CN115245746A - Membrane module aperture optimization method - Google Patents
Membrane module aperture optimization method Download PDFInfo
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- CN115245746A CN115245746A CN202110470437.1A CN202110470437A CN115245746A CN 115245746 A CN115245746 A CN 115245746A CN 202110470437 A CN202110470437 A CN 202110470437A CN 115245746 A CN115245746 A CN 115245746A
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- separation membrane
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention belongs to the field of membrane repair, and particularly relates to a membrane module aperture optimization method, which comprises the following steps: 1) Inquiring a separation membrane operating manual or a field experiment to obtain the bubble point pressure of the target separation membrane; 2) Pressing an optimizing agent into a separation membrane component through a water producing port at the pressure of target bubble point pressure, and enabling the optimizing agent to enter a raw water side from a water producing side through a large hole; 3) When the pore diameter is close to the pore diameter of a target membrane, the optimizing agent cannot permeate the membrane under the pressure, and the membrane component finishes optimizing and upgrading; the method of the invention can optimize the irreversibility reduction of the aperture of the membrane component in situ aiming at the special working condition that the size of the treated feed liquid is permanently reduced. The existing various membrane assemblies can be subjected to irreversible aperture reduction and upgrading, so that the cost is reduced and unnecessary consumption is reduced.
Description
Technical Field
The invention belongs to the field of membrane repair, and particularly relates to a membrane module aperture optimization method.
Background
The separating membrane has the advantages of high interception precision, good separation effect, energy conservation, high efficiency, simplicity, controllability and the like, and is widely applied to a plurality of fields of municipal administration, spinning, printing and dyeing, petrifaction, metallurgy and the like.
At present, the membrane module types comprise various types such as a hollow fiber type, a tubular type, a roll type, a butterfly type and the like, have respective uniqueness and have different application market prospects. After the membrane component is processed and formed, the characteristics of interception precision and the like of the membrane component are fixed according to the basic parameters of the selected membrane.
The aperture of the membrane module is fixed, namely the membrane module with a fixed model is used for treating feed liquid with a corresponding size range, when the size of the feed liquid is permanently reduced, a membrane model product with a smaller aperture is usually required to be replaced, the original membrane module can only be used for other purposes or even be discarded, for large-scale engineering application, the number of the membrane modules is huge, and the corresponding cost waste is huge.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a membrane module aperture optimization method.
In order to realize the purpose, the invention adopts the technical scheme that:
a membrane module pore size optimization method comprising the steps of:
1) Inquiring a separation membrane operating manual or a field experiment to obtain the bubble point pressure of the target separation membrane;
2) Pressing an optimizing agent into a separation membrane component through a water producing port at the pressure of target bubble point pressure, and enabling the optimizing agent to enter a raw water side from a water producing side through a large hole;
3) When the pore diameter is close to the pore diameter of a target membrane, the optimizing agent cannot permeate the membrane under the pressure, and the membrane component completes optimization and upgrading;
wherein, the optimizing agent comprises the following components in percentage by mass: 10-30 parts of target separation membrane main body material, 10-30 parts of solvent for dissolving the separation membrane main body material, and 40-80 parts of inert carrier agent which can not be singly dissolved and is blended with the separation membrane/solvent system.
The main material of the separation membrane is one or more of PVDF, PP, PVC, PE, PES and PS.
The solvent is one or a mixture of more of DMAc, DMF, NMP, tetrahydrofuran and sulfolane.
The inert carrier agent is one or a mixture of ethanol, polyethylene glycol and ethyl acetate.
The preparation method of the optimizing agent comprises the following steps: gradually adding a small amount of high polymer into the solvent at 25-100 deg.C, stirring to obtain uniform solution, adding inert carrier agent, stirring, standing to room temperature, and sealing for storage.
Compared with the prior art, the invention has the beneficial effects that:
the method of the invention can optimize the irreversibility reduction of the aperture of the membrane component in situ aiming at the special working condition that the size of the treated feed liquid is permanently reduced. The existing various membrane assemblies can be subjected to irreversible aperture reduction and upgrading, so that the cost is reduced and unnecessary consumption is reduced.
Detailed Description
In order to make the technical solutions of the present invention better understood by those skilled in the art, the present invention will be further described in detail with reference to the preferred embodiments.
The first embodiment is as follows: optimizing the aperture of the PVDF membrane, wherein a special optimizing agent for the PVDF membrane is required: PVDF 30wt%, DMAC 30wt% and ethanol 40wt%. Stirring continuously at 70 deg.C until dissolved to obtain uniform solution, standing to room temperature, and sealing for storage. The optimizing agent is pressed into the membrane component through a water producing port under the pressure of target bubble point pressure, and the optimizing agent can enter the raw water side from the water producing side through a large hole; when entering the raw water side, the membrane component is separated from incompatible liquid in the raw water side, high polymer in the optimizing agent is subjected to in-situ aggregation and filling of macropores after the phase separation of the high polymer in the macropores, and after 13min, the membrane component is optimized and upgraded.
Example two: the aperture of the PES membrane is optimized by using a special optimizing agent for the PES membrane: PES 20wt%, DMF 30wt%, and methanol 50wt%. Stirring continuously at 75 ℃ until the mixture is dissolved into a uniform solution, standing to room temperature, and sealing for storage. The optimizing agent is pressed into the membrane component through a water producing port under the pressure of target bubble point pressure, and the optimizing agent can enter the raw water side from the water producing side through a large hole; when entering the raw water side, the membrane component is separated from incompatible liquid in the raw water side, high polymer in the optimizing agent is subjected to in-situ aggregation and filling of macropores after the phase separation of the macropores, and after 20min, the membrane component is optimized and upgraded.
Example three: the pore diameter of the PVC membrane is optimized, and a special optimizing agent for the PVC membrane is required: 10wt% of PVC, 10wt% of NMP and 200 80wt% of polyethylene glycol. Stirring continuously at 60 ℃ until the mixture is dissolved into a uniform solution, standing to room temperature, and storing in a sealed manner for later use. The optimizing agent is pressed into the membrane component through a water producing port under the pressure of target bubble point pressure, and the optimizing agent can enter the raw water side from the water producing side through a large hole; when the water enters the raw water side, the water is separated from incompatible liquid in the raw water side, high polymer in the optimizing agent is subjected to phase separation at macropores and then is subjected to in-situ aggregation to fill the macropores, and after 10min, the membrane module is optimized and upgraded.
Example four: optimizing the pore diameter of the PP film, wherein a special optimizing agent for the PP film is required: 10wt% of PP, 15wt% of sulfolane and 200 wt% of polyethylene glycol. Stirring continuously at 60 ℃ until the mixture is dissolved into a uniform solution, standing to room temperature, and storing in a sealed manner for later use. The optimizing agent is pressed into the membrane component through a water producing port under the pressure of target bubble point pressure, and the optimizing agent can enter the raw water side from the water producing side through a large hole; when entering the raw water side, the membrane component is separated from incompatible liquid in the raw water side, high polymer in the optimizing agent is subjected to in-situ aggregation and filling of macropores after the phase separation of the high polymer in the macropores, and the membrane component is optimized and upgraded after 22 min.
Example five: optimizing the aperture of the PS membrane, wherein a special optimizing agent for the PS membrane is required: 20wt% of PS, 10wt% of tetrahydrofuran and 70wt% of ethyl acetate. Stirring continuously at 60 ℃ until the mixture is dissolved into a uniform solution, standing to room temperature, and storing in a sealed manner for later use. The optimizing agent is pressed into the membrane component through a water producing port under the pressure of target bubble point pressure, and the optimizing agent can enter the raw water side from the water producing side through a large hole; when entering the raw water side, the membrane component is separated from incompatible liquid in the raw water side, high polymer in the optimizing agent is subjected to in-situ aggregation and filling of macropores after the phase separation of the macropores, and the membrane component is optimized and upgraded after 19 min.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and amendments can be made without departing from the principle of the present invention, and these modifications and amendments should also be considered as the protection scope of the present invention.
Claims (5)
1. A membrane module pore size optimization method, comprising the steps of:
1) Inquiring a separation membrane operating manual or a field experiment to obtain the bubble point pressure of the target separation membrane;
2) Pressing an optimizing agent into a separation membrane component through a water producing port at the pressure of target bubble point pressure, and enabling the optimizing agent to enter a raw water side from a water producing side through a large hole;
3) When the pore diameter is close to the pore diameter of a target membrane, the optimizing agent cannot permeate the membrane under the pressure, and the membrane component completes optimization and upgrading;
wherein, the optimizing agent comprises the following components in percentage by mass: 10-30 parts of a target separation membrane main body material, 10-30 parts of a solvent for dissolving the separation membrane main body material, and 40-80 parts of an inert carrier agent which cannot be singly dissolved in the separation membrane but is blended with a separation membrane/solvent system.
2. The membrane module pore size optimization method according to claim 1, wherein the separation membrane main body material is one or more of PVDF, PP, PVC, PE, PES, PS.
3. The membrane module pore size optimization method according to claim 1, wherein the solvent is one or more of DMAc, DMF, NMP, tetrahydrofuran, and sulfolane.
4. The membrane module pore size optimization method according to claim 1, wherein the inert carrier agent is one or more selected from ethanol, polyethylene glycol, and ethyl acetate.
5. The membrane module pore size optimization method according to claim 1, characterized in that the preparation method of the optimizing agent is as follows: gradually adding a small amount of high polymer into the solvent at 25-100 deg.C, stirring to obtain uniform solution, adding inert carrier agent, stirring, standing to room temperature, and sealing for storage.
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| CN202110470437.1A CN115245746B (en) | 2021-04-28 | 2021-04-28 | Membrane module aperture optimization method |
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| CN202110470437.1A CN115245746B (en) | 2021-04-28 | 2021-04-28 | Membrane module aperture optimization method |
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| CN115245746B CN115245746B (en) | 2023-08-04 |
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Citations (10)
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|---|---|---|---|---|
| US4774039A (en) * | 1980-03-14 | 1988-09-27 | Brunswick Corporation | Dispersing casting of integral skinned highly asymmetric polymer membranes |
| WO1999040996A1 (en) * | 1998-02-16 | 1999-08-19 | B.P.T. Bio Pure Technology Ltd. | Selective membrane and process for its preparation |
| JP2001205056A (en) * | 2000-01-28 | 2001-07-31 | Mitsubishi Rayon Co Ltd | Method for inspecting leak of separation membrane |
| US20050011826A1 (en) * | 2001-07-20 | 2005-01-20 | Childs Ronald F. | Asymmetric gel-filled microporous membranes |
| JP2008229503A (en) * | 2007-03-20 | 2008-10-02 | Toshiba Corp | Membrane, membrane module and membrane filter system |
| CN102397756A (en) * | 2010-09-08 | 2012-04-04 | 天津工业大学 | Method for processing hydrophobic separation membrane |
| WO2015141653A1 (en) * | 2014-03-19 | 2015-09-24 | 東洋紡株式会社 | Composite separation membrane |
| JP2016068005A (en) * | 2014-09-29 | 2016-05-09 | ユニチカ株式会社 | Polyamide hollow fiber membrane |
| KR20180114820A (en) * | 2017-04-11 | 2018-10-19 | 재단법인 탄소순환형 차세대 바이오매스 생산전환 기술연구단 | Antifouling Hollow fiber membrane module, Method for preparing the same and Uses thereof |
| CN109569325A (en) * | 2019-01-17 | 2019-04-05 | 南京工业大学 | A kind of preparation method of filled-type gradient pore separation membrane |
-
2021
- 2021-04-28 CN CN202110470437.1A patent/CN115245746B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4774039A (en) * | 1980-03-14 | 1988-09-27 | Brunswick Corporation | Dispersing casting of integral skinned highly asymmetric polymer membranes |
| WO1999040996A1 (en) * | 1998-02-16 | 1999-08-19 | B.P.T. Bio Pure Technology Ltd. | Selective membrane and process for its preparation |
| JP2001205056A (en) * | 2000-01-28 | 2001-07-31 | Mitsubishi Rayon Co Ltd | Method for inspecting leak of separation membrane |
| US20050011826A1 (en) * | 2001-07-20 | 2005-01-20 | Childs Ronald F. | Asymmetric gel-filled microporous membranes |
| JP2008229503A (en) * | 2007-03-20 | 2008-10-02 | Toshiba Corp | Membrane, membrane module and membrane filter system |
| CN102397756A (en) * | 2010-09-08 | 2012-04-04 | 天津工业大学 | Method for processing hydrophobic separation membrane |
| WO2015141653A1 (en) * | 2014-03-19 | 2015-09-24 | 東洋紡株式会社 | Composite separation membrane |
| JP2016068005A (en) * | 2014-09-29 | 2016-05-09 | ユニチカ株式会社 | Polyamide hollow fiber membrane |
| KR20180114820A (en) * | 2017-04-11 | 2018-10-19 | 재단법인 탄소순환형 차세대 바이오매스 생산전환 기술연구단 | Antifouling Hollow fiber membrane module, Method for preparing the same and Uses thereof |
| CN109569325A (en) * | 2019-01-17 | 2019-04-05 | 南京工业大学 | A kind of preparation method of filled-type gradient pore separation membrane |
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| XIAOPAN JIN ET. AL.: ""A polymer-ceramic composite membrane for the oilwater separation with enhanced antifouling performance"", 《FERROELECTRICS》, vol. 565 * |
| 成功: ""EVOH和EVOH/PVDF改性膜的制备及抗污染性能研究"", 《工程科技Ⅰ辑》, no. 1 * |
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