CN109499374A - Suitable for hollow fiber pervaporation membrane interval restoration methods - Google Patents
Suitable for hollow fiber pervaporation membrane interval restoration methods Download PDFInfo
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- CN109499374A CN109499374A CN201811473281.7A CN201811473281A CN109499374A CN 109499374 A CN109499374 A CN 109499374A CN 201811473281 A CN201811473281 A CN 201811473281A CN 109499374 A CN109499374 A CN 109499374A
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- Prior art keywords
- hollow fiber
- pervaporation membrane
- fiber pervaporation
- restoration methods
- interval
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
-
- 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
- B01D63/02—Hollow fibre modules
Abstract
The present invention discloses one and is suitable for hollow fiber pervaporation membrane in the restoration methods of interval; the restoration methods of restoring are suitable for restoring and protecting the hollow fiber pervaporation membrane in interval; to protect the microcellular structure of vaporization film; the restoration methods keep vaporization film to be in drying regime always by way of vacuumizing and/or gas is swept; the vaporization film being saved can obtain the recovery close to 100%; it prevents film wire from swelling and structure change occurs, and effectively extends the service life of film wire.
Description
Technical field
The present invention relates to infiltrating and vaporizing membrane field, in particular to a kind of hollow fiber pervaporation membrane that is suitable for is between operation
Every restoration methods.
Background technique
It is that driving force realizes mass transfer that infiltration evaporation PV, which is using feed liquid film upstream and downstream component chemical potential difference, utilizes film pair
The difference of different component compatibility and resistance to mass tranfer realizes selectivity in feed liquid, and it is difficult to deal with to can be used for traditional separation means
Separation, the removing of minor amount of water and the removal of underwater micro- organic matter of azeotrope, nearly boiling object system, with energy-efficient, technique
Simple advantage, to be widely used.
Among these, film is the core in infiltration evaporation separation process, and the performance of film directly determines entire infiltration evaporation
The separative efficiency of process.Since infiltration evaporation isolation technics has very harsh requirement to membrane material, cause real on the market at present
The applicable membrane material product in border is very single, the cross-linking polyvinyl alcohol mainly only produced using German Sulzer as representative
(crosslinked PVA) polymeric membrane and with Mitsui (Mitsui) be representative NaA zeolite inoranic membrane.However both
Infiltrating and vaporizing membrane also exposes respective defect in practical applications: such as cross-linking polyvinyl alcohol film there are production technology complexity,
The defects such as unit area membrane flux is small, and processing capacity is low, that there are material costs is excessively high for zeolite molecular sieve inoranic membrane for another example, production
The defects of technique is extremely complex, high production cost.
Still need a kind of novel permeation vaporization that can effectively overcome two kinds of infiltrating and vaporizing membrane defects thereon on the market at present
Film, to meet the needs of practical infiltration evaporation.Moreover, the protection of novel permeation vaporization film in the actual application process
It is particularly significant.Specifically, due to feed liquid supply discontinuity, a variety of causes such as system maintenance and the system failure, in dehydrating operation
The shutdown of not timing is recurrent in the process, and in stopping process, novel permeation vaporization film is at interval
State, the at this time recovery to novel permeation vaporization film and protection are also that novel permeation vaporization film has to the big problem solved.
Summary of the invention
The purpose of the present invention is to provide one be suitable for hollow fiber pervaporation membrane running clearance restoration methods,
Described in restoration methods hollow fiber pervaporation membrane is saved by way of vacuumizing, remain at hollow infiltrating and vaporizing membrane
In drying regime, microcellular structure of the effective protection in it may make film properties to obtain the recovery close to 100%, prevent film wire from sending out
Raw swelling and structure change, and effectively extend the service life of film wire.
The purpose of the present invention is to provide one be suitable for hollow fiber pervaporation membrane interval restoration methods,
Described in restoration methods be equipped with while vacuumizing dry inert gas protection hollow fiber pervaporation membrane, guarantee hollow fibre
Structural stability of infiltrating and vaporizing membrane during preservation is tieed up, and dramatically improves the efficiency of preservation, avoids occurring
The bad phenomenons such as swelling and microstructure collapsing.
The purpose of the present invention is to provide it is a kind of suitable for hollow fiber pervaporation membrane interval restoration methods,
The infiltrating and vaporizing membrane being saved can be applied again after directly shelving processing, without influencing its permeability and separation performance, simplify and protect
The quality saved is improved while depositing program.
The purpose of the present invention is to provide it is a kind of suitable for hollow fiber pervaporation membrane interval restoration methods,
It does not need that equipment is extraly arranged during preservation, directly can carry out vacuum pumping using the vacuum pump in dehydration equipment,
To the simplicity operational sequence saved.
The purpose of the present invention is to provide it is a kind of suitable for hollow fiber pervaporation membrane interval restoration methods,
Wherein the restoration methods are easy to operate, and processing step is easy to accomplish, and preservation is at low cost, and effect is good.
The purpose of the present invention is to provide it is a kind of suitable for hollow fiber pervaporation membrane interval restoration methods,
Wherein the restoration methods are especially suitable for saving hollow fiber pervaporation membrane, wherein the hollow fiber pervaporation membrane has
There is the microcellular structure of special ultra-thin selection layer and supporting layer.
In order to realize that any of the above goal of the invention, the present invention provide one and be suitable for hollow fiber pervaporation membrane between operation
Every restoration methods, be applied to be preserved and recovered in interval hollow fiber pervaporation membrane, comprising the following steps: step
1: the liquid of emptying hollow fiber pervaporation membrane local environment；And step 2: in the true of the hollow fiber pervaporation membrane
Empty side vacuumizes, wherein the condition control vacuumized exists: vacuum degree 0.1-500mbar, duration are 1-500 minutes.
In some embodiments, gas is further included steps of in step S2 sweep the hollow fiber film assembly
1, wherein gas is dry inert gas, and the speed that control gas is swept is 0.1-5000m/min, and the duration is 1-120 minutes.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the osmotic, evaporating and dewatering equipment of an embodiment according to the present invention.
Fig. 2 is the structural schematic diagram of the hollow fiber film assembly of an embodiment according to the present invention.
Fig. 3 is the structural schematic diagram of the hollow fiber pervaporation membrane of an embodiment according to the present invention.
Fig. 4 is the schematic cross-section of the hollow fiber pervaporation membrane of an embodiment according to the present invention.
Fig. 5 is the preservation process schematic of the hollow fiber pervaporation membrane of an embodiment according to the present invention.
Fig. 6 is the preservation process schematic of hollow fiber pervaporation membrane according to another embodiment of the present invention.
Fig. 7 is the schematic diagram of the hollow fiber pervaporation membrane preservation effect of an embodiment according to the present invention.
In figure: 1- hollow fiber film assembly, 2- material liquid tank, 3- heating device, 4- feed liquid transmission pump, 5- bypass control valve,
6- flow control valve, 7- flowmeter, 8- condenser, 9- permeate flow container, 10- vacuum pump, 101- vacuum meter, 20- gas source, in 11-
Hollow fiber infiltrating and vaporizing membrane, 111- outer protective layer, 112- selective separation layer, 113- internal layer supporting layer, 121- liquor inlet,
The outlet of 122- penetrating fluid, 123- products export.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art's every other embodiment obtained belong to what the present invention protected
Range.
It will be understood by those skilled in the art that in exposure of the invention, term " longitudinal direction ", " transverse direction ", "upper",
The orientation of the instructions such as "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom" "inner", "outside" or position are closed
System is to be based on the orientation or positional relationship shown in the drawings, and is merely for convenience of description of the present invention and simplification of the description, without referring to
Show or imply that signified device or element must have a particular orientation, be constructed and operated in a specific orientation, therefore above-mentioned art
Language is not considered as limiting the invention.
It is understood that term " one " is interpreted as " at least one " or " one or more ", i.e., in one embodiment,
The quantity of one element can be one, and in a further embodiment, the quantity of the element can be it is multiple, term " one " is no
It can be interpreted as the limitation to quantity.
The present invention provides one and is suitable for hollow fiber pervaporation membrane in the restoration methods of interval, is applied to save
With recovery in interval hollow fiber pervaporation membrane, certainly, this method also has universality to other infiltrating and vaporizing membranes, herein
The hollow fiber pervaporation membrane referred to is by the present inventor by adjusting the formula of internal layer casting solution and outer layer casting solution, and is led to
Cross the unique infiltrating and vaporizing membrane that a step bilayer extrusion process obtains.
The structure for the hollow fiber pervaporation membrane that the present inventor is prepared is as shown in Figures 3 and 4, and the doughnut seeps
Film is vaporized thoroughly by sequentially forming internal layer supporting layer 113, selection separating layer 112 and outer protective layer 111 outside to film in film, wherein
The selection separating layer 112 is placed between the internal layer supporting layer 113 and the outer protective layer 111, the outer protective layer
111 have hydrophily, and the film outer diameter of the hollow fiber pervaporation membrane be 0.8-1.5mm, internal diameter 0.5-1.2mm,
Wall thickness is 0.1-0.2mm, the difference is that, the selection separating layer 112 is placed in two layers with the infiltrating and vaporizing membrane of the prior art
Among membrane structure, the separative efficiency and stability of the hollow fiber pervaporation membrane are improved, and infiltration vapour can be applied to
In change.
The hollow fiber pervaporation membrane is prepared by mode below:
Step 1: preparing internal layer casting solution, outer layer casting solution and core liquid, the internal layer casting solution, the outer layer casting solution
Hollow tubular liquid film is formed by spinning nozzle with the core liquid；
Step 2: the hollow tubular liquid film enters coagulating bath pond behind the air gap and is solidified by phase transformation, obtains hollow fibre
Tie up film wire；And
Step 3: handling the hollow fiber film thread, obtain hollow fiber pervaporation membrane；
Wherein the outer layer casting solution includes hydrophilic macromolecule and solvent, wherein the hydrophilic macromolecule includes but not
It is limited to sulfonated polysulfone, sulfonated polyphenyl sulfone, sulfonated polyether sulfone, sulfonated polyamide and sulfonated polyimide, polyvinyl alcohol, polyoxy second
Alkene, cellulose, cellulose ethanoate, hydrolyzed polyacrylonitrile, polyvinylpyrrolidone, chitosan, polyetheramine and polyethyleneimine
Amine；The solvent includes but is not limited to n- N-methyl-2-2-pyrrolidone N, n,N-dimethylacetamide, dimethylformamide, dimethyl
Sulfoxide, tetrahydrofuran, methylene chloride, chloroform；In an embodiment of the present invention, outer layer formula of casting is selected are as follows: sulfonation
The mixed liquor of polyphenylsulfone and n- N-methyl-2-2-pyrrolidone N, wherein the mass ratio of the sulfonated polyphenyl sulfone is between 10-35%, institute
The mass ratio of n- N-methyl-2-2-pyrrolidone N is stated in 65-90%, wherein ratio is 100% to the two formula altogether；Alternatively, selection
The mixed liquor of cellulose ethanoate and n- N-methyl-2-2-pyrrolidone N, wherein the mass ratio of the cellulose ethanoate is in 1-15%
Between, the mass ratio of the n- N-methyl-2-2-pyrrolidone N is in 85-99%, wherein ratio is 100% to the two formula altogether.
Wherein the internal layer casting solution includes polymeric, solvent and auxiliary agent, wherein the polymeric packet
Include but be not limited to polysulfones, polyether sulfone, polyphenylsulfone, polyamide, polyimides, polyamide-imides, polyvinylidene fluoride, poly- four
Vinyl fluoride, polypropylene is fine, polypropylene, polycarbonate, polybenzimidazoles, polyurethane；The solvent includes but is not limited to n- methyl-
2-Pyrrolidone, n,N-dimethylacetamide, dimethylformamide, dimethyl sulfoxide, tetrahydrofuran, methylene chloride, three chloromethanes
Alkane and the auxiliary agent include but is not limited to polyethylene glycol, ethylene glycol, glycerine, polyvinylpyrrolidone, water, ethyl alcohol, and third
Ketone, lithium chloride, lithium bromide, calcium chloride；In an embodiment of the present invention, select internal layer formula of casting: polyphenylsulfone, ethylene glycol and
The mixed liquor of n- N-methyl-2-2-pyrrolidone N, wherein the mass ratio of the polyphenylsulfone is in 10-30%, the mass ratio of the ethylene glycol
Between 2-20%, the mass ratio of the n- N-methyl-2-2-pyrrolidone N is in 50-88%, and wherein ratio is three's formula altogether
100%；Alternatively, the internal layer casting solution: the mixed liquor of polyetherimide, polyethylene glycol and n- N-methyl-2-2-pyrrolidone N is selected,
Wherein the mass ratio of the polyphenylsulfone is in 10-30%, and the mass ratio of the polyethylene glycol is between 1-10%, the n- methyl-
The mass ratio of 2-Pyrrolidone is in 60-89%, and wherein ratio is 100% to three's formula altogether.
Wherein the core liquid includes solvent, non-solvent and auxiliary agent, wherein the auxiliary agent includes but is not limited to polyethylene glycol, second
Glycol, glycerine, polyvinylpyrrolidone, water, ethyl alcohol, acetone, n-butanol.
When the mixed system that the hollow infiltrating and vaporizing membrane is applied to separation and purifies azeotropic or closely boils, the infiltration
Vaporization film composition infiltration vaporization membrane module, which is placed in an osmotic, evaporating and dewatering equipment, to be used, wherein the osmotic, evaporating and dewatering is set
As indicated with 1, the structural schematic diagram of the infiltration vaporization membrane module is as shown in Figure 2 for standby structural schematic diagram.
As illustrated in fig. 1 and 2, osmotic, evaporating and dewatering equipment includes hollow fiber film assembly 1, material liquid tank 2, heating device 3, material
Liquid transmission pump 4, bypass control valve 5, flow control valve 6, flowmeter 7, condenser 8, infiltration flow container 9 and vacuum pump 10, wherein
An at least hollow fiber pervaporation membrane 11 is set in the hollow fiber film assembly 1, wherein the doughnut infiltration evaporation
Film 11 is prepared by the method mentioned thereon, and liquor inlet 121, penetrating fluid outlet are formed on the hollow fiber film assembly 1
122 and products export 123, wherein the 122 connection condensers 8 of penetrating fluid outlet, the condenser 8 connect the infiltration
Transparent liquid tank 9 and the vacuum pump 10, the vacuum pump 10 is taken out the hollow fiber film assembly 1 and is pressed, by hollow fiber film assembly 1
Penetrating fluid after infiltration evaporation falls into the infiltration flow container 9 after being condensed by the condenser 8；The wherein liquor inlet
121 are sequentially connected the flowmeter 7 and the flow control valve 6, enter in the hollow fiber film assembly 1 for controlling
The flow of feed liquid, in addition, the material liquid outlet 123 is connected with material liquid tank 2, the side of the material liquid tank 2 is provided with heating device
3, the other end connects feed liquid transmission pump 4, and the feed liquid transmission pump 4 and the flow control valve 5 are commonly connected to bypass control valve 5
On.
The process being dehydrated about infiltration vaporization membrane module is the prior art, and this will not be repeated here, and emphasis of the present invention refers to
How infiltrating and vaporizing membrane is preserved and recovered when the osmotic, evaporating and dewatering equipment is out of service.
It is noted that the hollow fiber film assembly 1 for being provided with hollow fiber pervaporation membrane 11 was run in vacuum
Drying regime is remained in journey.That is, the inside of the hollow fiber pervaporation membrane 11 is inlet side, outside is feed liquid side,
Difference in chemical potential is formed between the inlet side and the feed liquid side, the Preferential adsorption component (infiltration from the feed liquid that feed liquid side enters
Liquid) enter in hollow fiber pervaporation membrane 11, and the vacuum of diffusion to film is surveyed in the form of a vapor in film, it is remaining
Product is flowed out from products export 123.In this process, the hollow fiber pervaporation membrane 11 is always in dry shape
State, i.e. penetrating fluid are spread in film in a gaseous form after film surface absorption.If feed liquid component is present in liquid form
In film, membrane material will be enabled to be swollen, so as to cause membrane separating property decline, in addition, in the case where this swelling, by film
Non-treated to dry, the microstructure of the infiltrating and vaporizing membrane can collapse, so that its performance can decline very much.So to protect
It holds hollow fiber pervaporation membrane 11 and is also at dry state when stored, keep the microcellular structure in film by this method.
Specifically, the present invention, which provides one, is suitable for hollow fiber pervaporation membrane in the restoration methods of interval, side
Case one, comprising the following steps:
Step 1: the liquid in emptying hollow fiber film assembly；And
Step 2: being vacuumized in the inlet side of the doughnut membrane module, wherein the condition control vacuumized exists: vacuum
Degree is 0.1-500mbar, and the duration is 1-500 minutes.
In the step 2, the vacuum degree control that preferably vacuumizes are as follows: 1-100mar, certainly, the vacuum degree can be with
Arbitrary value in 0.1-500mbar, including but not limited to 1,2,3,10,20,50,60,70,75,90,120,200,300,
450 is equivalent.
Preferably lasting for the time is 30-100 minutes, and certainly, the duration can wrap selected from the arbitrary value in 30-100 minutes
It includes but is not limited to 31,35,40,42,50,60,65,70,85 equivalences.
And it is noted that as shown in fig. 6, in the process of preservation, it is only necessary to close the bypass control valve 5
And the flow control valve 6, the vacuum pump 10 directly takes out true pressure to the hollow fiber film assembly 1, thus easy
The process saved shows vacuum degree furthermore it is possible to which vacuum meter 101 is arranged on vacuum pump 10.
In addition, additionally include the steps that gas sweeps hollow fiber film assembly 1 in the step 2 in scheme two,
That is, the step 2 further comprises step: gas sweeps the hollow fiber film assembly 1, and wherein gas is dry inert gas, control
The speed that gas processed is swept is 0.1-5000m/min, and the duration is 1-120 minutes.
Certainly, the dry inert gas can be selected from as nitrogen, helium, argon gas etc..
It is preferred that air velocity controls are as follows: 1-2000m/min, certainly, the vacuum degree can be in 0.1-5000m/min
Arbitrary value, including but not limited to 1,2,3,10,20,50,60,70,75,90 is equivalent.
It is preferred that the control duration is 5-30 minutes, certainly, the duration can be selected from 1-120 minutes arbitrary values, packet
It includes but is not limited to 5,17,20,32,45,57,63,77,88,91,95 equivalences.
As shown in figure 5, connecting flowmeter 7, the other end of the flowmeter 7 in the position of the liquor inlet 121 at this time
Side connects gas source 20, wherein the gas source 20 is built-in with dry inert gas, it is worth mentioning at this point that, it can be by dismantling the flow
Control valve 6 and the mode for being directly connected to the gas source 20, to simplify the preservation process for stating hollow membrane module 1.
Above-mentioned scheme one and scheme two can keep hollow fiber pervaporation membrane to be in drying regime always, in turn
The microcellular structure in film is kept not to be destroyed.
Both the above is saved scheme and is applied to practice in practice by the present inventor, obtains good experimental data, such as
Under:
Case 1: shutting down after ethanol dehydration experiment, and with the processing hollow fiber film assembly of scheme two, the processing time is
It 20 minutes, is shelved after processing 24 hours, then repeatedly ethanol dehydration is tested, and treated as the result is shown, and membrane flux is before handling
99% or more of membrane flux, separative efficiency that treated are 110% before processing.
Case 2: ethanol dehydration is shut down after testing, and handles hollow fiber film assembly with scheme two, the processing time is 10
Minute, it is shelved after processing 24 hours, then repeatedly ethanol dehydration is tested, and the membrane flux after result treatment is membrane flux before handling
99% or more, separative efficiency that treated is 100% before processing.
Case 3: ethanol dehydration is shut down after testing, and handles hollow fiber film assembly with scheme two, the processing time is 5 points
Clock is shelved 24 hours after processing, and then repeatedly ethanol dehydration is tested, and treated, and membrane flux is 93% of membrane flux before handling,
Separative efficiency that treated is 98% before processing.
Case 1 is compared to case 3 it is found that within certain processing time range, the processing time is longer, and treated film
Flux and separative efficiency are better, it might even be possible to more preferable than the film properties before processing.
Case 4: ethanol dehydration is shut down after testing, and handles hollow fiber film assembly with scheme one, the processing time is 30
Minute, it is shelved after processing 24 hours, then repeatedly ethanol dehydration is tested, and as a result treated as follows, and membrane flux is that processing cephacoria is logical
The 95% of amount, separative efficiency that treated are 60% before processing.
Case 5: ethanol dehydration is shut down after testing, and hollow fiber film assembly is handled in a manner of liquid filling, handles the time 24
Hour, then repeatedly ethanol dehydration is tested, and as a result as follows, treated, and membrane flux is 130% or more of membrane flux before handling, place
Separative efficiency after reason is 16% before processing.
Wherein liquid filling mode are as follows: liquid in emptying component, and liquid is poured into, it seals.Liquid can be water, alcohols such as first and second
Alcohol isopropanol, ketone such as acetone, alkanes such as n-hexane etc..
Case 6: ethanol dehydration is shut down after testing, space management hollow fiber film assembly, and the processing time is 24 hours,
Then ethanol dehydration experiment is repeated, treated, and membrane flux is 100% or more of membrane flux before handling, separative efficiency that treated
It is 57% before processing.
It can be seen that the restoration methods of two kinds of doughnut permeable membranes provided by the invention are to doughnut permeable membrane by good
Good preservation effect.
The present invention is not limited to above-mentioned preferred forms, anyone can show that other are various under the inspiration of the present invention
The product of form, however, make any variation in its shape or structure, it is all that there is skill identical or similar to the present application
Art scheme, is within the scope of the present invention.
Claims (10)
1. being suitable for hollow fiber pervaporation membrane in the restoration methods of interval, it is applied to be preserved and recovered between operation
Every hollow fiber pervaporation membrane, which comprises the following steps:
Step 1: the liquid of emptying hollow fiber pervaporation membrane local environment；And
Step 2: being vacuumized in the inlet side of the hollow fiber pervaporation membrane, wherein the condition control vacuumized exists: vacuum
Degree is 0.1-500mbar, and the duration is 1-500 minutes.
2. according to claim 1 be suitable for restoration methods of the hollow fiber pervaporation membrane in interval, feature
It is, gas is further included steps of in step S2 and sweeps the hollow fiber film assembly, wherein gas is dry inertia
Gas, the speed that control gas is swept are 0.1-5000m/min, and the duration is 1-120 minutes.
3. according to claim 1 or 2 any described hollow fiber pervaporation membranes that are suitable for are in the restoration methods of interval,
It is characterized in that, the speed that control gas is swept is 1-5000m/min, the duration is 5-30 minutes.
4. according to claim 1 or 2 any described hollow fiber pervaporation membranes that are suitable for are in the restoration methods of interval,
It is characterized in that, the vacuum degree is 1-100mar.
5. according to claim 3 be suitable for restoration methods of the hollow fiber pervaporation membrane in interval, feature
It is, the vacuum degree is 1-100mar.
6. according to claim 1 or 2 any described hollow fiber pervaporation membranes that are suitable for are in the restoration methods of interval,
It is characterized in that, the hollow fiber pervaporation membrane by, to internal layer supporting layer is sequentially formed outside film, selected in film separating layer with
And outer protective layer, wherein selection separation is placed between the internal layer supporting layer and the outer protective layer, it is described outer
Layer protective layer has hydrophily.
7. according to claim 6 be suitable for restoration methods of the hollow fiber pervaporation membrane in interval, feature
It is, the film outer diameter of the hollow fiber pervaporation membrane is 0.8-1.5mm, internal diameter 0.5-1.2mm, wall thickness 0.1-
0.2mm。
8. according to claim 5 be suitable for restoration methods of the hollow fiber pervaporation membrane in interval, feature
It is, the hollow fiber pervaporation membrane selects separating layer and outer layer by sequentially forming internal layer supporting layer outside to film in film
Protective layer, wherein selection separation is placed between the internal layer supporting layer and the outer protective layer, the outer layer protection
Layer has hydrophily, wherein the film outer diameter of the hollow fiber pervaporation membrane is 0.8-1.5mm, internal diameter 0.5-1.2mm, wall
Thickness is 0.1-0.2mm.
9. according to claim 8 be suitable for restoration methods of the hollow fiber pervaporation membrane in interval, feature
It is, the hollow fiber pervaporation membrane is in drying regime during infiltration evaporation.
10. according to claim 1 or 2 any described are suitable for hollow fiber pervaporation membrane in the recovery side of interval
Method, wherein the dry inert gas includes but is not limited to argon gas, nitrogen, helium.
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| CN201811473281.7A CN109499374B (en) | 2018-12-04 | 2018-12-04 | Recovery method suitable for operation interval of hollow fiber pervaporation membrane |
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| CN201811473281.7A CN109499374B (en) | 2018-12-04 | 2018-12-04 | Recovery method suitable for operation interval of hollow fiber pervaporation membrane |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04243527A (en) * | 1991-01-24 | 1992-08-31 | Nitto Denko Corp | Operation of pervaporation membrane apparatus |
| WO1999007459A1 (en) * | 1997-08-12 | 1999-02-18 | Unilever N.V. | Cleaning method for membranes |
| JPH1157415A (en) * | 1997-08-28 | 1999-03-02 | Kurita Water Ind Ltd | Operating method of membrane deaerator and apparatus for the same |
| CN100482602C (en) * | 2002-09-12 | 2009-04-29 | 化学处理私人有限公司 | Method of removing organic impurities from water |
| CN103877860A (en) * | 2012-12-21 | 2014-06-25 | 中国科学院大连化学物理研究所 | Regeneration method of hollow fiber film contactor |
-
2018
- 2018-12-04 CN CN201811473281.7A patent/CN109499374B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04243527A (en) * | 1991-01-24 | 1992-08-31 | Nitto Denko Corp | Operation of pervaporation membrane apparatus |
| WO1999007459A1 (en) * | 1997-08-12 | 1999-02-18 | Unilever N.V. | Cleaning method for membranes |
| JPH1157415A (en) * | 1997-08-28 | 1999-03-02 | Kurita Water Ind Ltd | Operating method of membrane deaerator and apparatus for the same |
| CN100482602C (en) * | 2002-09-12 | 2009-04-29 | 化学处理私人有限公司 | Method of removing organic impurities from water |
| CN103877860A (en) * | 2012-12-21 | 2014-06-25 | 中国科学院大连化学物理研究所 | Regeneration method of hollow fiber film contactor |
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|---|---|
| CN109499374B (en) | 2021-11-02 |
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