[go: up one dir, main page]

WO2002032533A2 - Module membranaire enroule en spirale a canal ouvert et concentration en saumure - Google Patents

Module membranaire enroule en spirale a canal ouvert et concentration en saumure Download PDF

Info

Publication number
WO2002032533A2
WO2002032533A2 PCT/US2001/031971 US0131971W WO0232533A2 WO 2002032533 A2 WO2002032533 A2 WO 2002032533A2 US 0131971 W US0131971 W US 0131971W WO 0232533 A2 WO0232533 A2 WO 0232533A2
Authority
WO
WIPO (PCT)
Prior art keywords
membrane
membrane module
spiral wound
feed
module
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.)
Ceased
Application number
PCT/US2001/031971
Other languages
English (en)
Other versions
WO2002032533A3 (fr
Inventor
Jack Herron
Robert Salter
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Osmotek Inc
Original Assignee
Osmotek Inc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from US09/688,611 external-priority patent/US6656361B1/en
Priority claimed from US09/688,612 external-priority patent/US6673242B1/en
Application filed by Osmotek Inc filed Critical Osmotek Inc
Priority to AU2002211694A priority Critical patent/AU2002211694A1/en
Publication of WO2002032533A2 publication Critical patent/WO2002032533A2/fr
Publication of WO2002032533A3 publication Critical patent/WO2002032533A3/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

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
    • B01D63/101—Spiral winding

Definitions

  • the present in ⁇ ention pro ⁇ ides a spiral-wound membrane module design for various membrane filtration techniques having significantly reduced fluid flow resistance in the feed stream path.
  • the inventive spiral-wound membrane module is designed having a corrugated entrance and exit spacers together over less than 10% of the length of the spiral wound module and a stiffener sheet wound to provide for uniform feed channel gap width.
  • the present invention further provides a membrane-assisted evaporation process for removing water added to brine. Specificalh", this process comprises using low-grade waste heat and air to evaporate water from diluted salt brine when water moves across a membrane in a liquid state. Background of the Invention In the field of pressure-driven membrane separations (e.g...
  • Feed fluid is forced to flow longitudinally through the module through the feed spacer, and fluid passing through the membranes flows inward in a spiral through the permeate spacer to the center tube.
  • the two membranes are glued to each other along their edges with the permeate spacer captured between them.
  • the feed spacer remains unglued.
  • a diagram of a cross-section of three wraps of a standard module is shown in Figure 1. Module assemblies are wound up to a desired diameter and the outsides are sealed. In operation, multiple modules are placed in a tubular housing and fluid is pumped through them in series. The center tubes are plumbed together lo allow removal of generated permeate.
  • Spiral wound membrane designs have been used successfully but can also foul ith higher fouling feed streams.
  • the fouling problem in standard spiral wound membranes is often due to the nature of the feed spacer that is required to be located through each of the feed channels.
  • the presence of the feed spacer creates significant resistance to fluid flow.
  • a typical feed spacer is a polymeric porous net-like material that the feed must be forced through in the longitudinal direction (I.e.. the length) of the spiral wound membrane. Therefore, spiral wound membrane designs can also have fouling problems in the feed spacer and membrane and incur significant fluid dynamic problems due to resistance of the feed spacer.
  • spiral wound designs are less expensive than alternatives for only less- fouling feed streams.
  • a tubular design membrane module For the most fouling feed streams (for examples, solutions containing high levels of suspended solids or tend to form gels upon concentration) a tubular design membrane module has been designed.
  • a tubular design provides the least amount of membrane surface area per module length, and is most expensive to manufacture due to labor-intensive procedures for "potting " the tubular membranes within a module. Moreo ⁇ er. the inlet and outlet chambers associated with tubular designs are also most expensive. Therefore, there is a need in the art to replace the tubular design with a less expensive design and still be able to process highly fouling feed streams.
  • the present invention was made to replace the tubular design with a spiral wound design for those feed streams that could not otherwise be processed (economically) in standard membrane modules having feed spacer designs.
  • Salt ca ⁇ erns have been used for storage of oil. particularly crude oil.
  • a brine solution is pumped in to replace the oil.
  • the brine concentrations are preferably within a range of 14-22.5% (by weight) of salt (mostly NaCl).
  • this brine solution is generally stored in ponds and the ponds generally can take in rainwater that results are a net dilution of the brine with pure water.
  • the effect of the diluted brine is a slow destruction of the salt cavern through removal of salt from the walls and eventual collapse of the cavern. Therefore, there is a need in the art to remove water from brine holding ponds and concentrate the brine to near saturation.
  • Salt caverns in Ontario. Canada and in Texas have ponds that take in an about 150.000 barrels (38 gallons to the barrel or about 140 liters to the barrel) or rainwater per year on average.
  • the refinery is forced to either develop a process to remo ⁇ e w ; ater from brine ponds or build indoor tanks to hold brine. Similar brine concentration issues are present in the chloralkali industry for treating cooling tower blowdown astewater.
  • the present invention provides a spiral wound membrane module having a length and a radius and a circular cross section, having reduced fluid flow resistance, comprising;
  • the stiffener means is composed of a hard shell sheet or an extruded or calendered rib. Most preferably, a rib stiffener means run in the same direction as permeate flow and provide permeate channels.
  • the structural assembly extends no more than 1 % of the length of the membrane module.
  • the structural assembly is located at both ends of the membrane module.
  • the membrane module further comprises a perforated or porous tube extended throughout the length of the membrane module and located axially around a cylinder axis of the membrane module, Most preferablv, the perforated or porous tube is used to collect permeate.
  • the stiffener in the form of a sheet is made from a rigid sheet having a thickness of from about 0. 1 mm to about 3 mm. most preferably from about 0.5 mm to about 1 mm.
  • the stiffener in the form of a sheet is made from a rigid material selected from the group consisting of PVC (polyvinyl chloride).
  • the stiffener sheet is polyethylene for food uses or PVC for non-food uses, or C- PVC for high temperature uses.
  • the structural assembly is a corrugated pattern ribbon.
  • the structural assembly is a rigid material, wherein the rigid material is selected from the group consisting of polyethylene, stainless steel, aluminum, acrylic, and polycarbonate.
  • the present invention further provides a process for making a spiral wound membrane module having a length and a radius and a circular cross section, having reduced fluid flow resistance, comprising (a) assembling an envelope sandwich having a width equal to the length of the membrane module and comprising a layer of membrane next to a layer of permeate spacer material next to a layer of stiffener means next to a layer of permeate spacer material next to a layer of membrane, and wherein the envelope sandwich is wrapped increasing the radius of the membrane module:
  • the stiffener means is composed of a hard shell sheet or an extruded or calendered rib. Most preferably, a rib stiffener means run in the same direction as permeate flow and provide permeate channels.
  • the process further comprises before step (c) adding glue to either end of the envelope sandwich.
  • the structural assembly extends no more than 10% of the length of the membrane module.
  • the membrane module further comprises a perforated or porous tube extending throughout the length of the membrane module and located axially around a cylinder axis of the membrane module and upon which the sandwich assembly is wrapped.
  • the stiffener in the form of a sheet is made from a rigid sheet having a thickness of from about 0.1 mm to about 3 mm. most preferably from about 0.5 mm to about 1 mm.
  • the stiffener in the form of a sheet is made from a rigid material selected from the group consisting of PVC (polyvinyl chloride). C-PVC (chlorinated polyvinyl chloride) polypropylene, polyethylene, acrylic, stainless steel, copper, tin, and aluminum.
  • the stiffener sheet is polyethylene for food uses or PVC for non-food uses, or C- PVC for high temperature uses.
  • the structural assembly is a corrugated pattern ribbon.
  • the structural assembly is a rigid material, wherein the rigid material is selected from the group consisting of polyethylene, stainless steel, aluminum, acrylic, and polycarbonate.
  • the present invention provides a process for concentrating diluted feed or brine or other aqueous solution for concentration, comprising:
  • the hydrophilic membrane is an asymmetric hydrophilic membrane further comprising a fabric layer on the second side of the membrane to provide mechanical strength to the membrane.
  • the fabric is a polyester net. ha ⁇ ing about 60% open area and about 0.07 mm thick.
  • the fabric is a silkscreen material.
  • the hydrophilic membrane is made from a cellulose material or polyvinyl alcohol. Most preferably, the cellulose material is selected from the group consisting of cellulose acetate, cellulose diacetate. cellulose triacetate, cellulose acetate butyrate. cellulose proprionate. and combinations thereof.
  • the diluted feed is heated using any available heat source to a temperature of from about 10 °C to about 95 °C. Most preferably, the diluted feed is heated to a temperature of from about 50° C to about 95 °C.
  • the air stream on the second side of the membrane is blown at a velocity of from about 5 cm/sec to about 100 m/sec. Most preferably, the velocity of the air across the membrane is about 100 cm/sec.
  • the present invention further provides a device for osmotic membrane evaporation of brine and other aqueous media (feed), comprising:
  • hydrophilic membrane having a first side and a second side, having a rejection property of 500 kDa cutoff or lower, wherein the hydrophilic membrane is not able to reject salt:
  • the hydrophilic membrane is an asymmetric hydrophilic membrane further comprising a fabric layer on the second side of the membrane to provide mechanical strength to the membrane.
  • the fabric is a polyester net, having about 60% open area and about 0.07 mm thick.
  • the fabric is a silkscreen material.
  • the hydrophilic membrane is made from a cellulose material or polyvinyl alcohol.
  • the cellulose material is selected from the group consisting of cellulose acetate. cellulose diacetate. cellulose triacetate, cellulose acetate butyrate, cellulose proprionate, and combinations thereof.
  • Figure 1 shows a prior art cut away in an axial direction showing product flow direction (through the length of a module) through a feed chamber having feed spacer (cross hatched) material contained within the entire area of the feed chamber.
  • feed spacer cross hatched
  • permeate spacer located throughout the permeate chamber.
  • the membrane is shown along with glue on the outer edges to maintain the integrity of the permeate chamber.
  • Figure 2 shows a cut away in the axial direction of the inventive spiral-wound membrane module design showing the novel open feed channels having a stiffener sheet between membrane layers. There is also a glued plug at either end. similar to the prior art design to form the permeate chamber. In addition there is a corrugated feed chamber spreader at either end to provide for a uniform feed chamber gap maintainer.
  • Figure 3 shows an outside view of the inventive spiral wound membrane module showing standard flow characteristics of feed and permeate.
  • the end view shows the corrugated feed chamber spreader at the end.
  • Figure 4 shows an end view close up again illustrating the corrugated feed chamber spreader and each layer having a membrane, permeate spacer, glue, permeate spacer and membrane.
  • Figure 5 shows an embodiment of the inventive spiral wound membrane module having ribs as the stiffener means.
  • Figure 6 provides a schematic of the inventive membrane evaporation process, wherein water in a liquid state (with salt) from a diluted brine solution crosses a membrane from the first side to the second side through absorbtivity and is evaporated into an air stream located on the second side of the membrane.
  • Figure 7 shows an overall schematic showing the membrane structure of Figure 6 on the left side and where a blower and a heat exchanger to capture and reuse excess heat generate airflow.
  • Figure 8 shows a graph of flux rates for brine solutions at increasing concentrations, as provided in Example 1.
  • the present invention provides an improved membrane design for spiral wound membranes that provide the cost advantages and space savings of spiral wound with superior flux and fouling characteristics.
  • the advantage of a spiral wound membrane design prior to the present invention is that it is inexpensive and has high membrane density ( ⁇ 30m 2 per 20 cm diameter by 100 cm long element). Its drawback is that it is highly susceptible to fouling since the feed must flow longitudinally through a net-like feed spacer. The fibers of the feed spacer allow suspended solids to become lodged and blind the membrane, degrading performance and inhibiting cleaning. Pressure drops are also high in the flow through the feed spacer, which makes it impossible to achieve the fluid velocities that have been shown to provide the best performance of membranes.
  • the invention is a spiral module design that does not require a feed spacer, thus pro ⁇ iding the advantages of unobstructed feed channels, at far lower cost than tubular modules.
  • the inventive membrane is a spiral wound design but without traditional spacer materials.
  • the present invention provides a spiral wound membrane module having a length and a radius and a circular cross section, having reduced fluid flow resistance, comprising (a) an envelope sandwich having a width equal to the length of the membrane module and comprising a layer of membrane ne.xt to a layer of permeate spacer material next to a layer of stiffener sheet next to a layer of permeate spacer material next to a layer of membrane, and wherein the envelope sandwich is wrapped increasing the radius of the membrane module: and (b) a structural assembly located between each wrap of the envelope sandwich to provide an open path for each feed chamber throughout the length of the membrane module.
  • the inventive membrane provides a "lay ered " approach to a spiral wound design with a stiff backing material and no spacer material through most of the flow path.
  • the layered membrane sandwich is shown in a cut-away view of three channels in Figure 2 wherein the sandwich layer for the middle section of the spiral wound module forms a membrane (green) on a permeate spacer material (red), on a polymeric stiffener material (dark blue), permeate spacer material (red), and another membrane (green).
  • the membrane is always between the permeate channel kept open by conventional spacer technology and a larger feed channel kept open by the polymeric stiffener (though the larger middle section of the module) and without conventional spacer technology.
  • the vast majority of the feed channel is open to significantly improve the flow rates and pressure drips, especially for high- suspended solids feed streams (e.g.. landfill leachate).
  • either end of the module has a feed channel spacer to align the polymeric stiffener sandwich to have open feed channels, preferably a corrugated plastic material as shown in Figure 2 and as a "corrugated spacer " in Figure 4. and glue ( Figure 2. light blue) to anchor the polymeric stiffener sandwich component and provide for permeate to be channeled to the center of the spiral wound module.
  • the inventive spiral wound module is designed in a similar fashion to a typical spiral wound membrane module except that there is no feed chamber spacer at all through most of the middle segment of the module (i.e.. 90%+ of the length) and the feed chamber remains patent with superior flow characteristics and pressure drops.
  • This inventh e design is illustrated in Figures 2-5.
  • the design is similar to a standard spiral wound design, except it requires no feed spacer.
  • the feed spacer material fills the entire feed channel.
  • a thick, corrugated spacer is used only at the front and back edge of the feed channel. Fluid pressure then keeps the membranes in contact with the permeate spacer and keeps the feed channels unobstructed.
  • a uniform feed channel width is ensured by employing a plastic stiffener in the permeate channel.
  • the stiffener is typically 0.5 mm to 1 mm thick and made from PVC. polypropylene, or polyethylene.
  • PVC polypropylene
  • polyethylene polyethylene
  • Ultrafiltration modules with the inventive design have been made and tested for performance criteria. Specifically. 24cm diameter by 60 cm long element with a feed channel gap width of 3 mm had a pressure drop of 1 kPa when feed fluid velocities inside the module were 0.5 m/sec. The module contained an effective membrane area of 10 m 2 . To put these data into perspective, the pressure drop experienced is about ten-fold lower than a conventional spiral wound device of about the same area and size having a conventional feed chamber spacer.
  • the inventive membrane module design can be applied to a variety of applications ranging from microfiltration through ultrafiltration to reverse osmosis.
  • Initial tests of the fouling resistance of the membrane have been conducted by ultrafiltration of a heavily soiled, machine shop cutting fluid containing emulsified oil. At 75% water removal. 0.5 m/sec cross- flow velocity, and 300 kpa pressure, the membrane flux declined less than 20% in 100 hours of operation without any cleanings. A similar membrane in a traditional spiral wound membrane module would foul and a much higher rate.
  • the inventive membrane evaporation process is an improvement over pervaporation and membrane distillation because the inventive process and device uses a hydrophilic membrane as opposed to a hydrophobic membrane required to be used in a pervaporation device. Another difference is that w f ater vapor is driven across the membrane in pervaporation driven by pressure gradients of water vapor through the pores in the membrane by a vacuum. Thus, a vapor pressure gradient drives the separation of water from salt as water is vaporized on the feed side of the hydrophobic membrane and drawn to the colder side a vapor. Low vapor pressures and microscopic pore diameters cause the flux in pervaporation to be slow.
  • the present process allows for water in a liquid state (and salt) transport across a hydrophilic membrane, such that the w ter evaporates directly into the air stream. Since the brine feed is heated, the cooler air that gets heated by contact with the membrane. allowing the air to hold more water, picks up water. High air flows improve the water evaporation rate because heat transfer through the membrane drives evaporation, and the most heat transfer occurs when the largest temperature differential occurs between the brine and the air. There is no vacuum pump as the air is blow n across the second side of the hydrophilic membrane. In the inventive process, near saturation, salt crystals will form on the second side of the hydrophilic membrane, indicating that the hydrophilic membrane is not rejecting salt. The crystals form when the water evaporates into the air flow on the second side of the hydrophilic membrane. The salt crystal formation is reversed when the air flow is temporarily turned off and the salt redissolves and diffuses back into the brine.
  • the inventive process and device uses a hydrophilic membrane.
  • the hydrophilic membrane thickness without a support layer is in the range of from about 1 to about 300 ⁇ m. in particular from about 20 to about 120 ⁇ m and ideally about 0, 1 mm thick.
  • the hydrophilic membrane is a cellulose-based membrane with ultrafiltration or tighter rejection properties.
  • Using a hydrophilic membrane allows for water lo transfer across the membrane as a liquid and evaporate from the back or second side of the membrane into an air stream. The evaporation process is augmented by heat transferred through from the feed solution being evaporated. Thus, the limiting resistance is heat transferred through the hydrophilic membrane.
  • a heat conductive membrane material such as cellulose, even cellulose triacetate, is preferred.
  • the more heat that can be transferred across the hydrophilic membrane couples with faster air flows across the second side of the hydrophilic membrane, will allow for faster evaporation and accelerating the process for brine concentration.
  • hydrophobic membranes such as those used in pervaporation processes, are too thermally insulating to be useful for the inventive process, Moreover, it is important to keep air flow on the second side of the hydrophilic membrane as high as possible.
  • a hydrophilic membrane is further important because in many brine solutions there are trace amounts of substances that will quickly foul hydrophobic membranes, requiring them to be cleaned frequently. In contrast, hydrophilic membrane will operate with infrequent cleanings in solutions containing a variety of foulants. such as fats, oils, proteins, parafins and other organics. In any salt evaporation process as the solution approaches saturation, salt crystal formation can hinder evaporation and cause frequent shut downs and cleanings. This is why cooling towers cannot make saturated brine solutions as they will rapidly cake up and collapse. Evaporators, even those made with expensive non-corrosive components, also cake up. However, according to the inventive process, salt crystals can form on the second side of the hydrophilic membrane, but turning off the air flow can reverse this crystallization. Moreover, the salt crystals on the second side of the hydrophilic membrane are hydroscopic and will help to pull water through the membrane.
  • This example illustrates the results of a study to reduce brine volume at a salt cavern associated with a refinery.
  • the salt caverns at refinery "X” annually take on about 1 0,000 barrels of rain water per year.
  • Refinery X needs a process to remove rain water from the brine.
  • the brine concentration ranges from 14 to 22.5% NaCl by weight.
  • a bench scale test was run and used to estimate the costs of rain water removal from the brine in terms of both capital costs and operating costs (electricity and membrane replacement).
  • Figure 7 showing the brine (feed) recirculated first through a heat exchanger, then passing an osmotic membrane evaporation module, and finally back to the tank.
  • the amount of water evaporated was calculated by recording tank level changes with time, Ambient (room) air was used and blown by a bench-scale regenerative blower on the second side of the hydrophilic membrane. Energy was provided by a set-point controlled electrical resistance heater that healed a recirculating loop. The heated water loop transferred its heat energy to the circulating brine in a heat exchanger.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

Cette invention a trait à un module membranaire enroulé en spirale, utilisable pour diverses filtrations sur membrane, lequel module n'offre qu'une résistance minime à un écoulement fluidique dans le trajet d'écoulement d'alimentation. Plus précisément, ce module membranaire comporte des éléments espaceurs ondulés, d'entrée et de sortie, sur moins de 10 % de la longueur dudit module, ainsi qu'un enroulement fait d'une feuille de renfort permettant de créer un canal d'alimentation de largeur uniforme. L'invention porte également sur un procédé d'évaporation sur membrane permettant d'extraire de l'eau saumurée. On utilise, dans le cadre de ce procédé, de la chaleur résiduelle à basse teneur et de l'air pour faire s'évaporer l'eau d'une solution saumurée diluée lorsque cette eau traverse la membrane en phase liquide.
PCT/US2001/031971 2000-10-15 2001-10-15 Module membranaire enroule en spirale a canal ouvert et concentration en saumure Ceased WO2002032533A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU2002211694A AU2002211694A1 (en) 2000-10-15 2001-10-15 Open-channeled spiral-wound membrane module and brine concentration

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US09/688,611 2000-10-15
US09/688,611 US6656361B1 (en) 2000-10-15 2000-10-15 Membrane assisted evaporation process and device for brine concentration
US09/688,612 2000-10-15
US09/688,612 US6673242B1 (en) 2000-10-15 2000-10-15 Open-channeled spiral-wound membrane module

Publications (2)

Publication Number Publication Date
WO2002032533A2 true WO2002032533A2 (fr) 2002-04-25
WO2002032533A3 WO2002032533A3 (fr) 2003-01-30

Family

ID=27104255

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2001/031971 Ceased WO2002032533A2 (fr) 2000-10-15 2001-10-15 Module membranaire enroule en spirale a canal ouvert et concentration en saumure

Country Status (2)

Country Link
AU (1) AU2002211694A1 (fr)
WO (1) WO2002032533A2 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7316780B1 (en) 1999-01-29 2008-01-08 Pall Corporation Range separation devices and processes
US8043512B2 (en) 2008-04-11 2011-10-25 Pall Corporation Fluid treatment arrangements and methods
US8048315B2 (en) 2008-07-28 2011-11-01 Pall Corporation Fluid treatment arrangements and methods
EP2755917A1 (fr) * 2011-09-16 2014-07-23 SABIC Innovative Plastics IP B.V. Procédé d'élimination du carbonate d'un effluent caustique d'épurateur
EP3171169A1 (fr) * 2015-11-19 2017-05-24 Sartorius Stedim Biotech GmbH Structure de membrane à motifs
CN115367946A (zh) * 2022-09-08 2022-11-22 碧菲分离膜（大连）有限公司 一种膜蒸馏海水淡化的方法

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3525682A1 (de) * 1985-07-18 1987-01-22 Robert Kohlheb Wickelmembran-filterkerze
US4906372A (en) * 1989-05-17 1990-03-06 Desalination Systems, Inc. Spiral-wound membrane cartridge
US4944877A (en) * 1989-10-10 1990-07-31 Maples Paul D Spacerless feed channel membrane filter element
US5137637A (en) * 1991-06-18 1992-08-11 Exxon Chemical Patents Inc. Rotational high flux membrane device
WO1993022038A1 (fr) * 1992-05-01 1993-11-11 Filmtec Corporation Element de membrane enroule en spirale

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7316780B1 (en) 1999-01-29 2008-01-08 Pall Corporation Range separation devices and processes
US8043512B2 (en) 2008-04-11 2011-10-25 Pall Corporation Fluid treatment arrangements and methods
US8048315B2 (en) 2008-07-28 2011-11-01 Pall Corporation Fluid treatment arrangements and methods
EP2755917A1 (fr) * 2011-09-16 2014-07-23 SABIC Innovative Plastics IP B.V. Procédé d'élimination du carbonate d'un effluent caustique d'épurateur
EP3171169A1 (fr) * 2015-11-19 2017-05-24 Sartorius Stedim Biotech GmbH Structure de membrane à motifs
WO2017084728A1 (fr) * 2015-11-19 2017-05-26 Sartorius Stedim Biotech Gmbh Structure de membrane à motifs
US11313854B2 (en) 2015-11-19 2022-04-26 Sartorius Stedim Biotech Gmbh Patterned membrane structure
CN115367946A (zh) * 2022-09-08 2022-11-22 碧菲分离膜（大连）有限公司 一种膜蒸馏海水淡化的方法

Also Published As

Publication number Publication date
AU2002211694A1 (en) 2002-04-29
WO2002032533A3 (fr) 2003-01-30

Similar Documents

Publication Publication Date Title
US6902672B2 (en) Open-channeled spiral-wound membrane module
US4857081A (en) Separation of water from hydrocarbons and halogenated hydrocarbons
US10441917B2 (en) Gas separation method
US9452390B2 (en) Spiral crossflow filter
CN110636894B (zh) 渗透压辅助的反渗透膜和模块
US6656361B1 (en) Membrane assisted evaporation process and device for brine concentration
CN104364203A (zh) 得到净化水的方法及其装置
JP6365542B2 (ja) 正浸透用中空糸膜エレメント及び膜モジュール
JP5802384B2 (ja) 膜モジュール及び浄化水製造装置
JP6222237B2 (ja) 正浸透用中空糸膜エレメント及び膜モジュール
WO2002032533A2 (fr) Module membranaire enroule en spirale a canal ouvert et concentration en saumure
JP2000000437A (ja) スパイラル型逆浸透膜エレメントおよびそれを用いた分離装置
JPH11114381A (ja) スパイラル型膜エレメント
JP7155862B2 (ja) 中空糸膜エレメント、中空糸膜モジュールおよび正浸透水処理方法
JP6517784B2 (ja) スパイラルクロスフロー濾過器
JP2001113139A (ja) 中空糸膜モジュールおよびその製造方法
WO2015129674A1 (fr) Module de membranes à fibres creuses
JP6565688B2 (ja) 中空糸型逆浸透膜エレメント及びモジュール
WO2015125755A1 (fr) Élément et module de membrane en fibres creuses
JP2019025419A (ja) 分離膜エレメント及びベッセル
JP7379835B2 (ja) 中空糸膜モジュール
US10315156B2 (en) Gas separation method
JP7443761B2 (ja) 中空糸膜モジュール
JP2025021430A (ja) スパイラル分離膜エレメント
JP2024049759A (ja) 分離膜エレメント

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A2

Designated state(s): AU BR CA CZ IL JP KR NO NZ PL RU

AL Designated countries for regional patents

Kind code of ref document: A2

Designated state(s): AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE TR

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: JP