Forward osmosis membrane and forward osmosis membrane module including the same

Abstract

To provide a practical forward osmosis membrane where physical durability to pressure in a direction to peel a separation function layer from a support membrane is high and performance as the forward osmosis membrane is good.SOLUTION: A forward osmosis membrane is constituted with a support membrane and a separation function layer. The support membrane is provided with at least a porous support and the separation function layer is provided on the porous support. The porous support is provided with a dense layer and a macro void layer in this order from a surface contacting with the separation function layer in a depth direction. The thickness of the dense layer is 1.0-9.5 μm. Macro void exists 0-0.20 piece / μm in a region A having a depth of 0-5.0 μm from a boundary surface between the separation function layer and the porous support and exists 0.04-0.40 piece / μm in a region B having a depth of 5.0-10.0 μm from the boundary surface between the separation function layer and the porous support.SELECTED DRAWING: Figure 2

Description

[Technical field]

[0001] The present invention relates to a forward osmosis membrane and a forward osmosis membrane module including the same. [Background technology]

[0002] Among the techniques for selectively separating liquid mixtures, membrane separation techniques are used in a wide range of fields, such as seawater desalination, ultrapure water production, wastewater treatment, and food industry. Well-known membranes used in membrane separation techniques include microfiltration membranes, ultrafiltration membranes, nanofiltration membranes, and reverse osmosis membranes. However, in recent years, forward osmosis using forward osmosis membranes has been attracting attention. A forward osmosis membrane has at least a separation functional layer and can achieve a high concentration that cannot be achieved by a reverse osmosis membrane. In the forward osmosis method, when a raw liquid and a draw solution with a higher osmotic pressure are brought into contact with each other through a forward osmosis membrane, the osmotic pressure difference that occurs on both sides of the separation functional layer serves as the driving force for the movement of a solvent (e.g., water) from the raw liquid to the draw solution.

[0003] In general, the separation functional layer is often a thin film, and therefore, in order to physically support the separation functional layer, a support membrane such as a porous support or a nonwoven fabric is used, and a composite semipermeable membrane formed by combining this support membrane with the separation functional layer is often used as a forward osmosis membrane. In the forward osmosis method, solutions are placed on both sides of the membrane. Therefore, pressure may be generated in a direction that peels off the separation functional layer from the support membrane. If the physical durability of the composite semipermeable membrane is low, such pressure may cause the separation functional layer to peel off from the support membrane or to break, resulting in a loss of membrane performance.

[0004] In this context, Patent Document 1 discloses a composite forward osmosis membrane having a support membrane and a separation functional layer, in which the support membrane contains a polymer having a specific functional group, and the thickness and compressive strength of the support membrane are set within a specific range, and it is described that this composite forward osmosis membrane is one in which peeling between the support membrane and the separation functional layer is suppressed. Patent Document 2 discloses a composite semipermeable membrane comprising a substrate, a porous support, and a separation functional layer, in which the porous support has a dense layer on the substrate side, and the thickness of the dense layer and the number of macrovoids present between the substrate and the dense layer are within specific ranges, and explains that this composite semipermeable membrane can maintain water permeability even when operated under applied high pressure.

[0005] Patent Document 3 discloses a separation membrane in which a membrane having a separation function is formed on a substrate made of a long-fiber nonwoven fabric. Patent Document 3 explains that by keeping the ratio of macrovoids at the interface between the substrate and the separation membrane within a specific range, it is possible to suppress peeling of the separation membrane from the substrate due to pressure fluctuations during use, etc. Patent Document 4 discloses a composite membrane having a separation functional layer provided on a polysulfone membrane, in which the average pore size, average porosity, and metaphenylenediamine diffusion amount of the layer in the range from the surface to a depth of 1 μm are within specific ranges. It is described that this composite membrane maintains a high salt rejection rate and has high water permeability while reducing the economic burden and the load on waste liquid treatment. Patent Document 5 discloses a separation membrane comprising a substrate made of polyester nonwoven fabric or the like, a support layer containing a polymer having a specific cellulose skeleton, and a polymer matrix layer made of polyamide or the like. This separation membrane is described as having high strength, high porosity, and high hydrophilicity, while also having excellent salt rejection properties. [Prior art documents] [Patent documents]

[0006] [Patent Document 1] International Publication No. 2020 / 059769 [Patent Document 2] JP 2018-039003 A [Patent Document 3] JP 2019-093366 A [Patent Document 4] JP 2011-194272 A [Patent Document 5] JP 2013-022588 A Summary of the Invention [Problem to be solved by the invention]

[0007] However, the composite forward osmosis membrane of Patent Document 1 is not sufficient in physical durability against peeling of the separation functional layer from the support membrane, and is not sufficient in membrane performance as a forward osmosis membrane, and there is room for improvement. The composite semipermeable membrane of Patent Document 2 is a membrane suitable for reverse osmosis, which selectively separates a liquid mixture by applying high pressure with the separation functional layer side as the positive side, and maintains water permeability in reverse osmosis, since the macrovoids in the porous support are not easily crushed during high pressure application. The separation membrane of Patent Document 3 has improved peel strength between the nonwoven fabric substrate and the porous support made of a polymer. The composite membrane of Patent Document 4 has improved performance as a reverse osmosis membrane, even without adding new chemicals after the membrane is manufactured. Furthermore, Patent Documents 2 to 5 do not consider the physical durability of the disclosed membranes against peeling between the support membrane and the separation functional layer, and Patent Documents 2 to 4 do not verify the practical use of the membranes as forward osmosis membranes.

[0008] An object of the present invention is to provide a practical forward osmosis membrane that has high physical durability against pressure in the direction of peeling off the separation functional layer from the support membrane and has good performance as a forward osmosis membrane, and a forward osmosis membrane module including the same. [Means for solving the problem]

[0009] An example of an embodiment of the present invention for achieving the above object is as follows. A forward osmosis membrane comprising a support membrane and a separation functional layer, The support membrane comprises at least a porous support, The separation functional layer is provided on the porous support, The porous support has a dense layer and a macrovoid layer in this order in a depth direction from a surface in contact with the separation functional layer, The macrovoid layer is a layer having macrovoids whose pores have a major axis of 1.0 μm or more, the dense layer is a layer having no macrovoids, The dense layer has a thickness of 1.0 to 9.5 μm, The macrovoids are are present in an area A from the interface between the separation functional layer and the porous support to a depth of 0 to 5.0 μm at a density of 0 to 0.20 particles / μm; and The particles are present at 0.04 to 0.40 particles / μm in a region B extending from the interface between the separation functional layer and the porous support to a depth of 5.0 to 10.0 μm. Forward osmosis membrane. Aspect 2: The forward osmosis membrane according to aspect 1, wherein the macrovoids are present in the region A at a density of 0 to 0.16 voids / μm. Aspect 3: The forward osmosis membrane according to aspect 1 or 2, wherein the macrovoids are present in the region B at 0.06 to 0.30 voids / μm. Aspect 4: The forward osmosis membrane according to any one of aspects 1 to 3, wherein the macrovoids are present in the region A at a density of 0 to 0.12 voids / μm. Aspect 5: The forward osmosis membrane according to any one of aspects 1 to 4, wherein the macrovoids are present in the region B at 0.08 to 0.20 voids / μm. Aspect 6: The forward osmosis membrane according to any one of aspects 1 to 5, wherein the number of the macrovoids in the region B is equal to or greater than the number of the macrovoids in the region A. Aspect 7: The forward osmosis membrane according to any one of aspects 1 to 6, wherein a support membrane of the forward osmosis membrane consists solely of the porous support. Aspect 8: The forward osmosis membrane according to any one of aspects 1 to 7, wherein the dense layer has a thickness of 8.0 μm or less. Aspect 9: The forward osmosis membrane according to any one of aspects 1 to 8, wherein the dense layer has a thickness of 1.5 to 6.0 μm. Aspect 10: The forward osmosis membrane according to any one of aspects 1 to 9, wherein the support membrane is a hollow fiber support membrane. Aspect 11: The forward osmosis membrane according to aspect 10, wherein the hollow fiber support membrane has the dense layer on at least an inner surface of the hollow fiber. Aspect 12: The forward osmosis membrane according to any one of aspects 1 to 11, wherein the forward osmosis membrane has a coefficient of variation of the average thickness of the separation functional layer of 60% or less. Aspect 13: The forward osmosis membrane according to any one of aspects 1 to 12, wherein the forward osmosis membrane has a coefficient of variation of the average thickness of the separation functional layer of 30% or less. Aspect 14: The forward osmosis membrane according to any one of aspects 1 to 13, wherein the porous support comprises one or more selected from polysulfone, polyethersulfone, and derivatives thereof. Aspect 15: The forward osmosis membrane according to any one of aspects 1 to 14, wherein the porous support comprises polysulfone. A forward osmosis membrane module comprising the forward osmosis membrane according to any one of Aspects 1 to 15 housed in a housing. Aspect 17: A hollow fiber membrane comprising at least a porous support, The porous support has a dense layer and a macrovoid layer in this order from an outer surface or an inner surface in a thickness direction of the membrane wall, The macrovoid layer is a layer having macrovoids whose pores have a major axis of 1.0 μm or more, the dense layer is a layer having no macrovoids, The dense layer has a thickness of 1.0 to 9.5 μm, The macrovoids are are present in an area A from the outer surface or inner surface of the porous support to a depth of 0 to 5.0 μm at a density of 0 to 0.20 particles / μm; and The porous support is provided with a region B having a depth of 5.0 to 10.0 μm from the outer or inner surface thereof, and the region B has a diameter of 0.04 to 0.40 μm / μm. Hollow fiber membrane. Aspect 18: The hollow fiber membrane according to aspect 17, wherein the macrovoids are present in region A at a density of 0 to 0.16 voids / μm. Aspect 19: The hollow fiber membrane according to aspect 17 or 18, wherein the macrovoids are present in region B at 0.06 to 0.30 voids / μm. Aspect 20: The hollow fiber membrane according to any one of Aspects 17 to 19, wherein the macrovoids are present in Region A at a density of 0 to 0.12 voids / μm. Aspect 21: The hollow fiber membrane according to any one of Aspects 17 to 20, wherein the number of macrovoids in Region B is equal to or greater than the number of macrovoids in Region A. Aspect 22: The hollow fiber membrane according to any one of Aspects 17 to 21, wherein the hollow fiber membrane consists solely of the porous support. Aspect 23: The hollow fiber membrane according to any one of Aspects 17 to 22, wherein the dense layer has a thickness of 8.0 μm or less. Aspect 24: The hollow fiber membrane according to any one of Aspects 17 to 23, wherein the dense layer has a thickness of 1.5 to 6.0 μm. Aspect 25: The hollow fiber membrane according to any one of Aspects 17 to 24, wherein the hollow fiber membrane has the dense layer at least on an inner surface of the hollow fiber. Aspect 26: The hollow fiber membrane according to any one of Aspects 17 to 25, wherein the porous support comprises one or more materials selected from polysulfone, polyethersulfone, and derivatives thereof. Aspect 27: The hollow fiber membrane according to any one of Aspects 17 to 26, wherein the porous support comprises polysulfone. Aspect 28: The hollow fiber membrane according to any one of Aspects 17 to 27, wherein the hollow fiber membrane is used as a support membrane for a forward osmosis membrane. A hollow fiber membrane module comprising a housing and the hollow fiber membrane according to any one of Aspects 17 to 28 housed therein. 30. A method for producing a double tubular nozzle, comprising the steps of: discharging a spinning dope containing a resin and a solvent from an outer flow passage of the double tubular nozzle; and discharging an internal coagulation liquid from an inner flow passage of the double tubular nozzle; The spinning dope discharged from the outer flow passage of the double tubular nozzle is immersed in an external coagulation liquid through an idle portion to coagulate the dope; and Winding up the solidified spinning dope while applying tension to the spinning dope. Including, The spinning dope contains a resin (polymer) and a solvent, The temperature of the spinning dope discharged from the double tubular nozzle is higher than the temperature of the internal coagulation liquid, and the temperature difference between the two liquids is 5°C or more and less than 35°C. A method for manufacturing hollow fiber membranes. <<Aspect 31>> The manufacturing method described in Aspect 30, wherein the tension is 4 g or more and 60 g or less. <<Aspect 32>> A manufacturing method described in aspect 30 or 31, wherein the temperature of the idling portion is 15°C or higher and 50°C or lower. <<Aspect 33>> The manufacturing method according to any one of Aspects 30 to 32, wherein the relative humidity of the free running portion is 40% or more and 100% or less. Effect of the Invention

[0010] A forward osmosis membrane according to one embodiment of the present invention can have both physical durability in the direction in which the separation functional layer is peeled off from the support membrane and good performance as a forward osmosis membrane. A hollow fiber membrane according to another embodiment of the present invention can be suitably used not only as a support membrane for a forward osmosis membrane, but also as a separation membrane that can exhibit a certain level of water permeability and pressure resistance even when used alone. [Brief description of the drawings]

[0011] [Figure 1] FIG. 1 is a cross-sectional schematic diagram of one embodiment of a hollow fiber membrane module. [Diagram 2] 1 is a scanning electron microscope image of a cross section of the forward osmosis membrane obtained in Example 1. [Diagram 3] Figure 2 is a reference diagram with auxiliary lines added for analysis purposes. [Figure 4] 1 is a scanning electron microscope image of a cross section of the forward osmosis membrane obtained in Comparative Example 1. [Diagram 5] FIG. 4 is a reference diagram with auxiliary lines added for analysis purposes. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0012] An example of this embodiment will be described in detail below. 《Forward osmosis membrane》 The forward osmosis membrane of this embodiment is A forward osmosis membrane composed of a support membrane and a separation functional layer, The support membrane comprises at least a porous support, The separation functional layer is provided on the porous support, The porous support has a dense layer and a macrovoid layer in this order in a depth direction from a surface in contact with the separation functional layer, The macrovoid layer is a layer having macrovoids whose pores have a major axis of 1.0 μm or more, the dense layer is a layer having no macrovoids, The dense layer has a thickness of 1.0 to 9.5 μm, The macrovoids are are present in an area A from the interface between the separation functional layer and the porous support to a depth of 0 to 5.0 μm at a density of 0 to 0.20 particles / μm; and The particles are present at 0.04 to 0.40 particles / μm in a region B extending from the interface between the separation functional layer and the porous support to a depth of 5.0 to 10.0 μm. It is a forward osmosis membrane.

[0013] <Support membrane> The support membrane in the forward osmosis membrane of the present embodiment includes at least a porous support. This support membrane may further include a substrate in addition to the porous support.

[0014] [Base material] The substrate plays a role in providing strength to the support membrane and thus to the forward osmosis membrane. The substrate is preferably porous so as to allow the passage of a solvent. The substrate is composed of, for example, a woven fabric, a nonwoven fabric, a mesh net, a foamed sintered sheet, etc. Examples of the material of the substrate include polymers, and specific examples thereof include polyester, polyamide, polyolefin, etc., and mixtures and copolymers thereof. The substrate is preferably a porous body having a pore size larger than those of the porous support and the separation functional layer. The thickness of the substrate is preferably within the range of 40 to 150 μm in order to balance between ensuring the strength of the support membrane and maintaining the water permeability of the resulting forward osmosis membrane. The substrate is generally a porous body having a pore size larger than that of the porous support and the separation functional layer. The average pore size of the substrate is generally 0.1 to 100 μm. More specifically, it is evaluated by the basis weight and the air permeability. The basis weight of the substrate is 20 to 150 g / m2 The air permeability of the substrate measured by the Frazier method is 0.5 to 30 cc / (cm 2 × sec).

[0015] In this embodiment, it is preferable that the support membrane does not have a substrate, and the forward osmosis membrane is substantially composed of only a porous support and a separation functional layer. A support membrane without a substrate has high diffusibility of the draw solution in the support membrane, and can achieve both high water permeability and low salt back diffusion amount. Here, the forward osmosis membrane "consists essentially of only a porous support and a separation functional layer" does not necessarily mean that the components of the forward osmosis membrane are strictly limited to only a porous support and a separation functional layer, but may also contain optional components other than these, such as a dispersant, a hydrophilizing agent, a coating agent, a moisturizing agent, a storage solution for the separation membrane, etc. These optional components may be inorganic compounds or organic compounds.

[0016] [Porous support] The porous support plays a role in providing strength to the separation functional layer. The porous support may have a separation performance of solvent-insoluble particles, etc., but preferably does not substantially have a separation performance of ions dissolved in a solvent. The fact that the porous support does not substantially have a separation performance means that the separation performance of ions, etc. when the porous support is used as a forward osmosis membrane is lower than the separation performance of the ions, etc. when the separation functional layer is used as a forward osmosis membrane. In this embodiment, the porous support has a dense layer and a macrovoid layer in this order from the surface in the thickness direction of the membrane wall.

[0017] (Dense layer) The dense layer is thought to assist in the formation of a uniform separation functional layer when it is formed on a porous support, and also has the function of maintaining the water permeability within an appropriate range when made into a forward osmosis membrane. The separation functional layer in the forward osmosis membrane of this embodiment is formed, for example, by interfacial polymerization of a polyfunctional amine and a polyfunctional acid halide, as described below. The dense layer retains and releases the polyfunctional amine solution supplied when forming the separation functional layer. This not only plays a role in supplying the polyfunctional amine solution to the polyamide polymerization site (the interface between the polyfunctional amine solution and the polyfunctional acid halide solution), but also plays a role as a starting point for the growth of pleats in the separation functional layer. Furthermore, the separation functional layer is formed by penetrating the fine irregularities of the dense layer, thereby enhancing the adhesion between the separation functional layer and the support membrane, and when pressure is applied to the separation functional layer in a direction in which it is peeled off from the support membrane, the pressure is evenly distributed and alleviated. If the dense layer is uniform, the advantageous effects such as the water permeability retention function and high adhesion between the separation functional layer and the support membrane are manifested not only in a part of the membrane but throughout the entire membrane, which is preferable. Also, if the dense layer is uniformly formed, when the forward osmosis membrane of the present embodiment is used as a module, the advantageous effects described above are manifested throughout the entire module, which is preferable. The dense layer being uniform means that the parameters such as thickness, pore size, etc. are within a predetermined range, regardless of the location of the dense layer, and the dense layer being uniform in a module means that the above parameters are within a predetermined range, regardless of the location of any forward osmosis membrane in the module.

[0018] In order to efficiently retain and release the polyfunctional amine solution, the dense layer preferably has interconnected pores. The dense layer is a layer that does not have macrovoids, which will be described later. As described later, macrovoids are holes with a major axis of 1.0 μm or more. Therefore, the dense layer refers to a layer that does not have holes, or, if it has holes, the major axis of the holes contained therein is less than 1.0 μm. The major axis of the holes contained in the dense layer is preferably 0.5 μm or less. The dense layer preferably contains pores with a major axis of less than 1.0 μm. The major axis of the pores contained in the dense layer is preferably 0.001 μm or more in order to suitably perform the above-mentioned role. The dense layer has a thickness of 1.0 to 9.5 μm, preferably 1.5 to 9.0 μm, more preferably 2.0 to 8.0 μm, even more preferably 2.5 to 7.5 μm, particularly preferably 3.0 to 7.0 μm, and particularly preferably 3.5 to 6.0 μm. When the dense layer has the above thickness, it can fulfill the above role and is preferable in that it can ensure water permeability because it does not significantly impede the permeation of the solvent.

[0019] The dense layer is preferably located on the outermost surface of the porous support. When the dense layer is located on the outermost surface of the porous support, the formation of the separation functional layer can be facilitated and defects can be reduced, and even when the porous support itself is used as a separation membrane, contamination of the inside of the membrane can be prevented while maintaining a high degree of separation function. When the porous support is in the form of hollow fibers, the dense layer is preferably present on the inner surface of at least the hollow fibers of the porous support. In the present embodiment, a plurality of dense layers may be present. When the porous support has a plurality of dense layers, it is preferable that a dense layer is present on each of the outermost surfaces on both sides of the porous support, for example.

[0020] In this embodiment, the dense layer in the support membrane is a layer that contacts the separation functional layer. However, when preparing the porous support constituting the support membrane, it is possible that the macrovoids accidentally reach the surface of the porous support and contact the separation functional layer. In this case, the layer that contacts the separation functional layer may be a macrovoid layer. However, in order to more advantageously exert the effect of this embodiment, it is preferable that the dense layer exists on most of the surface of the porous support that contacts the separation functional layer. This requirement can be confirmed by observing the cross section of the porous support under the conditions described below, where the number of cross-sectional images in which the macrovoids reach the surface of the porous support is 50% or less of the number of cross-sectional images observed. This ratio is most preferably 0%. In this way, when the macrovoids accidentally reach the support membrane surface, the term "interface between the separation functional layer and the dense layer" in this specification can be read as "interface between the separation functional layer and the support membrane" in a broader sense and applied.

[0021] (Macrovoid layer) The macrovoid layer is a layer containing voids (macrovoids) having a major axis of 1.0 μm or more. The thickness of the macrovoid layer is preferably 5 to 300 μm. The macrovoid layer may reach the surface on the opposite side of the porous support, or, if another dense layer exists on the surface on the opposite side of the porous support, may extend to the dense layer. The size and shape of the macrovoids are not particularly limited as long as they have a major axis of 1.0 μm or more. However, from the viewpoint of achieving both improved water permeability inside the porous support membrane and durability against pressure application (pressure resistance), the major axis of the macrovoids is preferably 200 μm or less, more preferably 150 μm or less, even more preferably 120 μm or less, and may be 100 μm or less or 80 μm or less. From the same viewpoint, the minor axis of the macrovoids is preferably 50 μm or less, more preferably 40 μm or less, even more preferably 30 μm or less, particularly preferably 20 μm or less, and may be 10 μm or less. The macrovoid layer contains macrovoids with a long diameter of 1.0 μm or more, and it is preferable that the average long diameter and average short diameter calculated for all macrovoids contained in the macrovoid layer are each within the above-mentioned ranges, and it is more preferable that the long diameter and short diameter of all macrovoids contained in the macrovoid layer are each within the above-mentioned ranges. If the long or short diameter of the macrovoids is larger than the range described above, the pressure resistance of the porous support membrane may be impaired, or the porous support membrane may deform during use, thereby impairing the expected performance. According to the study by the present inventors, the cross section of the macrovoid is often approximately elliptical. Furthermore, the major axis direction of the macrovoid is often approximately perpendicular to the interface direction with the dense layer inside the macrovoid layer. When the cross section of the macrovoid is approximately elliptical, the major axis means the length of the major axis of the ellipse, and the minor axis means the length of the minor axis of the ellipse.

[0022] (Area A and Area B, and the number of macrovoids in these areas) In the forward osmosis membrane of this embodiment, the range from a depth of 0 to 5.0 μm from the interface between the separation functional layer and the dense layer (the interface between the separation functional layer and the support membrane) is defined as "Region A", and the range from a depth of 5.0 to 10.0 μm from the interface between the separation functional layer and the dense layer (the interface between the separation functional layer and the support membrane) is defined as "Region B". Here, macrovoids having a major axis of 1.0 μm or more are present in the surface direction (the direction parallel to the film surface direction as shown in FIG. 2) at 0 to 0.20 voids / μm in region A. The number of macrovoids in region A is preferably 0 to 0.16 voids / μm, more preferably 0 to 0.12 voids / μm, and even more preferably 0.02 to 0.10 voids / μm. The number of macrovoids in region B is 0.04 to 0.40 / μm in the plane direction. The number of macrovoids in region B is preferably 0.06 to 0.30 / μm, more preferably 0.08 to 0.20 / μm, and even more preferably 0.10 to 0.19 / μm. The number of macrovoids in region B is preferably equal to or greater than the number of macrovoids in region A, and more preferably greater than the number of macrovoids in region A.

[0023] In this embodiment, the number of macrovoids in region A and region B satisfies these specific numerical ranges, thereby improving the adhesion between the separation functional layer and the support membrane. Furthermore, when pressure (back pressure) is applied in a direction in which the separation functional layer is peeled off from the support membrane, the pressure can be evenly distributed and alleviated, and high durability can be achieved. This is preferable because it allows greater freedom in device design, operating conditions, etc. when used as a forward osmosis membrane. Furthermore, a support membrane having the number of macrovoids in region B falling within the above-mentioned specific numerical range maintains the diffusibility of the draw solution within the support membrane when used as a forward osmosis membrane while maintaining physical durability, which improves the water permeability as a forward osmosis membrane, and as a result, enables highly efficient treatment of the solution. When the regions A and B of the porous support each have the above-mentioned specific number of macrovoids, the carrier of the porous support may be used as a separation membrane. In this case, by satisfying the above-mentioned requirement for the number of macrovoids in region A, both improvement in the separation performance of the membrane and reduction in contamination inside the membrane are achieved. Also, by satisfying the above-mentioned requirement for the number of macrovoids in region B, both high water permeability and high strength are achieved.

[0024] (Measurement of the thickness of the dense layer and the number of macrovoids in areas A and B) Whether or not the porous support satisfies the above conditions can be confirmed as follows. Cut the support membrane or forward osmosis membrane perpendicular to the membrane surface at any point to obtain a cross section. Observe this cross section under a microscope to obtain a cross section image with a width of at least 5 μm. In this cross section image, look for voids (macrovoids) with a major axis of 1.0 μm or more. If there is a macrovoid with a long diameter of 1.0 μm or more in the cross-sectional image, measure the shortest distance between the part (apex) of the outer edge of the macrovoid closest to the separation functional layer and the separation functional layer, and use this distance as the thickness of the dense layer. If there are multiple voids in the cross-sectional image, select the void whose apex is closest to the separation functional layer, measure the distance between the apex of that void and the separation functional layer, and use this distance as the thickness of the dense layer. If there are no voids with a major axis of 1.0 μm or more in the cross-sectional image, reduce the observation magnification and repeat the microscope observation with a wider field of view. If no voids with a major axis of 1.0 μm or more are still found, obtain up to 50 images at different locations, and use the 9 images with the greatest number of macrovoids in area B to calculate the average value.

[0025] The range from 0 to 5.0 μm deep from the interface between the separation functional layer and the dense layer is defined as "Region A," and the range from 5.0 to 10.0 μm deep from the interface between the separation functional layer and the dense layer is defined as "Region B." In these regions A and B, the number of macrovoids with a pore length of 1.0 μm or more is counted, and the number is divided by the width of the cross-section of the observed membrane to calculate the number of macrovoids in each of regions A and B.

[0026] The thickness of the dense layer and the number of macrovoids in regions A and B are measured with n=9, and the average is taken as the measured value. That is, nine membrane samples are prepared, and the above-mentioned operations are carried out for each sample, and each value is calculated as the average. The locations where the nine samples are taken may be appropriately set in accordance with the measurement of the coefficient of variation of the average thickness of the separation functional layer described below. For each membrane sample, the thickness of the dense layer of the porous support in the support membrane and the number of macrovoids in regions A and B can be measured by observing the interface where the porous support in the support membrane is in contact with the separation functional layer, or near the surface of the support membrane, using a scanning electron microscope or a transmission electron microscope.

[0027] An example of observation using a scanning electron microscope will be described below. In the case of a cross-sectional image taken with a scanning electron microscope, for example, a specimen can be prepared and observed as follows. The membrane sample is immersed in pure water, frozen using liquid nitrogen, and then dried by freeze-drying. The dried sample is cut or cut by broad ion beam (BIB) processing, preferably by BIB processing, to prepare a cross section perpendicular to the membrane surface direction. The obtained cross section is thinly coated with platinum, platinum / palladium, osmium tetroxide, or osmium, preferably osmium, to prepare an observation sample. The cross section of the observation sample is observed at an acceleration voltage of 1 to 6 kV, preferably 1 kV. The observation magnification may be any magnification that allows observation of the contact interface between the porous support and the separating functional layer, or the vicinity of the surface of the support membrane, and is, for example, preferably 1,000 to 20,000 times, more preferably 5,000 times.

[0028] From the obtained electron microscope photograph (cross-sectional image), the thickness of the dense layer, the size of the voids, etc. can be directly measured using a scale, and each value can be calculated using the above-mentioned procedure. Each measured value can be obtained as an average value in a measurement range of about 5 to 100 μm in cross section width, which is preferably 10 to 50 μm, more preferably 20 to 30 μm, and most preferably 25 μm.

[0029] In this embodiment, the contact interface between the porous support of the forward osmosis membrane and the separating functional layer can be specifically confirmed, for example, as follows. An example of the method is to import an image of a cross section of a forward osmosis membrane taken by a scanning electron microscope into a suitable image processing software and process the image. An example of the image processing software is ImageJ (developed by the National Institutes of Health, USA). The SEM image imported into ImageJ is binarized by a known binarization method, preferably the Otsu method, appropriately selected based on the obtained image. In the entire binarized image obtained, the average brightness in the horizontal direction to the membrane surface is calculated for each predetermined distance (for example, 1 pixel) from the membrane surface toward the depth direction. The average brightness is compared from the surface of the separation functional layer toward the support membrane side, and the horizontal direction of the part with the highest average brightness can be the contact interface between the porous support of the forward osmosis membrane and the separation functional layer. It is preferable to observe the forward osmosis membrane so that the surface of the separation functional layer is as horizontal as possible within the field of view. The observation magnification of the cross-sectional image is, for example, preferably 1,000 to 20,000 times, more preferably 5,000 times. The width of the cross section (the length in the direction parallel to the interface between the support membrane and the separation functional layer) can be 5 to 100 μm, preferably 10 to 50 μm, more preferably 20 to 30 μm, and most preferably 25 μm. Furthermore, even if the contact interface between the porous support of the forward osmosis membrane and the separation functional layer is wavy, the contact interface between the porous support of the forward osmosis membrane and the separation functional layer can be unambiguously identified by the above-mentioned method, unless the forward osmosis membrane is intentionally bent for observation.

[0030] (Porous support material) The material of the porous support is not particularly limited. However, from the viewpoint of ease of molding, the porous support is preferably formed from a resin, and more preferably from a thermoplastic resin. Here, the thermoplastic resin refers to a material made of a chain polymer, which exhibits the property of deforming or flowing when heated by an external force. Examples of thermoplastic resins include polysulfone, polyethersulfone, polyketone, polyamide, polyester, cellulose polymer, vinyl polymer, polyphenylene sulfide, polyphenylene sulfide sulfone, polyphenylene sulfone, polyphenylene oxide, etc., and these homopolymers or copolymers can be used alone or in a blend of two or more. In addition, derivatives of these polymers having any functional group in the main chain, side chain, or end can also be used as the resin constituting the porous support.

[0031] Here, examples of the cellulose polymer that can be used include cellulose acetate and cellulose nitrate, and examples of the vinyl polymer that can be used include polyethylene, polypropylene, polyvinyl chloride, chlorinated vinyl chloride, polyacrylonitrile, etc. Among these, one or more selected from polysulfone, polyacrylonitrile, polyamide, polyester, polyvinyl alcohol, polyphenylene sulfide sulfone, polyphenylene sulfone, polyphenylene sulfide, polyether sulfone, polyvinylidene fluoride, cellulose acetate, polyvinyl chloride, and chlorinated vinyl chloride are preferred. More preferred are cellulose acetate, polysulfone, polyethersulfone, polyketone, and polyacrylonitrile. Of these materials, polysulfone or polyethersulfone is preferred because of its high chemical, mechanical, and thermal stability and ease of molding. The porous support preferably contains the resins listed above or their derivatives as the main component. The term "main component" as used herein means that the resin is contained in an amount of 50% by mass or more based on the total mass of the porous support. In terms of ease of pore size control, polysulfone is more preferred as the material for the porous support.

[0032] (Thickness and shape of porous support) When the support membrane has a composite structure of a substrate and a porous support, the thickness of the porous support is preferably 0.02 to 0.10 mm from the viewpoint of achieving both water permeation resistance and strength. On the other hand, when the support membrane consists of only a porous support, from the viewpoint of achieving both water permeation resistance and strength, the thickness of the porous support is preferably 0.05 to 3.00 mm, more preferably 0.10 to 1.00 mm, and even more preferably 0.15 to 0.50 mm. When the support membrane is composed of only a porous support, the porous support is preferably in the form of a film (flat membrane), a tube, a hollow fiber, or the like, and may be in the form of a chemically or physically modified form of these. The porous support is more preferably in the form of a hollow fiber, since it is possible to store a membrane with a larger membrane area in a smaller space. Here, "hollow fiber" means a hollow tube shape with an outer diameter of approximately 5 mm or less, and "tube" means a hollow tube shape with an outer diameter of approximately more than 5 mm.

[0033] [Properties of the supporting film] The physical properties of the support membrane can be expressed by pure water permeability, compressive strength, and the like. Some of these physical properties can be measured in the state of a supported membrane module in which a single or multiple supported membranes are housed in a housing; they can be measured in the state of a supported membrane removed by dismantling the supported membrane module; and they can be measured in the state of a forward osmosis membrane with the separation functional layer removed using known techniques, to the extent that the properties of the support membrane are not significantly impaired. The physical properties are measured by the methods described in the Examples below.

[0034] [Pure water permeability] From the viewpoints of achieving both water permeation resistance and membrane strength, and facilitating the formation of a suitable separation functional layer, the pure water permeability of the hollow fiber support membrane is preferably 10 to 1000 (kg / (m 2 ×hr×bar), and more preferably 50 to 700 (kg / (m 2×hr×bar), and more preferably 100 to 700 (kg / (m 2 ×hr×bar), and particularly preferably 300 to 600 (kg / (m 2 ×hr×bar). [Compressive strength] From the viewpoint of imparting practical strength to the support membrane and achieving both water permeation resistance and strength, the compressive strength of the hollow fiber support membrane is preferably 0.25 to 1.5 MPa, more preferably 0.40 to 1.2 MPa, and even more preferably 0.50 to 1.0 MPa. By having the compressive strength of the support membrane within the above range, the performance of the forward osmosis membrane can be more reliably maintained. If the compressive strength is too high, the cross-sectional structure of the membrane is often too dense, and the water permeation resistance and internal concentration polarization become large. In this case, the water permeability as a forward osmosis membrane tends to decrease. In order to increase the compressive strength of the support membrane, it is effective to increase the polymer concentration during the formation of the porous support and to increase the thickness of the support membrane.

[0035] [Inner and outer diameter of hollow fiber support membrane] When the support membrane is a hollow fiber support membrane, the inner diameter and outer shape of the hollow fiber support membrane are not particularly limited. However, in consideration of the membrane production stability, ease of handling, membrane area when made into a module, etc., the outer diameter is preferably 0.10 to 3.00 mm and the inner diameter is 0.03 to 2.50 mm, and the outer diameter is more preferably 0.20 to 1.50 mm and the inner diameter is 0.10 to 1.00 mm. Furthermore, in consideration of compatibility between the ability to pass a raw material solution containing a hardly soluble substance through the hollow portion without any hindrance and strength, the outer diameter is preferably 0.50 to 1.35 mm and the inner diameter is 0.25 to 1.00 mm. The membrane thickness of the hollow fiber support membrane is preferably 0.02 to 1.00 mm from the viewpoint of strength, more preferably 0.05 to 0.50 mm from the viewpoint of achieving both strength and ease of handling, and further preferably 0.10 to 0.35 mm from the viewpoint of achieving both water permeation resistance and strength, and from the viewpoint of solution diffusibility in the membrane thickness portion (membrane wall portion) when used as a forward osmosis membrane.

[0036] [Separation functional layer] The separation functional layer essentially performs the function of separating solutes in the forward osmosis membrane. More specifically, it performs the function of separating the solvent in the liquid mixture from the solutes, such as ions, dissolved in the solvent. The composition, thickness, etc. of the separation functional layer are set according to the intended use of the forward osmosis membrane. The separation functional layer is disposed on the surface of the support membrane. If the support membrane has a front and back surface, it is preferable that the separation functional layer is disposed on either the front or back surface. However, the separation functional layer may be disposed on both sides of the support membrane or inside the pores of the support membrane. The separation functional layer may be present on only one side of the support membrane or on both sides of the support membrane. When the separation functional layer is present on both sides of the support membrane, the thickness, separation performance, salt blocking performance, etc. of each side may be the same or different.

[0037] When separation functional layers are disposed on both sides of the support membrane, the "separation functional layer side" in the present disclosure means the side of the layer that rejects the solute with a higher rejection rate in the entire forward osmosis membrane. The following method, for example, can be used to know the side that rejects the solute with a higher rejection rate. The amount of salt back-diffusion into the feed solution is evaluated when purified water is placed as the feed solution on one side of a forward osmosis membrane and the draw solution is placed on the other side, and when the arrangement of these solutions is reversed. When comparing these two evaluation results, the feed solution side with the arrangement that results in the smaller amount of salt back-diffusion can be the side that blocks the solutes of the draw solution with higher efficiency (the separation functional layer side). Here, as the draw solution, a 3.5% by mass aqueous sodium chloride solution or a 50% by mass aqueous isopropanol solution can be used, and it is preferable to use a 3.5% by mass aqueous sodium chloride solution.

[0038] Examples of materials for the separation functional layer include one or more selected from the group consisting of high molecular weight polymers, inorganic substances, organic-inorganic hybrid compounds, and compositions in which a specific inorganic or organic compound is dispersed or dissolved. The separation functional layer made of a high molecular weight polymer has a substantial separation performance, preferentially allowing the permeation of a solvent and blocking the permeation of a solute. Suitable examples of the high molecular weight polymer constituting such a separation functional layer include polyamide, polyvinyl alcohol, sulfonated polyethersulfone, polypiperazine amide, polyimide, and composite materials made of two or more of these materials.

[0039] [Polyamide separation layer] In this embodiment, a polyamide separation functional layer mainly composed of polyamide is preferably used from the viewpoint of easily forming a defect-free thin film on the porous support. Here, "mainly composed of polyamide" means a separation functional layer in which the mass ratio of polyamide to the total mass of the separation functional layer is 50 mass% or more, 75 mass% or more, or 95 mass% or more. The mass ratio of polyamide to the total mass of the separation functional layer may be 100 mass%. The polyamide separation functional layer is preferably a polycondensation product of a polyfunctional amine and a polyfunctional acid halide. The formation of the polyamide separation functional layer includes forming a polyamide skeleton by performing interfacial polycondensation on the surface of the porous support using an aqueous solution containing a polyfunctional amine and an organic solvent solution containing a polyfunctional acid halide. The organic solvent in the organic solvent solution containing the polyfunctional acid halide is preferably an organic solvent immiscible with water. The method for forming the polyamide separating functional layer will be described in detail later.

[0040] [Average thickness of separation functional layer] The average thickness of the separation functional layer is preferably as thin as possible without pinholes. However, in order to maintain mechanical strength and chemical resistance, it is desirable for the layer to have an appropriate thickness. Considering the film formation stability, water permeation resistance, etc., the average thickness of the separation functional layer (polymer thin film) made of a polymer is preferably 0.01 to 3 μm, more preferably 0.05 to 1 μm.

[0041] The average thickness of the separation functional layer is measured by microscopic observation. Specifically, for example, the separation membrane is embedded in a resin, and then cut to prepare ultrathin slices. The obtained slices are stained and observed with a transmission electron microscope (TEM) or a scanning electron microscope (SEM). A preferred method for measuring the thickness of the membrane is to import an image of a cross section of the separation functional layer in the thickness direction taken with a scanning electron microscope into a suitable image processing software and process the image. An example of the image processing software is ImageJ (developed by the National Institutes of Health). The outline of the separation functional layer is extracted from the SEM image imported into ImageJ, and the inside is filled in to calculate the area of ​​the separation functional layer, which can be converted into the average thickness of the separation functional layer in one image using a calibration curve prepared in advance. More specifically, the contour of the separation functional layer is extracted by, for example, binarizing the SEM image imported into ImageJ by a known binarization method, preferably the Otsu method, appropriately selected based on the obtained image. The contour at the contact interface between the porous support of the forward osmosis membrane and the separation functional layer is calculated by calculating the average brightness in the horizontal direction to the membrane surface at every predetermined distance (for example, 1 pixel) from the membrane surface in the depth direction in the entire obtained binarized image. The average brightness is compared from the surface of the separation functional layer toward the support membrane side, and the horizontal direction of the part with the highest average brightness is the contact interface between the porous support of the forward osmosis membrane and the separation functional layer, and the straight part is the contour. Regarding the contour of the surface of the separation functional layer, a curve obtained by connecting parts of the obtained binarized image that have a contrast difference with the background with a continuous line can be regarded as the contour of the surface of the separation functional layer. The contour of the thickness direction of the separation functional layer may be both ends of the obtained image. By connecting these lines, the contour of the separation functional layer can be extracted.

[0042] The observation magnification of the cross-sectional image is, for example, preferably 5,000 to 30,000 times, more preferably 10,000 times. The width of the cross section (the length in the direction parallel to the interface between the support membrane and the separation functional layer) is preferably about 5 to 100 μm, more preferably 5 to 50 μm, even more preferably 5 to 20 μm, and most preferably 13 μm. Furthermore, even if the contact interface between the porous support of the forward osmosis membrane and the separation functional layer is wavy, the contact interface between the porous support of the forward osmosis membrane and the separation functional layer can be unambiguously identified by the above-mentioned method, unless the forward osmosis membrane is intentionally bent for observation.

[0043] [Variation coefficient of average thickness of separation functional layer] In this embodiment, it is preferable that the coefficient of variation of the average thickness of the separation functional layer of the forward osmosis membrane is within a specific range. In this embodiment, the coefficient of variation is a value obtained by dividing the standard deviation of the average thickness by the average value of the average thickness, and is expressed as a percentage (%). The coefficient of variation of the average thickness of the separation functional layer is preferably 0 to 60%, more preferably 0 to 50%, even more preferably 0 to 40%, particularly preferably 0 to 30%, and most preferably 0 to 20%, from the viewpoints that partial functional defects of the separation functional layer are more effectively eliminated in the process of forming the separation functional layer and the effect of the heat treatment described below is enhanced.

[0044] In this embodiment, a preferred method for measuring the average thickness and the coefficient of variation of the separation functional layer is as follows. The hollow fiber membrane is divided into three equal parts in the longitudinal direction to obtain three samples. A cross section perpendicular to the membrane surface direction (longitudinal direction) is obtained at any location of these three samples, preferably at a portion where each sample is divided into two equal parts in the longitudinal direction, and observed under a microscope to measure the average thickness of the separation functional layer in each image. This operation is performed for three forward osmosis membranes or three forward osmosis membranes cut out from one forward osmosis membrane module, and the average thickness of the separation functional layer is measured in a total of nine images. The nine average thickness values ​​obtained are used to calculate the average value of the average thickness and the standard deviation of the average thickness, and the coefficient of variation is calculated from these values. When cutting out three forward osmosis membranes from one forward osmosis membrane module, it is preferable to cut them out from three locations in the radial direction of the forward osmosis membrane module: the outer periphery, the middle, and the center. By using such a cutting method, the variation of the entire module can be evaluated. In the case of a flat forward osmosis membrane, the membrane can be divided into nine parts to obtain nine samples, and a cross section can be obtained from the center of each sample, followed by microscopic observation.

[0045] The field of view of the microscope image when measuring the average thickness etc. of the separation functional layer is preferably about 5 to 100 μm, more preferably 5 to 50 μm, even more preferably 5 to 20 μm, and most preferably 13 μm, in cross-sectional width (length in a direction parallel to the interface between the support membrane and the separation functional layer). The magnification of the microscope image is preferably 5,000 times to 30,000 times, and more preferably 10,000 times.

[0046] In the forward osmosis membrane of the present embodiment, the structures of the support membrane and the separation functional layer are preferably uniform within the above-mentioned ranges. If the structures of the separation functional layer and the support membrane located close to the separation functional layer are uniform, the separation functional layer can exhibit the expected function and physical durability in any part of the separation functional layer. For example, in the case of a hollow fiber forward osmosis membrane, the structure of the forward osmosis membrane is preferably more uniform in at least one of the circumferential and longitudinal directions, more preferably more uniform in both the circumferential and longitudinal directions, and particularly preferably more uniform in all parts of the membrane when the hollow fibers are bundled together to form a module.

[0047] [Forward osmosis membrane and forward osmosis evaluation] The forward osmosis membrane of the present embodiment has high water permeability (Flux) and low salt back diffusion rate (RSF). The water permeability and salt back-diffusion amount of the forward osmosis membrane of this embodiment are evaluated by performing a forward osmosis treatment using purified water as the feed solution and a 3.5 mass% sodium chloride aqueous solution as the draw solution, with each solution at 25°C. When a forward osmosis membrane has a structure having a support membrane and a separation functional layer arranged on one side of the support membrane, the water permeability may vary significantly depending on whether the raw material liquid and the derivative solution are arranged on the separation functional layer side or the support membrane side, respectively. In this embodiment, when the forward osmosis membrane is put into practical use, in order to reduce the risk of contamination of the membrane, it is desirable to place the raw material solution on the separation functional layer side and the draw solution on the support membrane side. When evaluating the water permeability and salt back-diffusion amount of the forward osmosis membrane, it is desirable to place the raw material solution on the separation functional layer side and the draw solution on the support membrane side, so as to reflect the performance in practical use.

[0048] The salt back diffusion capacity of a forward osmosis membrane means the amount of draw solute that moves from the draw solution to the raw solution when the feed solution is placed on the separation functional layer side of the forward osmosis membrane and the draw solution with a higher osmotic pressure is placed on the support membrane side. The salt back diffusion capacity (RSF) is defined by the following formula (1). RSF = G / (M × H) (1) Here, G is the amount of lead solute transferred (g), and M is the effective membrane area of ​​the forward osmosis membrane (m 2 ) and H is time (hr). The lower the salt back diffusion capacity (RSF) of the forward osmosis membrane of this embodiment, the more preferable. The larger the salt back diffusion capacity, the greater the amount of draw solutes in the draw solution that are mixed into the feed solution; the greater the amount of solutes in the feed solution that are mixed into the draw solution; the purity of the feed solution concentrate decreases, causing a loss of component balance; the draw solution becomes contaminated; the draw solution becomes less rich in components over time; and the like. In one embodiment, the salt back diffusion capacity of the forward osmosis membrane of this embodiment is 2.0 g / (m 2 ×hr), and preferably 1.2 g / (m 2 ×hr), and more preferably 0.80 g / (m 2 ×hr), and more preferably 0.40 g / (m 2 ×hr), and particularly preferably 0.30 g / (m 2 From the viewpoint of ease of manufacturing the forward osmosis membrane, the salt back diffusion amount R of the forward osmosis membrane of this embodiment is 0.001 g / (m 2× hr) or more, and even if the salt back-diffusion amount R is within this range, the advantageous effects expected by the present invention are exhibited.

[0049] The permeability (flux) of a forward osmosis membrane means the amount of water that moves from the raw liquid to the draw solution when the raw liquid is flowed on the separation functional layer side of the forward osmosis membrane and a draw solution with a higher osmotic pressure is placed on the support membrane side. The permeability (flux) of a forward osmosis membrane is defined by the following formula (2). Flux=L / (M×H) (2) where L is the amount of water that has permeated (kg) and M is the effective surface area of ​​the forward osmosis membrane (m 2 ) and H is time (hr). The higher the water permeability (Flux) of the forward osmosis membrane of the present embodiment, the more preferable. From the viewpoint of achieving highly efficient solvent transfer, the water permeability of the forward osmosis membrane is 1.0 kg / (m 2 ×hr), and more preferably 3.0 kg / (m 2 ×hr) or more, and more preferably 5.0 kg / (m 2 ×hr), and particularly preferably 7.0 kg / (m 2 On the other hand, if the permeability is too high, the amount of back-diffusion of salts may become large. Therefore, the permeability of the forward osmosis membrane is set at 50 kg / (m 2 × hr) or less.

[0050] In this embodiment, the salt permeability RSF / Flux (unit: g / kg) is defined as the value obtained by dividing the salt back diffusion amount (RSF) by the permeability (Flux), and is an index that indicates the selectivity between the permeation of the solvent and the permeation of the salt. The lower the salt permeability value, the more difficult it is for the salt to permeate and the more easily the solvent can permeate. Therefore, the lower this value, the more preferable it is. In conventional forward osmosis membranes, when the amount of salt back diffusion is low, the water permeability is often significantly low, and as a result, the RSF / Flux value is often high. However, the forward osmosis membrane of the present embodiment shows a sufficiently low RSF / Flux value. From the viewpoint of practicality of concentrating the raw material liquid and highly efficient solvent transfer, the RSF / Flux value of the forward osmosis membrane of this embodiment is preferably 0.20 g / kg or less, more preferably 0.16 g / kg or less, even more preferably 0.08 g / kg or less, particularly preferably 0.06 g / kg or less, and most preferably 0.04 g / kg or less. The RSF / Flux value is ideally 0 g / kg, but from the viewpoint of ease of manufacturing the forward osmosis membrane, it may be, for example, 0.0001 g / kg or more.

[0051] In this embodiment, the physical durability of the forward osmosis membrane can be evaluated by applying a predetermined transmembrane pressure difference and performing a forward osmosis process. The transmembrane pressure difference may be applied with either side of the forward osmosis membrane as the positive side. However, for example, by applying a transmembrane pressure difference with the support membrane side and the draw solution side of the forward osmosis membrane as the positive side to perform forward osmosis evaluation, both the forward osmosis membrane performance and physical durability can be evaluated simultaneously. In this case, pressure is applied in the direction of peeling the separation functional layer from the support membrane. Therefore, if the physical durability of the forward osmosis membrane is low, it may not be able to withstand this pressure, and a part of the separation functional layer may peel off from the support membrane, or a part of the separation functional layer may crack. In this case, the separation functional layer is irreversibly altered, and the draw solution becomes more likely to permeate to the raw material liquid side, and as a result, the salt back diffusion amount and salt permeability values ​​become significantly large. Therefore, by performing a forward osmosis process while applying a predetermined transmembrane pressure difference and measuring the amount of salt back diffusion and salt permeability, the degree of physical durability of the forward osmosis membrane, particularly the separation functional layer, can be examined.

[0052] A specific method for evaluating the physical durability of a forward osmosis membrane is, for example, as follows. First, purified water is used as the raw material liquid, and a 3.5% by mass aqueous solution of sodium chloride is used as the draw solution. Each solution is subjected to forward osmosis treatment for 5 minutes or more at 25°C under a standard pressure of 20 kPa, with the support membrane side and the draw solution side being positive, to determine the water permeability and salt back diffusion amount, which are used as the standard value. Next, the forward osmosis membrane is thoroughly washed with water, and the transmembrane pressure difference is changed to a predetermined pressure higher than the standard pressure, and forward osmosis treatment is performed under the same conditions except for the above, to determine the water permeability (Flux) and salt back diffusion amount (RSF). After washing the forward osmosis membrane with water again, forward osmosis treatment is performed under the above standard pressure, and the water permeability (Flux) and salt back diffusion amount (RSF) are determined. These values ​​are the water permeability and salt back diffusion amount after the application of a predetermined transmembrane pressure difference, and the value of RSF / Flux after the application of a predetermined pressure is calculated.

[0053] The performance maintenance rate (%) after application of a predetermined pressure can be evaluated as the percentage of the reference value RSF / Flux divided by the RSF / Flux after application of a predetermined pressure. In the forward osmosis membrane of this embodiment, the performance maintenance rate after application of a predetermined transmembrane pressure difference is preferably 40% or more, and more preferably 50% or more. However, although it is generally believed that the smaller the RSF / Flux value, the better the performance of the forward osmosis membrane, the RSF / Flux value often changes when the membrane undergoes structural or compositional changes, and therefore it may not always be appropriate to compare the physical durability of a forward osmosis membrane with the performance retention rate relative to the standard value of RSF / Flux. From this viewpoint, in this embodiment, it is more appropriate to directly compare the values ​​of RSF / Flux after application of a given transmembrane pressure difference. The smaller the RSF / Flux value after application of the same transmembrane pressure difference, the higher the physical durability of the forward osmosis membrane and the higher its performance as a forward osmosis membrane, and therefore the higher its practical usefulness.

[0054] The predetermined transmembrane pressure difference applied to evaluate the physical durability of the forward osmosis membrane is, for example, 50 to 200 kPa. Specifically, for example, forward osmosis treatment with the transmembrane pressure difference increased by 10 to 50 kPa and forward osmosis treatment under standard conditions can be repeatedly performed to obtain the RSF / Flux value after each transmembrane pressure difference application. In the forward osmosis membrane of the present invention, the RSF / Flux value after application of a transmembrane pressure difference of 200 kPa is preferably 0.25 g / kg or less, more preferably 0.15 g / kg or less, even more preferably 0.10 g / kg or less, particularly preferably 0.08 g / kg or less, and most preferably 0.06 g / kg or less.

[0055] [Shape of forward osmosis membrane] The forward osmosis membrane of the present embodiment is preferably a hollow fiber type. The hollow fiber type forward osmosis membrane has reduced defects in the separation functional layer, and therefore tends to have high performance as a forward osmosis membrane. In addition, when the forward osmosis membrane of the present embodiment is used in a modularized form, the forward osmosis membrane is preferably a hollow fiber type from the viewpoint of increasing the effective membrane area per module volume. In a hollow fiber forward osmosis membrane, it is preferable that at least one separation functional layer is on the inner surface of the hollow fiber support membrane in order to prevent physical damage to the separation functional layer.

[0056] [Inducing solution] The draw solution is a solution that exhibits a higher osmotic pressure than the feed solution and has the function of moving the solvent from the feed solution through the forward osmosis membrane. This draw solution exhibits a high osmotic pressure by containing a high concentration of the draw solute. Examples of the derived solute include alkali metal salts, alkaline earth metal salts, ammonium salts, sugars, monoalcohols, glycols, water-soluble polymers, etc. Specific examples of these include: As alkali metal salts, for example, sodium chloride, potassium chloride, sodium sulfate, sodium thiosulfate, sodium sulfite, etc.; Alkaline earth metal salts, for example, magnesium chloride, calcium chloride, magnesium sulfate, etc.; Ammonium salts, for example, ammonium chloride, ammonium sulfate, ammonium carbonate, etc.; Examples of sugars include common sugars such as sucrose, fructose, and glucose, as well as special sugars such as oligosaccharides and rare sugars; As monoalcohols, for example, methanol, ethanol, 1-propanol, 2-propanol, etc.; Glycols, for example, ethylene glycol, propylene glycol, etc.; Examples of water-soluble polymers include polyethylene oxide, polypropylene oxide, and copolymers of ethylene oxide and propylene oxide; Each of them can be mentioned.

[0057] [Module] The support membrane and forward osmosis membrane in this embodiment can be used as a module (support membrane module, or forward osmosis membrane module) in which a plurality of membranes are housed in a housing. The shape of the module is not particularly limited. However, it is preferable that a section in which liquid comes into contact with only one surface side of the membrane and a section in which liquid comes into contact with only the other surface side of the membrane are configured to be separated by an adhesive resin that fixes the membrane to the module housing. For example, in the case where the support membrane or the forward osmosis membrane is in the form of a hollow fiber membrane, a hollow fiber membrane module is preferably configured in which a plurality of hollow fiber membranes are stored in a housing, and a compartment in which liquid comes into contact only with the inner surface side of the hollow fiber membranes and a compartment in which liquid comes into contact only with the outer surface side of the membranes are separated from each other. The size of the housing is not particularly limited. However, for example, a cylindrical housing having a diameter of 5 to 500 mm and a length of 20 to 10,000 mm can be used. As the adhesive resin, for example, a urethane-based or epoxy-based adhesive can be used.

[0058] FIG. 1 is a schematic cross-sectional view showing the structure of an example of a hollow fiber membrane module. The hollow fiber membrane module (1) shown in FIG. 1 has a structure in which a fiber bundle consisting of a plurality of hollow fiber membranes (4) is packed in a cylindrical housing, and both ends of the hollow fiber bundle are fixed to the cylinder with adhesive fixing parts (5, 6). The housing has outer conduits (2, 3) on its side and is sealed by headers (7, 8). Here, the adhesive fixing parts (5, 6) are solidified so as not to block the hollow parts of the hollow fiber membranes. The headers (7, 8) each have inner conduits (9, 10) that communicate with the inside (hollow part) of the hollow fiber membranes (4) but do not communicate with the outside. These inner conduits (9, 10) allow liquid to be introduced into or removed from the inside of the hollow fiber membranes (4). The outer conduits (2, 3) each communicate with the outside of the hollow fiber membranes (4) but do not communicate with the inside. This hollow fiber membrane module (1) is so structured that the liquid flowing inside and the liquid flowing outside are in contact only via the hollow fiber membranes (4).

[0059] [Membrane area] In this embodiment, the membrane area refers to the area of ​​the support membrane or the forward osmosis membrane that is in contact with the feed liquid and can exhibit a separation function, i.e., the area of ​​the forward osmosis membrane that is in contact with the feed liquid or the draw solution. Specifically, for example, in the case of a module of hollow fiber forward osmosis membranes in which the raw material liquid is supplied to the inside, the membrane area (the inner surface area of ​​the hollow fiber forward osmosis membrane) is defined by the following formula (2) based on the length, inner diameter, and number of hollow fiber forward osmosis membranes excluding the adhesive fixing parts in the module. a=c×π×b×n (2) Here, a is the inner surface area of ​​the hollow fiber forward osmosis membrane (m 2 ), b is the length (m) of the hollow fiber forward osmosis membrane excluding the adhesive fixing portion, c is the inner diameter (m) of the hollow fiber forward osmosis membrane, and n is the number of hollow fiber forward osmosis membranes. Regarding the hollow fiber supported membrane module in which the supported membrane is in the form of a hollow fiber, the internal surface area can be calculated in a similar manner to that described above. The length of the hollow fibers of a modularized hollow fiber support membrane or hollow fiber forward osmosis membrane, excluding the adhesive fixing portion, is sometimes referred to as the "effective length".

[0060] <<Method of manufacturing forward osmosis membrane>> The method for producing a forward osmosis membrane in this embodiment includes at least a step of forming a separation functional layer, and may include a step of producing a support membrane by forming a porous support. The step of forming the porous support preferably includes a step of solidifying a resin solution obtained by dissolving a resin in a good solvent in a coagulation bath containing a non-solvent for the resin.

[0061] <Method for producing the support membrane> The methods for producing a hollow fiber support membrane and a flat membrane support membrane will be described in detail below. [Manufacturing method of hollow fiber support membrane] In this embodiment, a particularly preferred hollow fiber support membrane (hollow fiber membrane) consisting of only a hollow fiber-shaped porous support can be produced by a known dry / wet membrane production method, melt membrane production method, wet membrane production method, etc., using a material selected from the above-mentioned thermoplastic resins. Among these, the production method described below is preferred. discharging a spinning dope from an outer flow passage of a double tubular nozzle and an internal coagulation liquid from an inner flow passage of the double tubular nozzle; The spinning dope discharged from the outer flow passage of the double tubular nozzle is coagulated by immersing it in an external coagulation bath through an idle portion; and Winding up the solidified spinning dope while applying tension to the spinning dope. Including, The spinning dope contains a resin (polymer) and a solvent, The temperature of the spinning dope discharged from the double tubular nozzle is higher than the temperature of the internal coagulation liquid, and the temperature difference between the two liquids is 5°C or more and less than 35°C. A method for manufacturing hollow fiber membranes. After being wound on the winding machine, the hollow fiber membrane may be cut to a predetermined length.

[0062] (Spinning solution) The spinning dope contains a resin (polymer) and a solvent, and is preferably a solution obtained by dissolving a resin in a good solvent. In this method, aprotic polar organic solvents such as N-methyl-2-pyrrolidone, dimethylacetamide, and dimethylformamide are preferably used as the solvent (good solvent) of the spinning solution. The spinning solution may contain a non-solvent for the resin. As the non-solvent in the spinning solution, glycols such as polyethylene glycol and polypropylene glycol, as well as electrolytes, polyvinylpyrrolidone, and the like can be used. Among these, glycols are preferred because of their spinnability and the quality of the resulting membrane. The content ratio of the non-solvent in the spinning solution is preferably set so that the mass ratio of non-solvent / (good solvent+non-solvent) is within the range of 50 to 90% of the weight ratio at the compatibility limit. The compatibility limit refers to the point at which the polymer solution cannot become a homogeneous solution and undergoes phase separation. Since the compatibility limit is generally a function of temperature, the content ratio of the non-solvent needs to be set based on the compatibility limit at the spinning temperature. If the mass ratio of non-solvent / (good solvent + non-solvent) is less than 50% of the weight ratio at the compatibility limit, the viscosity of the spinning dope may be too low, resulting in poor spinnability, whereas if this value exceeds 90%, the controllability of the cross-sectional shape of the hollow fiber support membrane may be poor. For the same reason, the temperature of the spinning solution during the formation of a hollow fiber-shaped porous support membrane is preferably 30 to 80°C, more preferably 35 to 60°C.

[0063] The polymer concentration in the spinning dope is preferably 10 to 30% by mass, more preferably 15 to 25% by mass. The polymer concentration in the spinning dope is particularly related to the strength of the hollow fiber support membrane to be obtained. When the polymer concentration in the spinning dope is in the above range, a hollow fiber support membrane having excellent membrane strength can be obtained. When preparing the spinning dope, the spinning dope may be stirred at a predetermined temperature for 24 hours or more and then degassed under reduced pressure.

[0064] (Internal coagulation liquid) When forming a membrane of a hollow fiber-shaped porous support, for example, as described above, a double spinneret is used, and the spinning dope is discharged from the outer cylindrical port (outer flow path) and the internal coagulation liquid is discharged from the inner port (inner flow path). As the internal coagulation liquid, for example, an aqueous solution containing water as a main component and one or more additives selected from alcohols, ethylene glycols, and amide-based solvents can be used. Examples of alcohols include methanol, ethanol, and isopropyl alcohol. Examples of ethylene glycols include triethylene glycol, tetraethylene glycol, and glycerin. Examples of amide solvents include N-methyl-2-pyrrolidone, N,N-dimethylacetamide, and N,N-dimethylformamide. By adding such additives to the internal coagulation liquid, the rate of coagulation can be controlled, and a porous support having a desired structure can be easily obtained. For example, adding an additive to the internal coagulation liquid slows down the coagulation and makes the pore size of the surface coarse. However, if too much additive is added to the internal coagulation liquid, the spinning stability may deteriorate, or the surface pore size may become coarse, making it difficult to form a separation functional layer.

[0065] As the internal coagulation liquid, it is preferable to use water or a mixture of water and a small amount of additives from the viewpoint of spinning stability and variability of membrane performance. When, for example, glycols are added as the internal coagulation liquid additive, the amount added is preferably 60 mass% or less, more preferably 40 mass% or less, even more preferably 20 mass% or less, particularly preferably 10 mass% or less, and most preferably 5 mass% or less, based on the total mass of the solvent contained in the internal coagulation liquid. If this value exceeds 60 mass%, it becomes difficult to maintain the balance of the pore sizes on the inner and outer surfaces of the obtained hollow fiber membrane, and the pores on the inner surface in particular tend to become coarse. It is particularly preferable to use water as the internal coagulation liquid, since this allows the formation of a dense layer with an appropriate thickness while forming macrovoids in the vicinity of the surface of the porous support.

[0066] It is preferable that the internal coagulation liquid is adjusted to an appropriate temperature before being subjected to spinning. If the temperature of the internal coagulation liquid is too high, the dense layer on the inner surface side of the hollow fiber membrane becomes too thin, and the structure near the inner surface tends to become non-uniform. On the other hand, if the temperature of the internal coagulation liquid is too low, the dense layer on the inner surface side of the hollow fiber membrane may become too thick. If the dense layer is too thick, the monomer may not be properly supplied during the formation of the separation function layer of the forward osmosis membrane, which may reduce the performance of the forward osmosis membrane, and the resistance of the dense layer may reduce the water permeability of the forward osmosis membrane. For these reasons, the temperature of the internal coagulation liquid is preferably 5 to 50°C, more preferably 10 to 40°C, and further preferably 15 to 35°C.

[0067] In order to appropriately control the structure of the inner surface side of the hollow fiber support membrane, it is preferable to set the temperature of the spinning dope higher than that of the internal coagulation liquid. More preferably, the temperature of the spinning dope is set to 30 to 80°C, even more preferably to 35 to 60°C, the temperature of the internal coagulation liquid is preferably set to 5 to 50°C, even more preferably to 10 to 35°C, and the temperature difference between the spinning dope and the internal coagulation liquid is preferably set to 5°C or more and less than 35°C, more preferably 5 to 33°C, even more preferably 5 to 30°C. By setting the temperatures in this way, it is easy to control the structure of the inner surface side of the hollow fiber membrane, the structure is easily made uniform, and the spinning stability also tends to be high. These temperature settings are merely examples, and can be appropriately adjusted depending on the composition of each solution.

[0068] In addition, by setting the temperature of the spinning dope and the temperature of the external coagulation liquid within an appropriate range, it is possible to control the structure of the outer surface of the hollow fiber membrane or the surface of the flat membrane. However, the outer surface of the hollow fiber membrane and the surface of the flat membrane are easily affected by the temperature rise of the spinning dope during continuous production, the composition change of the external coagulation liquid, the temperature and humidity of the atmosphere, etc. Therefore, from the viewpoint of uniformity of the surface structure and ease of production, it is easier and more preferable to control the structure of the inner surface of the hollow fiber membrane. In addition, the internal coagulation liquid for manufacturing hollow fiber membranes has a low flow rate and a smaller liquid volume than a coagulation bath. Therefore, the internal coagulation liquid set to a predetermined temperature can lower the temperature of only the surface layer part of the inner surface of the hollow fiber membrane. Therefore, only the surface layer part of the hollow fiber membrane can be thickened, and phase separation proceeds before the macrovoids grow excessively, forming a dense layer. Furthermore, by appropriately setting the temperature difference between the spinning dope and the internal coagulation liquid, the thickness of the dense layer on the inner surface of the hollow fiber membrane can be controlled. That is, when the temperature difference between the two liquids is increased, the low-temperature region on the inner surface of the hollow fiber membrane becomes thicker, and the dense layer becomes thicker. On the other hand, when the temperature difference between the two liquids is decreased, the low-temperature region on the inner surface of the hollow fiber membrane becomes thinner, and the dense layer becomes thinner. In either case, the viscosity is relatively low in the region inside the surface layer where the temperature is low, and macrovoids can grow faster than coagulation, and the above-mentioned macrovoid layer can be formed. For these reasons, it is more preferable to control the inner surface structure of the hollow fiber membrane, since this makes it easier to obtain a desired membrane structure.

[0069] (external coagulation liquid) The spinning dope discharged from the spinneret is immersed in an external coagulation bath through an idling portion and coagulated. The external coagulation liquid used as the coagulation bath can be one or more selected from water, the non-solvents exemplified above as additives to the internal coagulation liquid, other organic solvents, and the like. The external coagulation liquid may be a liquid having the same composition as the internal coagulation liquid, or a liquid having a different composition. As the external coagulation liquid, it is preferable to use water or a mixture of water and the non-solvent exemplified above as an additive to the internal coagulation liquid.

[0070] When a mixture of water and an alcohol, ethylene glycols, or an amide solvent is used as the external coagulation liquid, the amount of the additive selected from the alcohol, ethylene glycols, and amide solvent is preferably 40% by mass or less, more preferably 30% by mass or less, even more preferably 15% by mass or less, and particularly preferably 5% by mass or less, based on the total mass of the external coagulation liquid. When the amount of the additive in the external coagulation liquid is within this range, coagulation on the outer surface side of the hollow fiber proceeds appropriately, macrovoids of a good size are easily formed, and the shape of the hollow fiber membrane becomes uniform, which is preferable. The most preferred external coagulation liquid is water. During spinning, the external coagulation liquid is contaminated with the solvent of the spinning dope that leaks out of the hollow fiber membrane. Therefore, in order to maintain the composition of the external coagulation liquid within a certain range, it is necessary to renew the external coagulation liquid. When water is used as the external coagulation liquid, it is particularly preferred because it is easy to control the composition of the external coagulation liquid by simply pouring water over it.

[0071] The temperature of the coagulation bath is preferably 10 to 60°C, more preferably 20 to 50°C, and further preferably 25 to 40°C. If the temperature of the coagulation bath is high, the structure of the obtained hollow fiber support membrane tends to be sparse, and the water permeability of the hollow fiber support membrane tends to be high, and accordingly the water permeability of the forward osmosis membrane also tends to be high. If the temperature of the coagulation bath is too high, the internal and external structure of the hollow fiber support membrane is easily disturbed by thermal vibration. Therefore, the uniformity of the structure including the surface of the hollow fiber support membrane decreases, and defects occur when a chemical solution is passed through the separation function layer formation process, and the amount of salt back diffusion in the forward osmosis membrane may increase. On the other hand, when the temperature of the coagulation bath is low, the structure of the support membrane tends to be dense, and the water permeability of the support membrane and the forward osmosis membrane tends to be low. The lower the temperature of the coagulation bath, the higher the spinning stability and the more uniform the structure of the obtained hollow fiber membrane tends to be.

[0072] In this embodiment, the temperature of the coagulation bath is preferably lower than the temperature of the spinning dope. The difference between the temperature of the coagulation bath and the temperature of the spinning dope is preferably 40°C or less, and more preferably 3°C or more and 40°C or less. If the temperature difference between the spinning dope and the coagulation liquid is too large, or if the temperature of the coagulation bath is higher than the temperature of the spinning dope, the structure near the outer surface of the hollow fiber membrane will become uneven, which may result in reduced performance when used as a forward osmosis membrane, and reduced physical durability, such as the separation functional layer being prone to peeling off in parts.

[0073] (idle running part) The spinning dope discharged from the spinneret passes through a portion having a certain free running distance and then reaches the coagulation bath. The free running distance from the spinneret to the coagulation bath should be appropriately adjusted according to the spinning conditions, the size of the spinneret, etc. However, in terms of the structure of the hollow fiber support membrane, the uniformity of the surface pore size, etc., the free running distance is preferably 100 to 500 mm, more preferably 200 to 400 mm. By setting an appropriate free running distance, the structure of the entire hollow fiber support membrane is stabilized, especially while the outer surface structure becomes moderately sparse. Therefore, when a separation functional layer is formed inside the hollow fiber to form a forward osmosis membrane, the draw solution diffuses well in the separation functional layer, so that the water permeability of the forward osmosis membrane tends to be high. Furthermore, by appropriately controlling the temperature and humidity of the free-running portion, hollow fibers with a more uniform structure can be obtained. From this viewpoint, the temperature of the free-running portion is preferably 15 to 50° C., and more preferably 25 to 40° C. Furthermore, from the viewpoint of stabilizing the overall structure of the hollow fiber support membrane while making the outer surface structure appropriately coarse, the humidity of the free-running portion is preferably 40 to 100%, more preferably 70 to 100%, and even more preferably 90 to 100% in terms of relative humidity.

[0074] (winding) The tension during winding of the hollow fiber membrane can be adjusted by the discharge speed of the spinning dope, the winding speed, the type and number of turn rolls, etc. The tension when winding the hollow fiber membrane is preferably set appropriately taking into consideration the composition of the spinning dope and the like. In this embodiment, the tension (unit: g) during winding is a value measured by clamping the running hollow fiber membrane with a tensiometer. The tension during winding of the hollow fiber membrane is preferably 4 to 60 g, more preferably 10 g or more and less than 40 g, and even more preferably 10 to 38 g, from the viewpoint of not causing thread breakage. When the tension during winding is 5 g or more, the hollow fiber membrane does not meander or sag during winding, and can be spun stably, and the structure and membrane properties of the obtained hollow fiber membrane also have small fluctuations, which is preferable. When the tension during winding is less than 40 g, the distortion of the membrane thickness center of the hollow fiber can be suppressed, and the compressive strength can be increased. The tension during winding is particularly preferably 10 g or more and 35 g or less. By keeping the tension within this range and appropriately adjusting the temperature and humidity of the spinning dope, the empty transport section, the internal coagulation liquid, and the external coagulation liquid, spinning stability can be obtained and the uniformity of the surface structure of the hollow fiber membrane can be increased, which is more preferable.

[0075] [Method of manufacturing flat support membrane] The flat support membrane can be produced, for example, by the following method using the resin solution exemplified above as the one used in the production of the hollow fiber support membrane. The flat membrane-shaped support membrane consisting of a substrate and a porous support is, for example, A method in which a resin solution is applied onto a substrate, and then the substrate is immersed in a coagulating liquid (e.g., water) to coagulate the resin solution; A method in which the substrate is immersed in a resin solution and then immersed in a coagulating liquid (e.g. water) to coagulate; A method in which the base material and resin solution are extruded through a slit-shaped nozzle into a coagulating liquid to coagulate; etc. On the other hand, a flat support membrane consisting only of a porous support can be obtained, for example, by applying a resin solution onto a glass substrate, immersing it in a coagulation liquid to coagulate it, and then peeling off the coagulated support membrane from the glass substrate. The membrane forming conditions, such as the composition of the resin solution and the composition of the coagulation liquid, can be appropriately determined by those skilled in the art with reference to known techniques and the above-mentioned manufacturing method for the hollow fiber support membrane. The flat membrane of the present embodiment is more preferably a support membrane consisting of only a porous support.

[0076] [Heat treatment] The support film obtained as described above may be subjected to a heat treatment. The heat treatment of the support membrane may be carried out in the same manner as the heat treatment of the forward osmosis membrane after the formation of the separation functional layer described below, or by a method appropriately modified by a person skilled in the art.

[0077] [Separation functional layer formation process] A forward osmosis membrane can be obtained by forming a separation functional layer on the support membrane obtained as described above. An example of a method for forming a separation functional layer containing polyamide as a main component on a support film will be described below. A separation functional layer mainly composed of polyamide can be formed by performing interfacial polycondensation on the surface of a porous support using an aqueous solution containing a polyfunctional amine and an organic solvent solution containing a polyfunctional acid halide. In the present embodiment, a preferred method for forming the separation functional layer is, for example, a method in which a first solution containing one of the polyfunctional amine and the polyfunctional acid halide and a second solution containing the other are passed through the support membrane in sequence. An embodiment in which both the polyfunctional amine and the polyfunctional acid halide are contained in one solution is not preferred. In this embodiment, for example, the first solution may include a multifunctional amine and the second solution may include a multifunctional acid halide.

[0078] [Multifunctional amine] A polyfunctional amine is an amine having at least two or more primary amino groups and at least one of secondary amino groups in one molecule, and at least one of the amino groups is a primary amino group. For example, aromatic polyfunctional amines such as o-phenylenediamine, m-phenylenediamine, p-phenylenediamine, o-xylylenediamine, m-xylylenediamine, p-xylylenediamine, 1,3,5-triaminobenzene, 1,2,4-triaminobenzene, 3,5-diaminobenzoic acid, 3-aminobenzylamine, and 4-aminobenzylamine; aliphatic amines such as ethylenediamine and propylenediamine; and alicyclic polyfunctional amines such as 1,2-diaminocyclohexane, 1,4-diaminocyclohexane, 4-aminopiperidine, and 4-aminoethylpiperazine. Among them, considering separation performance, water permeation resistance, and heat resistance, an aromatic polyfunctional amine having at least two to four primary amino groups and at least one of secondary amino groups in one molecule is preferable. As such polyfunctional aromatic amines, m-phenylenediamine, p-phenylenediamine, or 1,3,5-triaminobenzene are preferably used. In particular, m-phenylenediamine is more preferably used because of its availability and ease of handling. These polyfunctional amines can be used alone or as a mixture of two or more kinds. When mixing two or more kinds of polyfunctional amines, the above amines may be combined with each other, or the above amines may be combined with an amine having at least two secondary amino groups in one molecule. Examples of amines having at least two secondary amino groups in one molecule include piperazine and 1,3-bispiperidylpropane.

[0079] [Polyfunctional acid halides] A polyfunctional acid halide is an acid halide having at least two halocarbonyl groups in one molecule. For example, Examples of trifunctional acid halides include trimesic acid chloride, 1,3,5-cyclohexanetricarboxylic acid trichloride, and 1,2,4-cyclobutanetricarboxylic acid trichloride. Examples of the bifunctional acid halides include aromatic bifunctional acid halides such as biphenyldicarboxylic acid dichloride, azobenzenedicarboxylic acid dichloride, terephthalic acid chloride, isophthalic acid chloride, and naphthalenedicarboxylic acid chloride; aliphatic bifunctional acid halides such as adipoyl chloride and sebacoyl chloride; and alicyclic bifunctional acid halides such as cyclopentanedicarboxylic acid dichloride, cyclohexanedicarboxylic acid dichloride, and tetrahydrofurandicarboxylic acid dichloride. Considering the reactivity with the polyfunctional amine, the polyfunctional acid halide is preferably a polyfunctional acid chloride. Also, considering the separation performance and heat resistance of the resulting forward osmosis membrane, the polyfunctional acid chloride is more preferably a polyfunctional aromatic acid chloride having 2 to 4 carbonyl chloride groups in one molecule. In particular, from the viewpoints of availability and ease of handling, it is preferable to use trimesoyl chloride. These polyfunctional acid halides can be used alone or in combination of two or more kinds.

[0080] [Solvent and monomer solution concentration] The polyfunctional amine and the polyfunctional acid halide are each dissolved in a suitable solvent, and subjected to interfacial polycondensation as a first solution or a second solution. The solvents for the first and second solutions are preferably those which dissolve the monomers contained therein, and which, when the two solutions come into contact with each other, are incompatible with each other, form a liquid-liquid interface, and do not destroy the support film.More preferably, the solvents are inactive against polyfunctional amine compounds and polyfunctional acid halides. Examples of such solvents include the following solvents: The solvent for the polyfunctional amine may be one or more selected from water, alcohol, etc. The solvent for the polyfunctional acid halide may be one or more selected from hydrocarbon solvents such as n-hexane, cyclohexane, n-heptane, n-octane, n-nonane, n-decane, etc.

[0081] By selecting the above-mentioned solvents as the solvents for the polyfunctional amine and the polyfunctional acid halide, the polyfunctional amine solution and the polyfunctional acid halide solution become immiscible, and the interfacial polycondensation reaction proceeds, resulting in a thin film of a polymer (polyamide). The composition and concentration of each solution should be set according to the type of monomer, the distribution coefficient to the solvent, etc., and are not particularly limited, and can be appropriately set according to the desired separation function. For example, in the case of interfacial polycondensation using an aqueous m-phenylenediamine solution as the polyfunctional amine solution and an n-hexane solution of trimesoyl chloride as the polyfunctional acid halide solution, the appropriate monomer concentrations are as follows: The concentration of m-phenylenediamine is preferably 0.1 to 10% by mass, more preferably 0.5 to 5.0% by mass. The concentration of trimesoyl chloride is preferably 0.01 to 10% by mass, more preferably 0.04 to 2.0% by mass. If the concentration of these solutions is too low, the formation of the polyamide separation functional layer by interfacial polycondensation is incomplete and defects are likely to occur, leading to a decrease in separation performance when used as a forward osmosis membrane. Conversely, if the concentration of these solutions is too high, the formed polyamide separation functional layer becomes too thick, which may decrease the water permeability and increase the amount of residual unreacted material in the separation functional layer, thereby adversely affecting the performance as a forward osmosis membrane.

[0082] [Polymerization additives] The polyfunctional amine solution or the polyfunctional acid halide solution may contain polymerization additives such as surfactants, organic solvents (excluding the organic solvent in the polyfunctional acid halide solution), organic acid salts, basic compounds, and antioxidants, as long as they do not significantly interfere with the reaction between the polyfunctional amine and the polyfunctional acid halide. The surfactant has the effect of improving the wettability of the porous support surface and reducing the interfacial tension between the amine solution and the non-polar solvent. The organic solvent may act as a catalyst for the interfacial polycondensation reaction, so the addition of the organic solvent may make the interfacial polycondensation reaction more efficient. The organic acid salts can change the wettability of the support surface, which may improve the membrane formability and the separation performance when used as a forward osmosis membrane. The basic compound can remove the hydrogen halide produced by polymerization, which may promote the polymerization.

[0083] Examples of the polymerization additives include surfactants such as sodium dodecylbenzenesulfonate, sodium dodecyl sulfate, and sodium lauryl sulfate; organic solvents such as ethanol, isopropanol, N,N-dimethylformamide, and ε-caprolactam; organic acid salts composed of amines such as triethylamine and organic acids such as camphorsulfonic acid; basic compounds such as sodium hydroxide, trisodium phosphate, and triethylamine; phenol-based antioxidants, amine-based antioxidants, sulfur-based antioxidants, phosphorus-based antioxidants, and acylation catalysts.

[0084] In addition, in this embodiment, it is particularly preferable to perform a heat treatment (curing) after forming the polymer thin film by interfacial polycondensation. It is presumed that this heat treatment improves the high-order structure of the polymer thin film and increases the crosslinking density, thereby improving the physical durability and solvent resistance of the polymer thin film and reducing the amount of salt back-diffusion in the forward osmosis membrane. In other words, it is considered that a forward osmosis membrane with reduced partial functional defects in the separation functional layer can be formed by performing a heat treatment on the forward osmosis membrane by an appropriate method.

[0085] In the method for producing a forward osmosis membrane of the present embodiment, it is preferable to form a support membrane having a porous support having a dense layer and a macrovoid layer, each of which has a specific structure, and then provide a separation functional layer on the dense layer, followed by a heat treatment. It is further preferable to carry out the heat treatment in a wet state. Examples of heat treatment methods in a wet state include permeation of a wet gas (e.g., nitrogen or air containing moisture) heated through a heat source, permeation of hot water, permeation of water vapor, exposure to water vapor, and the like. Here, "permeation" refers to a process of supplying a fluid to a forward osmosis membrane to bring the separation functional layer and the support membrane of the forward osmosis membrane into contact with the fluid. For example, in the case of a forward osmosis membrane using a hollow fiber support membrane consisting of only a porous support, a preferred permeation method is to supply a fluid to the inside or outside of the hollow fiber, or both, to bring the front side, back side, and interior of the separation functional layer, and the inside of the support membrane into contact with the fluid.

[0086] When heat treatment is performed in a dry state, the forward osmosis membrane may be excessively dried, and in particular, the pores of the support membrane may shrink, the support membrane may be deformed, etc. When the pores of the support membrane shrink, the water permeability of the resulting forward osmosis membrane may decrease. In addition, when the support membrane is deformed, deformation of the separation functional layer may be induced, the salt blocking performance of the separation functional layer may decrease, and the amount of salt back diffusion may increase. Therefore, when heat treatment is performed in a dry state, the heat treatment time is preferably 15 minutes or less from the viewpoint of avoiding excessive drying of the forward osmosis membrane.

[0087] In this embodiment, the term "heat treatment" refers to a treatment in which an object to be treated is heated at a temperature of 50° C. or higher, preferably at a temperature of 70° C. or higher. The heat treatment in this embodiment is more effective when the coefficient of variation of the thickness of the separation functional layer of the forward osmosis membrane is in the above-mentioned range. When the coefficient of variation of the thickness of the separation functional layer is in the above-mentioned range, the performance of the molecular functional layer as a whole can be improved by a predetermined heat treatment, and even if there is a defect in part of the separation function, the defect can be prevented from expanding.

[0088] The heat treatment in this embodiment can be performed, for example, by a method of supplying hot water to the forward osmosis membrane after the formation of the separation functional layer, a method of immersing the forward osmosis membrane after the formation of the separation functional layer in hot water, a method of supplying high-temperature steam to the forward osmosis membrane, etc. Among these, the method of supplying hot water to the forward osmosis membrane after the formation of the separation functional layer or the method of supplying high-temperature steam to the forward osmosis membrane is preferable. It is preferable to supply hot water to at least the separation functional layer side of the forward osmosis membrane. This is particularly preferable because heat is uniformly transferred to the separation functional layer and residual monomers and the like in the support membrane are washed away, making it difficult for unintended reactions to occur during the heat treatment. The temperature of the hot water is preferably 50 to 100° C., and more preferably 70 to 95° C. Such a heating treatment is advantageous in that the heat of the hot water is efficiently transferred to the separation functional layer, accelerating the crosslinking reaction of the polymer thin film that constitutes the separation functional layer. The hot water supply time is preferably 5 minutes to 2 hours. When the hot water supply time is 5 minutes or more, the crosslinking reaction, structural change, etc. of the separation functional layer proceeds well. However, even if the hot water is supplied for more than 2 hours, the effect of the heat treatment does not increase in proportion to the hot water supply time, so the hot water supply time is preferably 2 hours or less.

[0089] When performing heat treatment by supplying high-temperature steam to a forward osmosis membrane, "high-temperature steam" refers to water in a gaseous state at 100°C or higher, particularly under high-pressure conditions. Such high-temperature steam can be generated in a pressure cooker such as an autoclave that is generally used for high-pressure steam sterilization. The temperature of the high-temperature steam is preferably 100 to 160°C, more preferably 100 to 140°C. Setting the temperature of the high-temperature steam within this range is advantageous in that it promotes crosslinking reactions of the polymer thin film that constitutes the separation functional layer, and does not significantly damage the support membrane or the separation functional layer, or both, resulting in an extremely low amount of salt back diffusion in the forward osmosis membrane. The time for which high-temperature steam is supplied to the forward osmosis membrane is preferably 1 minute to 4 hours. If the supply time is 1 minute or more, the crosslinking reaction etc. proceeds well. Even if high-temperature steam is supplied for more than 4 hours, the effect of the heat treatment does not increase in proportion to the supply time of high-temperature steam, so the supply time of steam is preferably 4 hours or less.

[0090] As the heat treatment in this embodiment, only one type of heat treatment may be performed, or two or more types of heat treatment may be combined, or the same treatment may be repeated multiple times.

[0091] When forming a separation functional layer made of a polymer thin film on a support membrane, if at least one of the first monomer and the second monomer contains a monomer having three or more reactive groups and the three-dimensional polymer thin film formed by them is subjected to the above-mentioned heat treatment in a wet state, the above-mentioned effect is more pronounced. As a result, the strength and durability of the forward osmosis membrane are improved, and the amount of salt back diffusion in forward osmosis is further reduced, which is particularly preferable. EXAMPLES

[0092] The present invention will be described in more detail below with reference to examples and comparative examples, but the present invention is not limited to these examples in any way. Unless otherwise stated, operations were carried out at 25°C.

[0093] [Measurement of the thickness of the dense layer, and the size and number of voids] The thickness of the dense layer of the porous support in the support membrane, as well as the size and number of voids, were measured by observing nine electron microscope layers (cross-sectional images) obtained from the forward osmosis membrane. In the case of hollow fiber forward osmosis membranes, one forward osmosis membrane was taken from each of three locations in the radial direction of the forward osmosis membrane module (a total of three membranes), and each was cut into three equal parts in the longitudinal direction to obtain nine samples. A cross section perpendicular to the membrane surface direction (longitudinal direction) was taken at the center of each sample, and the obtained cross section was observed. In the case of a flat forward osmosis membrane, each side of the membrane was divided into three equal parts to obtain nine samples. Then, a cross section was taken from the center of each sample, and the obtained cross section was observed. In both the hollow fiber forward osmosis membrane and the flat membrane forward osmosis membrane, the measured value was calculated as the average value of nine samples. For each sample, a scanning electron microscope was used to photograph the area near the interface where the porous support and the separation functional layer were in contact, and the obtained images (cross-sectional images) were analyzed to distinguish between the dense layer and the macrovoid layer of the porous support in the support membrane, and the size of the voids in the macrovoid layer was determined. In this example, the thickness of the dense layer of the support membrane and the size and number of voids were measured after the membrane was made into a forward osmosis membrane. It was confirmed that these measurements were the same within the error range even when the membrane was measured alone.

[0094] Cross-sectional images of each sample were obtained as follows. The sample was immersed in pure water in a special glass container, frozen with liquid nitrogen, and then dried by freeze-drying. A cross section perpendicular to the membrane direction was prepared for the dried sample using the Broad Ion Beam (BIB) processing method (processing device: E-3500, Hitachi High-Tech Corporation), and a thin coating of osmium was applied to prepare an observation sample. Images of the observation sample were taken using a scanning electron microscope (S-4800, Hitachi High-Tech Corporation) under the following conditions. Acceleration voltage: 1.0 kV Emission current: 10μA Probe current:Normal Detector:Upper Magnification: 5,000x Number of pixels: 1280 x 960 Working distance: 5.0mm

[0095] The observation field was determined so that an area of ​​25 μm in width in the film surface direction of the sample was included within the field of view. The cross-sectional image was acquired as an 8-bit grayscale image under conditions where the brightness value was not saturated and the contrast was as high as possible. For the cross-sectional images obtained, the thickness of the dense layer of the porous support, the size of voids, etc. were directly measured using a scale. The contact interface between the porous support of the forward osmosis membrane and the separation functional layer was determined by importing the obtained cross-sectional image into ImageJ (developed by the National Institutes of Health, USA), binarizing it using the Otsu method, calculating the average brightness on the membrane surface and in the horizontal direction, and comparing the average brightness from the surface of the separation functional layer toward the support membrane side.The horizontal direction where the average brightness was highest was determined to be the contact interface between the porous support of the forward osmosis membrane and the separation functional layer.

[0096] As an example of measuring a cross-sectional image, cross-sectional images of an observation sample prepared from the center in the longitudinal direction of a hollow fiber forward osmosis membrane taken from the radially intermediate part of the forward osmosis membrane module of Example 1 are shown in Figures 2 and 3. Figure 2 is an electron microscope image, and Figure 3 is a view in which auxiliary lines have been added to Figure 2. Looking at Figures 2 and 3, four macrovoids with major axes of 1 μm or more were observed in the entire cross-sectional image. The dense layer was from the support membrane surface (the interface between the separation functional layer and the dense layer) to the shallowest part of the macrovoid, and its thickness was 4.7 μm. One macrovoid was observed in region A of this cross section (a region 0 to 5 μm deep from the interface between the separation functional layer and the dense layer). Therefore, the number of macrovoids in region A of this cross section was 0.04 voids / μm. On the other hand, three macrovoids were observed in region B (a region 5.0 to 10.0 μm deep from the interface between the separation functional layer and the dense layer). Since the width of the observation field was 25 μm, the number of macrovoids in region B of this cross section was calculated to be 0.12 voids / μm (3 voids / 25 μm). Such calculations were performed for images from nine visual fields, and the thickness of the dense layer and the number of macrovoids were calculated as the average values.

[0097] [Measurement of the average thickness and its coefficient of variation of the separation functional layer] The average thickness and its coefficient of variation of the separation functional layer were measured using nine electron microscope layers (cross-sectional images) obtained by a method similar to [Measurement of dense layer thickness, and size and number of voids] above, using the same nine samples as used in [Measurement of dense layer thickness, and size and number of voids] above, with a magnification of 10,000x and a field of view set so that a width of 13 μm in the membrane surface direction of the sample fell within the field of view. First, the contour of the separation functional layer was extracted in each cross-sectional view by the following method. The obtained cross-sectional image was imported into image processing software (ImageJ; developed by the National Institutes of Health, USA) and binarized by Otsu's method. In the obtained binarized image, the average brightness in the horizontal direction to the membrane surface was calculated, and the average brightness was compared from the surface of the separation functional layer toward the support membrane side, and the horizontal direction of the part with the highest average brightness was taken as the contact interface (contour) between the porous support of the forward osmosis membrane and the separation functional layer. The contour of the separation functional layer surface was taken as a curved line connecting the parts with a contrast difference from the background in the obtained binarized image with a continuous line. The contour in the thickness direction was taken as both ends of the obtained image. The contour of the separation functional layer was extracted by connecting these lines. The inside of the obtained contour was filled in to calculate the area of ​​the separation functional layer, and the area was converted to the average thickness of the separation functional layer in one image using a calibration curve prepared in advance. The average value of the nine measured values ​​obtained was taken as the average thickness of the separation functional layer in each comparative example, and the coefficient of variation was calculated.

[0098] [Evaluation of resistance to applied transmembrane pressure difference in forward osmosis performance] The effect of the forward osmosis performance on the applied transmembrane pressure was investigated. First, for the forward osmosis membranes obtained in each of the Examples and Comparative Examples, forward osmosis operation was performed under the following conditions, and then the water permeability (Flux) and salt back diffusion rate (RSF) were obtained, and the salt permeability (RSF / Flux) was calculated. Raw material liquid: Purified water, 25℃, membrane surface linear velocity 3cm / sec Draw solution: 3.5% by mass sodium chloride aqueous solution, 25°C, membrane surface linear velocity 3 cm / sec Transmembrane pressure difference: 20kPa Driving time: 1 hour The forward osmosis operation was carried out while adding a saturated aqueous sodium chloride solution to the draw solution to maintain the concentration of the draw solution constant. The transmembrane pressure difference was set by manipulating the back pressure valve on the draw solution side so that the draw solution side (the support membrane side of the forward osmosis membrane) was positive (high pressure).

[0099] The salt permeability (RSF / Flux) obtained by the above measurement was used as the reference salt permeability value. After the above measurements were completed, the forward osmosis membrane was washed with water for 2 hours, and the transmembrane pressure difference was changed to 50 kPa, and the forward osmosis treatment was carried out again under the same conditions as above. Next, the forward osmosis membrane was washed with water again, and the transmembrane pressure difference was returned to 20 kPa, and the forward osmosis treatment was carried out under the same conditions as above. The permeability (Flux) and salt back diffusion rate (RSF) were obtained, and the salt permeability (RSF / Flux) was calculated. This was the salt permeability value after operation at 50 kPa. After the measurements were completed, the forward osmosis membrane was washed again with water, and the transmembrane pressure difference was changed to 100 kPa. Except for this, the forward osmosis treatment was carried out again under the same conditions as above. The transmembrane pressure difference was then returned to 20 kPa and operation was continued. After that, the flux and salt back diffusion rate (RSF) were measured, and the salt permeability after operation at 100 kPa was calculated. In this way, forward osmosis was performed by increasing the transmembrane pressure by 50 kPa up to 200 kPa, with an operation at a transmembrane pressure of 20 kPa in between. After each transmembrane pressure application, the salt permeability after operation at a transmembrane pressure of 20 kPa was determined. The reference salt permeability value, the salt permeability values ​​after application of 100 kPa and 200 kPa, and the performance retention rate are shown in Table 3. The performance retention rate is expressed as a percentage by dividing the reference salt permeability value by the salt permeability value after application of each transmembrane pressure difference.

[0100] [Support membrane dimensions] As dimensions of the support membrane, the inner diameter, outer diameter, and membrane thickness were measured for the hollow fiber support membrane, and the membrane thickness was measured for the flat membrane support membrane. In the case of hollow fiber support membranes, the measurements were made using optical microscope photographs (cross-sectional images) of the cross sections obtained by cutting the membrane along a plane perpendicular to the membrane surface direction (longitudinal direction). The outer and inner diameters of the cross-sectional images were measured using a scale. The membrane thickness was calculated by dividing the difference between the outer and inner diameters by 2. The outer and inner diameters referred to here are the outer and inner diameters of the hollow fiber, respectively. In the case of a flat support membrane, the thickness was measured using an optical microscope photograph (cross-sectional image) of a cross section obtained by cutting the membrane in a plane perpendicular to the membrane surface direction. The membrane thickness of this cross-sectional image was measured using a scale. In this example, the inner diameter, outer diameter, and membrane thickness of the support membrane were measured after the membrane was made into a forward osmosis membrane. It was confirmed that the measurements were the same within the margin of error even when the membrane was measured alone.

[0101] [Pure water permeability of hollow fiber support membrane] The hollow fiber support membrane was cut to an effective length of 10 cm, and pure water at a temperature of 25°C was poured into one end of the membrane, and the other end was sealed after venting air. Next, an average pressure of 100 kPa (1 bar) was applied to the inside of the hollow fiber for 10 minutes to perform internal pressure filtration, and the amount of filtered water was measured to calculate the pure water permeation amount per unit area of ​​the inner surface of the support membrane per unit time. Here, the hollow fiber was handled so as not to reach a completely dry state, and the pores of the hollow fiber were wetted with a 90% by mass aqueous ethanol solution before measurement, and then washed with water before measurement. The pure water permeation amount was measured using n=5 single fibers of the hollow fiber support membrane, and the average value was adopted as the measured value.

[0102] [Compressive strength of hollow fiber support membrane] The hollow fiber support membrane cut to an effective length of 10 cm was immersed in a pressure vessel filled with pure water at 40°C. In this state, one end of the hollow fiber support membrane was sealed, and the other end was connected to a nozzle leading to the outside of the vessel via a syringe needle. The pressure vessel was sealed, and water pressure was applied. When the pressure was maintained at 0.10 MPa for 30 seconds, the amount of water (g) that had permeated to the inside of the hollow fiber was measured, and the water permeation amount was calculated. The above operation was repeated while increasing the pressure by 0.05 MPa, and the pressure at the point where the water permeation amount started to decrease was recorded. The compressive strength was measured using a single fiber of the hollow fiber support membrane (n=2), and the average value was used as the measured value.

[0103] [Example 1] [Preparation of hollow fiber support membrane] A uniform polymer solution consisting of 19% by mass of polysulfone (Udel-P3500, manufactured by Solvay Specialty polymers), 61% by mass of N-methyl-2-pyrrolidone (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.), and 20% by mass of tetraethylene glycol (manufactured by Tokyo Chemical Industry Co., Ltd.) was prepared as a spinning dope. The dope was filled into a wet hollow fiber spinning machine equipped with a double spinneret. The dope at 40°C and an internal coagulation liquid (water) at 25°C were discharged from the double spinneret, and the dope was run for 250 mm in air with a relative humidity of 98% and a temperature controlled at 30°C, after which it was coagulated in a coagulation bath (external coagulation liquid) filled with water at 30°C, and wound up at a tension of 30 g using a free roll as a turn roll to obtain a hollow fiber support membrane. The outer diameter of the obtained hollow fiber support membrane was 1.02 mm, the inner diameter was 0.62 mm, the membrane thickness was 0.20 mm, and the pure water permeability of the support membrane was 425 kg / (m 2 The fiber spinning stability was good, and no significant fluctuation in the inner and outer diameters of the hollow fiber membrane was observed.

[0104] [Fabrication of supported membrane module] 130 pieces of the hollow fiber support membrane were cut to 120 mm and packed into a cylindrical plastic housing with a diameter of 20 mm and a length of 100 mm. Both ends were fixed with adhesive, and the housing was cut to open the ends. A header was then attached to create the structure shown in Figure 1, with an effective length of 80 mm and an effective inner membrane surface area of ​​0.02 m. 2 A supported membrane module was fabricated.

[0105] [Formation of separation functional layer] An aqueous solution (first solution) containing 2.0% by mass of m-phenylenediamine and 0.15% by mass of sodium lauryl sulfate was passed through the inside of the hollow fiber support membrane in the support membrane module for 20 minutes. After the first solution was removed by gravity from the piping at the bottom of the module, the outer part of the support membrane module was depressurized to 90 kPaG (11 kPaA) while the inside of the hollow fiber was wet with the first solution, and the depressurization was maintained for 1 minute. Then, air was passed through the inside of the hollow fiber at a linear speed of 210 cm / sec for 1 minute to remove excess first solution. Next, an n-hexane solution (second solution) containing 0.20% by mass of trimesic acid chloride was passed through the inside of the hollow fiber for 2 minutes to perform interfacial polymerization, and a separation functional layer was formed on the inner surface of the hollow fiber. Thereafter, excess second solution was removed by flowing nitrogen gas, and then hot water at 85° C. was flowed inside the hollow fiber at a linear speed of 5 cm / sec for 30 minutes. The module was then placed in an autoclave (AC; SX-500, manufactured by Tommy Seiko Co., Ltd.) with both ends of the hollow fiber support membrane open, and curing was performed by passing high-temperature steam at 121°C through the autoclave for 20 minutes. Furthermore, the inside of the hollow fiber support membrane was washed with water at 20°C for 30 minutes to obtain a forward osmosis membrane module. [evaluation] The obtained forward osmosis membrane module was used for various evaluations. In addition, cross-sectional images of the observation sample prepared from the center in the length direction of the hollow fiber-shaped forward osmosis membrane taken from the radial middle part of the obtained forward osmosis membrane module are shown in Figures 2 and 3.

[0106] [Example 2] A forward osmosis membrane module was prepared in the same manner as in Example 1, except that in preparing the hollow fiber support membrane, a solution consisting of 98% by mass of water and 2% by mass of tetraethylene glycol was used as the internal coagulation liquid and the temperature of the internal coagulation liquid was set to 30°C. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0107] [Example 3] In preparing the hollow fiber support membrane, a uniform polymer solution consisting of 19.2 mass% polysulfone (Udel-P3500, manufactured by Solvay Specialty Polymers), 60.5 mass% N-methyl-2-pyrrolidone (manufactured by Fuji Film Wako Pure Chemical Industries, Ltd.), and 20 mass% tetraethylene glycol (manufactured by Tokyo Chemical Industry Co., Ltd.) was used as the spinning dope, and the temperature of the internal coagulation liquid was set to 20°C. A forward osmosis membrane module was prepared in the same manner as in Example 1. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0108] [Example 4] In preparing the hollow fiber support membrane, a uniform polymer solution consisting of 19 mass% polyethersulfone (BASF, Ultrason E2020P), 61 mass% N-methyl-2-pyrrolidone (Fujifilm Wako Pure Chemical Industries, Ltd.), and 20 mass% tetraethylene glycol (Tokyo Chemical Industry Co., Ltd.) was used as the spinning dope, a solution consisting of 95 mass% water and 5 mass% tetraethylene glycol was used as the internal coagulation liquid, and the temperature of the internal coagulation liquid was 35°C. A forward osmosis membrane module was prepared in the same manner as in Example 1, except that the spinning dope was a uniform polymer solution consisting of 19 mass% polyethersulfone (BASF, Ultrason E2020P), 61 mass% N-methyl-2-pyrrolidone (Fujifilm Wako Pure Chemical Industries, Ltd.), and 20 mass% tetraethylene glycol (Tokyo Chemical Industry Co., Ltd.). Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0109] [Example 5] A forward osmosis membrane was prepared in the same manner as in Example 1, except that in preparing the hollow fiber support membrane, the temperature of the internal coagulation liquid was set to 40°C, the temperature of the external coagulation liquid was set to 35°C, and in the separation function layer formation process, a separation function layer was formed on the outside of the hollow fiber. In the present examples, various measurements and evaluations were performed by appropriately changing the measurement position, the direction of pressure application, etc., taking into consideration that the separation functional layer was located on the outside of the hollow fiber support membrane.

[0110] [Example 6] [Preparation of flat support membrane] A uniform polymer solution was prepared consisting of 19% by mass of polysulfone (Udel-P3500, manufactured by Solvay Specialty polymers), 61% by mass of N-methyl-2-pyrrolidone (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.), and 20% by mass of tetraethylene glycol (manufactured by Tokyo Chemical Industry Co., Ltd.). The temperature of this solution was adjusted to 40°C, and the solution was cast onto a glass plate using a doctor blade to a thickness of 250 μm. The solution was then immediately immersed in a coagulation bath filled with water at 10°C and coagulated for 5 minutes to produce a flat support membrane. The thickness of the resulting support membrane was 0.20 mm.

[0111] [Formation of separation functional layer] An aqueous solution (first solution) containing 2.0% by mass of m-phenylenediamine and 0.15% by mass of sodium lauryl sulfate was dropped onto the entire surface of the flat membrane support membrane (the surface not in contact with the glass plate) and left to stand for 20 minutes. After that, air was flowed horizontally on the membrane surface of the support membrane for 1 minute so that the linear speed relative to the surface of the first solution application side was 210 cm / sec, and excess first solution was removed. Next, an n-hexane solution (second solution) containing 0.20% by mass of trimesic acid chloride was dropped onto the entire surface of the first solution application side, and then left to stand for 2 minutes to perform interfacial polymerization, thereby forming a separation functional layer on the porous support. Thereafter, nitrogen gas was passed over the surface on which the separation functional layer was formed to remove excess second solution, and hot water at 85° C. was passed over the surface on which the separation functional layer was formed for 30 minutes at a linear speed of 5 cm / sec. The flat membrane after passing the hot water was placed in an autoclave (SX-500 manufactured by Tommy Seiko Co., Ltd.) and high-temperature steam at 121°C was passed through the autoclave chamber for 20 minutes. The flat membrane was then washed with water at 20°C for 30 minutes to obtain a flat forward osmosis membrane.

[0112] [Preparation of flat membrane cell] The flat membrane forward osmosis membrane obtained above was cut into a rectangle of 140 mm x 140 mm, and the flat membrane forward osmosis membrane was placed in a rectangular housing of 200 mm length, 200 mm width, and 300 mm thickness to prepare a flat membrane cell.

[0113] [evaluation] Using the obtained flat membrane cell, various evaluations were carried out. In the case of a flat membrane, the position of the dense layer of the support membrane and the position of the separation functional layer are indicated by the front and back of the membrane. The back here refers to the side that was in contact with the glass plate when the support membrane was produced, and the front refers to the side opposite the back.

[0114] [Example 7] In [Formation of separation functional layer], a forward osmosis membrane module was prepared in the same manner as in Example 1, except that the reduced pressure on the outer part of the support membrane module after draining the first solution was changed to 10 kPaG (91 kPaA) and the time for which air was allowed to flow after the reduced pressure was changed to 5 minutes. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0115] [Example 8] In [Formation of separation functional layer], a separation functional layer was formed on the inner surface of the hollow fiber support membrane, nitrogen gas was passed through to remove excess second solution, and the membrane was then placed in a dryer at 50°C for 5 minutes and further washed with water at 20°C for 30 minutes. Except for this, a forward osmosis membrane module was produced in the same manner as in Example 1. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0116] [Example 9] In [Preparation of hollow fiber support membrane], a uniform polymer solution consisting of 21 mass% polysulfone (Udel-P3500, manufactured by Solvay Specialty polymers), 59 mass% N-methyl-2-pyrrolidone (manufactured by Fuji Film Wako Pure Chemical Industries, Ltd.), and 20 mass% tetraethylene glycol (manufactured by Tokyo Chemical Industry Co., Ltd.) was used as the spinning dope, and the temperature of the internal coagulation liquid was set to 15°C. A forward osmosis membrane module was prepared in the same manner as in Example 1. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0117] [Comparative Example 1] [Preparation of hollow fiber support membrane] A uniform polymer solution consisting of 18% by mass of polyethersulfone (manufactured by BASF, Ultrason E2020PSR) with hydroxylated ends, 57% by mass of N,N-dimethylacetamide (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.), and 25% by mass of tetraethylene glycol (manufactured by Tokyo Chemical Industry Co., Ltd.) was prepared as a spinning dope. The dope was filled into a wet hollow fiber spinning machine equipped with a double spinneret. The dope at 40°C and the internal coagulation liquid at 45°C were discharged from the double spinneret, and the dope was run for 200 mm in air with a relative humidity of 98% adjusted to 30°C, after which it was coagulated in a coagulation bath (external coagulation liquid) filled with water at 50°C, and wound up at a tension of 10 g using a free roll as a turn roll to obtain a hollow fiber support membrane. At this time, a solution consisting of 50% by mass of water and 50% by mass of tetraethylene glycol was used as the internal coagulation liquid. The outer diameter of the obtained hollow fiber support membrane was 1.00 mm, the inner diameter was 0.70 mm, the membrane thickness was 0.15 mm, and the pure water permeability of the support membrane was 1,850 kg / (m 2 × hr × bar) and the compressive strength was 0.43 MPa.

[0118] [Fabrication of support membrane module] and [Formation of separation functional layer] A forward osmosis membrane module was produced in the same manner as in Example 1, except that the above hollow fiber support membrane was used. [evaluation] Various evaluations were performed using the obtained forward osmosis membrane module. In addition, cross-sectional images of an observation sample prepared from the center in the length direction using a hollow fiber-shaped forward osmosis membrane taken from the radial middle part of the obtained forward osmosis membrane module are shown in Figs. 4 and 5. Fig. 4 is an electron microscope image, and Fig. 5 is a diagram in which auxiliary lines are added to Fig. 4. In the forward osmosis membrane of Comparative Example 1, the dense layer is thin at 0.2 μm, so the dense layer can hardly be confirmed in the cross-sectional images of Figs. 4 and 5. In addition, in the cross-sectional image of Fig. 5, the number of macrovoids in region A is described as "0.60 pieces / μm", which does not match the number of macrovoids in region A described in Table 1, which is "0.61 pieces / μm". This is because the values ​​in Fig. 5 are values ​​obtained from one cross-sectional image, while the values ​​in Table 1 are the average values ​​of the values ​​in nine fields of view.

[0119] [Comparative Example 2] A forward osmosis membrane module was produced in the same manner as in Example 1, except that in [Production of a support membrane module], the temperature of the internal coagulation liquid was set to 37°C. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0120] [Comparative Example 3] A forward osmosis membrane module was produced in the same manner as in Example 9, except that in [Production of a support membrane module], the temperature of the internal coagulation liquid was set to 5°C. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0121] [Comparative Example 4] A forward osmosis membrane module was produced in the same manner as in Example 8, except that a hollow fiber support membrane module obtained in the same manner as in Comparative Example 1 was used, and a separation functional layer was formed on the inner surface of the hollow fiber support membrane. Using the obtained forward osmosis membrane module, various evaluations were carried out.

[0122] [Comparative Example 5] [Preparation of flat support membrane] and [Formation of separation functional layer] A uniform polymer solution consisting of 20% by mass of polysulfone (Udel-P3500, manufactured by Solvay Specialty polymers) and 80% by mass of N,N-dimethylformamide (manufactured by Fujifilm Wako Pure Chemical Industries, Ltd.) was prepared. The temperature of this solution was adjusted to 40°C, and the solution was cast onto a glass plate using a doctor blade to a thickness of 250 μm. The solution was then immediately immersed in a coagulation bath filled with water at 40°C and coagulated for 5 minutes to produce a flat membrane-like support membrane. The thickness of the obtained support membrane was 0.20 mm. The dense layer of the prepared support membrane was more than 15 μm. A flat membrane cell including a flat forward osmosis membrane was prepared in the same manner as in Example 6, except that the hollow fiber support membrane obtained above was used. [evaluation] Using the obtained flat membrane cell, various evaluations were carried out.

[0123] [Reference examples 1~4] In [Preparation of hollow fiber support membrane], a hollow fiber support membrane was prepared in the same manner as in Example 1, except that the winding conditions after spinning and coagulating the spinning dope were changed as shown in Table 1, and the physical properties of the membrane were evaluated. In Reference Example 2, the physical properties of the hollow fibers obtained by spinning were unstable and varied greatly depending on the location, and the spinning stability was poor.

[0124] The results are shown in Tables 1 to 3.

[0125] [Table 1]

[0126] [Table 2]

[0127] In Table 1, the abbreviations in the column for spinning dope stand for the following: PSf: Polysulfone PES: Polyethersulfone PES-OH: Hydroxy-terminated polyethersulfone NMP: N-methyl-2-pyrrolidone DMAc: N,N-dimethylacetamide DMF: N,N-dimethylformamide TEG: Tetraethylene glycol

[0128] [Table 3]

[0129] [Table 4]

[0130] Referring to Tables 1 to 3, the forward osmosis membrane modules of Examples 1 to 9 have high water permeability of the forward osmosis membrane. Even after being subjected to a history of transmembrane pressure difference with the support membrane side (draw solution side) being positive, a small salt permeability (RSF / Flux) value was maintained. This demonstrated that the forward osmosis membranes included in the modules of Examples 1 to 9 are practical forward osmosis membranes that have high performance as forward osmosis membranes and high physical durability.

[0131] In contrast, the forward osmosis membrane modules of Comparative Examples 1 and 4 had high forward osmosis performance when the transmembrane pressure difference with the support membrane side (draw solution side) positive was small, but the performance degradation was significant after being subjected to a history of high transmembrane pressure difference. Specifically, the forward osmosis membrane module of Comparative Example 1 had a significant decrease in performance retention rate, and the forward osmosis membrane module of Comparative Example 4 had a very large salt permeability (RSF / Flux) value. This is thought to be due to the particularly large number of macrovoids in region A and the thin thickness of the dense layer. This behavior is thought to be due to the unstable state of the interface between the separation functional layer and the support membrane, and the presence of parts with low adhesion between the separation functional layer and the support membrane, which meant that the separation functional layer could not withstand the pressure in the direction of peeling it off from the support membrane and suffered irreversible deterioration.

[0132] In addition, the forward osmosis membrane of Comparative Example 2 has an appropriate number of macrovoids in region B, but has a large number of macrovoids in region A, and the thickness of the dense layer is also thin. Therefore, even when the transmembrane pressure difference with the support membrane side (drawing solution side) being positive is low, the performance as a forward osmosis membrane is slightly lower than that of Examples 1 to 3. Furthermore, after being subjected to a history of high transmembrane pressure difference, the performance significantly decreased and the performance retention rate was low. The reason why the performance was slightly lower when the transmembrane pressure difference was small is thought to be because the number of macrovoids in the support membrane was not appropriate, which caused the supply balance of each monomer during interfacial polymerization to be lost, resulting in a low separation performance of the formed separation functional layer. The reason why the performance retention rate was low after the application of a high transmembrane pressure difference is thought to be because there are parts where the adhesion between the separation functional layer and the support membrane is low due to the thin dense layer and the presence of macrovoids near the surface, etc.

[0133] Furthermore, in the forward osmosis membranes of Comparative Examples 3 and 5, there were almost no macrovoids in the regions A and B of the support membrane. Therefore, although the obtained forward osmosis membranes had physical durability, their performance as forward osmosis membranes when the transmembrane pressure difference was small was low. This is believed to be because the increased density of the support membrane significantly reduced the diffusivity of the draw solution, reducing the permeability of the forward osmosis membrane and, as a result, increasing the effect of free diffusion of salt.

[0134] From the above, it was found that in order to obtain a practical forward osmosis membrane that combines physical durability and performance as a forward osmosis membrane, it is important to control the structure of the porous support in the support membrane and to control the method of forming the separation functional layer. [Explanation of symbols]

[0135] 1. Hollow fiber membrane module 2, 3 Outer conduit 4. Hollow fiber membrane 5, 6 Adhesive fixing part 7, 8 Header 9, 10 Inner duct

Claims

1. A forward osmosis membrane composed of a support membrane and a separation functional layer, The support membrane comprises at least a porous support, The separation functional layer is provided on the porous support, The porous support has a dense layer and a macrovoid layer in this order in a depth direction from a surface in contact with the separation functional layer, The macrovoid layer is a layer having macrovoids whose pores have a major axis of 1.0 μm or more, the dense layer is a layer having no macrovoids, The dense layer has a thickness of 1.0 to 9.5 μm, The macrovoids are are present at 0 to 0.20 particles / μm in a region A from the interface between the separation functional layer and the porous support to a depth of 0 to 5.0 μm, and 0.04 to 0.40 particles / μm are present in a region B from the interface between the separation functional layer and the porous support to a depth of 5.0 to 10.0 μm, Forward osmosis membrane.

2. The forward osmosis membrane according to claim 1, wherein the macrovoids are present in the region A in a range of 0 to 0.16 voids / μm.

3. The forward osmosis membrane according to claim 1, wherein the macrovoids are present in the region B at 0.06 to 0.30 voids / μm.

4. The forward osmosis membrane according to claim 2, wherein the macrovoids are present in the region A at 0 to 0.12 voids / μm.

5. The forward osmosis membrane according to claim 3, wherein the macrovoids are present in the region B at 0.08 to 0.20 voids / μm.

6. The forward osmosis membrane according to any one of claims 1 to 5, wherein the number of macrovoids present in the region B is equal to or greater than the number of macrovoids present in the region A.

7. The forward osmosis membrane according to any one of claims 1 to 5, wherein the support membrane of the forward osmosis membrane consists only of the porous support.

8. The forward osmosis membrane according to any one of claims 1 to 5, wherein the dense layer has a thickness of 8.0 µm or less.

9. The forward osmosis membrane according to claim 8, wherein the dense layer has a thickness of 1.5 to 6.0 μm.

10. The forward osmosis membrane according to any one of claims 1 to 5, wherein the support membrane is a hollow fiber support membrane.

11. 11. The forward osmosis membrane of claim 10, wherein the hollow fiber support membrane has the dense layer at least on an inner surface of the hollow fiber.

12. The forward osmosis membrane according to any one of claims 1 to 5, wherein the coefficient of variation of the average thickness of the separation functional layer in the forward osmosis membrane is 60% or less.

13. The forward osmosis membrane according to any one of claims 1 to 5, wherein the coefficient of variation of the average thickness of the separation functional layer in the forward osmosis membrane is 30% or less.

14. The forward osmosis membrane according to any one of claims 1 to 5, wherein the porous support comprises one or more selected from polysulfone and polyethersulfone, and derivatives thereof.

15. The forward osmosis membrane of any one of claims 1 to 5, wherein the porous support comprises polysulfone.

16. A forward osmosis membrane module comprising a housing containing the forward osmosis membrane according to any one of claims 1 to 5.

17. A hollow fiber membrane comprising at least a porous support, The porous support has a dense layer and a macrovoid layer in this order from an outer surface or an inner surface in a thickness direction of the membrane wall, The macrovoid layer is a layer having macrovoids whose pores have a major axis of 1.0 μm or more, the dense layer is a layer having no macrovoids, The dense layer has a thickness of 1.0 to 9.5 μm, The macrovoids are The porous support has a density of 0 to 0.20 particles / μm in a region A extending from the outer surface or inner surface of the porous support to a depth of 0 to 5.0 μm, and The porous support is present in a region B having a depth of 5.0 to 10.0 μm from the outer surface or inner surface thereof at 0.04 to 0.40 particles / μm. Hollow fiber membrane.

18. The hollow fiber membrane according to claim 17, wherein the macrovoids are present in the region A at 0 to 0.16 voids / μm.

19. The hollow fiber membrane according to claim 17, wherein the macrovoids are present in the region B at 0.06 to 0.30 voids / μm.

20. The hollow fiber membrane according to claim 18, wherein the macrovoids are present in the region A at 0 to 0.12 voids / μm.

21. The hollow fiber membrane according to claim 19, wherein the number of macrovoids in the region B is equal to or greater than the number of macrovoids in the region A.

22. The hollow fiber membrane according to any one of claims 17 to 21, wherein the hollow fiber membrane consists only of the porous support.

23. The hollow fiber membrane according to any one of claims 17 to 21, wherein the dense layer has a thickness of 8.0 µm or less.

24. The hollow fiber membrane according to any one of claims 17 to 21, wherein the dense layer has a thickness of 1.5 to 6.0 µm.

25. The hollow fiber membrane according to any one of claims 17 to 21, wherein the hollow fiber membrane has the dense layer at least on an inner surface of the hollow fiber.

26. The hollow fiber membrane according to any one of claims 17 to 21, wherein the porous support comprises one or more selected from polysulfone, polyethersulfone, and derivatives thereof.

27. The hollow fiber membrane according to any one of claims 17 to 21, wherein the porous support comprises polysulfone.

28. The hollow fiber membrane according to any one of claims 17 to 21, wherein the hollow fiber membrane is used as a support membrane for a forward osmosis membrane.

29. A hollow fiber membrane module comprising a housing and the hollow fiber membrane according to any one of claims 17 to 21 housed therein.

30. Discharging a spinning dope from an outer flow passage of a double tubular nozzle and an internal coagulation liquid from an inner flow passage of the double tubular nozzle; The fiberizable liquid discharged from the outer flow passage of the double tubular nozzle is coagulated by immersing it in an external coagulation bath through an idle portion; and Winding up the solidified spinning dope while applying tension to the spinning dope. Including, The spinning dope contains a resin (polymer) and a solvent, The temperature of the spinning dope discharged from the double tubular nozzle is higher than the temperature of the internal coagulation liquid, and the temperature difference between the two liquids is 5° C. or more and less than 35° C. A method for manufacturing hollow fiber membranes.

31. The method of claim 30, wherein the tension is 4 g or more and 60 g or less.

32. The method according to claim 30 or 31, wherein the temperature of the free running portion is 15°C or higher and 60°C or lower.

33. The method according to claim 30 or 31, wherein the relative humidity of the free running portion is 40% or more and 100% or less.

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