FI20195123A1 - Feed spacer for cross-flow membrane element - Google Patents
Feed spacer for cross-flow membrane element Download PDFInfo
- Publication number
- FI20195123A1 FI20195123A1 FI20195123A FI20195123A FI20195123A1 FI 20195123 A1 FI20195123 A1 FI 20195123A1 FI 20195123 A FI20195123 A FI 20195123A FI 20195123 A FI20195123 A FI 20195123A FI 20195123 A1 FI20195123 A1 FI 20195123A1
- Authority
- FI
- Finland
- Prior art keywords
- feed
- flow
- feed spacer
- membrane
- channel
- Prior art date
Links
- 125000006850 spacer group Chemical group 0.000 title claims abstract description 66
- 239000012528 membrane Substances 0.000 title claims abstract description 63
- 229910052729 chemical element Inorganic materials 0.000 claims description 2
- 210000004379 membrane Anatomy 0.000 description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 30
- 239000012466 permeate Substances 0.000 description 20
- 239000000126 substance Substances 0.000 description 16
- 239000000243 solution Substances 0.000 description 13
- 238000011084 recovery Methods 0.000 description 12
- 238000001223 reverse osmosis Methods 0.000 description 12
- 239000012141 concentrate Substances 0.000 description 9
- 235000008504 concentrate Nutrition 0.000 description 9
- 238000001914 filtration Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 8
- 230000010287 polarization Effects 0.000 description 7
- 238000000746 purification Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005374 membrane filtration Methods 0.000 description 4
- 229910003460 diamond Inorganic materials 0.000 description 3
- 239000010432 diamond Substances 0.000 description 3
- 238000011070 membrane recovery Methods 0.000 description 3
- 239000008399 tap water Substances 0.000 description 3
- 235000020679 tap water Nutrition 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 235000020188 drinking water Nutrition 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000007493 shaping process Methods 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 231100000357 carcinogen Toxicity 0.000 description 1
- 239000003183 carcinogenic agent Substances 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000010411 cooking Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 230000035622 drinking Effects 0.000 description 1
- 235000021271 drinking Nutrition 0.000 description 1
- 239000003621 irrigation water Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- -1 microbes Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 230000000116 mitigating effect Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000003053 toxin Substances 0.000 description 1
- 231100000765 toxin Toxicity 0.000 description 1
- 108700012359 toxins Proteins 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- 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
- B01D63/10—Spiral-wound membrane modules
-
- 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
- B01D63/06—Tubular membrane modules
-
- 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
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
-
- 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
- B01D61/14—Ultrafiltration; Microfiltration
-
- 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
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- 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
- B01D69/04—Tubular membranes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/14—Specific spacers
- B01D2313/143—Specific spacers on the feed side
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/20—Prevention of biofouling
Abstract
This invention relates to a feed spacer, used in a cross-flow membrane element (1) comprising a feed spacer element (2) equipped with a feed channel input end and a feed channel output end, which feed spacer element (2) is arranged to keep the feed channel open for a feed flow (4). The feed spacer element (2) is formed in such a way that its fill ratio increases in the direction of the feed flow (4) from the feed channel input end to the feed channel output end.
Description
FEED SPACER FOR CROSS-FLOW MEMBRANE ELEMENT The object of the invention 1s a feed spacer according to claim 1 for a cross-flow membrane element.
Large areas in the world suffer from poor or non-usable drink- ing water. Also, in many areas of the world tap water is not suitable for drinking or cooking. The most problematic areas are densely populated areas, such as China, India, Indonesia, Africa but the problem is very common also in Southern Europe, America and in the rest of Asia.
Several techniques to solve the clean water problem has been introduced. One of the most promising water treatment tech- nigue is reverse osmosis (RO) system.
Reverse osmosis (RO) systems are effective for suspended and dissolved solids, microbes, toxins and carcinogens. However, low cost RO systems of prior art suffer from poor water econo- my. Typically, about 500 litres of water is needed to produce 100 litres of purified water. More effective RO systems need electric power and are more expensive. In spite of their dis- advantages, RO systems are the most common Point-0f-Use sys- tems, as they are most effective, removing practically all the contaminants from the water.
However, increasing volume of domestic POU systems using RO = methods according to the prior art solutions can be a future N threat to the whole mankind because the water consumption S 30 would tremendously grow. The recovery rate of prior art POU e systems is only 10-30%, which means that 70-90% of the used E tap water is wasted.
0) N The operation of a membrane filter, which can be also called a 3 35 membrane separator, can be described in a simplified manner as & follows: The permeable membrane to be used, which possesses certain properties, allows a substance to be purified, e.g.
water, to pass through it and retains other materials. In practice, the separation of membrane filters is not perfect, in which case the result of the separation is the permeate that has passed through the membrane and the concentrate, or corresponding, obtained from the material to be filtered.
A generally used membrane filtration method for liquids is so- called cross flow filtering. Cross flow filtering is in use in many different types of membrane filtering methods, e.g. in reverse osmosis filtration, nanofiltration, ultrafiltration and microfiltration. In cross flow filtering the material to be purified is brought to flow in the direction of the surface of the filtering membrane in which case, although some of the material filters through the membrane, the material to be pu- rified rinses the surface of the membrane and in this way keeps the membrane permeable while preventing clogging or a large local concentration on the surface of the membrane. The driving force in membrane filtration is a pressure difference across the membrane. Energy is also needed, apart from over- coming the resistance caused by the membrane, for moving and conducting the liquids in the different phases of the process as well as for raising the pressure of the liguid to the oper- ating pressure needed. Membrane filter devices and their components are generally available for various purposes. Membrane filter plants and devices are fabricated from commercially available components and are based on generally known technigues. For example, re- = verse osmosis filters are commercially available for various N applications and suitably also for the treatment of various S 30 solutions and for the separation of many types of substances, 2 and, inter alia, filters for salt removal can be optimized and E also the salt content ratio of the water to be treated can be a selected. 3 35 The Membrane filter device comprises typically an enclosure N with tap water inlet and outlets for a permeate and concen- trated water, a central tube for the permeate, a reverse osmo-
sis membrane and a feed spacer. The feed spacer serves as a passageway through which raw water is led. One important parameter in cross-flow filtering is the mem- brane recovery ratio = ratio between the part of the feed flow which permeates the membrane to the inputted feed flow. The higher the recovery ratio, the simpler the systems can be made, and in cases where it is not possible to increase recov- ery by the purifying system structure, the better is the water economy i.e. less water wasted as rejected concentrate. Maximum recommended recovery ratio of typical spiral wound membrane element is usually about 20%. Reason for this is con- centrate polarization and foulants collecting on membrane sur- face and/or feed spacer, blocking the feed water flow through the feed channel and blocking the membrane surface. To reduce the polarization and fouling the flow velocity in the feed channel needs to be high enough and preferably turbulent to flush away the foulants and to reduce the polarization layer.
Primary purpose of the feed spacer is to form a feed channel and keep the feed channel open. Other purposes of the feed spacer are to make the flow turbulent and have as small flow resistance as possible.
Typically, the feed spacer is a diamond shaped mesh. Usually the feed spacer is made of plastic, where the mesh nodes, = where the filaments cross, contact the membrane surfaces and N support the membranes, while in other parts of the mesh (where S 30 there is just a single filament in the channel, or the mesh 2 eye) water can flow. The "zig-zag” filaments cause turbulence E intensifying the flush. Typically, the mesh is positioned so N that the mesh filaments are at about 45 deg angle to the flow S direction.
N As feed water is entered in the feed channel from one end of the channel and part of the water permeates the membrane, the flow velocity in feed channel reduces in flow direction as the feed channel cross section is constant. Reduced flow velocity causes increasing fouling, concentrate polarization and clog- ging on the surface of the membrane and thus remarkable reduc- tion of the membrane element recovery rate.
In this regard, there is a need for an improved feed spacer capable of improving the membrane element recovery rate by maintain or even increasing the feed flow velocity and miti- gating concentration polarization.
The problem can be solved with different, more complicated membrane element structures, like Pentair GRO membranes, which are spiral would membranes, but with radial feed flow, or with making the element from a stack of round discs with radial feed flow. However, these are quite expensive structures, and the invention is also applicable in these structures to im- prove them further. One solution trying to solve the problem is a patent publication EP 3415224 Al, which however has no solution for decreasing feed flow velocity and improved mem- brane element recovery rate. The problem this invention solves is increasing the membrane element recovery ratio by making the feed spacer such that the cross section of the feed channel reduces in the flow direc- tion, thus keeping the feed flow relatively constant or even increasing towards the output end of the feed channel. By this means the amount of water permeating the membrane can be in- = creased without increasing fouling or concentrate polarization N and thus having a higher recovery rate. S 30 2 The aim of this invention is to achieve an effective, inexpen- E sive, reliable and well-functioning feed spacer for the cross- N flow membrane element. More particularly the invention aims N for reverse osmosis filtration solutions, nanofiltration solu- 3 35 tions, ultrafiltration solutions and microfiltration solutions N and especially the type of solutions that are suitable for use in the reverse osmosis enrichment or reverse osmosis purifica- tion of aqueous solutions. Further, one aim is to achieve a filtering solution in a membrane filtration by which water consumption can be reduced as close as possible to minimum.
The feed spacer for the cross-flow membrane element according 5 to the invention is characterized by what is presented in the characterization part of claim 1. Other embodiments of the invention are characterized by what is presented in the other claims.
An aspect of the invention is to provide a feed spacer for the cross-flow membrane element, which is comprising a feed spacer element equipped with a feed channel input end and a feed channel output end, which feed spacer element is arranged to keep the feed channel open for a feed flow. The feed spacer element is formed in such a way that its fill ratio increases in the direction of the feed flow from the feed channel input end to the feed channel output end.
The substance to be filtered, for example pressurized tab wa- ter is later called as input substance. The clean substance that has passed through the membrane filter is later called as permeated substance or permeate. The part of the input sub- stance, which is not passing through the membrane filter is later called as unpermeated substance or concentrate. The mem- brane filtration unit comprises an enclosure or pressure keep- ing structure, which is closed and sealed with a cap or by another way. The enclosure cap or the enclosure itself com- = prises one inlet for the input substance, one outlet for the N permeated substance and second outlet for the unpermeated sub- S 30 stance or concentrate that is led, for instance, to the drain. © E The basic idea of this invention is that the feed spacer is N made such that its fill ratio increases towards the output end = of the feed channel. The feed spacer fill ratio in this con- 3 35 text means the surface area of the filaments in the specific N area of the feed spacer element comparing the surface area of the mesh apertures in the same specific area of the feed spac- er element. Advantageously, the thickness of filament of the feed spacer element is equal throughout the width and length of the feed spacer element.
The fill ratio increase can be based on a gradual fill ratio increase, or the fill ratio can be formed by connecting to- gether a group of sections having different fill ratio.
The effect can be made in numerous ways, e.g. 1f the feed spacer is a diamond shaped mesh aperture by: - decreasing the mesh aperture size towards the output side of a feed channel, - increasing the filament width towards the output side, - shaping the filament to take more space towards the output side, or - a combination of above
Benefit is gained from the improved feed spacer at least in many ways: - the membrane recovery is improved, - the water economy is increased, - smaller flow losses, as feed spacer can be with smaller fill ratio at the input side of the channel, - low cost effects, and - fits in existing manufacturing process.
In addition, upgrading existing cross-flow membrane elements with improved feed spacer to existing water purification = units, is very simple and inexpensive.
With the invention, N both large and small plants can be upgraded energy-efficiently <Q without pressure exchangers or corresponding energy recovery - 30 devices being needed.
With the solution increased membrane E recovery ratio and better water economy can be achieved, which n is important e.g. in water purification, in which pretreatment = and/or the untreated water has a significant proportion in the 2 total costs.
N 35 The invention is particularly advantageous in water purifica- tion applications, e.g. in desalination, in making process water, boiler water or plant water, in preparing irrigation water or drinking water, and even for the purification of waste water. The invention is also suited to the enrichment of dissolved substances, e.g. in the food industry or in the min- ing industry. The primary conceived use of the invention is the application of it in reverse osmosis separation. Many effects or technical solutions are very similar in other membrane separation tech- niques. Within the scope of applicability, the inventive solu- tions can therefore be extended to be used in other membrane separation procedures also, although the description and ex- planations of the technical solutions are presented here in this context most often in a reverse osmosis device environ- ment. In the following the invention will be described in more de- tail by the aid of examples of its embodiments with reference to the attached simplified drawings, wherein Fig. 1 presents in an obligue top view an opened cross- flow membrane element and a feed flow applicable to the invention, Fig. 2 presents one embodiment of a feed spacer element of the invention, and = Fig. 3 presents another embodiment of the feed spacer N element of the invention. S 30
D E Fig. 1 presents in an cobligue top view and in a simplified n way an opened cross-flow membrane element 1 and a feed flow 4 = applicable to the invention and Fig. 2 presents one embodi- D 35 ment of a feed spacer element 2 of the invention. The feed N flow 4 is fed into cross-flow membrane element 1 from its first end, also called a feed channel input end.
The cross-flow membrane element 1 of a membrane filter device comprises at least a permeate channel 8, the feed spacer ele- ment 2 and a permeate pouch 3. The feed spacer element 2 and the permeate pouch 3 are rolled as a spiral around the perme- ate channel 8. The lower surface 3b and side surfaces of the permeate pouch 3 are impermeable, and the upper surface of the permeate pouch 3 is a membrane film 3a allowing a permeate 7 penetration 5 from the feed flow 4 to the hollow channel of the permeate pouch 3. The permeate 7 flows spirally inside the of the permeate pouch 3 towards the permeate channel 8. An unpermeated substance, a concentrate 6, of the feed flow 4 not penetrating to the permeate pouch 3 is flowing out from the second end of the cross-flow membrane element 1, also called a feed channel output end.
The feed spacer element 2 has a diamond shaped mesh, where mesh filaments are at about 45 degrees angle to the flow di- rection. The substance feed flow 4 is flowing in the feed spacer element 2 layer with a certain pressure from the feed channel input end of the cross-flow membrane element 1 to the feed channel output end of the cross-flow membrane element 1. A fill ratio of the feed spacer element 2 increases towards the output end of the feed channel. The feed spacer element 2 comprises three sections 2a, 2b and 2c each having different fill ratio. In the first section 2a, the filament width is low, which gives more space to the feed flow 4 substance and the feed spacer element 2 fill ratio is low. In the second = section 2b, the filament width is medium, which gives less N space to the feed flow 4 substance and the feed spacer element S 30 2 fill ratio is medium. In the third section 2c, the filament 2 width is high, which gives even less space to the feed flow 4 E substance and the feed spacer element 2 fill ratio is high. n The increased fill ratio of the feed spacer element 2 towards = the output end of the feed channel is made by increasing the D 35 filament width of the feed spacer element 2 from section 2a to i section 2b to section 2c.
Fig. 2 presents another embodiment of a feed spacer element 2 of the invention. The increased fill ratio of the feed spacer element 2 is made by increasing the number of mesh apertures 2e towards the output side of feed channel. Also, other meth- ods increasing fill ratio of the feed spacer element 2 can be done, for example by shaping the filament to take more area towards the output side of feed channel. Low feed spacer element 2 fill ratio in the first end of the membrane element 1 provides high permeating rate and smaller flow losses, since free membrane film 3a surface area is high. Increasing spacer element 2 fill ratio towards downstream maintains or even increases the feed flow 4 speed, improving the membrane recovery rate. The amount of the permeate 7 is increased without increasing a fouling or the concentrate 6 polarization and thus having a higher recovery rate and in- creasing the overall water economy. The cross-flow membrane element 1 with improved feed spacer element 2 according to this invention can be very simply and inexpensively upgraded to existing water purification units. It is obvious to the person skilled in the art that the in- vention is not limited to the examples described above, and it may be varied within the scope of the claims presented below as well as of the description and the drawing present- ed. For example, the shape or width of the feed spacer ele- = ment can be different that presented in above. Also, the feed N spacer element fill ratio can be increased gradually instead S 30 of sectorial. The most important technical effect of this 2 invention is, however, that the fill ratio of the feed spacer E element is increasing towards the downstream of the cross- N flow membrane element.
N 3 35 Also, the membrane element type can be different than the NN examples described above. For example, the membrane element may comprise more than one membrane pouches and feed spacer elements connected to the permeate channel.
Claims (5)
1. Feed spacer, used in a cross-flow membrane element (1) com- prising a feed spacer element (2) equipped with a feed channel input end and a feed channel output end, which feed spacer element (2) is arranged to keep the feed channel open for a feed flow (4), characterized in that the feed spacer element (2) is formed in such a way that its fill ratio increases in the direction of the feed flow (4) from the feed channel input end to the feed channel output end.
2. Feed spacer according to claim 1, characterized in that the filament width of the feed spacer element (2) is arranged to increase towards the output end of the feed channel.
3. Feed spacer according to claim 1 or 2, characterized in that the number of mesh apertures (2e) of the feed spacer ele- ment (2) increases towards the output end of the feed channel.
4. Feed spacer according to claim 1, 2 or 3, characterized in that the feed spacer element (2) comprises more than one sec- tions (2a, 2b, 2c) each having different fill ratio that is arranged to increase section by section towards the output end of the feed channel.
5. Feed spacer according to claim 1, 2 or 3, characterized in that the fill ratio of the feed spacer element (2) is arranged o 5 to increase gradually towards the output end of the feed chan-
N i nel.
N <Q 30 00
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O
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Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20195123A FI20195123A1 (en) | 2019-02-18 | 2019-02-18 | Feed spacer for cross-flow membrane element |
| PCT/FI2020/050097 WO2020169883A1 (en) | 2019-02-18 | 2020-02-17 | Feed spacer for cross-flow membrane element |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI20195123A FI20195123A1 (en) | 2019-02-18 | 2019-02-18 | Feed spacer for cross-flow membrane element |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| FI20195123A1 true FI20195123A1 (en) | 2020-08-19 |
Family
ID=72144806
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| FI20195123A FI20195123A1 (en) | 2019-02-18 | 2019-02-18 | Feed spacer for cross-flow membrane element |
Country Status (2)
| Country | Link |
|---|---|
| FI (1) | FI20195123A1 (en) |
| WO (1) | WO2020169883A1 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB202103267D0 (en) * | 2021-03-09 | 2021-04-21 | G20 Water Tech Limited | Component for a spiral wound membrane |
| CN114849482A (en) * | 2022-06-21 | 2022-08-05 | 杭州苏博瑞驰科技有限公司 | Flow stabilizing type flow channel membrane element and production process |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2004089763A (en) * | 2002-08-29 | 2004-03-25 | Japan Organo Co Ltd | Spiral membrane element, separation membrane module, separation membrane apparatus, and water treatment method using the same |
| CN1761515A (en) * | 2003-03-14 | 2006-04-19 | 齐侬环境有限公司 | Nanofiltration system for water softening with internally staged spiral wound modules |
| WO2015153116A1 (en) * | 2014-03-31 | 2015-10-08 | Dow Global Technologies Llc | Spiral wound membrane module with defined flow resistance sections within feed spacer |
| WO2019117479A1 (en) * | 2017-12-12 | 2019-06-20 | 주식회사 엘지화학 | Feed spacer and reverse osmosis filter module including same |
| JP7133357B2 (en) * | 2018-05-18 | 2022-09-08 | 日東電工株式会社 | Channel spacer and spiral membrane element |
-
2019
- 2019-02-18 FI FI20195123A patent/FI20195123A1/en not_active Application Discontinuation
-
2020
- 2020-02-17 WO PCT/FI2020/050097 patent/WO2020169883A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| WO2020169883A1 (en) | 2020-08-27 |
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| Date | Code | Title | Description |
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| FD | Application lapsed |