CN110871036A - Hollow fiber membrane solidification equipment and method - Google Patents
Hollow fiber membrane solidification equipment and method Download PDFInfo
- Publication number
- CN110871036A CN110871036A CN201811004088.9A CN201811004088A CN110871036A CN 110871036 A CN110871036 A CN 110871036A CN 201811004088 A CN201811004088 A CN 201811004088A CN 110871036 A CN110871036 A CN 110871036A
- Authority
- CN
- China
- Prior art keywords
- cooling
- passage
- channel
- solidification
- central channel
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
- B01D67/0002—Organic membrane manufacture
- B01D67/0009—Organic membrane manufacture by phase separation, sol-gel transition, evaporation or solvent quenching
- B01D67/0016—Coagulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/08—Hollow fibre membranes
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Dispersion Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Manufacturing & Machinery (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a hollow fiber membrane solidification device which comprises a cooling device, a solidification bath device, a circulating device and a circulating pipeline, wherein the cooling device comprises a cooling container and a central channel positioned in the cooling container, the central channel is in a hollow structure with two open ends and longitudinally penetrates through the bottom surface of the cooling container, and the upper end surface of the central channel is lower than the upper end surface of the cooling container, so that a cooling medium in the cooling container enters the central channel through overflow and then returns to the solidification bath device. The invention adopts the cooling device to carry out primary solidification on the hollow fiber membrane, the pressure on the membrane filaments in the solidification process is small, the shaping is easy, and the uniformity of the membrane is kept.
Description
Technical Field
The invention relates to a hollow fiber membrane solidification device and a hollow fiber membrane solidification method.
Background
Hollow fiber membranes are one of the most widely used separation membrane types at present, and the scale of application in industries such as industrial sewage treatment, municipal sewage treatment, seawater desalination, drinking water, food, medicine and the like is gradually enlarged. Hollow fiber membranes are classified into microfiltration and ultrafiltration according to pore size. The market for hollow fiber membrane products has been on the rise year after year in recent years, and ultrafiltration membranes alone are expected to reach $ 46 billion in the global market in 2021. Numerous companies have been producing various hollow fiber separation membrane materials at home and abroad. The main preparation methods of the hollow fiber membrane are phase inversion methods, including an immersion precipitation method (NIPS) and a Thermally Induced Phase Separation (TIPS) method. The NIPS method is the most commonly used method in current industrial membrane modules, a large amount of water-soluble organic solvent is used to dissolve the polymer in the production process, water is used to clean and remove the organic solvent in the membrane in the forming process, and a solvent-containing aqueous solution is commonly used as a core solution, so that a large amount of sewage containing the organic solvent is generated, and environmental protection pressure is brought. In the process of preparing the hollow fiber membrane by the TIPS method, a water-soluble solvent is difficult to adopt, so that organic liquid is required to be used as a coagulating bath and a core solution, the coagulating bath generally adopts a water tank, the spun membrane filaments vertically enter the coagulating bath for a certain depth after passing through a section of air bath, are turned back through a godet wheel after primary coagulation, and are further solidified in the coagulating bath for a period of time to be collected. If the depth of the vertical entering coagulation bath is not enough in the process of coagulation, the initial coagulation is not enough, the membrane wire can deform under stress when the godet wheel turns back, and if the coagulation bath is too deep, a large amount of organic liquid needs to be used, so that the operation is not convenient. On the other hand, if gas is used as the core liquid, the pressure difference between the membrane filaments in the air bath and the coagulation bath is large, particularly, the inside of the membrane filament is gas, the outside of the membrane filament is in a liquid state and vertically enters the coagulation bath for a certain depth, the pressure of the liquid increases along with the depth when the membrane filament is not solidified, the gas of the core liquid is easy to bubble, the uniformity of the membrane filament is seriously influenced, if the membrane filament does not vertically enter the coagulation bath and is solidified only on the surface of the coagulation bath, the cooling rate of the contact surface of the membrane filament and the air is greatly different, the shape of the membrane filament is irregular, and the performance of the hollow fiber membrane is.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a hollow fiber membrane solidification device, which can realize rapid solidification of a membrane by improving the traditional solidification device and adding a cooling device, and the membrane is subjected to small pressure during solidification. The equipment is simple and easy to operate, the use of liquid core liquid is omitted, the extraction agent recycling difficulty is reduced while the dosage of the extraction agent is reduced, the production cost is further reduced, the equipment is particularly suitable for gas core liquid, and the problem that the uniformity of membrane filaments is difficult to control by using the gas core liquid is solved.
According to a first aspect of the present invention, there is provided a hollow fiber membrane coagulation apparatus comprising a cooling device, a coagulation bath device, a circulation device, and a circulation pipe, wherein the cooling device comprises a cooling vessel and a central passage located in the cooling vessel, the cooling device is located above the coagulation bath device, an inlet of the circulation pipe is connected to the coagulation bath device, an outlet of the circulation pipe is connected to the cooling vessel, the circulation device is used for conveying a cooling medium in the coagulation bath device to the cooling device, the central passage is a hollow structure with two open ends and longitudinally passes through the bottom of the cooling vessel, and an upper end surface of the central passage is lower than an upper end surface of the cooling vessel, so that the cooling medium in the cooling vessel overflows into the central passage and then returns to the coagulation bath device.
In the invention, the circulating device conveys the cooling medium in the coagulating bath device to the cooling device, the cooling medium enters a cavity between the cooling container and the central channel in the cooling device, and because the upper end surface of the central channel is lower than the upper end surface of the cooling container, when the cooling medium in the cooling container rises to the upper end surface of the central channel, the cooling medium enters the central channel through overflow and then returns to the coagulating bath device.
According to a preferred embodiment of the present invention, the central channel includes a first channel and a second channel that are integrally connected, the first channel is located below the second channel, the first channel is a circular tubular channel, and the diameter of the second channel gradually increases from bottom to top.
According to a preferred embodiment of the invention, the cooling vessel is an open vessel.
According to a preferred embodiment of the invention, the side edges of the axial cross-section of the second channel are curved.
According to a preferred embodiment of the present invention, the inner diameter of the first passage is not less than 2mm, preferably 5mm or more. The first channel with the size can ensure that the membrane filaments pass through the central channel from top to bottom, if the inner diameter of the first channel is too small, the membrane filaments are difficult to pass through, and turbulence is easily formed in the channel when a solidification medium circulates, so that the stability of the membrane filaments during passing is influenced.
According to a preferred embodiment of the invention, the maximum inner diameter of the second channel is 50-300mm, preferably 100-250 mm.
According to a preferred embodiment of the invention, the height of the central channel is 5-2000mm, preferably 10-1500 mm.
According to a preferred embodiment of the invention, the material of the central channel is chosen such that the contact angle of the cooling medium to the material of the central channel is less than 120 °, preferably less than 110 °; the material of the central channel is selected from metal or resin materials resistant to organic liquids. For example, the material of the central channel is preferably selected from one or more of stainless steel, nylon, polypropylene, polyethylene and polytetrafluoroethylene. If the contact angle of the cooling medium to the material of the central channel is too large, it is not advantageous for the solidified medium to overflow uniformly through the central channel from top to bottom. For example, the cooling medium is soybean oil, and the material of the central channel can be polytetrafluoroethylene; the cooling medium is water, and the material of the central channel can be stainless steel.
According to a preferred embodiment of the present invention, the circulation device comprises a circulation pump and a flow meter, preferably the circulation pump is a gear metering pump, and the flow rate of the circulation pump is preferably in the range of 10-1000 mL/min.
According to a preferred embodiment of the invention, the coagulation bath arrangement comprises a coagulation bath and a temperature control arrangement. The cooling medium is contained in the coagulating bath device, the temperature control device controls the temperature of the cooling medium in the coagulating bath, and preferably, the temperature range of the cooling medium is-15-95 ℃.
According to another aspect of the present invention, there is also provided a method for solidifying a hollow fiber membrane, wherein, using the apparatus as described above, the membrane filaments are discharged from the filament outlet holes of the spinneret and passed through an air bath of 5-300mm into the central passage, the membrane filaments are primarily solidified by contacting with the cooling medium overflowing into the central passage, and the membrane filaments discharged from the central passage are further solidified by being introduced into the solidifying bath device together with the cooling medium.
According to a preferred embodiment of the invention, the cooling device is located directly below the spinneret, the film filaments flow out of the spinneret, pass through the air bath, enter the cooling device vertically, pass through the central channel from top to bottom, and enter the coagulation bath device, and then the film filaments pass through a distance on the surface of the cooling medium and are solidified and enter a subsequent processing device, such as a filament collecting device or an extraction device.
According to a preferred embodiment of the invention, the temperature of the cooling medium is between-15 ℃ and 95 ℃, preferably between-10 ℃ and 60 ℃. The cooling medium that can be used in the present application may be exemplified by one or more of water, liquid paraffin, soybean oil, dibutyl phthalate, dioctyl phthalate, diphenyl ether, carnauba wax, tallow amine, acetyl tributyl citrate, triacetin, diacetin, tributyl citrate, propylene carbonate, dioctyl adipate, diisooctyl adipate, castor oil, diphenyl carbonate, glycerol, benzophenone, polyethylene glycol, and 1, 2-propanediol.
The invention has the following beneficial effects:
the invention adopts the cooling device to carry out primary solidification on the hollow fiber membrane, the pressure on the membrane filaments in the solidification process is small, the shaping is easy, and the uniformity of the membrane is kept.
The membrane filaments do not need to be deeply immersed in the coagulating bath tank in the solidifying process, the resistance is small, the operation is convenient, the consumption of the coagulating medium and the core liquid can be saved, the volume of the coagulating bath tank is reduced, the efficiency of the membrane filaments in the extracting process is improved, the consumption of organic raw materials is reduced, the discharge of waste liquid is reduced, the production cost is further reduced, and the method is particularly suitable for gas core liquid spinning.
The equipment provided by the invention has a remarkable influence on the improvement of the production technology of the hollow fiber membrane, and has a good application prospect.
Drawings
FIG. 1 is a schematic view of a coagulation apparatus of a hollow fiber membrane of the present invention;
the system comprises a cooling container 1, a first channel 2, a second channel 3, a coagulating bath 4, a temperature control device 5, a circulating pump 6, a flow meter 7 and a circulating pipeline 8.
Detailed Description
The present invention will be described in detail with reference to examples, but the present invention is not limited to the examples.
Example 1
As shown in figure 1, the hollow fiber membrane solidification equipment comprises a cooling device, a solidification bath device, a circulating device and a circulating pipeline, wherein the cooling device comprises a cooling container and a central channel which is positioned in the cooling container, the cooling device is positioned above the solidification bath device, the inlet of the circulating pipeline is connected with the solidification bath device, the outlet of the circulating pipeline is connected with the cooling container, the circulating device is used for conveying a cooling medium in the solidification bath device into the cooling device, the central channel is of a hollow structure with two open ends and longitudinally penetrates through the bottom of the cooling container, the upper end face of the central channel is lower than the upper end face of the cooling container, namely the height H of the cooling container2Greater than the height H of the central channel relative to the bottom of the cooling container1So that the cooling medium in the cooling vessel flows by overflow into the central channel and then returns to the coagulation bath device.
The cooling container is an open container with high H2Is 200 mm.
The central channel comprises a first channel and a second channel which are integrally connected, the first channel is positioned below the second channel, the first channel is a circular tubular channel, and the diameter D of the first channel is1Is 5mm, the diameter of the second passage gradually increases from bottom to top, namely D2Greater than D1Of a second channelMaximum diameter D2Is 250mm, the minimum diameter of the second channel is the diameter of the first channel, and the side line of the axial section of the second channel is arc-shaped.
The height of the first channel is 500mm and the height of the second channel is 300 mm.
The central channel is made of stainless steel, and the cooling medium is water.
The circulating device comprises a circulating pump and a flowmeter, the circulating pump is a gear metering pump, and the flow range of the circulating pump is preferably 10-1000 mL/min.
The coagulating bath device comprises a coagulating bath groove and a temperature control device. The cooling medium is contained in the coagulating bath device, the temperature control device controls the temperature of the cooling medium in the coagulating bath, and the temperature range of the cooling medium is-15-95 ℃.
Example 2
A method for solidifying a hollow fiber membrane, using the apparatus of example 1, wherein the apparatus of example 1 is such that a solidifying bath is filled with a cooling medium, the cooling medium is fed to a cooling device by a circulating device, the cooling medium enters a cavity between a cooling container and a central passage, and when the level of the cooling medium in the cooling device exceeds the upper end surface of the central passage, the cooling medium overflows into the central passage and then flows into the solidifying bath.
In the process of preparing the hollow fiber membrane, membrane filaments flow out from filament outlet holes of a spinning nozzle, vertically enter a central channel positioned right below the spinning nozzle through an air bath of 5mm, are contacted with a cooling medium overflowing into the central channel for primary solidification, enter a solidification bath device together with the cooling medium, and then are solidified after passing through a certain distance on the surface of the cooling medium and enter a subsequent treatment device, such as a filament collecting device and/or an extraction device. The cooling medium is water, and the temperature of the cooling medium is-45 ℃.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described with reference to exemplary embodiments, but the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (10)
1. A hollow fiber membrane solidification device comprises a cooling device, a solidification bath device, a circulating device and a circulating pipeline, wherein the cooling device comprises a cooling container and a central channel which is arranged in the cooling container, the cooling device is arranged above the solidification bath device, the inlet of the circulating pipeline is connected with the solidification bath device, the outlet of the circulating pipeline is connected with the cooling container, the circulating device is used for conveying a cooling medium in the solidification bath device to the cooling device, the central channel is of a hollow structure with two open ends and longitudinally penetrates through the bottom surface of the cooling container, and the upper end surface of the central channel is lower than the upper end surface of the cooling container, so that the cooling medium in the cooling container enters the central channel through overflow and then returns to the solidification bath device.
2. The apparatus of claim 1, wherein the central passage comprises a first passage and a second passage which are integrally connected, the first passage is located below the second passage, the first passage is a circular tubular passage, and the diameter of the second passage gradually increases from bottom to top.
3. The apparatus of claim 2, wherein the side line of the axial cross-section of the second channel is arcuate.
4. The apparatus according to claim 2 or 3, wherein the inner diameter of the first channel is not less than 2mm, preferably above 5 mm; and/or the inner diameter of the second channel at the largest is 50-300mm, preferably 100-250 mm.
5. An apparatus according to any one of claims 1-4, wherein the height of the central channel is 5-2000mm, preferably 10-1500 mm.
6. The apparatus according to any of claims 1 to 5, wherein the circulation means comprises a circulation pump and a flow meter, preferably the circulation pump is a gear metering pump, and the flow rate of the circulation pump is preferably in the range of 10-1000 mL/min.
7. The apparatus according to any one of claims 1 to 6, wherein the coagulation bath arrangement comprises a coagulation bath and a temperature control arrangement.
8. The device according to any of claims 1-7, wherein the material of the central channel is preferably selected from a metallic material or a resin material, further preferably one or more of stainless steel, nylon, polypropylene, polyethylene and polytetrafluoroethylene.
9. A method for coagulating hollow fibre membranes, using an apparatus as claimed in any one of claims 1 to 8, wherein the membrane filaments are discharged from the outlet orifices of the spinneret and passed through a 5-300mm air bath into the central passage, the membrane filaments are initially coagulated by contact with a cooling medium which overflows into the central passage, and the membrane filaments discharged from the central passage are further coagulated by passage together with the cooling medium in a coagulation bath apparatus.
10. Solidification method according to claim 9, characterised in that the temperature of the cooling medium is between-15 ℃ and 95 ℃, preferably between-10 ℃ and 60 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811004088.9A CN110871036B (en) | 2018-08-30 | 2018-08-30 | Hollow fiber membrane solidification equipment and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811004088.9A CN110871036B (en) | 2018-08-30 | 2018-08-30 | Hollow fiber membrane solidification equipment and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110871036A true CN110871036A (en) | 2020-03-10 |
| CN110871036B CN110871036B (en) | 2022-10-21 |
Family
ID=69715220
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811004088.9A Active CN110871036B (en) | 2018-08-30 | 2018-08-30 | Hollow fiber membrane solidification equipment and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110871036B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4708800A (en) * | 1984-10-09 | 1987-11-24 | Terumo Kabushiki Kaisha | Hollow fiber membrane and method for manufacture thereof |
| US5139529A (en) * | 1987-01-20 | 1992-08-18 | Terumo Kabushiki Kaisha | Porous polypropylene membrane and methods for production thereof |
| US5489382A (en) * | 1987-10-29 | 1996-02-06 | Terumo Kabushiki Kaisha | Oxygenator using porous hollow fiber membrane |
| CN1552960A (en) * | 2003-06-05 | 2004-12-08 | 天津膜天膜工程技术有限公司 | Preparing method and apparatus for hollow fibrous membrane |
| JP2006342451A (en) * | 2005-06-08 | 2006-12-21 | Teijin Techno Products Ltd | Dry-wet spinning method and apparatus therefor |
| CN101138706A (en) * | 2006-09-04 | 2008-03-12 | 胡萍 | Bunchiness hollow fiber film and method of preparing the same |
| CN106861447A (en) * | 2017-03-02 | 2017-06-20 | 北京航空航天大学 | A kind of preparation method of polysulfone fibre film |
| KR20180076078A (en) * | 2016-12-27 | 2018-07-05 | 주식회사 휴비스 | Apparatus For Producing Aramid Fibers Composed Of Multi-stage Coagulation Baths And Aramid Fibers |
-
2018
- 2018-08-30 CN CN201811004088.9A patent/CN110871036B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4708800A (en) * | 1984-10-09 | 1987-11-24 | Terumo Kabushiki Kaisha | Hollow fiber membrane and method for manufacture thereof |
| US5139529A (en) * | 1987-01-20 | 1992-08-18 | Terumo Kabushiki Kaisha | Porous polypropylene membrane and methods for production thereof |
| US5489382A (en) * | 1987-10-29 | 1996-02-06 | Terumo Kabushiki Kaisha | Oxygenator using porous hollow fiber membrane |
| CN1552960A (en) * | 2003-06-05 | 2004-12-08 | 天津膜天膜工程技术有限公司 | Preparing method and apparatus for hollow fibrous membrane |
| JP2006342451A (en) * | 2005-06-08 | 2006-12-21 | Teijin Techno Products Ltd | Dry-wet spinning method and apparatus therefor |
| CN101138706A (en) * | 2006-09-04 | 2008-03-12 | 胡萍 | Bunchiness hollow fiber film and method of preparing the same |
| KR20180076078A (en) * | 2016-12-27 | 2018-07-05 | 주식회사 휴비스 | Apparatus For Producing Aramid Fibers Composed Of Multi-stage Coagulation Baths And Aramid Fibers |
| CN106861447A (en) * | 2017-03-02 | 2017-06-20 | 北京航空航天大学 | A kind of preparation method of polysulfone fibre film |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110871036B (en) | 2022-10-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| Wibisono et al. | Two-phase flow in membrane processes: A technology with a future | |
| RU2426586C1 (en) | Hollow-fibre membrane module, method of its production, assembly unit with said module and method of suspended water treatment thereby | |
| JP4919183B1 (en) | Hollow fiber type reverse osmosis membrane and method for producing the same | |
| US7717405B2 (en) | Hollow fiber membrane contact apparatus and process | |
| WO2013118859A1 (en) | Hollow fiber semipermeable membrane, method for manufacturing same, module, and water treatment method | |
| JP2015061727A (en) | Skin-formed hollow fiber membrane and production method thereof | |
| CN104174303A (en) | Enhanced hollow polyvinylidene fluoride fiber ultrafiltration membrane and preparation method thereof | |
| JP6122525B1 (en) | Cleaning method for hollow fiber membrane module | |
| CN105163836A (en) | Central baffle, pressurized hollow fiber separation membrane module comprising same, and method for washing same | |
| WO2018179502A1 (en) | Method for washing hollow fiber membrane module and hollow fiber membrane filtration device | |
| CN110871037A (en) | Hollow fiber separation membrane and preparation method thereof | |
| CN104710034A (en) | Advanced treatment method for oilfield produced water | |
| JP2018103184A (en) | Manufacturing method of hollow fiber type semipermeable membrane | |
| CN110871036B (en) | Hollow fiber membrane solidification equipment and method | |
| WO2014192433A1 (en) | Filtration device and immersed filtration method using same | |
| JP2013198893A (en) | Hollow-fiber type semipermeable membrane, method for manufacturing the same, and module | |
| JPWO2017122673A1 (en) | Hollow fiber type semipermeable membrane for reverse osmosis or forward osmosis | |
| CN109420433B (en) | Operation method of hollow fiber membrane module | |
| CN206359670U (en) | A kind of hollow fiber spinning machine | |
| KR101392755B1 (en) | Wastewater disposal plant using tubular membrane | |
| CN103086477B (en) | Beverage waste water membrane-method recycling method and device | |
| KR20160123864A (en) | Water treatment apparatus and operation control method of the same | |
| CN104841278A (en) | Detachable glass sand core dialysis device | |
| JP7213711B2 (en) | Water treatment device and water treatment method | |
| CN110234419A (en) | Hollow fiber film assembly |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |