Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
  • B01D71/06—Organic material
  • B01D71/56—Polyamides, e.g. polyester-amides
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
  • B01D67/0002—Organic membrane manufacture
  • B01D67/0009—Organic membrane manufacture by phase separation, sol-gel transition, evaporation or solvent quenching
  • B01D67/0011—Casting solutions therefor
• • 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
  • B01D69/12—Composite membranes; Ultra-thin membranes
  • B01D69/125—In situ manufacturing by polymerisation, polycondensation, cross-linking or chemical reaction
  • B01D69/1251—In situ manufacturing by polymerisation, polycondensation, cross-linking or chemical reaction by interfacial polymerisation
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2325/00—Details relating to properties of membranes
  • B01D2325/02—Details relating to pores or porosity of the membranes
  • B01D2325/0283—Pore size
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2325/00—Details relating to properties of membranes
  • B01D2325/20—Specific permeability or cut-off range

Definitions

• Filtration membranes are commonly used to separate fluid mixtures and solutions.
• reverse osmosis (RO) and nanofiltration (NF) membranes are commonly used to remove salts, minerals and other dissolved ions in the desalination of seawater or brackish water, the production of dairy products, recovery of paint solids and other substances in metal finishing applications, and the like.
• Typical operating pressures for RO filtration systems range from 200 - 1200 psi.
• the typical operating pressure range for NF systems is 150-300 psi.
• Such membranes may be produced by coating a support material with layer of an aqueous casting solution and contacting a second aqueous solution layer to the aqueous casting solution layer to cause interfacial polymerization.
• U.S. Patent No. 4,277,344 to Cadotte (the "Cadotte reference”) describes an aromatic polyamide membrane produced by the interfacial reaction of a aromatic polyamine with at least two primary amine substituents and an acyl halide having at least three acyl halide substituents.
• a porous support is coated with a layer of aqueous solution containing a monomeric aromatic polyamine reactant.
• the coated support is then contacted with an aqueous solution containing a monomeric, aromatic, amine-reactive polyfunctional acyl hahde (preferably dissolved in a nonpolar organic liquid) and then dried.
• the Cadotte reference describes the use of trichlorotrifiuoroethane (commonly known by the trade name "FREON").
• U.S. Patent No. 5,246,587 to Tomaschke describes an aromatic polyamide RO membrane that is made by coating a porous support material with a casting solution containing a polyamine reactant and an amine salt on a porous support material.
• suitable polyamine reactants include aromatic primary diamines (such as, m-phenylenediamine or p-phenylenediamine or substituted derivatives thereof wherein the substituent is an alkyl group, an alkoxy group, a hydroxy alkyl group, a hydroxy group or a halogen atom); aromatic secondary diamines (such as, N, N'-diphenylethylene diamine), cycloaliphatic primary diamines (such as, cyclohexane diamine); cycloaliphatic secondary diamines (such as, piperazine or trimethylene dipiperidine); and xylylene diamines (such as m-xylylene diamine).
• aromatic primary diamines such as, m-phenylened
• the support material is typically made of a polyarylether sulfone, such as a polysulfone and a polyether sulfone; a polyimide; or a polyvinylidene fluoride.
• the layer of casting solution is then contacted with a organic solvent solution containing a monomeric, aromatic, amine-reactive reactant, causing interfacial polymerization.
• the product is then dried to form a water permeable membrane.
• U.S. Patent No. 6,245,234 to Koo et al. describes a composite polyamide RO membrane that is made by first coating a porous polysulfone support with an aqueous solution containing: 1) a polyfunctional primary or secondary amine; 2) a polyfunctional tertiary amine; and 3) a polar solvent. The excess aqueous solution is removed and the coated support is then dipped in an organic solvent solution of trimesoyl chloride (TMC) and a mixture of alkanes having from eight to twelve carbon atoms. The resulting composite membrane is then rinsed in a 0.2% sodium carbonate (Na2CO3) aqueous solution.
• TMC trimesoyl chloride
• U.S. Patent No. 6,177,011 to Hachisuka et al. describes a RO membrane comprising a sponge layer and a separation layer formed on the sponge layer.
• the separation layer either contains or is coated with an electrically-neutral organic substance or polymer, such that the suface zeta potential of the layer is with +/- .10 millivolts at pH 6.
• U.S. Patent No. 6,183,640 to Wang describes a polymer membrane having permanent, internal anionic charges. The membrane is cast on a porous support structure from a solution containing a sulfone polymer, an anionic charge-modifying agent, a nonsolvent and a solvent.
• Embodiments of the present invention are directed to methods of manufacturing a filtration membrane, such as a RO or NF membrane, with high fluid flux and salt rejection properties, as well as to membranes produced by such methods.
• Membranes according embodiments of the present invention may be made by depositing an aqueous amine solution containing propionic acid and a non-amine base on a microporous substrate. The aqueous amine solution may then be contacted with a second solution containing an acyl halide and an organic solvent to cause interfacial polymerization to occur between the two solution layers. The aqueous amine solution may be produced using a propionate salt.
• Filtration membranes made according to method embodiments of the present invention may be cast upon a microporous substrate.
• the substrate may be prepared by casting a solution containing the substrate material on a non-woven polyester fabric or other backing material.
• the substrate may be made of polysulfone.
• a casting solution may be prepared by dissolving polysulfone polymer pellets (e.g., Udel-3500 available from BP Amoco Chemicals, Inc. of Alpharetta, Georgia) in a solvent, such as dimethyl formamide.
• Polyvinylpyrrolidone e.g., K-15 available from International Specialty Products of Wayne, New Jersey having an average molecular weight of 10,000 may be added to the casting solution.
• the casting solution may contain 17.00% polysulfone, 82.50% dimethyl formamide and 0.50% polyvinylpyrrolidone by weight.
• the casting solution may be applied to the backing material and may be gelled into a solid polysulfone substrate using a membrane casting machine.
• Alternative substrate materials may be used and the selection of a particular substrate material may depend on many factors (e.g., chemical environment involved in the commercial application of the membrane, polymerization solutions being interacted, etc.
• An aqueous amine solution is made by mixing an organic acid, such as propionic acid, into water.
• the solution is at least partially neutralized by the addition of a non-amine base (i.e., the pH of the solution may be raised).
• a non-amine base i.e., the pH of the solution may be raised.
• Sodium hydroxide has been found to be a suitable and cost-effective base for this purpose, although other bases may also be used.
• the aqueous amine solution may be prepared directly from a salt, such as sodium propionate, rather than indirectly from an acid and a non-amine base.
• amine such as piperazine powder, if a RO membrane is being produced, or m- poly(phenylenediamine) (MPD), if a NF membrane is being produced, is mixed into this solution and dissolved.
• MPD m- poly(phenylenediamine)
• the selection of a particular amine component of the aqueous amine solution may vary depending upon the type of membrane being produced.
• the substrate is then wetted with the aqueous amine solution. Any excess solution may be removed from the surface of the substrate, e.g., by evaporation or by blowing air over the surface of the substrate.
• the wetted substrate may then be brought into contact with an acyl halide solution that contains a small quantity of an acyl halide, such as, trimesoyl chloride (TMC), cyclohexane- 1,3,5-tricarbonyl chloride, isophthaloylchloride, and tetraphthaloyl chloride.
• TMC trimesoyl chloride
• cyclohexane- 1,3,5-tricarbonyl chloride isophthaloylchloride
• tetraphthaloyl chloride tetraphthaloyl chloride.
• the acyl halide may be dissolved in naphtha or a similar organic solvent.
• the solvent is preferable one that is immiscible in water, does not react with acyl halides and is chemically compatible with the selected substrate material.
• the chosen solvent does not pose a fire hazard and that the solvent can be easily removed from the membrane during a drying process within an optimal temperature range.
• interfacial polymerization instantaneously occurs, creating a thin-film polymeric membrane on the surface of the substrate.
• the excess quantity of the acyl halide solution may be removed by air-drying or by drying the membrane in an oven at high temperature. The latter may be preferred for naphtha or other organic solvents that generally have higher boiling points.
• a NF membrane thus prepared may be continuously rolled and stored in dry condition.
• Such membranes typically exhibit 45-65 % salt rejection for a 2000 ppm aqueous NaCl solution at 110 psi and 77DF.
• the membranes also exhibited fluxes of 80-110 gallons/ft2 D day (gfd).
• membranes currently on the market demonstrate fluxes within the range of 25- 40 gfd. [Replace with magnesium sulfate rejection characteristics if you have this data available (both for the invented membranes and those on the market)]
• the higher flux membranes of the present invention are advantageous insofar as they allow for higher throughput of product fluid and use less energy to achieve the same output.
• the layers be applied evenly to ensure consistent polymerization across the surface of the membrane.
• the thickness of the applied layers is generally not crucial, so long as the correct molar quantities of each of the solutions are provided so that polymerization can take place at the interface.
• the use of an interfacial polymerization process will yield produce a polymeric layer with high molecular weight. High molecular weight polymers are preferred both for their higher mechanical strength as well as for their superior rejection properties.
• aqueous amine solution is described above, it may be possible to use non-aqueous amine solutions, depending on the nature of the amine and other components of the solution and the nature of the substrate. If a non-aqueous amine solution is used, an aqueous acyl halide solution may also be used. However, it is important that the acyl halide solution and the aqueous amine solution be substantially immiscible.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Dispersion Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Manufacturing & Machinery (AREA)
• Separation Using Semi-Permeable Membranes (AREA)
• Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)

Priority Applications (5)

Applications Claiming Priority (2)

Publications (2)

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• 2001
  • 2001-10-09 US US09/974,637 patent/US6833073B2/en not_active Expired - Lifetime
• 2002
  • 2002-10-07 DE DE60212670T patent/DE60212670T2/de not_active Expired - Lifetime
  • 2002-10-07 DK DK02799154T patent/DK1434647T3/da active
  • 2002-10-07 WO PCT/US2002/032004 patent/WO2003031036A2/en not_active Ceased
  • 2002-10-07 EP EP02799154A patent/EP1434647B1/en not_active Expired - Lifetime
  • 2002-10-07 JP JP2003534060A patent/JP2005505406A/ja active Pending
  • 2002-10-07 AU AU2002362749A patent/AU2002362749A1/en not_active Abandoned
  • 2002-10-07 ES ES02799154T patent/ES2266623T3/es not_active Expired - Lifetime
  • 2002-10-07 CA CA2463369A patent/CA2463369C/en not_active Expired - Fee Related
  • 2002-10-07 AT AT02799154T patent/ATE330695T1/de not_active IP Right Cessation

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