CN117654297A - Hydrophilic large-flux desalination composite membrane and preparation method thereof - Google Patents
Hydrophilic large-flux desalination composite membrane and preparation method thereof Download PDFInfo
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- CN117654297A CN117654297A CN202311519256.9A CN202311519256A CN117654297A CN 117654297 A CN117654297 A CN 117654297A CN 202311519256 A CN202311519256 A CN 202311519256A CN 117654297 A CN117654297 A CN 117654297A
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- 239000012528 membrane Substances 0.000 title claims abstract description 102
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 55
- 239000002131 composite material Substances 0.000 title claims abstract description 39
- 238000002360 preparation method Methods 0.000 title abstract description 7
- 239000008346 aqueous phase Substances 0.000 claims abstract description 33
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 22
- 239000004952 Polyamide Substances 0.000 claims abstract description 18
- 230000004907 flux Effects 0.000 claims abstract description 18
- 229920002647 polyamide Polymers 0.000 claims abstract description 18
- UWCPYKQBIPYOLX-UHFFFAOYSA-N benzene-1,3,5-tricarbonyl chloride Chemical compound ClC(=O)C1=CC(C(Cl)=O)=CC(C(Cl)=O)=C1 UWCPYKQBIPYOLX-UHFFFAOYSA-N 0.000 claims abstract description 16
- -1 amino phosphonic acid compound Chemical class 0.000 claims abstract description 15
- 238000012695 Interfacial polymerization Methods 0.000 claims abstract description 12
- 229920000768 polyamine Polymers 0.000 claims abstract description 12
- 239000000178 monomer Substances 0.000 claims abstract description 11
- 239000000243 solution Substances 0.000 claims description 43
- QQVDJLLNRSOCEL-UHFFFAOYSA-N (2-aminoethyl)phosphonic acid Chemical compound [NH3+]CCP(O)([O-])=O QQVDJLLNRSOCEL-UHFFFAOYSA-N 0.000 claims description 16
- 239000012074 organic phase Substances 0.000 claims description 14
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000004695 Polyether sulfone Substances 0.000 claims description 9
- 238000011033 desalting Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 9
- 229920002492 poly(sulfone) Polymers 0.000 claims description 9
- 229920006393 polyether sulfone Polymers 0.000 claims description 9
- MGRVRXRGTBOSHW-UHFFFAOYSA-N (aminomethyl)phosphonic acid Chemical compound NCP(O)(O)=O MGRVRXRGTBOSHW-UHFFFAOYSA-N 0.000 claims description 8
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- GSZQTIFGANBTNF-UHFFFAOYSA-N (3-aminopropyl)phosphonic acid Chemical compound NCCCP(O)(O)=O GSZQTIFGANBTNF-UHFFFAOYSA-N 0.000 claims description 6
- WZCQRUWWHSTZEM-UHFFFAOYSA-N 1,3-phenylenediamine Chemical group NC1=CC=CC(N)=C1 WZCQRUWWHSTZEM-UHFFFAOYSA-N 0.000 claims description 6
- VJKULOSOYPRBSS-UHFFFAOYSA-N 2-aminopropylphosphonic acid Chemical compound CC(N)CP(O)(O)=O VJKULOSOYPRBSS-UHFFFAOYSA-N 0.000 claims description 6
- 238000004140 cleaning Methods 0.000 claims description 6
- 239000011248 coating agent Substances 0.000 claims description 6
- 238000000576 coating method Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 229940018564 m-phenylenediamine Drugs 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 238000002791 soaking Methods 0.000 claims description 6
- 239000002904 solvent Substances 0.000 claims description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 4
- 239000007864 aqueous solution Substances 0.000 claims description 3
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 16
- PTMHPRAIXMAOOB-UHFFFAOYSA-N phosphoramidic acid Chemical class NP(O)(O)=O PTMHPRAIXMAOOB-UHFFFAOYSA-N 0.000 abstract description 4
- 238000006116 polymerization reaction Methods 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 10
- 238000001223 reverse osmosis Methods 0.000 description 8
- 238000001728 nano-filtration Methods 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 6
- 238000011156 evaluation Methods 0.000 description 5
- 239000008367 deionised water Substances 0.000 description 4
- 229910021641 deionized water Inorganic materials 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 239000012527 feed solution Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000035699 permeability Effects 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- 238000012696 Interfacial polycondensation Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 235000019341 magnesium sulphate Nutrition 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
The invention discloses a hydrophilic large-flux desalination composite membrane and a preparation method thereof, comprising an ultrafiltration base membrane and a polyamide desalination layer which is arranged on the ultrafiltration base membrane and is formed by interfacial polymerization of polyamine monomers and trimesoyl chloride, wherein the polyamide desalination contains aminophosphonic acid compounds. According to the invention, the amino phosphonic acid compound is directly added into the aqueous phase solution of interfacial polymerization and participates in polymerization reaction, so that the amino phosphonic acid group doped is introduced into the structure of the polyamide layer, the hydrophilicity of the prepared desalination membrane is greatly improved, and higher water flux is obtained.
Description
Technical Field
The invention belongs to the technical field of desalination membranes, and particularly relates to a hydrophilic large-flux desalination composite membrane and a preparation method thereof.
Background
The desalination membrane is a semipermeable membrane and has selective permeability. The water molecule can retain salt and most of organic matters while allowing water molecules to pass through, can be used for separating various fluids, and is widely applied to the fields of petrochemical industry, pharmacy, food, municipal sewage treatment and the like.
Desalination membranes are generally divided into reverse osmosis membranes and nanofiltration membranes according to the differences in the entrapment of monovalent and multivalent salts. In the manufacturing process of the desalination membrane, the prior art generally adopts polyamine and trimesoyl chloride to carry out interfacial polycondensation reaction on the surface of a porous polysulfone/polyethersulfone support membrane to form a polyamide desalination layer.
The polyamide layer of the desalination membrane prepared by interfacial polymerization is a key to influence the water permeability (flux) and salt rejection (desalination rate) of the membrane. Therefore, how to optimize the structure and properties of the polyamide layer, thereby improving the membrane flux and rejection rate, has been the direction of efforts by researchers in this field. If the desalination membrane with higher water flux and better hydrophilicity can be obtained, the equipment energy consumption can be reduced in the actual application process, the equipment investment and the operation cost can be saved, and the efficiency can be improved. Therefore, developing a desalination membrane with higher hydrophilicity and higher flux is an important technical problem to be solved in the art.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a hydrophilic large-flux desalination composite membrane.
The invention also aims to provide a preparation method of the hydrophilic large-flux desalination composite membrane.
The technical scheme of the invention is as follows:
a hydrophilic high-flux desalination composite membrane comprises an ultrafiltration base membrane and a polyamide desalination layer which is arranged on the ultrafiltration base membrane and is formed by interfacial polymerization of a polyamine monomer and trimesoyl chloride, wherein the polyamide desalination contains an aminophosphonic acid compound.
In a preferred embodiment of the present invention, the aminophosphonic acid compound is at least one of aminomethylphosphonic acid, 2-aminoethylphosphonic acid, 2-aminopropylphosphonic acid, and 3-aminopropylphosphonic acid.
Further preferably, the aminophosphonic acid compound is aminomethylphosphonic acid, 2-aminoethylphosphonic acid, 2-aminopropylphosphonic acid, or 3-aminopropylphosphonic acid.
In a preferred embodiment of the present invention, the ultrafiltration membrane is made of polyethersulfone or polysulfone.
In a preferred embodiment of the present invention, the polyamine monomer is m-phenylenediamine and/or piperazine.
In a preferred embodiment of the present invention, the polyamine monomer is m-phenylenediamine and/or piperazine, the aminophosphonic acid compound is aminomethylphosphonic acid or 2-aminoethylphosphonic acid, and the ultrafiltration membrane is made of polyethersulfone or polysulfone.
The preparation method of the hydrophilic large-flux desalination composite membrane comprises the following steps:
(1) Preparing an aqueous solution containing polyamine monomer and aminophosphonic acid compound;
(2) Soaking an ultrafiltration base membrane in the aqueous phase solution, taking out, and squeezing out redundant aqueous phase solution to ensure that no visible liquid drops exist on the surface of the membrane;
(3) Coating the trimesic acid chloride organic phase solution on the surface of the ultrafiltration base membrane soaked in the aqueous phase solution obtained in the step (2), carrying out room-temperature contact reaction for 10-60s, and carrying out interfacial polymerization to form a polyamide desalting layer to obtain a wet composite membrane; wherein, the solvent of the trimesic acid chloride organic phase solution is aliphatic alkane;
(4) And (3) carrying out heat treatment on the wet composite membrane obtained in the step (3) at 50-120 ℃ for 1-5min, and then cleaning to obtain the hydrophilic large-flux desalination composite membrane.
In a preferred embodiment of the present invention, the aliphatic alkane is at least one of n-hexane, n-heptane, n-octane, isoparaar G and isoparaar L.
In a preferred embodiment of the present invention, the polyamine monomer is contained in an amount of 0.2 to 6wt% and the aminophosphonic acid compound is contained in an amount of 0.01 to 0.1wt% in the aqueous phase solution.
Further preferably, the content of the trimesic acid chloride in the trimesic acid chloride organic phase solution is 0.1-0.2wt%.
The beneficial effects of the invention are as follows:
1. according to the invention, the amino phosphonic acid compound is directly added into the aqueous phase solution of interfacial polymerization and participates in polymerization reaction, so that the amino phosphonic acid group doped is introduced into the structure of the polyamide layer, the hydrophilicity of the prepared desalination membrane is greatly improved, and higher water flux is obtained.
2. The preparation process of the invention can completely use the original production equipment, does not need large-scale equipment investment, has controllable production cost, and is suitable for large-scale industrial production.
Detailed Description
The technical scheme of the invention is further illustrated and described through the following specific embodiments.
Example 1
(1) Preparing a piperazine with the mass concentration of 0.5wt% and an aminomethylphosphonic acid mixed aqueous phase solution with the mass concentration of 0.05wt%, and fully stirring to completely dissolve the aqueous phase solution to obtain the aqueous phase solution.
(2) Soaking the polysulfone ultrafiltration base membrane in the aqueous phase solution for 30s, taking out, and squeezing out the redundant aqueous phase solution by using a rubber roller so that no visible liquid drops are formed on the surface of the membrane.
(3) And (3) coating the trimesic acid chloride organic phase solution with the mass concentration of 0.1wt% on the surface of the polysulfone ultrafiltration base membrane soaked with the aqueous phase solution obtained in the step (2), carrying out contact reaction for 30s, and carrying out interfacial polymerization to form a polyamide desalting layer, thereby obtaining the wet composite membrane. Wherein the organic phase solvent is isoparaar G.
(4) And (3) performing heat treatment on the wet composite membrane obtained by the reaction in the step (3) in a hot air oven at 110 ℃ for 2min, and then cleaning the wet composite membrane by deionized water at 50 ℃ to obtain the hydrophilic large-flux desalination composite nanofiltration membrane (recorded as SNF-1).
Example 2
(1) Preparing a piperazine with the mass concentration of 0.3wt% and a 2-aminopropyl phosphonic acid mixed aqueous phase solution with the mass concentration of 0.02wt%, and fully stirring to completely dissolve the mixed aqueous phase solution to obtain the aqueous phase solution.
(2) And (3) soaking the polyethersulfone ultrafiltration membrane in the aqueous phase solution for 60s, taking out, and squeezing out the redundant aqueous phase solution by using a rubber roller so that no visible liquid drops are formed on the surface of the membrane.
(3) And (3) coating the trimesoyl chloride organic phase solution with the mass concentration of 0.1wt% on the surface of the polyethersulfone ultrafiltration membrane soaked with the aqueous phase solution obtained in the step (2), carrying out contact reaction for 45s, and carrying out interfacial polymerization to form a polyamide desalting layer, thereby obtaining the wet composite membrane. Wherein the organic phase solvent is isoparaar L.
(4) And (3) performing heat treatment on the wet composite membrane obtained by the reaction in the step (3) in a hot air oven at 120 ℃ for 2min, and then cleaning the wet composite membrane by deionized water at 50 ℃ to obtain the hydrophilic large-flux desalination composite nanofiltration membrane (recorded as SNF-2).
Example 3
(1) Preparing m-phenylenediamine with the mass concentration of 4wt% and 2-aminoethylphosphonic acid mixed aqueous phase solution with the mass concentration of 0.1wt%, and fully stirring to completely dissolve the solution to obtain aqueous phase solution.
(2) And (3) soaking the polyethersulfone ultrafiltration membrane in the aqueous phase solution for 60s, taking out, and squeezing out the redundant aqueous phase solution by using a rubber roller so that no visible liquid drops are formed on the surface of the membrane.
(3) And (3) coating the trimesoyl chloride organic phase solution with the mass concentration of 0.15wt% on the surface of the polyethersulfone ultrafiltration membrane soaked with the aqueous phase solution obtained in the step (2), carrying out contact reaction for 60 seconds, and carrying out interfacial polymerization to form a polyamide desalting layer, thereby obtaining the wet composite membrane. Wherein the organic phase solvent is n-hexane.
(4) And (3) performing heat treatment on the composite membrane obtained by the reaction in the step (3) in a hot air oven at 60 ℃ for 5min, and then cleaning the composite membrane by deionized water at 50 ℃ to obtain the hydrophilic large-flux desalination composite reverse osmosis membrane (named as SRO-1).
Example 4
(1) Preparing m-phenylenediamine with the mass concentration of 3wt percent and 3-aminopropyl phosphonic acid mixed aqueous phase solution with the mass concentration of 0.08wt percent, and fully stirring to completely dissolve the solution to obtain aqueous phase solution.
(2) Soaking the polysulfone ultrafiltration base membrane in the aqueous phase solution for 60s, taking out, and squeezing out the redundant aqueous phase solution by using a rubber roller so that no visible liquid drops are formed on the surface of the membrane.
(3) And (3) coating the trimesic acid chloride organic phase solution with the mass concentration of 0.1wt% on the surface of the polysulfone ultrafiltration base membrane soaked with the aqueous phase solution obtained in the step (2), carrying out contact reaction for 60 seconds, and carrying out interfacial polymerization to form a polyamide desalting layer, thereby obtaining the wet composite membrane. Wherein the organic phase solvent is n-heptane.
(4) And (3) performing heat treatment on the composite membrane obtained by the reaction in the step (3) in a hot air oven at 80 ℃ for 5min, and then cleaning the composite membrane by deionized water at 50 ℃ to obtain the hydrophilic large-flux desalination composite reverse osmosis membrane (named as SRO-2).
Comparative example 1
An unmodified desalination composite nanofiltration membrane (designated NF-1) was prepared using the same procedure and parameters as in example 1, except that aminomethylphosphonic acid was not added in step (1).
Comparative example 2
An unmodified desalination composite nanofiltration membrane (designated NF-2) was prepared using the same procedure and parameters as in example 2, except that 2-aminopropylphosphonic acid was not added in step (1).
Comparative example 3
A non-modified desalination composite reverse osmosis membrane (designated RO-1) was prepared by the same procedure and parameters as in example 3, except that 2-aminoethylphosphonic acid was not added in step (1).
Comparative example 4
A non-modified desalination composite reverse osmosis membrane (designated RO-2) was prepared by the same procedure and parameters as in example 4, except that 3-aminopropyl phosphonic acid was not added in step (1).
Example 5 the evaluation methods used in the above examples and comparative examples are illustrated:
1. evaluation of desalination Rate and flux
Desalination rate and flux are two important parameters for evaluating the separation performance of desalination membranes. In this example, the separation performance of the desalination membrane in this example was evaluated according to GB/T32373-2015 "reverse osmosis membrane test method" and GB/T34242-2017 "nanofiltration membrane test method".
The desalination rate (R) is defined as: under certain operating conditions, the salt concentration (Cf) of the feed liquid and the salt concentration in the permeate liquidDegree (C) p ) The difference is divided by the salt concentration (Cf) of the feed solution, as shown in formula (1).
Flux is defined as: under certain operating conditions, the volume of water which is transmitted through the unit membrane area in unit time is L/(m) 2 ·h)。
The operating conditions used for the performance of the desalination membrane in this example were:
examples 1-2, comparative examples 1-2: the feed solution was 2000ppm of an aqueous solution of magnesium sulfate at a pH of 7.0.+ -. 0.5, an operating pressure of 0.69MPa and an operating temperature of 25 ℃.
Examples 3-4, comparative examples 3-4: the feed solution was 2000ppm sodium chloride in water at pH 7.0.+ -. 0.5, operating pressure 1.5MPa and operating temperature 25 ℃.
2. Evaluation of hydrophilicity
The hydrophilicity of the desalination membrane has an important influence on the performance of the membrane, and the high hydrophilicity is not only beneficial to the passage of water molecules, but also ensures that the membrane has better anti-pollution performance, saves the running cost and prolongs the service life. In the embodiment, a contact angle tester is adopted to drop a water drop on the surface of the reverse osmosis membrane, and the hydrophilicity and hydrophobicity of the membrane material are represented by measuring the contact angle of the water drop on the surface of the membrane. The smaller the contact angle value, the better the hydrophilicity of the film surface.
In the embodiment, a JCY-1 optical contact angle tester is adopted to test the contact angle of the membrane, and in order to ensure the accuracy of analysis results, the membrane is detected at different positions of the desalination membrane for more than 5 times, and an average value is obtained. The test conditions were as follows: ambient temperature: 25.0.+ -. 2.0 ℃ relative humidity: 60% ± 5%.
Analysis of test results:
desalination rate, flux, and contact angle tests were performed on desalination membranes prepared in examples and comparative examples, and the results are shown in the accompanying table 1.
TABLE 1 desalination Rate, flux, hydrophilicity evaluation results
As can be seen from the evaluation results of Table 1, regardless of the comparison between nanofiltration desalination membranes SNF-1, SNF-2 and NF-1, NF-2 prepared in examples 1-2 and comparative examples 1-2, or the comparison between reverse osmosis desalination membranes SRO-1, SRO-2 and RO-1, RO-2 prepared in examples 3-4 and comparative examples 3-4, the permeation flux of the prepared desalination membranes was greatly improved after the aminophosphonic acid compound was added to the aqueous phase, while the desalination rate was maintained at a high desalination rate level (> 99%) without significant decrease. In addition, the contact angle data show that the hydrophilicity of the polyamide desalting layer is obviously improved after amino phosphonic acid doping, and the contact angle is obviously reduced.
As can be seen from the performance test results, the desalination membrane prepared by the invention has the characteristics of high hydrophilicity and large flux, and has good application prospects in the fields of water treatment, industrial separation processes and the like.
The foregoing description is only illustrative of the preferred embodiments of the present invention and is not to be construed as limiting the scope of the invention, i.e., the invention is not to be limited to the details of the invention.
Claims (10)
1. A hydrophilic large flux desalination composite membrane is characterized in that: comprises an ultrafiltration base membrane and a polyamide desalting layer which is arranged on the ultrafiltration base membrane and is formed by interfacial polymerization of a polyamine monomer and trimesoyl chloride, wherein the polyamide desalting layer contains an aminophosphonic acid compound.
2. A hydrophilic high flux desalination composite membrane as defined in claim 1, wherein: the amino phosphonic acid compound is at least one of aminomethylphosphonic acid, 2-amino ethyl phosphonic acid, 2-amino propyl phosphonic acid and 3-amino propyl phosphonic acid.
3. A hydrophilic high flux desalination composite membrane as defined in claim 2, wherein: the amino phosphonic acid compound is aminomethylphosphonic acid, 2-amino ethyl phosphonic acid, 2-amino propyl phosphonic acid or 3-amino propyl phosphonic acid.
4. A hydrophilic high flux desalination composite membrane as defined in claim 1, wherein: the ultrafiltration base membrane is made of polyethersulfone or polysulfone.
5. The method of manufacturing according to claim 1, wherein: the polyamine monomer is m-phenylenediamine and/or piperazine.
6. The method of manufacturing according to claim 1, wherein: the polyamine monomer is m-phenylenediamine and/or piperazine, the aminophosphonic acid compound is aminomethylphosphonic acid or 2-aminoethylphosphonic acid, and the ultrafiltration base membrane is made of polyethersulfone or polysulfone.
7. A method of preparing a hydrophilic high flux desalination composite membrane as defined in any one of claims 1 to 6, characterized in that: the method comprises the following steps:
(1) Preparing an aqueous solution containing polyamine monomer and aminophosphonic acid compound;
(2) Soaking an ultrafiltration base membrane in the aqueous phase solution, taking out, and squeezing out redundant aqueous phase solution to ensure that no visible liquid drops exist on the surface of the membrane;
(3) Coating the trimesic acid chloride organic phase solution on the surface of the ultrafiltration base membrane soaked in the aqueous phase solution obtained in the step (2), carrying out room-temperature contact reaction for 10-60s, and carrying out interfacial polymerization to form a polyamide desalting layer to obtain a wet composite membrane; wherein, the solvent of the trimesic acid chloride organic phase solution is aliphatic alkane;
(4) And (3) carrying out heat treatment on the wet composite membrane obtained in the step (3) at 50-120 ℃ for 1-5min, and then cleaning to obtain the hydrophilic large-flux desalination composite membrane.
8. The method of manufacturing according to claim 7, wherein: the aliphatic alkane is at least one of normal hexane, normal heptane, normal octane, isoparaar G and isoparaar L.
9. The method of claim 7 or 8, wherein: in the aqueous phase solution, the content of the polyamine monomer is 0.2-6wt%, and the content of the aminophosphonic acid compound is 0.01-0.1wt%.
10. The method of preparing as claimed in claim 9, wherein: in the trimesic acid chloride organic phase solution, the content of trimesic acid chloride is 0.1-0.2wt%.
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