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WO2017140927A1 - Ensemble de membranes à fibre creuse et leurs applications - Google Patents

Ensemble de membranes à fibre creuse et leurs applications Download PDF

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Publication number
WO2017140927A1
WO2017140927A1 PCT/ES2017/070039 ES2017070039W WO2017140927A1 WO 2017140927 A1 WO2017140927 A1 WO 2017140927A1 ES 2017070039 W ES2017070039 W ES 2017070039W WO 2017140927 A1 WO2017140927 A1 WO 2017140927A1
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WO
WIPO (PCT)
Prior art keywords
hollow fiber
membrane
fiber membranes
module
mesh
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/ES2017/070039
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English (en)
Spanish (es)
Inventor
Mohamed Khayet Souhaimi
María del Carmen GARCÍA PAYO
Julio Antonio SANMARTINO RODRÍGUEZ
Juan Pablo POCOSTALES BUENAVIDA
Rocío RODRÍGUEZ AGUILERA
Abel Riaza Frutos
Francisco Javier BERNAOLA ECHEVARRÍA
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.)
Abengoa Water SL
Original Assignee
Abengoa Water SL
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
Application filed by Abengoa Water SL filed Critical Abengoa Water SL
Publication of WO2017140927A1 publication Critical patent/WO2017140927A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • B01D61/364—Membrane distillation
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • the present invention relates to a set of hollow fiber membranes entwined in a mesh and its application in the membrane distillation process for the treatment and / or desalination of fluids.
  • Membrane distillation (DM) for the treatment and / or desalination of water is a non-isothermal membrane process, whose driving force is the vapor pressure gradient across a membrane that must meet the following characteristics: i) porous with high porosity,
  • At least one side of the membrane must be in direct contact with the solution to be treated, it is at a higher temperature than the permeate.
  • DM differs from other membrane processes in that the membrane is not an active part in the separation and only serves as a support for a liquid / vapor infer. Due to its hydrophobicity, water in liquid phase or the solution to be treated cannot penetrate inside the pores, unless a hydrostatic pressure greater than the filling pressure of the pores that is determined by the angle is applied of contact of the solution with the membrane (degree of hydrophobicity), the surface tension of the liquid and the maximum pore size. As noted above, the driving force in this process is the difference in vapor pressure between both ends of the pores. To produce the distillation, therefore, a liquid / vapor infer is created at each pore end preventing the hydrostatic pressure from being greater than the filling pressure of the pores.
  • These DM systems can have one or more membrane modules using flat membranes or hollow fiber membranes. These modules can be flat, spiral or other configurations.
  • membrane distillation there are different configurations of membrane distillation, such as:
  • the linear arrangement of the hollow fiber membranes in a wrap has several limitations: temperature polarization occurs inside the hollow fiber membrane and presents machining difficulties, since the hollow fiber membranes arranged in a wrap when being rolled up to Insert them into the spiral-shaped module and slide in relation to the envelope.
  • EP20721 12 discloses a distillation system with one or more modules of hollow fiber membranes to obtain distillates from a concentrated liquid as food, arranged in series, in parallel, or in a combination of both options . It consists of a DMCD method, whereby the food (previously heated and pressurized) flows inside the module in which there are flow regulators that cause longer contact time of the food with the hollow fiber membranes and greater turbulence. Inside the hollow fiber membranes the distillate flows at a lower temperature.
  • this patent does not describe a set of hollow fiber membranes spirally wound around a condensation surface.
  • WO2003000389 describes a DM system with hollow fiber membranes that works in both DMCD and DMV.
  • This system stands out for being able to recover heat from the permeate vapor (extracted from the module and compressed externally), which is recirculated by an exchanger / condenser to heat the food before it enters the module.
  • this patent also does not describe a set of hollow fiber membranes spirally wound around a condensation surface.
  • the chamber through which the refrigerant fluid circulates does not comprise baffles that create turbulence in the refrigerant fluid to decrease the polarization by temperatures on the permeate side.
  • modules comprising hollow fiber membranes have another limitation due to their manufacturing process. These modules have hollow fiber membranes arranged in parallel and in a vertical position (parallel to the central axis of the spiral). Specifically, hollow fiber membranes are usually arranged spirally wound around the condensation surface. With this arrangement, it is difficult to introduce and remove the hollow fiber membranes, especially when the condensation surfaces have a certain stiffness, the placement and fixing of the hollow fiber membranes in the module being a challenge.
  • the present invention relates to a set of hollow fiber membranes entwined in a mesh for use in a membrane distillation module.
  • the present invention solves the problems due to the laminar regime without increasing the fluid pressure in the hollow fiber membranes. This is achieved by interlacing the hollow fiber membranes in a mesh, which generates some curvature in the hollow fiber membranes so that the turbulence of the flow is increased, decreasing the polarization phenomenon.
  • the assembly consisting of a mesh and hollow fiber membranes of the invention is easily removable from the distillation module, which facilitates the assembly of the hollow fiber membranes in the distillation module regardless of the stiffness of the condensation surfaces.
  • the mesh and hollow fiber membrane assembly is highly versatile and manageable, so it can be easily integrated into the spiral structure or other geometries that could be designed.
  • DMCD Direct Contact Membrane Distillation
  • DMCA Air Chamber Membrane Distillation
  • DMV Vauum Membrane Distillation
  • DMCL Distillation Distillation Membrane with Liquid Chamber
  • DMGB Mistillation Distillation by Scanning Gas
  • DMGBT distillation in Membrane by Thermostated Scanning Gas
  • set of hollow fiber membranes in the context of the invention is meant the set of hollow fiber membranes and a mesh, where the hollow fiber membranes are transversely intertwined in the warp of the mesh.
  • a first aspect of the present invention relates to a set of hollow fiber membranes supported on a mesh characterized in that the hollow fiber membranes are transversely interwoven between the warp of the mesh.
  • a second aspect of the present invention relates to a membrane module comprising the hollow fiber membrane assembly as described above.
  • a third aspect of the present invention relates to a system comprising at least one membrane module of the present invention.
  • a fourth aspect of the present invention relates to the use of a membrane distillation module as described above or a membrane distillation system as described above for the treatment and / or desalination of fluids.
  • FIG. 1 Shows a scheme of the mesh and interlacing of the hollow fiber membrane (FIG. 1A) and curvature diameter of the hollow fiber membrane MD (FIG. 1 B); U: warp; T: plot; F: hollow fiber membrane; d c : curvature diameter.
  • FIG. 2 Braided in the mesh of hollow fiber membranes and detail of the groups of three interwoven hollow fiber membranes.
  • FIG. 3 Longitudinal section of a module comprising the set of interwoven hollow fiber membranes of the invention.
  • FIG. 4 Cross section of a module comprising the set of intertwined hollow fiber membranes of the invention. DETAILED DESCRIPTION OF THE INVENTION
  • a first aspect of the present invention relates to a set of hollow fiber membranes supported on a mesh characterized in that the hollow fiber membranes are transversely interwoven between the warp of the mesh (fig. 1A).
  • the hollow fiber membrane is a porous membrane in the form of a flexible hollow filament, so it is possible to interlace it in a plastic mesh or of some flexible material with a light greater than the outer diameter of the hollow fiber membrane.
  • the process of interlacing the hollow fiber membrane consists in crosslinking the hollow fiber membrane between the holes of the mesh, leaving or not empty spaces between each interbreeding.
  • This mesh must have an appropriate light size and stiffness so that the hollow fiber membrane can be intertwined without being damaged.
  • the mesh on which the hollow fiber membranes are intertwined performs several functions:
  • the mesh acts as a support for hollow fiber membranes. By interweaving the hollow fiber membranes, they can be packaged within the body of a membrane distillation module without sliding of the hollow fiber membranes with respect to a condensation surface.
  • packing density is understood as the effective membrane area that is available per membrane module volume, excluding the volume occupied by the cooling chamber.
  • the interlacing of the hollow fiber membranes has a curvature diameter (d c ) of about 2 cm to 5 cm and more preferably 2.5 cm to 3.5 cm (fig. . 1 B).
  • the mesh must be of a flexible material and it must be avoided that it has edges.
  • the mesh is made of plastic to avoid oxidation problems.
  • the materials composing the mesh are preferably selected from fiberglass or a plastic material selected from polyvinylchloride (PVC), polypropylene (PP) or polyethylene (PE).
  • the mesh has a light grid of between 1.5 mm and 8 mm and more preferably from 2 mm to 5 mm and a density of between 0.2 and 2 g / cm 3 and more preferably between 0.4 g / cm 3 and 1 g / cm 3 . More preferably, the mesh has a thickness between 0.1 mm and 0.5 mm, and even more preferably between 0.2 mm and 0.3 mm.
  • the distance between each warp is between 1 mm and 3 mm, more preferably between 1.5 mm and 2.5 mm; the distance between each frame is between 0.1 mm to 1 mm, more preferably between 0.3 mm and 0.8 mm; and a weight between 40 and 150 g / m 2 , more preferably between 60 g / m 2 and 100 g / m 2 .
  • the mesh has a tensile strength greater than 400N.
  • the hollow fiber membranes are composed of a porous hydrophobic material that It may or may not be combined with a layer of a hydrophilic material.
  • they are composed of at least one of the following materials selected from polytetrafluoroethylene (PTFE), vinylidene polyfluoride (PVDF), polypropylene (PP), polyvinylidene-co-hexafluoride polypropylene (PVDF-HFPP), fluorinated polyoxadiazoles (POD) , fluorinated polyoxatriazoles (POTF) or any combination thereof. More preferably they are composed of a material selected from polypropylene and vinylidene polyfluoride.
  • the hollow fiber membranes have a pore size range between 0.01 ⁇ -5 ⁇ , preferably between 0.01 ⁇ and 1 ⁇ , more preferably between 0.2 ⁇ -0.6 ⁇ and even more preferably between 0.3 ⁇ -0.4 ⁇ .
  • a second aspect of the present invention relates to a module comprising the hollow fiber membrane assembly of the present invention as described above.
  • the module in addition to the hollow fiber membrane assembly of the invention as described above that includes a mesh, comprises:
  • cooling chamber comprising at least two condensation surfaces.
  • module body consisting of a cooling jacket, in addition to covers and connections for refrigerant, food and permeate inlets and outlets.
  • the cooling chamber is a chamber through which the cooling fluid circulates, and comprising at least two condensing surfaces (preferably one on each side of the chamber).
  • the cooling chamber is fed by the cooling fluid inlet to the chamber and has a cooling fluid outlet.
  • the cooling chamber has the task of acting as a steam condensation surface in the air and vacuum chamber configurations.
  • its function is to cool the permeate inside the module and favor a higher temperature gradient in the process.
  • the cooling chamber must cool the entrainment gas inside the module equally.
  • the cooling jacket serves to cool the module, favoring the condensation of the permeate as well as being used as insulation of the module with the outside.
  • another objective is to recover heat from the assembly with these chambers, which can be used to preheat the food or the food itself can be used as a refrigerant.
  • the module construction process consists of the formation of a spiral, constituted by the cooling chamber, inside the membrane distillation module and inserting the mesh with hollow fiber membranes entwined in the spiral chamber of the cooling chamber, so that it is arranged in the form of a spiral wound together with the cooling chamber.
  • a cooling chamber with sufficient rigidity is available to remain vertically on its own spiral-shaped base.
  • the number of hollow fiber membranes in a module is of the order of several hundred, so the mesh is useful to facilitate packing, preventing the hollow fiber membranes from moving with respect to the cooling chamber that can have various geometries, For example, spiral.
  • the membrane module may have an external cooling jacket that allows thermostatizing and better isolating the module, also aiding in condensation and therefore can increase the water production rate. at the same time that heat can be recovered.
  • thermostatizing it is meant to keep the temperature constant within the module and by insulating, minimizing the energy transfer between the module and the exterior thereof.
  • the feed inlet temperature is between 10 ° C and 100 ° C, preferably between 40 ° C and 90 ° C, and more preferably between 60 ° C and 75 ° C.
  • the inlet temperature of the cooling streams is between -25 ° C to 80 ° C, and more preferably between 0 ° C and 50 ° C and more preferably between 10 ° C and 30 ° C.
  • the module comprises a food inlet, a food outlet, an inlet and an outlet of the permeate, a spiral-shaped central part composed of a refrigeration chamber having at least two condensation surfaces, and by at least one set of hollow fiber membranes and a mesh described in the present invention, an inlet and an outlet of the cooling fluid from the cooling chamber and, optionally a cooling jacket arranged surrounding the central part.
  • a cooling fluid circulates through the cooling jacket with an inlet and outlet.
  • Cooling fluid means any fluid used to exchange heat with the walls of the chamber / jacket that contains them.
  • the cooling fluid that circulates through the cooling chamber and the fluid that circulates through the cooling jacket can be the same fluid or different fluids.
  • the refrigerant fluid is the food before being heated. In this way the heat of the product obtained in the process is used to preheat the food.
  • the module will have a permeate outlet for DMCD, which can be air or gas inlet in DMCA, DMGB, DMGBT and permeate outlet in DMCL.
  • DMCD permeate outlet for DMCD
  • DMGB permeate output for DMCD
  • DMV permeate outlet in DMCL
  • the condensation surfaces are made of a thermal conductive material and compatible with the fluid to be treated as well as the fluid used as a refrigerant.
  • the thermal conductivity of the condensation surface must be as high as possible to favor the transmission of heat through the surface, increasing the condensation of steam on it and the recovery of that latent heat of condensation in the process itself.
  • the thermal conductivity of the condensation surface must be high in order to keep the permeate at a suitable temperature and prevent it from heating up in the module in the DMCD configuration and, on the other hand, increasing the condensate rate in the condensation surface DMCA and DMV settings.
  • the temperature of the gas must be kept as low as possible during its passage through the module.
  • the range of thermal conductivity values that can be used ranges between tens (eg Titanium, 21 W / mK) and hundreds (eg Copper, 385 W / mK). The optimal range is between 200-400 W / m K.
  • the materials for the construction of the condensation surface have a moderate-high corrosion resistance of effluents of high salinity, so that seawater or the food itself can be used as cooling fluids.
  • Examples of materials could range from metals such as copper, aluminum, tin or some type of alloy and, to a lesser extent, plastic materials (they have low conductivity but it is possible to find plastic materials with improved thermal conductivities) or even laminated graphite materials .
  • Other materials that can be used are aluminum-magnesium alloys (eg Magnealtok® 50 with a thermal conductivity of 116 W / mK).
  • the material for the condensation surface is preferably of easy forming and good weldability.
  • the thickness range of the condensation surfaces of the cooling chamber must be small enough so that the heat transfer is very good and so that it can be easily screwed in (form the spiral) but, at the same time, it must have a sufficient thickness to allow welding without damaging the material.
  • the range of thicknesses is 0.8 to 1 mm.
  • the material used for the manufacture of the spirally wound refrigeration chamber together with the hollow fiber membrane assembly of the present invention must be rigid enough so that it can be arranged, wound or machined in a spiral and that it keep vertically supported on the base of the spiral without it crumbling or touching the surfaces of it.
  • the elastic limit also called the yield limit or yield limit, which is the maximum tension to which a material can be subjected without permanent deformation, that is, when the load ceases the piece recovers Its initial form.
  • the condensation surface has a low elastic limit so that it is easily deformable
  • the range of elastic limit may vary between 5 and 150 N / mm 2 , for example annealed copper having a value of 9 N / mm 2 or an aluminum-magnesium alloy (5052) having an elastic limit of 90 can be used N / mm 2 It also has a Brinell Hardness with a maximum of 100 HB, for example for annealed copper it is 35 HB and for the 5052 aluminum-magnesium alloy it is 60 HB.
  • the condensation surface material is a plastic, graphite or metal material, more preferably the condensation surface is a metallic material, even more preferably copper or an aluminum-magnesium alloy.
  • the hollow fiber membranes next to the mesh, described in the present invention form a fabric that is preferably spirally arranged.
  • This fabric has to be found together with a spiral-wound flat cooling chamber.
  • the cooling chamber in turn can function as an internal heat exchanger by preheating the food before being introduced inside the hollow fiber membranes.
  • Inside the hollow fiber membranes circulates the food or solution to be purified, which is at a temperature higher than the condensation surface.
  • the condensation surface is made of a thermally conductive material, preferably metallic, for example copper plate. Water vapor and volatiles from the food solution are able to cross the membrane due to the difference in vapor pressure on both sides of the membrane.
  • the degree of rejection is 100% when the food is electrolytes and non-volatile electrolytes, for example NaCI or glucose, dissolved in water and does not comprise any other volatile element.
  • This vapor reaches the condensation surface by condensing in it as water of greater purity in the DMCA, DMGBT and DMV configurations.
  • this permeate ends up being collected at the bottom of the module.
  • DMV vacuum
  • the food is circulated inside the hollow fiber membranes and condense the permeate on a nearby cold surface if working in DMCA or maintaining the permeate (gas or liquid) in contact with hollow fiber membranes for DMCD, DMCL, DMGB and DMGBT.
  • the permeate is kept as cold as possible to increase the driving force of the DM process.
  • the pressure inside the membrane module can be lowered by means of a water tube or a vacuum pump connected to the permeate of the module giving rise to the DMV.
  • the cooling chamber is a thin hollow chamber of thickness (about 1 cm) formed by condensation surfaces, through which the coolant flows. In this way an increase in the temperature difference within the module can be achieved.
  • the cooling chamber Inside the refrigeration chamber there is a number of speakers that give it a mechanical resistance and, at the same time, a better distribution of the fluid inside.
  • the idea is to wind the cooling chamber on a central axis and a mesh with braided hollow fiber membranes to form a roll in a spiral configuration (fig. 4).
  • the module is equipped with an external cooling jacket to insulate the outside and help the condensation phenomenon of the steam produced.
  • the module can be placed vertically or inclined with a degree between 0 or 90 °, preferably between 45 ° and 60 ° on the horizontal, to facilitate the collection of permeate and to guarantee a tangential circulation of the food in contact with the entire membrane.
  • the module as described above can be presented in any configuration and preferably has a selected configuration of DMCD (Direct Contact Membrane Distillation), DMCA (Membrane Distillation by Chamber of Air), DMV (Vacuum Membrane Distillation), DMCL (Liquid Chamber Membrane Distillation), DMGB (Sweep Gas Membrane Distillation) and DMGBT (Thermostatic Swept Membrane Distillation).
  • a third aspect of the present invention relates to a membrane distillation system comprising at least one membrane module of the present invention. Several modules can be arranged in series or in parallel, increasing production. On the other hand, the performance can be increased by arranging several modules in series.
  • a fourth aspect of the present invention relates to the use of a membrane distillation module as described above or a membrane distillation system as described above for the treatment and / or desalination of fluids.
  • the food is a fluid that is to be treated and / or desalinated and that is formed by an aqueous solution containing any type of soluble or insoluble substance that it is desired to remove or decrease from the aqueous solution
  • the feed inlet temperature is between 10 ° C and 100 ° C, preferably between 40 ° C and 90 ° C, and more preferably between 60 ° C and 75 ° C.
  • the inlet temperature of the cooling streams is between -25 ° C to 80 ° C, and more preferably between 2 ° C and 50 ° C and more preferably between 5 ° C and 30 ° C.
  • membrane distillation module of the invention or of a system comprising at least one module may have the following applications:
  • azeotropic mixtures for example hydrochloric acid - water or formic acid - water.
  • the membrane distillation module comprises the set of hollow fiber membranes entwined in a mesh of the invention and a spirally wound cooling chamber and a body formed by a cooling jacket, 2 stainless steel caps and threads, and connections stainless steel for the exit and entrance of the refrigeration chamber, the cooling jacket, the permeate / condensate and the food.
  • ACCUREL® PP Q3 / 2 hollow fiber membranes were used under the DMCD, DMCA and DMV configurations. However, it could work in the same way with any other type of hollow fiber membranes.
  • the ACCUREL® PP Q3 / 2 hollow fiber membranes can be used for other configurations such as DMGB, DMGBT and DMCL.
  • the module comprises an inlet of the food (1), an outlet (V) of the food, an inlet (2) and an outlet (2 ') of the cooling fluid to the cooling chamber.
  • the central part of the module is composed of the spiral-shaped cooling chamber (2 ") (consisting of two condensing surfaces, 2"') and at least one set of hollow fiber membranes (3) interwoven in one mesh (5). This central part is surrounded by a cooling jacket (4) through which a cooling fluid circulates with an inlet and an outlet (4 ', 4 ", respectively).
  • the module covers have permeate outlet (6) for DMCD, DMCL or air or gas inlet in DMCA, DMGB, DMGBT and permeate inlet (6 ') for DMCD, permeate outlet for DMCA, DMGB, DMGBT, DMV (in DMCL must be closed.)
  • the internal diameter of the cooling jacket is 12.5 cm, with a jacket thickness of 1.25 cm, a spiral-shaped cooling chamber made of copper, annealed copper was placed inside the module because it is the one with the highest thermal conductivity, easily formed and good weldability, to form the cooling chamber.
  • the thickness of each copper plate is 0.8 mm, 30 cm high with an external and internal plate length that forms the walls of the cooling chamber, 71 , 3 cm and 61, 2 cm, respectively (external and internal development of the spiral l)
  • the cooling chamber is formed with three turns around its central axis and a thickness of the hollow cooling chamber of 0.7 cm (2 "in fig.
  • the technical specifications of the mesh are the following: grid (light): 4 x 4 mm; thickness: 0.2 mm; warp: 1, 7 mm; weft: 0.2 mm; weight: 82 g / m 2 ; density: 0.40 g / cm 3 ; and tensile strength (stiffness): ⁇ 400 N.
  • the number of hollow fiber membranes in the mesh is approximately 300.
  • the length of the mesh is 55 cm long and 30 cm high. If we take into account the length of the mesh, the density of the hollow fiber membranes is 5.45 hollow fiber membranes / cm.
  • the volume inside the spiral formed by the hollow of the cooling chamber (1 x 55 x 30) is 1650 cm 3 and the effective area of the hollow fiber membranes is 2600 cm 2
  • the packing density defined as the effective area of the membrane per volume of membrane module, excluding the volume occupied by the cooling chamber, is 1.58 cm 2 / cm 3 .
  • the most limiting value for the distillation process is the flow of food inside the hollow fiber membranes whose Re is in a clearly laminar regime whereby the effect by temperature polarization and concentration is important.
  • distillate flows of 3.7 LMH (lm “2 h “ 1 ) were obtained in the air chamber configuration and 7.7 LMH (lm “2 h “ 1 ) in the vacuum configuration using a vacuum pressure of 0.3 bar.
  • the thermal efficiency, ⁇ ⁇ has been defined as the ratio between the amount of heat transferred through the membrane and the heat actually used for the permeate flow obtained, that is:

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un ensemble de membranes à fibre creuse entrelacées dans une maille et son application dans des procédés de distillation membranaire pour le traitement et/ou la désalinisation de fluides.
PCT/ES2017/070039 2016-02-19 2017-01-25 Ensemble de membranes à fibre creuse et leurs applications Ceased WO2017140927A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ESP201630188 2016-02-19
ES201630188A ES2633154B1 (es) 2016-02-19 2016-02-19 Conjunto de membranas de fibra hueca y sus aplicaciones

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Publication Number Publication Date
WO2017140927A1 true WO2017140927A1 (fr) 2017-08-24

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Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20190168163A1 (en) * 2017-12-01 2019-06-06 Stuart Miller Ultra-filtration membrane and method of forming the same

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4140637A (en) * 1977-10-06 1979-02-20 Walter Carl W Permeability separatory method and apparatus
EP1270063A2 (fr) * 2001-06-21 2003-01-02 Celgard Inc. Contacteur a membrane en fibres creuses
WO2004071973A1 (fr) * 2003-02-13 2004-08-26 Zenon Environmental Inc. Appareil et procede a film biologique sur support
WO2008088293A1 (fr) * 2007-01-18 2008-07-24 Hyflux Membrane Manufacturing (S) Pte Ltd Contacteur à membrane
WO2013059216A1 (fr) * 2011-10-17 2013-04-25 Aptwater, Inc. Conception de modules pour une utilisation dans et un fonctionnement d'un réacteur à biofilm à membrane ayant un bio-encrassement réduit

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4140637A (en) * 1977-10-06 1979-02-20 Walter Carl W Permeability separatory method and apparatus
EP1270063A2 (fr) * 2001-06-21 2003-01-02 Celgard Inc. Contacteur a membrane en fibres creuses
WO2004071973A1 (fr) * 2003-02-13 2004-08-26 Zenon Environmental Inc. Appareil et procede a film biologique sur support
WO2008088293A1 (fr) * 2007-01-18 2008-07-24 Hyflux Membrane Manufacturing (S) Pte Ltd Contacteur à membrane
WO2013059216A1 (fr) * 2011-10-17 2013-04-25 Aptwater, Inc. Conception de modules pour une utilisation dans et un fonctionnement d'un réacteur à biofilm à membrane ayant un bio-encrassement réduit

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ES2633154B1 (es) 2018-08-02

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