A high permeability reverse osmosis membrane based on pH response regulation of monomer diffusion and a preparation method thereof
By introducing the pH-responsive regulator 4-phenylbutylamine during the reverse osmosis membrane preparation process, the MPD diffusion behavior was controlled, the problem of polyamide layer density was solved, and a reverse osmosis membrane with high permeability and high desalination rate was prepared, which is suitable for seawater desalination and wastewater treatment.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Patents(China)
- Current Assignee / Owner
- TIANJIN POLYTECHNIC UNIV
- Filing Date
- 2026-03-31
- Publication Date
- 2026-06-19
Smart Images
Figure CN121927447B_ABST
Abstract
Description
Technical Field
[0001] This invention belongs to the field of reverse osmosis membrane technology, and in particular relates to a high-permeability reverse osmosis membrane based on pH response-regulated monomer diffusion and its preparation method. Background Technology
[0002] As a water treatment material with highly efficient desalination capabilities, polyamide composite reverse osmosis membranes play an irreplaceable role in brackish water desalination and industrial wastewater reuse, with market demand continuing to grow. The polyamide separation layer is a key functional layer that determines the salt removal rate and water permeability of the composite reverse osmosis membrane. Enhancing the water permeability of the reverse osmosis membrane while ensuring a high salt removal rate can significantly improve the recovery rate of freshwater resources, thereby greatly alleviating the shortage of freshwater resources needed for industrial production.
[0003] The polyamide separation layer on the surface of reverse osmosis membranes is typically prepared by interfacial polymerization of m-phenylenediamine (MPD) aqueous monomer and trimesoyl chloride (TMC) organic monomer. During interfacial polymerization, the diffusion behavior of the monomers plays a decisive role in the polyamide network structure formed, thus affecting the performance of the reverse osmosis membrane. However, the migration of MPD monomers from the aqueous phase to the interface is often rapid and disordered, resulting in a large amount of randomly diffused MPD and TMC participating in the interfacial polymerization reaction. This often leads to a denser polyamide layer structure, which is detrimental to the rapid transport of water molecules and the improvement of water permeability. Therefore, how to precisely control the diffusion behavior of MPD to participate in the interfacial reaction in a more ordered and controllable manner has become one of the key issues restricting the development of high-permeability reverse osmosis membranes.
[0004] Introducing co-solvents or surfactants into aqueous solutions can regulate monomer diffusion behavior during interfacial polymerization by altering the water / organic phase interfacial tension or miscibility, thereby optimizing the polyamide layer structure. However, due to the inherent physical properties of these additives, they typically continuously promote / inhibit monomer diffusion. The regulation process often struggles to dynamically respond to changes in the microenvironment, ultimately leading to polyamide layers that are either too dense or too loose. Consequently, this reduces the water permeability or salt removal rate of the reverse osmosis membrane. Therefore, developing a strategy for dynamically regulating monomer diffusion behavior is crucial for preparing high-permeability reverse osmosis membranes. Summary of the Invention
[0005] In view of this, the present invention aims to propose a high-permeability reverse osmosis membrane based on pH response-regulated monomer diffusion and its preparation method, so as to improve the water permeability of the reverse osmosis membrane.
[0006] To achieve the above objectives, the technical solution of the present invention is implemented as follows:
[0007] In a first aspect, the present invention provides a method for preparing a high-permeability reverse osmosis membrane based on pH-responsive regulation of monomer diffusion, the preparation method comprising the following steps:
[0008] S1. Mix m-phenylenediamine, camphor sulfonic acid, triethylamine and 4-phenylbutylamine with water to obtain an aqueous solution;
[0009] S2. Pour the aqueous solution onto the surface of the polysulfone ultrafiltration membrane, let it stand and then dry to obtain an aqueous adsorption membrane.
[0010] S3. Pour the organic phase solution containing trimesoyl chloride onto the surface of the aqueous phase adsorption membrane obtained in step S2. After standing, remove the excess organic phase solution to obtain the interfacial polymerization precursor membrane.
[0011] S4. The interfacial polymerization precursor membrane obtained in step S3 is subjected to heat treatment to obtain the high-permeability reverse osmosis membrane.
[0012] Furthermore, in S2, the polysulfone ultrafiltration membrane has a pure water permeation flux of 150~300 L·m at 0.1 MPa. -2 ·h -1 The bovine serum albumin retention rate was 91.5%–93.5%.
[0013] Further, in step S2, the mass fraction of intermediate phenylenediamine in the aqueous solution is 1.5~2.0%, the mass fraction of camphor sulfonic acid is 1.5~2.5%, the mass fraction of triethylamine is 0.5~1.5%, and the mass fraction of 4-phenylbutylamine is 0.002~0.008%.
[0014] Furthermore, in step S2, the surface area of the polysulfone ultrafiltration membrane to the volume ratio of the aqueous solution is 80~100 cm². 2 : 0.01~0.05 L.
[0015] Furthermore, in step S2, the settling time is 30~120s.
[0016] Further, in step S3, the mass fraction of pyromellitic chloroformyl chloride in the organic phase solution is 0.1~0.15%.
[0017] Further, in step S3, the surface area ratio of the polysulfone ultrafiltration membrane to the volume ratio of the organic phase solution is 80~100 cm². 2 : 0.01~0.05 L.
[0018] Further, in step S3, the solvent of the organic phase solution includes one or more of n-hexane, isoalkanes G, H, L, and M; preferably n-hexane.
[0019] Furthermore, in step S3, the settling time is 30~120s.
[0020] Furthermore, in step S4, the heat treatment temperature is 80~120℃ and the heat treatment time is 180~300s.
[0021] In a second aspect, the present invention provides a high-permeability reverse osmosis membrane prepared according to the preparation method described in the first aspect.
[0022] Furthermore, the high-permeability reverse osmosis membrane has a NaCl rejection rate ≥98.85% and a permeation flux ≥70.4 L·m -2 ·h -1 .
[0023] Thirdly, the present invention provides the application of a high-permeability reverse osmosis membrane prepared according to the preparation method described in the first aspect or the high-permeability reverse osmosis membrane described in the second aspect in seawater desalination or wastewater treatment.
[0024] Interfacial polymerization reactions typically occur at pH values between 10 and 11. According to the interfacial polymerization equation, when MPD and TMC polymerize at the interface, they continuously release a large amount of HCl molecules. These HCl molecules dissolve in water, causing dynamic pH changes in the vicinity of the interface. However, this in-situ pH change in the reaction region further alters the form and reactivity of the aqueous monomer MPD: at higher pH (alkaline), MPD exists in molecular form, and based on the principle of "like dissolves like," it readily diffuses into the organic phase, ultimately undergoing interfacial polymerization with the organic monomer TMC at the interface; at lower pH (acidic), the -NH2 in the MPD molecule is converted to -NH3. + At this time, the ionic state of MPD-H + It is readily soluble in the aqueous phase, and its diffusion rate into the organic phase is significantly reduced, and the ionic state of MPD-H + Since it cannot undergo nucleophilic substitution with TMC, the polymerization reaction at the two-phase interface will ultimately be inhibited. That is, the in-situ pH change during the interfacial polymerization reaction becomes a potential "switch" for regulating monomer diffusion and reaction behavior.
[0025] In summary, when the interfacial polymerization regulator has an acidity / alkalinity (pKa value between 10-11) that matches the dynamic pH changes at the polymerization interface, it can effectively consume the HCl molecules released during the interfacial polymerization process, thus inhibiting the conversion of the aqueous monomer MPD to the ionic state MPD-H. +The transformation reduces the uncertainty in the interfacial polymerization process. On the other hand, when the interfacial polymerization regulator can interact with MPD (such as hydrogen bonding, π-π interactions, etc.), the orderliness of MPD diffusion and polymerization can be improved by leveraging the interaction between the regulator and MPD. This invention utilizes the dynamic changes in pH during the interfacial polymerization process to design a pH-responsive agent that exhibits reversible protonation behavior and physical interaction with MPD within a specific pH range. By dynamically and orderly controlling the diffusion behavior of MPD at different stages of the polymerization reaction, a more porous, uniform, and larger free volume high-permeability polyamide separation layer structure is induced, thereby improving the water permeability of the reverse osmosis membrane.
[0026] This invention selects 4-phenylbutylamine (pKa=10.21), whose acidity (pKa) falls within the pH window (pH 10-11) of interfacial polymerization, as a pH-responsive agent to effectively regulate MPD diffusion. Before and during the interfacial polymerization reaction, the protonated / unprotonated state of 4-phenylbutylamine is in dynamic equilibrium, which can act as an in-situ "regulatory switch": In the initial stage of the interfacial polymerization reaction, unprotonated 4-phenylbutylamine and MPD diffuse together towards the water / organic phase interface. Due to the smaller molecular weight of MPD, it diffuses faster and reaches the interface first, reacting with TMC and releasing HCl. This results in a large amount of HCl being generated at the interface, lowering the pH value, and causing the relatively slower-diffusion-rate 4-phenylbutylamine to protonate at the interface. The protonated 4-phenylbutylamine ion possesses both ionic and organic groups, enhancing its amphiphilicity. It interpenetrates at the water / organic phase interface. Simultaneously, the protonated 4-phenylbutylamine exhibits strong hydrogen bonds and π-π interactions with the MPD monomer, enhancing the orderly distribution and diffusion of MPD at the interface. As the pH at the interface fluctuates, the protonated / unprotonated forms of 4-phenylbutylamine dynamically change, altering its influence on MPD. Therefore, based on the pH-responsive characteristics of 4-phenylbutylamine's forms, its "interfacial anchoring and channel diffusion" effect effectively improves the orderliness of MPD diffusion, reduces the protonation rate of MPD, and effectively inhibits excessive crosslinking between MPD and TMC. This results in a more uniform, porous polyamide reverse osmosis membrane with a higher free volume, achieving a significant improvement in water permeability.
[0027] Compared with existing technologies, the high-permeability reverse osmosis membrane and its preparation method based on pH response-regulated monomer diffusion described in this invention have the following advantages:
[0028] (1) The high-permeability reverse osmosis membrane of the present invention introduces 4-phenylbutylamine with reversible protonation properties and utilizes the local pH change caused by the gradual release of HCl during the interfacial polymerization reaction to achieve staged regulation of MPD diffusion behavior. Unlike the prior art that uses surfactants and other additives to fix and regulate monomer diffusion, the diffusion regulation behavior of the present invention changes automatically with the reaction process, effectively avoiding the problem of continuous promotion / inhibition of monomer diffusion during interfacial polymerization.
[0029] (2) The high-permeability reverse osmosis membrane of the present invention not only effectively reduces the diffusion rate of MPD by dynamically controlling the diffusion behavior of MPD, but also transforms the diffusion of MPD from the original approximately free diffusion to a diffusion mode with certain orientation and path constraint, so that the prepared reverse osmosis membrane exhibits a more uniform surface structure, a looser free volume and a higher roughness.
[0030] (3) The diffusion regulation mechanism of the high-permeability reverse osmosis membrane preparation method of the present invention does not require additional process control, but is entirely induced by the byproducts of the interfacial polymerization reaction itself. Therefore, the preparation method of the present invention has good compatibility with existing reverse osmosis membrane preparation processes, does not require substantial modification to existing production processes, and is conducive to its promotion and application on an industrial scale. At the same time, experimental results show that the reverse osmosis membrane prepared by the preparation method of the present invention has a significantly higher water flux than the control membrane without added regulator when the desalination rate meets the requirements for industrial wastewater desalination (desalination rate > 96%).
[0031] (4) This invention proposes a new strategy for controlling monomer diffusion based on changes in the intrinsic environment of interfacial polymerization reaction. This idea can be extended to other amine monomers with similar pKa values or similar interfacial polymerization systems, providing a new technical path for the design of high-performance separation membrane materials. Attached Figure Description
[0032] The accompanying drawings, which form part of this invention, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:
[0033] Figure 1 This is a scanning electron microscope image of the surface of the reverse osmosis membrane prepared in Comparative Example 1 of the present invention.
[0034] Figure 2 This is a scanning electron microscope image of the surface of the reverse osmosis membrane prepared in Example 3 of the present invention.
[0035] Figure 3 This is a scanning electron microscope image of the surface of the reverse osmosis membrane prepared in Example 4 of the present invention.
[0036] Figure 4This is a surface roughness characterization diagram of the reverse osmosis membrane prepared in Comparative Example 1 of the present invention.
[0037] Figure 5 This is a surface roughness characterization diagram of the reverse osmosis membrane prepared in Example 4 of the present invention.
[0038] Figure 6 This is a simulation diagram of the free volume fraction of the reverse osmosis membrane prepared in Comparative Example 1 of the present invention.
[0039] Figure 7 This is a simulation diagram of the free volume fraction of the reverse osmosis membrane prepared in Example 4 of the present invention. Detailed Implementation
[0040] It should be noted that, unless otherwise specified, the embodiments and features described in the present invention can be combined with each other.
[0041] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.
[0042] The main raw materials and reagents used in the embodiments and comparative examples of this invention are as follows:
[0043] Polysulfone ultrafiltration membrane, purchased from Jiangsu Qicheng Purification Technology Co., Ltd.;
[0044] m-Phenylenediamine (MPD), 99%, purchased from Shanghai Aladdin Biochemical Technology Co., Ltd.;
[0045] Trimethylpyridine chloride (TMC), 98%, purchased from Shanghai Aladdin Biochemical Technology Co., Ltd.;
[0046] n-Hexane, >98%, purchased from Shanghai Aladdin Biochemical Technology Co., Ltd.
[0047] Camphor sulfonic acid (CSA), >98%, purchased from TCI (Shanghai) Chemical Industry Development Co., Ltd.
[0048] Sodium chloride (NaCl), analytical grade, purchased from Tianjin Kemeo Chemical Reagent Co., Ltd.
[0049] Triethylamine (TEA), 99%, purchased from Tianjin Kemeo Chemical Reagent Co., Ltd.
[0050] 4-Phenylated butyramine (4-PBA), 98%, purchased from Shanghai Aladdin Biochemical Technology Co., Ltd.
[0051] Isoalkanes G, H, L, and M, >98%, purchased from ExxonMobil, USA.
[0052] Nitrogen gas was purchased from Tianjin Huanyu Gas Co., Ltd.
[0053] Example 1:
[0054] This embodiment describes a method for preparing a high-permeability reverse osmosis membrane based on pH-responsive monomer diffusion, comprising the following steps:
[0055] (1) The surface area is 81 cm² 2 A polysulfone ultrafiltration membrane with no liquid droplets on its surface is fixed on a frame;
[0056] (2) Dissolve 0.025 L of 2.0 wt.% m-phenylenediamine, 2.3 wt.% camphor sulfonic acid, 1.3 wt.% triethylamine and 0.002 wt.% 4-phenylbutylamine in deionized water to obtain an aqueous solution. Pour the aqueous solution onto the surface of the polysulfone ultrafiltration membrane, let it stand for 90 s, remove the residual aqueous solution and blow the membrane surface dry with nitrogen.
[0057] (3) Pour 0.025 L of a 0.1 wt.% solution of pyromellitic chlorohexane onto the surface of the membrane obtained in step (2), let it stand for 60 s, and then remove the excess organic phase solution.
[0058] (4) The membrane obtained in step (3) is heat-treated at 80°C for 300s, cooled, rinsed with deionized water and dried to obtain the high-permeability reverse osmosis membrane.
[0059] Example 2:
[0060] The difference between this embodiment and embodiment 1 is that in step (2), the mass fraction of 4-phenylbutyramine is 0.004 wt.%, and the other conditions remain unchanged.
[0061] Example 3:
[0062] The difference between this embodiment and embodiment 1 is that in step (2), the mass fraction of 4-phenylbutyramine is 0.006 wt.%, and the other conditions remain unchanged.
[0063] Example 4:
[0064] The difference between this embodiment and embodiment 1 is that in step (2), the mass fraction of 4-phenylbutanylamine is 0.008 wt.%, and the other conditions remain unchanged.
[0065] Comparative Example 1:
[0066] The difference between this comparative example and Example 1 is that in step (2), the mass fraction of 4-phenylbutyramine is 0 wt.%, and the other conditions remain unchanged.
[0067] Comparative Example 2:
[0068] The difference between this comparative example and Example 1 is that in step (2), the mass fraction of 4-phenylbutyramine is 0.01 wt.%, and the other conditions remain unchanged.
[0069] Comparative Example 3:
[0070] The difference between this comparative example and Example 1 is that in step (2), the mass fraction of 4-phenylbutanamine is 0.03 wt.%, and the other conditions remain unchanged.
[0071] Performance testing:
[0072] The reverse osmosis membranes obtained in Examples 1-4 and Comparative Examples 1-3 were tested using a cross-flow filtration device.
[0073] The obtained membrane sample was placed in three parallel filtration units, with an effective filtration area of 23.55 cm². 2 A 2000 mg / L NaCl aqueous solution was used as the feed solution, with a pH of 7.0 ± 0.5. The prepared reverse osmosis membrane was first pre-pressurized for 30 min at 1.55 MPa and 25 ± 1 °C, and then filtered at a pressure of 1.55 MPa and 80 L·h⁻¹. -1 Permeate was collected at a cross-flow rate.
[0074] Water permeation flux is calculated using formula (1):
[0075] (1)
[0076] In the formula, F is the water permeability flux, with units of L / (m²). 2 ·h); A is the effective membrane area, in m². 2 t represents the infiltration time, in hours (h). It is within a certain time. The volume of infiltrated water collected internally, in liters (L).
[0077] The NaCl rejection rate is calculated using formula (2):
[0078] (2)
[0079] In the formula, R is the NaCl rejection rate, expressed as a percentage (%), and C... p and C f These are the salt concentrations of the permeate and feed solution, respectively, in mg / L.
[0080] The characterization and test results of the reverse osmosis membrane are shown in Table 1.
[0081] Table 1 Characterization and test results of reverse osmosis membranes
[0082]
[0083] As shown in Table 1, due to the large amount of HCl generated during the interfacial polymerization process, the pH value of the aqueous solution after the reaction ranged from 8.2 to 9.5, all below 10. Comparative Example 1, without the addition of 4-phenylbutylamine, had the lowest pH value at only 8.2. The pH value gradually increased with increasing 4-phenylbutylamine concentration. Since the pH values of Examples 1-4 and Comparative Examples 2 and 3 were all lower than the pKa value of 4-phenylbutylamine, it can be inferred that 4-phenylbutylamine underwent a neutralization reaction with the HCl generated during the interfacial polymerization process. During the consumption of HCl, 4-phenylbutylamine was converted to a protonated form (ionic state). The ionic groups have stronger hydrophilicity and are easily soluble in the aqueous phase, while the phenyl groups have stronger hydrophobicity and are easily soluble in the organic phase, exhibiting an interpenetrating state at the interface between the aqueous and organic phases. The ionic 4-phenylbutylamine interpenetrating at the water-organic interface provides a more ordered transport channel for MPD diffusion, promoting the formation of a more suspended and taller polyamide microstructure.
[0084] Meanwhile, as the concentration of 4-phenylbutylamine molecules increases, the diffusion rate of MPD monomers slowly decreases from 0.0062 g / L. -1 s -1 (Comparative Example 1) decreased to 0.0028 g / L -1 s -1 (Comparative Example 3). This is because as the concentration of 4-phenylbutamine molecules increases and the proportion of protonated 4-phenylbutamine in the polymerization reaction increases, the protonated 4-phenylbutamine at the interface of the two phases enhances the inhibition of MPD diffusion based on hydrogen bonding and π-π interactions, effectively reducing the diffusion rate of MPD. Therefore, it is more conducive to improving the orderliness of MPD monomer diffusion and interfacial polymerization process.
[0085] The surface morphology and roughness of the examples and comparative examples were analyzed. Comparative Example 1, without the addition of 4-phenylbutylamine, had the lowest surface roughness, only 55.38 nm. With increasing 4-phenylbutylamine concentration, the surface roughness of the reverse osmosis membrane continuously increased from 60.48 nm (Example 1) to 86.75 nm (Comparative Example 3). Figure 4-5 As shown in the figure, the ionic 4-phenylbutylamine intercalating at the interface between the two phases promotes the formation of a higher polyamide structure, and the increased surface roughness of the reverse osmosis membrane is beneficial to the improvement of permeation flux. Simultaneously, the surface morphology of the reverse osmosis membrane gradually changes. The results are as follows... Figure 1-3As shown, the reverse osmosis membrane without 4-phenylbutylamine (Comparative Example 1) has a surface composed of the typical "nodular" structure of polyamide, exhibiting the wrinkled state characteristic of the polyamide separation layer. When 0.006 wt.% of 4-phenylbutylamine is added during the preparation process (Example 3), the number of blade-like structures on the surface of the polyamide separation layer increases significantly, and the structure becomes more uniform and three-dimensional. When the concentration of 4-phenylbutylamine is further increased to 0.008 wt.% (Example 4), the polyamide separation layer structure gradually transforms into a more expansive "blade-like" structure. The more expansive structure on the surface of the reverse osmosis membrane is beneficial for increasing the water permeation area and improving the water permeation flux.
[0086] The free volume fraction within the polyamide structure was analyzed using molecular dynamics simulations (as shown in Table 1). Figure 6-7 (As shown). Because the protonated 4-phenylbutylamine at the two-phase interface effectively reduces the diffusion rate of MPD, the number of MPDs participating in the polymerization process decreases, effectively increasing the free volume fraction of the polyamide separation layer at the molecular level. Therefore, the free volume fraction of Comparative Example 1 without added 4-phenylbutylamine is the lowest, at only 24.9%. As the concentration of 4-phenylbutylamine increases, the free volume fraction of the prepared high-permeability polyamide reverse osmosis membrane gradually increases from 25.6% to 35.7%. The increase in free volume fraction is beneficial for improving the permeability of the reverse osmosis membrane.
[0087] Regarding permeate flux and desalination rate, when the concentration of 4-phenylbutylamine is below 0.008 wt.% (Examples 1-4), the reverse osmosis membrane maintains a stable NaCl rejection rate of over 98%, meeting the conventional desalination requirements for industrial wastewater (desalination rate >96%), while the pure water flux significantly increases to 70.4 L·m -2 ·h -1 In particular, when the concentration of 4-phenylbutylamine was 0.008 wt.% (Example 4), the reverse osmosis membrane maintained a high desalination rate of 98.85% while increasing the permeate flux to 70.4 L·m. -2 ·h -1 Compared to Comparative Example 1 without 4-phenylbutylamine, the permeation flux increased by 28.3%. However, when the concentration of 4-phenylbutylamine was further increased to 0.01 wt.% and 0.03 wt.% (Comparative Examples 2-3), although permeability significantly improved, the desalination rate decreased to below 98%. Addressing the dependence of the interfacial polymerization process on specific pH conditions, this invention utilizes the dynamic response of 4-phenylbutylamine molecules to the HCl generated during the interfacial polymerization reaction. By controlling the monomer diffusion rate through the protonation effect of 4-phenylbutylamine, a high-permeability polyamide reverse osmosis membrane with larger free volume, higher surface roughness, and relatively uniform structure was successfully prepared.
[0088] In summary, this invention provides a method for effectively slowing down the diffusion rate of MPD by introducing 4-phenylbutylamine with reversible protonation properties, based on the pH response characteristics during interfacial polymerization. This achieves dynamic and orderly control of MPD diffusion behavior, thereby improving the uniformity of the reverse osmosis membrane structure and uniformly increasing the free volume of the reverse osmosis membrane. System characterization and performance testing results show that this preparation strategy can significantly improve the permeation performance of the membrane material while maintaining a high desalination rate.
[0089] The embodiments described above are only some embodiments of the present invention, not all embodiments. Other embodiments obtained by those skilled in the art based on the embodiments of the present invention without creative effort are all within the scope of protection of the present invention.
Claims
1. A method for preparing a high-permeability reverse osmosis membrane based on pH-responsive regulation of monomer diffusion, characterized in that, The preparation method includes the following steps: S1. Mix m-phenylenediamine, camphor sulfonic acid, triethylamine and 4-phenylbutylamine with water to obtain an aqueous solution, wherein the mass fraction of 4-phenylbutylamine in the aqueous solution is 0.002~0.03%; S2. Pour the aqueous solution onto the surface of the polysulfone ultrafiltration membrane, let it stand and then dry to obtain an aqueous adsorption membrane. S3. Pour the organic phase solution containing trimesoyl chloride onto the surface of the aqueous phase adsorption membrane obtained in step S2. After standing, remove the excess organic phase solution to obtain the interfacial polymerization precursor membrane. S4. The interfacial polymerization precursor membrane obtained in step S3 is subjected to heat treatment to obtain the high-permeability reverse osmosis membrane.
2. The preparation method according to claim 1, characterized in that: In step S2, the aqueous solution contains 1.5-2.0% intermediate-phenylenediamine, 1.5-2.5% camphor sulfonic acid, 0.5-1.5% triethylamine, and 0.002-0.008% 4-phenylbutylamine.
3. The preparation method according to claim 1, characterized in that: In step S2, the settling time is 30~120s.
4. The preparation method according to claim 1, characterized in that: In step S3, the mass fraction of pyromellitic chloroformyl chloride in the organic phase solution is 0.1~0.15%.
5. The preparation method according to claim 1, characterized in that: In step S3, the volume of the organic phase solution includes one or more of the following: n-hexane, isoalkanes G, H, L, and M.
6. The preparation method according to claim 1, characterized in that: In step S3, the settling time is 30~120s.
7. The preparation method according to claim 1, characterized in that: In step S4, the heat treatment temperature is 80~120℃ and the heat treatment time is 180~300s.
8. A high-permeability reverse osmosis membrane prepared by any one of the preparation methods according to claims 1-7.
9. The high-permeability reverse osmosis membrane according to claim 8, characterized in that, The high-permeability reverse osmosis membrane has a NaCl rejection rate of ≥98.85% and a permeation flux of ≥70.4 L·m -2 ·h -1 .
10. The application of the high-permeability reverse osmosis membrane prepared by any one of the preparation methods according to claims 1-7 or the high-permeability reverse osmosis membrane according to claim 8 or 9 in seawater desalination or wastewater treatment.