High desalination anti-pollution reverse osmosis membrane and preparation method and application thereof

Abstract

The application discloses a high-desalination anti-pollution reverse osmosis membrane and a preparation method and application thereof. The reverse osmosis membrane comprises a non-woven fabric layer, a polysulfone support layer, an ethylenediamine cyclen organic cage intermediate layer and a polyamide separation functional layer which are arranged in a stack, wherein the reverse osmosis membrane comprising the ethylenediamine cyclen organic cage intermediate layer has obvious improvements in permeation flux, desalination rate and pollution cleaning recovery performance. The prepared reverse osmosis membrane has excellent pollution cleaning recovery performance on the basis of high desalination.

Description

Technical Field

[0001] This invention relates to the field of membrane separation technology, and in particular to a high desalination and antifouling reverse osmosis membrane, its preparation method, and its application. Background Technology

[0002] Currently, the mainstream reverse osmosis membrane is the cross-linked aromatic polyamide composite reverse osmosis membrane. It utilizes m-phenylenediamine and trimesoyl chloride to form a polyamide separation functional layer on the surface of a polysulfone-based membrane through an interfacial polymerization reaction. This type of reverse osmosis membrane is widely used in industrial pure water production, industrial wastewater treatment, and seawater desalination. However, during its use, inorganic salt precipitation, organic matter, and microorganisms in the water can cause continuous fouling of the membrane surface, leading to a decrease in water production. Therefore, improving the biofouling resistance of reverse osmosis membranes is of great significance.

[0003] Currently disclosed technologies mainly improve the antifouling performance of reverse osmosis membranes by surface coating or grafting hydrophilic polymers and surface-modified inorganic nanoparticles. For example, CN 105008031A coats the surface of the polyamide separation functional layer with cross-linked polyvinyl alcohol. By changing the hydrophilicity, roughness, and zeta potential of the membrane surface, it simultaneously achieves high permeation flux and high desorption of pollutants, thereby maintaining its long-term stable performance. CN 211800078U disperses porous copper-coated titanium dioxide nanoparticles with antibacterial properties into the polyamide separation functional layer. Due to the porous structure of the particles and their antibacterial properties, this not only helps to increase the permeation flux of the reverse osmosis membrane but also significantly improves its antifouling performance, thereby reducing its use and maintenance costs.

[0004] Although some technical solutions for improving the antifouling performance of reverse osmosis membranes have been developed in the existing technology, further improvements are needed in improving the desalination rate of reverse osmosis membranes while simultaneously enhancing their fouling cleanup and recovery performance. Summary of the Invention

[0005] To address the aforementioned deficiencies in the prior art, this invention provides a high-desalination and anti-fouling reverse osmosis membrane, its preparation method, and its application. The prepared reverse osmosis membrane exhibits high desalination and excellent fouling cleaning and recovery performance.

[0006] To achieve the above-mentioned objectives, the first aspect of the present invention provides a high desalination and antifouling reverse osmosis membrane, wherein the reverse osmosis membrane comprises a nonwoven fabric layer, a polysulfone support layer, an ethylenediamine cycloimide organic cage intermediate layer, and a polyamide separation functional layer stacked together.

[0007] A second aspect of this invention provides a method for preparing a high-desalination, fouling-resistant reverse osmosis membrane, comprising the following steps:

[0008] S1: A polysulfone-containing solution is coated onto the surface of a nonwoven fabric to obtain base film A;

[0009] S2: Immerse base membrane A in an aqueous solution containing ethylenediamine cycloimine organic cage and soluble carbonate, remove it and remove excess aqueous solution to obtain base membrane B;

[0010] S3: Coat the surface of the base film B with an aqueous solution containing a polyfunctional amine, remove the excess aqueous solution, and obtain the base film C;

[0011] S4: Coat the surface of the base membrane C with an organic solution containing polyacrylamide chloride, remove excess organic solution to obtain the nascent reverse osmosis membrane and clean it.

[0012] In this invention, the ethylenediamine cycloimide organic cage can effectively adjust the pore size of the base membrane surface, which includes a nonwoven fabric layer and a polysulfone support layer. The addition of the organic cage makes the pore size of the base membrane surface tend to be similar to that of the organic cage, thereby making the pore size distribution of the base membrane surface more uniform. During the interfacial polymerization process, the multifunctional amine monomers pass through the uniform pores constructed by the organic cage structure, contact and react with the polyacrylamide chloride, forming a uniform and defect-free polyamide separation functional layer. Furthermore, the blades on the surface of the polyamide layer are more uniformly distributed, and the surface roughness is lower. On the one hand, this greatly improves the desalination rate of the reverse osmosis membrane; on the other hand, it can effectively resist the adhesion of contaminants on the surface of the reverse osmosis membrane, thus improving the fouling resistance of the reverse osmosis membrane. Firstly, the cleaning process restores performance. Secondly, based on the principle of "like dissolves like," the ethylenediamine cyclic imine organic cage containing imine bonds can effectively promote the diffusion of polyfunctional amines within its pores, enabling them to react rapidly with polyacrylamide chlorides to form a denser polyamide separation functional layer, thereby improving the desalination rate of the reverse osmosis membrane. Thirdly, the CO2 generated by the reaction of acid produced by interfacial polymerization with carbonates is stored in the cage structure. The heat generated by the interfacial polymerization further degasses the CO2, making it easier for uniform large blades to form on the bubble surface. This effectively resists the adhesion of contaminants and increases the effective filtration area of ​​the polyamide separation functional layer, thereby improving the permeation flux of the reverse osmosis membrane.

[0013] In some embodiments of the present invention, the soluble carbonate in step S2 is one or more of lithium carbonate, sodium carbonate, and potassium carbonate.

[0014] In some embodiments of the present invention, in the aqueous solution containing ethylenediamine cycloimide organic cage and soluble carbonate in step S2, the mass percentage of the ethylenediamine cycloimide organic cage is 0.1-1.0 wt%. Exemplary examples include 0.1 wt%, 0.2 wt%, 0.3 wt%, 0.4 wt%, 0.5 wt%, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt%, 1.0 wt%, etc. Setting the mass percentage within the above range can effectively adjust the pore size of the base film surface, making the pore size distribution of the base film surface more uniform.

[0015] In some embodiments of the present invention, in the aqueous solution containing ethylenediamine cycloimide organic cage and soluble carbonate in step S1, the mass percentage of soluble carbonate is 0.1-1.0 wt%, exemplarily 0.1 wt%, 0.2 wt%, 0.3 wt%, 0.4 wt%, 0.5 wt%, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt%, 1.0 wt%, etc. Setting the mass percentage within the above range can appropriately consume the hydrochloric acid produced by the interfacial polymerization reaction and generate an appropriate amount of CO2 to promote the formation of large leaves.

[0016] Preferably, the mass ratio between the ethylenediamine cycloimide organic cage and the soluble carbonate is 0.8:1-1.2:1; exemplary ratios include 0.8:1, 0.9:1, 1:1, 1.1:1, 1.2:1, etc. Setting the mass ratio within the above range allows the ethylenediamine cycloimide organic cage molecules to be loaded with an appropriate amount of CO2 molecules, thereby forming a more uniform polyamide large leaf structure.

[0017] In some embodiments of the present invention, the polyfunctional amine in step S3 is an aromatic amine containing at least two primary amino groups and / or an aliphatic amine containing at least two primary amino groups. Preferably, the aromatic amine is one or more of phenylenediamine, phenylenediamine, and 1,3,5-triaminobenzene, and the aliphatic amine is one or more of ethylenediamine, propylenediamine, and piperazine. More preferably, the polyfunctional amine is m-phenylenediamine. Preferably, in the aqueous solution containing the polyfunctional amine, the mass percentage of the polyfunctional amine is 1.0-5.0 wt%, exemplarily 1 wt%, 1.5 wt%, 2.0 wt%, 2.5 wt%, 3.0 wt%, 3.5 wt%, 4.0 wt%, 4.5 wt%, 5.0 wt%, etc.

[0018] In some embodiments of the present invention, rubber extrusion rollers are used to remove excess aqueous solution in steps S2 and S3.

[0019] In some embodiments of the present invention, the polyacrylamide chloride in step S3 is an aromatic polyacrylamide chloride and / or an aliphatic polyacrylamide chloride, preferably the aromatic polyacrylamide chloride is pyromellitic tricarboxylate chloride and / or terephthaloyl chloride, and the aliphatic polyacrylamide chloride is adipyl chloride and / or cyclopropane tricarboxylate chloride, more preferably the polyacrylamide chloride is pyromellitic tricarboxylate chloride. The polyfunctional amine and the polyacrylamide chloride serve as reactive monomers, and their appropriate concentrations and ratios form the desired polyamide separation functional layer.

[0020] In some embodiments of the present invention, the solvent used in the organic solution in step S4 is a nonpolar or weakly polar organic solvent, preferably n-decane; preferably, the mass percentage of the polyacrylamide chloride in the organic solution containing polyacrylamide chloride is 0.1-0.2 wt%. Exemplarily, it is 0.1 wt%, 0.15 wt%, 0.2 wt%, etc. Setting it to the above mass percentage range allows it to react with polyfunctional amine monomers to generate a thin and dense polyamide separation functional layer.

[0021] In some embodiments of the present invention, air purging is used in step S4 to remove excess organic solution.

[0022] In some embodiments of the present invention, the cleaning in step S4 is pure water cleaning; preferably, the temperature of the pure water cleaning is 70-90°C and the time is 1-5 minutes.

[0023] Another object of the present invention is to provide a high-desalination, anti-fouling reverse osmosis membrane prepared by the above method.

[0024] Another object of the present invention is to provide an application of a high desalination and fouling-resistant reverse osmosis membrane, wherein the reverse osmosis membrane is the reverse osmosis membrane described above or prepared by the above method, and the reverse osmosis membrane is used in the fields of industrial pure water production, industrial wastewater treatment and seawater desalination, preferably in the fields of industrial pure water production, industrial wastewater treatment and seawater desalination that require a high desalination and fouling-resistant reverse osmosis membrane.

[0025] Compared with the prior art, the present invention has the following advantages:

[0026] This invention provides a high-desalination, fouling-resistant reverse osmosis membrane, comprising a nonwoven fabric layer, a polysulfone support layer, an ethylenediamine cycloimide organic cage intermediate layer, and a polyamide separation functional layer. The nonwoven fabric layer is at the bottom, providing mechanical strength to the reverse osmosis membrane; the polysulfone support layer is in the middle, providing channels for the separation functional layer; and the polyamide separation functional layer is at the top, playing the main separation role. Compared to a reverse osmosis membrane without an intermediate layer, the reverse osmosis membrane containing the ethylenediamine cycloimide organic cage intermediate layer exhibits an 11.6% increase in permeate flux, a 0.35% increase in desalination rate, and a 15% reduction in flux decay rate after fouling compared to the membrane without the intermediate layer. Furthermore, the flux recovery rate after cleaning is nearly 15% higher. Compared to reverse osmosis membranes containing other organic cage structures (such as MIL-101(Cr)), the reverse osmosis membrane containing the ethylenediamine cycloimide organic cage intermediate layer demonstrates significant advantages in permeate flux, desalination rate, and fouling cleanup recovery performance. Therefore, reverse osmosis membranes containing an ethylenediamine cycloimide organic cage intermediate layer have high desalination and excellent fouling cleaning and recovery performance.

[0027] Other features and advantages of the present invention will be described in detail through the following specific embodiments. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of the structure of the high desalination and antifouling reverse osmosis membrane prepared in Example 1 of the present invention.

[0029] The markings are as follows: 1-Nonwoven fabric layer, 2-Polysulfone support layer, 3-Ethylenediamine cycloimide organic cage intermediate layer, 4-Polyamide separation functional layer. Detailed Implementation

[0030] The following will clearly and completely describe the concept and technical effects of this application in conjunction with embodiments, so as to fully understand the purpose, features and effects of this application. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Other embodiments obtained by those skilled in the art based on the embodiments of this application without creative effort are all within the scope of protection of this application.

[0031] Unless otherwise specified, all reagents used in the following examples or comparative examples are commercially available conventional reagents. Information on the main reagents is shown in Table 1.

[0032] Table 1 Main Reagent Information

[0033]

[0034]

[0035] The following examples or comparative examples illustrate the performance evaluation methods for reverse osmosis membranes:

[0036] 1. Evaluation of permeation flux and desalination rate

[0037] Permeation flux and desalination rate are two important parameters for evaluating the separation performance of reverse osmosis membranes. This invention evaluates the separation performance of reverse osmosis membranes according to GB / T32373-2015 "Test Methods for Reverse Osmosis Membranes".

[0038] Permeation flux is defined as the volume of water that permeates through a unit membrane area per unit time under certain operating conditions, and its unit is L·m. -2 ·h -1 .

[0039] Desalination rate (R) is defined as: under certain operating conditions, the salt concentration (C) of the feed solution... f ) and the salt concentration in the permeate (C p The difference between the two is then divided by the feed solution salt concentration (C). f ),Right now:

[0040]

[0041] The operating conditions used for the reverse osmosis membrane performance test in this invention are as follows: the feed solution is an aqueous solution of 2000 ppm sodium chloride, the solution pH is 7.0 ± 0.5, the operating pressure is 225 psi (1.55 MPa), and the operating temperature is 25 ± 1℃.

[0042] 2. Evaluation of the performance of pollution cleaning and restoration

[0043] The operating conditions used for the reverse osmosis membrane fouling flux decay performance test in this invention are as follows: the feed solution is an aqueous solution of 2000 ppm sodium chloride and 10 ppm bovine serum albumin, the solution pH is 7.0 ± 0.5, the operating pressure is 225 psi (1.55 MPa), and the operating temperature is 25 ± 1℃. The formula for calculating the flux decay rate is as follows:

[0044]

[0045] The operating conditions used in the reverse osmosis membrane cleaning flux recovery performance test of this invention are as follows: A sodium hydroxide aqueous solution with a pH of 12.0 ± 0.5 is circulated in the equipment for 30 minutes instead of a sodium chloride aqueous solution, followed by static soaking for 60 minutes. Then, the sodium hydroxide aqueous solution is drained from the equipment, and the equipment is rinsed with pure water for 15 minutes. Next, a citric acid / hydrochloric acid mixed solution with a pH of 1.0 ± 0.5 is used to replace the pure water, and the equipment is run for 30 minutes, followed by static soaking for 60 minutes. The citric acid / hydrochloric acid mixed solution is drained from the equipment, and the equipment is rinsed with pure water for 15 minutes. Finally, the permeation flux of the reverse osmosis membrane is tested using a 2000 ppm sodium chloride aqueous solution. The formula for calculating the flux recovery rate is as follows:

[0046]

[0047] Example 1

[0048] A solution of N,N-dimethylformamide containing 16.5 wt% polysulfone was prepared, filtered, and degassed before being uniformly coated onto a polyester nonwoven fabric with a coating thickness of 140 μm. After being left in air for 1.5 s, it was immersed in a pure water coagulation bath to obtain base membrane A. Base membrane A was then immersed in an aqueous solution containing 0.5 wt% ethylenediamine cycloimide organic cage and 0.5 wt% sodium carbonate. After removal, excess aqueous solution was removed using a rubber squeeze roller to obtain base membrane B. An aqueous solution containing 3.0 wt% m-phenylenediamine was coated onto the surface of base membrane B, and after standing for 30 s, excess aqueous solution was removed using a rubber squeeze roller. A solution of n-decane containing 0.15 wt% trimesoyl chloride was then coated onto its surface with a coating thickness of 120 μm. After standing for 30 s, excess organic solution was removed by air purging to obtain nascent reverse osmosis membrane C. Nascent reverse osmosis membrane C was washed in pure water at 80 °C for 3 min to obtain the reverse osmosis membrane.

[0049] Figure 1This is a schematic diagram of the high desalination and antifouling reverse osmosis membrane prepared in Example 1 of the present invention. From bottom to top, it includes a non-woven fabric layer, a polysulfone support layer, and a polyamide separation functional layer. The non-woven fabric layer is at the bottom, providing mechanical strength for the reverse osmosis membrane; the polysulfone support layer is in the middle, providing channels for the separation functional layer; and the polyamide separation functional layer is at the top, playing the main separation role. The non-woven fabric and polysulfone support layers can be manually peeled apart; the polyamide separation functional layer is relatively thin and difficult to peel off manually from the polysulfone support layer, but there is still a clear boundary; the organic cage layer is generally located between the support layer and the separation functional layer, but there is no clear boundary between it and the two. This is because the organic cage layer is relatively thin, and because part of the organic cage enters the channels of the support layer, and a small amount of polyamide generated by the interfacial polymerization reaction also enters the channels of the support layer, so the boundary is not obvious.

[0050] Example 2

[0051] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the mass percentages of ethylenediamine cycloimide organic cage, sodium carbonate, m-phenylenediamine, and pyromellitic acid chloride were 0.1 wt%, 1.0 wt%, and 0.1 wt%, and the pure water washing temperature was 70°C for 1 min.

[0052] Example 3

[0053] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the mass percentages of ethylenediamine cycloimide organic cage, sodium carbonate, m-phenylenediamine, and pyromellitic acid chloride were 1.0 wt%, 5.0 wt%, and 0.2 wt%, and the pure water washing temperature was 90°C for 5 min.

[0054] Example 4

[0055] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the soluble carbonate was lithium carbonate, the polyfunctional amine was ethylenediamine, and the polyacrylamide chloride was terephthaloyl chloride.

[0056] Example 5

[0057] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the mass percentages of ethylenediamine cycloimide organic cage and sodium carbonate were both 0.05 wt%, the mass percentage of m-phenylenediamine was 0.5 wt%, the mass percentage of trimesoyl chloride was 0.05 wt%, and the pure water washing temperature was 60°C for 0.5 min.

[0058] Example 6

[0059] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the mass percentages of ethylenediamine cycloimide organic cage, sodium carbonate, m-phenylenediamine, and pyromellitic acid chloride were 2.0 wt%, 6.0 wt%, and 0.3 wt%, and the pure water washing temperature was 95°C for 6 min.

[0060] Example 7

[0061] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the soluble carbonate was ammonium carbonate, the polyfunctional amine was 1,4-butanediamine, and the polyacrylamide chloride was isophthaloyl chloride.

[0062] Example 8

[0063] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the ethylenediamine cycloimide organic cage was 0.5 wt% and the sodium carbonate was 0.05 wt%.

[0064] Example 9

[0065] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the ethylenediamine cycloimide organic cage was 0.4 wt% by mass.

[0066] Example 10

[0067] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the ethylenediamine cycloimide organic cage was 0.6 wt% by mass.

[0068] Comparative Example 1

[0069] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the preparation process did not include the step of immersing the base membrane A in an aqueous solution containing an ethylenediamine cycloimide organic cage and sodium carbonate, followed by removing excess aqueous solution with a rubber squeeze roller. In Comparative Example 1, because the ethylenediamine cycloimide organic cage and sodium carbonate were not involved in the formation of the polyamide layer, the resulting polyamide blades were smaller and uneven in size, resulting in poorer flux, desalination rate, and fouling recovery performance.

[0070] Comparative Example 2

[0071] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the organic cage was MIL-101(Cr). In Comparative Example 2, because MIL-101(Cr) lacks a cyclic imine structure, the diffusion of m-phenylenediamine molecules to the water-oil interface is hindered, reducing the reaction rate and resulting in poor flux, desalination rate, and fouling cleanup and recovery performance.

[0072] Comparative Example 3

[0073] The reverse osmosis membrane was obtained using the same method as in Example 1, except that the base membrane A was immersed in an aqueous solution of ethylenediamine cycloimide organic cage without the addition of sodium carbonate. In Comparative Example 3, the lack of carbonate consumption of hydrochloric acid produced by the interfacial polymerization reaction, and the absence of space for CO2 formation to promote large blade formation, resulted in a lower reaction rate and smaller blades, leading to poorer flux, desalination rate, and fouling cleanup and recovery performance.

[0074] Table 2 Performance of the reverse osmosis membranes obtained in the examples and comparative examples

[0075]

[0076]

[0077] As can be seen from the experimental results in Table 2, the reverse osmosis membranes containing the ethylenediamine cycloimide organic cage intermediate layer in Examples 1-10 of this invention exhibit high desalination and excellent fouling cleaning and recovery performance. It is worth noting that in Example 5, due to insufficient use of soluble carbonates, organic cages, polyfunctional amines, and polyacrylamide chlorides, the interfacial polymerization reaction was insufficient, resulting in excessive flux but a significant sacrifice in desalination rate, and severe flux decay after fouling. In Example 6, due to excessive use of soluble carbonates, organic cages, polyfunctional amines, and polyacrylamide chlorides, the polyamide separation functional layer formed by interfacial polymerization was thick, resulting in a high desalination rate but a significant decrease in flux and poor cleaning and recovery performance after fouling. In Example 7, the types of soluble carbonates, polyfunctional amines, and polyacrylamide chlorides used were not optimal, resulting in a predominantly linear network structure in the polyamide, leading to a low desalination rate. In Example 8, due to a low concentration of soluble carbonates, the hydrochloric acid produced by interfacial polymerization could not be fully consumed, resulting in an insufficient interfacial polymerization reaction; furthermore, insufficient CO2 was generated, preventing the formation of a uniform polyamide large-blade structure.

[0078] Obviously, the above embodiments of the present invention are merely examples for clearly illustrating the present invention, and are not intended to limit the implementation of the present invention. Those skilled in the art can make other variations or modifications based on the above description. It is impossible to exhaustively list all embodiments here. All obvious variations or modifications derived from the technical solutions of the present invention are within the spirit and scope of the present invention.

Claims

1. A high-desalination, fouling-resistant reverse osmosis membrane, characterized in that, The reverse osmosis membrane comprises a nonwoven fabric, a polysulfone support layer, an ethylenediamine cycloimide organic cage intermediate layer, and a polyamide separation functional layer, all stacked together.

2. A method for preparing the reverse osmosis membrane of claim 1, characterized in that, The method includes the following steps: S1: A polysulfone-containing solution is coated onto the surface of a nonwoven fabric to obtain base film A; S2: Immerse base membrane A in an aqueous solution containing ethylenediamine cycloimine organic cage and soluble carbonate, remove it and remove excess aqueous solution to obtain base membrane B; S3: Coat the surface of the base film B with an aqueous solution containing a polyfunctional amine, remove the excess aqueous solution, and obtain the base film C; S4: Coat the surface of the base membrane C with an organic solution containing polyacrylamide chloride, remove excess organic solution to obtain the nascent reverse osmosis membrane and clean it.

3. The method according to claim 2, characterized in that, In the aqueous solution containing ethylenediamine cycloimide organic cage and soluble carbonate described in step S2, the mass percentage of ethylenediamine cycloimide organic cage is 0.1-1.0 wt%; and / or, the mass percentage of soluble carbonate is 0.1-1.0 wt%.

4. The method according to claim 2 or 3, characterized in that, The ratio between the ethylenediamine cycloimide organic cage and the soluble carbonate is 0.8:1 to 1.2:

1.

5. The method according to claim 2, characterized in that, The soluble carbonate mentioned in step S2 is one or more of lithium carbonate, sodium carbonate, and potassium carbonate.

6. The method according to claim 2, characterized in that, The polyfunctional amine in step S3 is an aromatic amine containing at least two primary amino groups and / or an aliphatic amine containing at least two primary amino groups.

7. The method according to claim 6, characterized in that, The aromatic amine is one or more of phenylenediamine, phenylenediamine, and 1,3,5-triaminobenzene, and the aliphatic amine is one or more of ethylenediamine, propylenediamine, and piperazine.

8. The method according to claim 7, characterized in that, The polyfunctional amine is m-phenylenediamine; in the aqueous solution containing the polyfunctional amine, the mass percentage of the polyfunctional amine is 1.0-5.0 wt%.

9. The method according to claim 2, characterized in that, The polyacryl chloride in step S4 is an aromatic polyacryl chloride and / or an aliphatic polyacryl chloride; and / or, the mass percentage of the polyacryl chloride in the organic solution containing the polyacryl chloride is 0.1-0.2 wt%.

10. The method according to claim 9, characterized in that, The aromatic polyacryl chloride is pyromellitic tricarboxylate chloride and / or terephthaloyl chloride, and the aliphatic polyacryl chloride is adipyl chloride and / or cyclopropane tricarboxylate chloride.

11. The method according to claim 10, characterized in that, The polyacyl chloride is pyromellitic trimethylol chloride.

12. The method according to claim 2, characterized in that, The organic solvent used in the organic solution described in step S4 is a nonpolar or weakly polar organic solvent; and / or, In step S4, excess organic solution is removed by air purging; and / or, The cleaning described in step S4 is a pure water cleaning.

13. The method according to claim 12, characterized in that, The organic solvent in step S4 is n-decane; the temperature of the pure water washing in step S4 is 70-90℃, and the time is 1-5 min.

14. Use of a reverse osmosis membrane, wherein the reverse osmosis membrane is the reverse osmosis membrane according to claim 1, or a reverse osmosis membrane prepared by the method according to any one of claims 2-13, and the reverse osmosis membrane is used in the fields of industrial pure water production, industrial wastewater treatment and seawater desalination.

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