to the reverse osmosis membrane device 10 or the multi-stage separation membrane device 28 in this example include industrial water, tap ice, and recovered water. There is no particular limitation on the turbidity of raw water. For a spiral membrane element with a turbidity of about 2, even if it has a high turbidity, the flow direction of the raw water is reversed regularly or irregularly. During long-term operation, the water pressure difference will not increase. In addition, since the raw water is supplied after being heated to 40 to 60 ° C, it is preferable to prevent and remove sludge (s 1 i in e) generated on the membrane surface. If the temperature of raw water is less than 40 ° C, the effect of removing sludge is scarce. If it exceeds 60 ° C, the effect of removing sludge is exceeded, but it exceeds the heat-resistant temperature of water treatment equipment. In addition, raw water heated to 40 to 60 ° C can be supplied continuously or intermittently. The intermittent supply can be performed intermittently at intervals of more than 1 hour and less than 1 week, and it is preferable to remove the sludge generated on the film surface without unnecessary energy consumption. If the supply interval is less than 1 hour, it will cause excessive heating and waste energy for no reason. On the other hand, if it exceeds one week side, sludge generation is likely to occur, thereby reducing the effect. In addition, the p Η value is 2.  0 or more 7.  If the acidic state is less than 0, acidic water has a large germicidal effect. It can suppress the generation of sludge and reduce the accumulation of turbidity on the membrane surface. If ρ Η is less than 2.  0, there will be a problem of chemical resistance of the system, if ρ Η value exceeds 7.  At 0, the effect of suppressing the generation of sludge cannot be expected. In addition, when coarse particles such as sand grains are included in the raw water, a dispersant is added to prevent the treated water, scale, and slag from passing through a large-mesh filter in advance. With the addition of dispersed and homogenized turbidity, turbidity can be further suppressed. 28 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 Accumulation of raw water separators and membrane surfaces. Examples of the dispersant include commercially available "hypersperseMSI300" and "hypersperseMDC200" (both manufactured by ARGO SCIENTIFIC). As the spiral membrane element mounted on the separation membrane module used in the present invention, there is no particular limitation as long as the bag-shaped separation membrane can be wound around the outer peripheral surface of the permeate water collecting pipe together with the raw water separator. The raw water separator (I) is composed of a first wire and a second wire extending in a meandering shape from the inflow side of the raw water to the outflow side, and the first wire is along the opposite side in the separation membrane. One of the membrane surfaces extends to form a raw water flow path between the adjacent first wires, and the second wire extends along the other membrane surface on the opposite side of the separation membrane to form between the adjacent second wires. Another raw water flow path, where the first wire and a part of the second wire overlap and are formed at the overlapping part; (Π) is a raw water inflow side end or a raw water inflow side end fixed to the separation membrane (M) in the above (Π), a method of fixing a raw water separator to a raw water inflow side end of the separation membrane, or a method of raw water inflow side end and concentrated water outflow side end Is to fold the raw water separator into two to clamp it from both sides (IV) The average number of intersections of the wires constituting the raw water separator is 50 or more and 100 or less per 1 in2 of the spacer; (V) constitutes The intersection density of the wires of the raw water separator is gradually reduced along the flow direction of the raw water, or it is intermittently decreased; (VI) The intersection density of the wires constituting the raw water separator may also be gradually increased along the flow direction of the raw water, or Increasing intermittently. In the above (I), the shape with the soft curve meandering is made into a regular shape without bending points, and the ratio (H / L) of the amplitude Η to the wavelength L is 0.  0 2 29 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 ~ 2, and each 1 m of a wire is 1 ~ 100 wavelength, the number of intersection points is in a more suitable range, At the same time, while the raw water slowly snakes in the raw water flow path, it flows in a substantially straight line from the inflow side to the outflow side, which can further prevent the accumulation of turbid matter in the raw water flow path, which is ideal. In the above (Π) and (Π), the lengths of the raw water inflow side end or concentrated water outflow side end of the separation membrane with respect to the length of the permeated water collecting pipe in the longitudinal direction are respectively from the raw water inflow into the separation membrane. The side end or the concentrated water outflow side end faces inward, and it is preferably 1 to 10% of the length in the length direction of the permeated water collecting pipe. In the operating method of the separation membrane module of the present invention, a separation membrane module equipped with a spiral membrane element including the raw water separators of the above (I), (Π), (ΠI), and (IV) can be applied to the above. Any of the first embodiment to the seventh embodiment. A separation membrane module equipped with a spiral membrane element including the above-mentioned raw water separators (V) and (VI), because the number density of the intersections of the raw water separators is limited by the flow direction of the raw water, so it cannot be applied to raw water. The directions of the first embodiment, the second embodiment, the fifth embodiment, and the sixth embodiment are changed to the opposite directions. The separation membrane module equipped with the spiral membrane element including the raw water separator (V) described above is cleaned in the reverse direction of the third embodiment and the seventh embodiment, but it must be deliberately near the entrance of the raw water separator. Adopt a structure that accumulates turbidity. In addition, a separation membrane module having a spiral-type membrane element provided with the raw water separator (VI) described above can be applied to the above-mentioned third and seventh embodiments. Examples of the raw water separators of (Π) to (IV) include a mesh-shaped separator composed of a plurality of first wires and a plurality of second wires. In this case, although there are no particular restrictions on the shape of the mesh as 30 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601, rhombuses, quadrangles, and corrugations can be cited as the cross-shape of the wires. Although not particularly limited, there may be mentioned a configuration in which the wires are woven with each other, a cross configuration in a plain weave, and a cross configuration in a twill weave. The intersection point refers to a point at which the first wire and the second wire intersect. For example, if the first wire and the second wire are corrugated, the first wire and the second wire may have a slightly overlapping portion. The cross-sectional shapes of the first wire and the second wire are not particularly limited, and examples thereof include a triangle and a quadrangle. The first wire and the second wire are made of the same size and the same cross-sectional shape. The thickness of the raw water separator is matched to the diameter of the first wire and the diameter of the second wire, or it is slightly thinner, which is 0. 4 ~ 3.  Omm range. In addition, although the material of the raw water separator is not particularly limited, the use of polypropylene and polyethylene is preferable in terms of moldability and cost. In addition, although the manufacturing method of the raw water separator is not particularly limited, a known method such as an injection molding method can be applied, and it is preferable from the viewpoint of cost and accuracy. The spiral membrane element is a bag-shaped separation membrane that is wound around the outer peripheral surface of a permeate water collecting pipe together with the raw water separator, and a bag-shaped separation membrane that can be wound around one sheet or a plurality of bag-shaped separation membranes. Separation membrane. Examples of the separation membrane include a precision filtration membrane, an outer-limiting filtration membrane, and a reverse osmosis membrane. Among them, the reverse osmosis membrane is used for the purpose of separating ionic components and low-molecular components from the atoms, and the effect can be further exerted in consideration of the case where a pre-treatment is required in the past. Examples of the reverse osmosis membrane include a normal reverse osmosis membrane having a high removal rate of 90% or more with respect to sodium chloride in saline, a nanofiltration membrane with a low dechlorination rate, and a low ion removal rate reverse osmosis membrane ( 1 ο 〇se R 0). Nanofiltration membrane, low 31 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 Ion removal rate Reverse osmosis membrane has dechlorination performance, but it has lower dechlorination performance than ordinary reverse osmosis membranes. Those who have the ability to separate hardness components such as Ca and Mg. In addition, a nanofiltration membrane and a low ion removal rate reverse osmosis membrane may be referred to as a NF membrane. The reverse osmosis membrane module used in this example is not particularly limited as long as it is provided with the above-mentioned spiral-type membrane element. For example, a reverse osmosis membrane module having a structure shown in Fig. 4 may be mentioned. As shown in FIG. 4, a bag-shaped reverse osmosis membrane 61 and a raw water separator are spirally wound around the outer peripheral surface of the permeate water collecting pipe 60, and the upper part is covered with an outer body 62. Then, in order to prevent the reverse osmosis of the permeable membrane 61 in a spiral shape, the stretchable stopper 64 having a plurality of radial flanges is attached to both ends. In this way, the permeate water collecting pipe 60, the reverse osmosis membrane 61, the outer body 62, and the retractable stopper 64 are formed into a spiral membrane element 65. A connector (not shown) and each permeate water collecting pipe are formed. 60 communicates, and a plurality of spiral membrane elements 65 are installed in the chamber 66. A gap 6 7 is formed between the outer periphery of the spiral membrane element 65 and the inner periphery of the chamber 66, but it is closed by a salt seal (B r n e s e a 1) 6 8. A raw water inflow pipe (not shown) for flowing raw water into the interior of the room is attached to one end of the chamber 66, or a treated water pipe (not shown) and a non-permeable water pipe (not shown) connected to the permeate water collecting pipe 60 are provided at the other end. (Not shown), the reverse osmosis membrane module 69 is constituted by the chamber 66, its internal parts, piping (nozzle), and the like. When the raw water is processed by the reverse osmosis membrane module 69 constructed in this way, raw water is pressed into the raw water from one end of the chamber 66 using a water pump. As shown in FIG. 4, the raw water passes through each of the retractable stoppers 64. Radial flanges 6 and 3 penetrate into the original spiral membrane element 65, and a portion of raw water passes through the spiral membrane 32 312 / Invention Specification (Supplement) / 9241/92122684 200404601 between the membranes of element 6 5 The raw water flow path separated by the raw water separator reaches the next spiral membrane element 65, and the remaining raw water passes through the reverse osmosis membrane 6 1 to become permeate water, and the reverse water is collected by the permeate water collecting pipe 60. . After that, the raw water continuously passes through the spiral membrane element 65, and the raw water that has not passed through the reverse osmosis membrane is extracted from the other end of the permeate water collection pipe 60 as concentrated water containing turbidity and ionic impurities at a high concentration. The permeated water that has passed through the reverse osmosis membrane is taken out of the chamber 66 through the permeated water collecting pipe 60. In addition, the reverse osmosis membrane module used in the present invention may be one in which a plurality of spiral membrane elements are mounted, for example, one in which a spiral membrane element is mounted. The multi-stage separation membrane device of this example is to sequentially supply the intermediate concentrated water obtained from the separation membrane device or the separation membrane module group of the separation membrane device group to the separation membrane device or the separation membrane device group of the separation membrane device group in order. The multi-stage separation membrane module device with two or more stages of the module may also include, for example, a group of separation membrane devices 7 1 a to 7 1 d arranged in parallel in front of each other. 7 2 a, parallel In the middle of the separation membrane module 7 1 e, 7 1 f, the separation membrane device group 7 2 b and the separation membrane device group 7 1 g in the rear stage are arranged in parallel. Type 4 — 2 — 1 type three-stage separation membrane device composed of c (see FIG. 5); three-stage separation membrane modules 7 4 a to 7 4 c are arranged in parallel to the front stage separation membrane device group 7 3 a And in parallel arranged two separation membrane modules 7 4 d, 7 4 e in the rear stage separation membrane device group 7 3 b composed of 3-2 type two-stage separation membrane device (refer to Figure 6 (A)); Separate membrane module groups 7 6 a and 7 6 b in front of two separation membrane modules 7 6 a and parallel arrangement in parallel Membrane module 7 6 c The separation membrane device group 7 5 b consisting of 2-1 type two-stage separation membrane device (refer to Figure 33 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 6 ( B)); from the separation membrane module 7 8 a arranged in parallel arranged 7 8 a separation membrane group 7 7 a and the separation membrane device group arranged 7 7 b arranged in parallel arranged in the first stage of the type 1-1 Set in two stages (refer to Figure 6 (C)). Fig. 6 (B) is the same as Fig. 3, and Figs. 5 and 6 are schematic diagrams from the separation membrane module line. Although the concentrated water flows out of the first pipe and the concentrated water flows out, it is different from the actual arrangement position. These multi-stage separation membranes can be set to the state required for the water recovery rate and the water treatment amount. The multi-stage separation membrane device of the present invention can simply implement the operation method of the multi-stage separation membrane module of the present invention. (Embodiment) Hereinafter, the present invention will be described in more detail by taking an example as an example, and the present invention is not limited thereto. < Example 1 > Industrial water with a turbidity rate of 2 OmS / m was treated by a reverse osmosis membrane device of the flow shown in Fig. 1. Under the following operating conditions, hourly and durable operation. The reverse osmosis membrane device uses one reverse set, and this reverse osmosis membrane module is equipped with an 8-inch element ES-10 (made by Nitto Denko) wound around a mesh. Reverse osmosis membrane mold: Valence, measured at the beginning of operation and the water pressure at 2000 hours; i after f 2 0 0 hours under the amount of water flow (1 / min) and the conductivity (mSm) of permeated water , Disassemble the reverse osmosis membrane module and observe the adhesion status of the raw water quality. Table 1 shows the results of the measured values, and the results of visual observation of the flow path are shown. 312 / Invention Specification (Supplement) / 92-11 / 92122684 The front-end sub-module 7 8 b type separation membrane installation configuration. The 2 outflow second piping, the device is indeed by the appropriate shape of the device, these are only 2 degrees, conductive to conduct the performance of the raw water diaphragm cylinder 2 0 0 0 permeability membrane mold L (MPa) 透 f . In addition, the turbid 2 in the flow path shows raw water 34 200404601 (operating conditions) As shown in the second embodiment example, when the flow direction of the raw water changes, three flushes are carried out alternately from both directions to perform the initial stage. The method of washing is performed in a direction opposite to the flow direction of the raw water flowing just before the washing is started. In other words, the original processing time is 8 hours-60 seconds in the reverse direction-60 seconds in the forward direction-60 seconds in the reverse direction-1 cycle, and this operation is repeated. The forward rinsing means rinsing in the same direction as the flow direction of the raw water flowing immediately before the rinsing. Permeation treatment conditions: operating pressure is 0.75 MPa, concentrated water flow is 2.7 m3 / hour, water temperature is 25 ° C, and pΗ value of raw water is 7.0. Flushing conditions: Fully open valve c or d, flushing flow rate is 8. 0 m3 / hour, and water temperature is 25 ° C. < Example 2 > During each flushing in Example 1, except that the air was mixed in such a way that the volume ratio of raw water to air became 1: 1, the other operations were performed in the same manner as in Example 1. 20 0 0 hours of durable operation. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 3 > Except that instead of continuously supplying raw water at a temperature of 25 ° C for raw water treatment, raw water was supplied once a day and intermittently for 1 hour at a temperature of 50 ° C. All of them were operated for 2000 hours in the same manner as in Example 1. Raw water at 50 ° C is obtained by heating raw water at 25 ° C with a heater. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. 35 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 < Example 4 > Except that instead of raw water having a ρ Η value of 7.0 for raw water treatment, raw water having a p Η value of 4.0 was used instead, and the other operations were performed in the same manner as in Example 1. 2000 hours of durable operation. The raw water having a pH value of 4.0 is prepared by adding hydrochloric acid to the raw water having a pH value of 7.0. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 5 > Except that 5ing / l of a dispersant "hypersperse MSI300" (manufactured by ARG0 SCIENTIFIC) was added to industrial water having a turbidity of 2 degrees and a conductivity of 20 mS / m, the other examples were used. 1The same operation method is used for 2000 hours of durable operation. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 6 > The reverse osmosis membrane device of the flow shown in FIG. 2 was used to process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 m S / m. Under the following operating conditions, it was performed for 2000 hours. Durable operation. The reverse osmosis membrane module 10 A at the front stage and the reverse osmosis membrane module 10 B at the rear stage are 8-inch elements ES-10 (manufactured by Nitto Denko) with one raw water separator wound around the mesh. Modules, reverse osmosis membrane devices use one of these modules. The performance evaluation of the reverse osmosis membrane module was performed by the same operation method as in Example 1. (Operating Conditions) The front-stage reverse osmosis membrane module 10 A and the rear-stage reverse osmosis membrane module 10 B, with an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7 m3 / hour, and a water temperature of Conditions of 25 ° C and pH of raw water of 7.0, only in the reverse osmosis membrane module 36 312 / Invention Manual (Supplement) / 92-11 / 92122684 200404601 1 0 A at the previous stage, once every 8 hours, The same rinsing as in Example 1 was performed. The change of the flow direction of the raw water is performed only in the first-stage reverse osmosis membrane module 1 line, and not in the latter stage of the reverse osmosis membrane module 10 B. In addition, Table 1 shows the values of the rear-stage reverse osmosis membrane module. < Comparative Example 1 > A known pretreatment device composed of a membrane treatment was placed in the front stage, and the flow direction of raw water was changed and rinsed. The procedure was performed in the same manner as in Example 1. < Comparative Example 1 > That is, industrial water with a temperature of 2 degrees and a conductivity of 20 mS / m is processed by a pre-treatment device, and then the processed water is processed normally by a conventional commercially available reverse membrane module. Tables 1 and 2 show the results. < Comparative Example 2 > Except that the operating conditions of Example 1 were replaced with the following operating conditions, the other methods were performed in the same manner as in Example 1. < Comparative Example 2 > In other words, the pre-treatment device is used for industrial applications that have a turbidity of 2 degrees and a conductivity of 20 mS / m. The conventional processing membrane modules directly perform conventional processing 1 and Table 2 shows the results. In Comparative Example 2, the flow pressure difference was extremely high at about 800, and the permeated water could not be obtained. Therefore, the operation was stopped at the point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7m3 / hour, a temperature of 25 ° C, and a p 水 value of raw water of 7.0. In addition, the treatment is to interrupt the treatment of raw water every 8 hours, and the valve c attached to the first branch pipe 1 5 1 of the concentrated water is fully opened to feed the treated raw water through 312 / Invention Manual (Supplement) / 92-11 / 92122684 In addition, the value of 0A is not improved, and the turbidity is not permeated, so that the water cannot be removed. On the left side of the table at this time, the raw water flows out at about three times the flow rate of 37 200404601. Raw water flows into the reverse osmosis membrane module for 60 seconds, and the so-called forward flushing for washing and drainage from the concentrated water outflow pipe is performed. [Table 1] Differential pressure of water flow "MPal Permeated water volume (1 / min) Permeated water conductivity [mS / m] 2000hr in the initial period of operation 2000hr in the initial period of operation 2000hr in the initial period of operation Example 1 0.020 0.035 20 15 0. 30 0. 45 Example 2 0.020 0.031 20 16 0. 30 0. 42 Example 3 0. 020 0.035 20 17 0.30 0. 39 Example 4 0.020 0.035 20 17 0. 30 0.39 Example 5 0.020 0. 033 20 18 0. 30 0. 38 Example 6 0.020 0.020 20 20 0.03 0. 03 Comparative Example 1 0.020 0.022 20 20 0. 30 0.30 Comparative Example 2 0.020-20-0.30-[Table 2] Visual observation of raw water flow path after 2 0 0 0 hours As a result tnj. JnJ. Fnj. JJ. Rnj. JJ. Tuj. Ruj The food order order is divided and the order is set to be more effective than it is more effective than the actual ratio 45 6 (the previous paragraph R 0) 6 (Back stage R 0) 1 2 completely obstructs the original sticky turbidity and turbidity. Attachment 6¾ turbidity and turbidity. ^ Turbidity and turbidity. Attachment and turbidity.少少 少 无 无 无 ^ Slightly slightly slightly almost ^ Slightly slightly extremely extremely < Example 7 > The multi-stage separation membrane device of the flow shown in Fig. 7 was used to process industrial water with a turbidity of 2 degrees and a conductivity of 20 mS / m. Under the following operating conditions, it was durable for 2000 hours. Running. The multi-stage separation membrane device uses a separation membrane module equipped with an 8-inch element E S-10 (made by Toto Denko) with a mesh-shaped raw water separator wound around it. The performance evaluation of the separation membrane module is based on measuring the initial operating pressure of the separation membrane module in the first stage and the water pressure difference (MPa), the amount of permeated water (1 / min), and the conductivity of the permeated water at 2000 hours. (MS / m). In addition, after 2000 hours, the separation membrane module of the first stage was disassembled, and the turbidity of the raw water 38 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 was observed. In addition, Table 8 shows the results of each measurement value of the separation membrane module in the first stage, and Table 9 shows the raw water flow path of the separation membrane module in the first stage (the part where the raw water separator in the separation membrane module exists). Visual observation. The results of Examples 8 to 12 and Comparative Examples 3 to 5 of Tables 8 and 9 are also the same. (Operating Conditions) Each valve is opened and closed according to the step table shown in Table 3. The steps of No. 1 to No. 16 of Table 3 are taken as one cycle, and this operation is repeated. Permeation treatment conditions (water extraction A and B) are based on operating pressure of 0 · 7 5 Μ Pa, concentrated water flow (final stage) of 2 · 7 m3 / hour, water temperature of 2 5 ° C, p 水 value of raw water A condition of 7 · 0. In addition, the flushing conditions (flushing A1, A2, B1, and B 2) are a flushing water flow of 8.0 m3 / hour and a water temperature of 25 ° C. [table 3]

No. L step | Hold time a3 b3 c3 d3 6 3 fghijkm 1 Water collection A 1 2 time ▲ -1 A 2 Release pressure ~ Γ 10 seconds ▲ ππο ▲ 3 Flush B1 60 seconds 4 Flush ΊβΤ 60 seconds 5 Flush ΤΓ 60 seconds 6 Rinse time ~ 60 seconds 7 Rinse time 30 seconds 8 Rinse time 30 seconds 9 Water collection 1 2 time ▲ ▲ 10 Release I 10 seconds ▲ ▲ 11 Rinse A1 60 seconds I 12 Rinse 60 seconds 13 Rinse 60 seconds 14 Rinse 60 seconds 15 punches ΑΙ * 30 seconds 16 flushes ΤΓ 30 0 seconds (Note) empty column: valve fully closed,: valve fully open, ▲: to become appropriate pressure 39 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 Forced valve opening < Embodiment 8 > When flushing A1, A2, B1, and B 2 in each of Embodiment 7, the air was mixed in such a way that the volume ratio of raw water to air became 1: 1 The others are operated for 2000 hours in the same manner as in Example 7. Table 8 and Table 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 9 > Instead of continuously supplying raw water at a temperature of 25 ° C for raw water treatment, instead of supplying raw water at 25 ° C for 2 3 hours, intermittent supply was performed for 1 hour. 5 Except for the operation of raw water at 0 ° C, the endurance operation was performed for 2000 hours in the same operation method as in Example 7. Raw water at 50 ° C is obtained by heating raw water at 25 ° C with a heater. Tables 8 and 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 1 0 > The same operation method as in Example 7 was used except that raw water with a ρ Η value of 7.0 was used instead of raw water treatment, and raw water with a ρ Η value of 4.0 was used instead. 20,000 hours of running for a long time. Raw water having a pH value of 4.0 is prepared by adding hydrochloric acid to raw water having a pH of 7.0. Tables 8 and 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 1 1 > A 50 mg / l dispersant "hypersperse MSI300" (manufactured by ARG0 SCIENTIFIC) was added to industrial water having a turbidity of 2 degrees and a conductivity of 20 mS / m. The same operation method of Example 7 was performed for 2000 hours of endurance operation. Tables 8 and 9 show the performance evaluation results of 40 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 for the reverse osmosis membrane module. < Comparative Example 3 > The method was performed in the same manner as in Example 7 except that the filtration device with a known limit for the purpose of previous processing was placed in the front stage and only the water collecting step in Table 4 was performed. That is, the pre-treatment device processes industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m, and then a multi-stage membrane separation device connected to a conventional commercially available separation membrane module is used for the treated water. deal with. Table 8 and Table 9 show the results. [Table 4 ]

No. Step holding time a3 b3 c3 d3 e3 fghijkm 1 Water extraction 2 0 0 0 time ▲ ▲ (Note) Empty column: valve is fully closed, valve is fully open, ▲: valve is opened to a proper pressure < comparative example 4 > The procedure was the same as in Example 7 except that the following operating conditions were changed. That is, instead of processing industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m by a pre-treatment device, normal processing is directly performed by a two-stage membrane separation device connected to a conventional commercially available separation membrane module in two stages. . Table 8 and Table 9 show the results. Further, in Comparative Example 4, at around 800 hours, the differential pressure of the water flow was extremely increased, and permeated water could not be obtained. Therefore, the operation was stopped at this point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7 m3 / hour, a water temperature of 25 ° C, and a p 水 value of raw water of 7.0. In addition, each valve is opened and closed according to the procedure in Table 5, and Ν 〇. 1 and Ν 0.2 are used as a cycle, and 41 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 is repeatedly operated. [table 5 ]

No. Step holding time a3 b3 c3 d3 e3 fghijkm 1 Water extraction 8 hours ▲ A 2 Rinse for 60 seconds (Note) Blocking: valve fully closed, valve fully open, ▲: Open the valve with a pressure of 1 as appropriate < Example 1 2 > The multi-stage separation membrane device of the flow shown in FIG. 3 was used to process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 in S / in for 2000 hours under the following operating conditions. Durable operation. The performance evaluation of the multi-segment separation membrane device is based on measuring the initial operating pressure of the separation membrane module 20 a in the first stage and the water pressure difference (MPa), permeated water volume (1 / min), and permeation at 2000 hours. Conducted at water conductivity (mSm). In addition, after 2000 hours, the separation membrane module 20 a in the first stage was disassembled, and the turbidity adhesion state in the raw water flow path was observed. In addition, Table 8 shows the results of the measured values, and Table 9 shows the results of visual observation of the raw water flow path. (Operating Conditions) Open and close each valve according to the procedure table shown in Table 6, and repeat the operation by repeating the steps of No. 1 · N to 0.1 6 in Table 6 as one cycle. The permeation treatment conditions (water extraction A and B) are based on the operating pressure of 0 · 7 5 MPa, the flow rate of the concentrated water (the final stage) is 4.4 m3 / hour, the water temperature is 25 ° C, and the p 水 value of the raw water The condition is 7.0, and the flushing conditions (flushing A1, A2, B1, and B2) are a flushing water flow of 8. Om3 / hour and a water temperature of 25 ° C. 42 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 [Table 6]

No. Step holding time a 1 a2 bl b2 cl c2 dl d2 el e 2 fghijkm 1 water extraction A 1 2 time ▲ ▲ ▲ 2 release A 10 seconds ▲ ▲ ▲ 3 rinse B1 60 seconds 4 rinse B2 60 seconds 5 rinse A1 60 seconds 6 flush A2 60 seconds 7 flush B1 30 seconds _ 8 flush B2 30 seconds 9 water B 1 2 time ▲ ▲ 10 release B 10 seconds ▲ ▲ 11 flush A1 60 seconds 12 flush A2 60 seconds 13 flush B1 60 seconds _ 14 Flush B2 for 60 seconds _ 15 Flush A1 for 30 seconds 16 Flush A2 for 30 seconds (Note) Empty column: Valve is fully closed,: Valve is fully open, ▲: Valve is opened to a proper pressure < Comparative Example 5 > Except for the following operating conditions, everything was performed in the same manner as in Example 12. That is, the pre-treatment device does not process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m, but a conventional multi-layer membrane of a commercially-available separation membrane module directly connecting two in the front stage and one in the back stage. The separation device performs normal processing. Table 8 and Table 9 show the results. Further, in Comparative Example 5, the water passing pressure difference extremely increased at about 800 hours, and permeated water could not be obtained. Therefore, the operation was stopped at this point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.7 5 MPa, a flow rate of concentrated water of 4.4 m3 / hour, a water temperature of 25 ° C, and a p Η value of raw water of 7.0. In addition, according to the procedure of Table 7 43 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601, each valve is opened and closed, and N ο. 1 and Ν ο. 2 are used as a cycle to repeat the operation. [Table 7]

No. Step holding time a 1 a 2 bl b2 cl c2 dl d2 el e2 fghijkm 1 8 hours of water collection ▲ ▲ ▲ 2 Flush for 60 seconds (Note) Empty column: valve fully closed: valve fully open, ▲: to become appropriate pressure Open the valve [Table 8] Water differential pressure "MPa 1 Permeable water volume (1 / min) Permeable water conductivity" mS / m] Initial operation 2000hr Operation initial 2000hr Operation initial 2000hr Example 7 0. 020 0. 035 20 15 0.30 0.45 Example 8 0. 020 0. 031 20 16 0. 30 0. 42 Example 9 0. 020 0. 035 20 17 0. 30 0.39 Example 10 0., 020 0., 035 20 17 0. 30 0. 39 Example 11 0., 0 2 0, .033 20 18 0. 30 0. 38 Example 12 0., 0 2 0 0, 0 35 20 15 0. 30 0. 45 Comparative Example 3 0. 020 0. 022 20 20 0. 30 0. 30 Comparative example 4 0. 020-20-0. 30-Comparative example 5 0 · 020-20 — 0. 30-[Table 9] Visual inspection of raw water flow path after 2 0 0 0 hours Observation results 0 12 οο ον 11 11 11 οο-ΫηΊΨ ΐπΊΨ ΊΊ fnMW ΐηΊΨ rnj fniw Make the splitting and mediation tampering and applying the application. The application is more sticky than sticky. Qualitative degree Extremely, very few plugs, and the resistance is completely complete. In Examples 1 to 6 using a one-stage separation membrane device and Examples 7 to 12 using a multi-stage separation membrane device, almost no after 2000 hours. The increase in the water pressure difference has not decreased the amount of permeated water, and the quality of the permeated water is also high. 312 / Invention Specification (Supplement) / 92-11 / 92122684 44 u -i.; Mi 200404601 at 2000 hours In the subsequent performance evaluation, although Comparative Example 1 is not inferior to Examples 1 to 6, and Comparative Example 3 is not inferior to Examples 7 to 12, the results are because the pre-processing device is provided, and there is unnecessary Necessary for installation place, installation cost, etc. By doing this, the comparison target of Examples 1 to 5 is Comparative Example 2, the comparison target of Examples 7 to 11 is Comparative Example 4, and the comparison target of Example 12 is Comparative Example. 5, but any of Comparative Examples 2, 4, and 5 was cloudy at about 800 hours and the amount of permeated water became 0. Adhesion is quite serious. The comparison target of Example 6 is Comparative Example 1, but Example 6 shows very excellent performance and is inexpensive. (Industrial Applicability) According to the operation method of the separation membrane module of the present invention, the turbidity accumulated on the intersection portion of the raw water separator can be easily peeled off and removed. In addition, there is no problem in reducing the flushing flow rate caused by the low-pressure or ultra-low-pressure reverse osmosis membrane module. At the same time, it also has a back pressure generated immediately after the valve on the water side is closed to deposit on the membrane surface. The effect of alleviating the tightness of the contaminated substances can further improve the flushing effect. In addition, the pressure against the membrane surface can be relieved by removing the pressure on the supply side of the raw water. Therefore, the membrane is slightly loosened, and the dense pressure of the turbidity accumulated on the membrane surface and the raw water separator can be relaxed. According to the separation membrane device of the present invention, the above-mentioned operation method can be carried out reliably by a simple device. [Brief description of the drawings] Fig. 1 is a flowchart showing a device for implementing a method for operating a separation membrane module according to an embodiment of the present invention. Fig. 2 is a flow chart showing a device for operating a method of separation membrane module 45 312 / Invention Specification (Supplement) / 92 · 11/92122684 200404601 which implements another embodiment of the present invention. Fig. 3 is a flowchart showing an apparatus for implementing a method for operating a separation membrane module according to still another embodiment of the present invention. Fig. 4 is a diagram showing an example of the structure of a separation membrane module according to this embodiment. Fig. 5 is a flowchart showing a multi-segment separation membrane device according to an example of this embodiment. Figs. 6 (A) to (C) are another flowcharts showing the multi-segment separation membrane device according to this embodiment. Fig. 7 is a flowchart showing a multi-stage separation membrane device used in Examples 1 to 11; FIG. 8 is a schematic diagram of a conventional reverse osmosis membrane module. FIG. 9 is a flowchart of an example of a conventional multistage separation membrane device. (Description of component symbols) a 1st valve al valve b 2nd valve bl valve c valve cl valve d valve dl valve e valve el valve 46 312 / Instruction Manual (Supplement) / 92-11 / 92122684 200404601 f Raw water flows out Piping valve g valve h valve I valve J valve K valve 1 valve m raw water outflow second piping valve (raw water outflow piping valve in the later stage) 10 reverse osmosis membrane device 1 0 A reverse osmosis membrane module 10a reverse osmosis membrane device 1 0 B Reverse osmosis membrane module at the rear 11 Raw water supply pump 12 Raw water supply first pipe 13 Raw water supply second pipe 14 Permeate water outflow pipe 15 Flow direction changeover pipe 16 Permeate water outflow pipe 17 Concentrated water outflow pipe 18 Return pipe 28 Multi-stage separation membrane unit 29a Front stage separation membrane unit group 29b Rear stage separation membrane unit group 3 0a Separation membrane module 47

312 / Invention Manual (Supplement) / 92-11 / 92122684 794 200404601 30b Separation membrane module 31a Separation membrane device 31b Separation membrane device 31c Separation membrane device 32a Raw water supply first pipe 33a Raw water supply second pipe 34a Permeate water outflow pipe 34b Permeate water outflow pipe 35a Flow direction switching pipe 3 6a Concentrated water outflow first branch pipe 3 6b Concentrated water outflow first pipe 3 7a Concentrated water outflow second branch pipe 37b Concentrated water outflow second pipe 38 Raw water supply main pipe 39 Raw water outflow first pipe 4 0a Raw water supply branched pipe 4 0b Raw water supply branched pipe 4 1 First concentrated water supply main pipe (raw water supply main pipe) 42 Raw water supply second pipe 43 Permeate water outflow pipe 45 Concentrated water outflow in first pipe .4 6 Concentrated water outflow second pipe 4 7 Raw water outflow second pipe (raw water outflow pipe) 48 Separation membrane module 48

312 / Instruction of the invention (Supplement) / 92-11 / 92122684 200404601 50 Pump 5 1 Concentrated water collecting pipe 6 0 Permeate water collecting pipe 6 1 Reverse osmosis membrane 62 Outer body 63 Flange 64 Retractable stop 65 Screw Type membrane element 66 chamber 67 gap 68 salt seal 69 reverse osmosis membrane module 7 1 a ~ 71 d min i separation membrane module 71 e ^ 71 f min i _membrane module 71g separation membrane module 72a separation membrane device group 72b Separation membrane device group 72c, Separation membrane device group 73a, Separation membrane device group 73b, Separation membrane device group 7 4a ~ 74 C Separation and separation J 瞑 Modules 74d, 74 e minutes i] 瞑 Module 75a Separating membrane device group 75b Separating membrane device group 312 / Invention Manual (Supplement) / 92-11 / 92122684

49 200404601 7 6 a, 7 6 b Separation membrane module 7 6c Separation membrane module 77a Separation membrane device group 77b in the front stage 78a Separation membrane module group 78b Separation membrane module 78b Separation membrane module 121 Concentrated water flows out of the second branch Piping

151 Concentrated water flows out of the first branch pipe

312 / Invention Specification (Supplement) / 92-11 / 92122684 50

Claims (1)

200404601 Scope of patent application: 1. A method for operating a separation membrane module is to install a spiral-shaped membrane element composed of a bag-shaped separation membrane and a raw water separator wound around the outer peripheral surface of a water-collecting pipe. The operation method of a separation membrane module is characterized in that the flow direction of raw water of the separation membrane module is changed periodically or irregularly in the opposite direction. 2. The operation method of the separation membrane module according to item 1 of the scope of patent application, wherein when the flow direction of the raw water is changed, a plurality of washings are performed alternately from two directions. 3. For the operation method of the separation membrane module in the second item of the patent application, wherein the first stage of each flushing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing get on. 4. A method for operating a separation membrane module, which is a method for operating a separation membrane module equipped with a spiral membrane element composed of a bag-shaped separation membrane and a raw water separator wound around an outer peripheral surface of a water collecting pipe. It is characterized in that the operation method includes one or more flushes on the way, and the flushing performed in the initial stage of the flushing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. 5. — A method for operating a separation membrane module, which is to concentrate concentrated water in the front stage separation membrane module or separation membrane module group installed with spiral membrane elements arranged in parallel or arranged as one or two or more. A method for operating a two-stage or more multi-segment separation membrane module equipped with a spiral membrane element arranged in one or two or more spiral-type membrane elements in parallel, or a multi-segment separation membrane module of a separation membrane module group, is characterized by: 51 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 Periodically or irregularly, the direction of raw water flow of the separation membrane module is changed in the opposite direction. 6. The operation method of the separation membrane module according to item 5 of the patent application, in which, when the flow direction of the raw water is changed, the washing is repeated several times from two directions. 7. The operating method of the separation membrane module according to item 6 of the patent application, wherein the first stage of each flushing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. get on. 8. —A method for operating a separation membrane module is to concentrate concentrated water in the front section of a separation membrane module or a group of separation membrane modules installed with spiral membrane elements arranged in parallel or arranged as one or two or more. A method for operating a two-stage or more multi-segment separation membrane module equipped with a spiral-type membrane element arranged in one or two or more in parallel, or a multi-stage separation membrane module of a separation membrane module group, is characterized by: The operation method includes one or more flushes on the way. The flushing performed in the first stage of the flushing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. 9. For the operation method of the separation membrane module according to item 8 of the patent application, wherein the above-mentioned washing is divided into each separation membrane module or each separation module group in each stage. 1. A separation membrane membrane device, comprising: a first water supply pipe, which is connected to a raw water supply pump and a first valve; a second water supply pipe, which is connected to a first valve and a separation membrane module; the separation Membrane module; 52 312 / Invention Specification (Supplement) / 92-11 / 92122684 200404601 Permeate water outflow pipe is connected to the permeate water side of the separation membrane module; the flow direction conversion pipe has a connection to the raw water supply section 1 piping and the concentrated water outflow side of the separation membrane module, the concentrated water flows out of the first branch piping and the second valve; and the concentrated water flows out of the second branch piping, branching from the raw water supply to the second piping, and the outflow and the flow direction of the raw water Concentrated water in the case of the opposite direction. 1 1. A multi-stage separation membrane membrane device is a process for sequentially supplying intermediate concentrated water obtained from a separation membrane device or a separation membrane module group of a separation membrane device group in a preceding stage to a separation membrane device or a separation membrane device group in a subsequent stage. The multi-stage separation membrane membrane device of a separation membrane module having two or more stages is characterized in that: the separation membrane device constituting the separation membrane device or the separation membrane device group includes a first water supply pipe and is connected to the first valve; The second supply pipe is connected to the first valve and the separation membrane module; the separation membrane module; the permeate water outflow pipe is connected to the permeate side of the separation membrane module; the flow direction conversion pipe is connected to the raw water supply The first pipe and the concentrated water outflow side of the separation membrane module are provided with a second valve; the concentrated water outflow of the first pipe is connected to the flow direction conversion pipe and a third valve is provided; and the concentrated water is discharged The second pipe is branched from the raw water supply second pipe, and a fourth valve is provided. 53 312 / Invention Specification (Supplement) / 92-11 / 92122684