Classifications

• • 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
  • B01D67/0081—After-treatment of organic or inorganic membranes
  • B01D67/0093—Chemical modification
  • B01D67/00931—Chemical modification by introduction of specific groups after membrane formation, e.g. by grafting
• • 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
  • B01D69/08—Hollow fibre membranes
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2323/00—Details relating to membrane preparation
  • B01D2323/30—Cross-linking

Definitions

• This invention relates to microporous filter membranes, and more particularly to charge modified microporous membranes in the form of hollow tubes suitable for the filtration of aqueous fluids, such as biological liquids, and for plasmapheresis and other cross-flow filtration applications.
• Microporous membranes in both flat sheet and in hollow tube form are well known in the art.
• U.S. Patent No. 3,876,738 to Marinaccio et al (1975) describes a process for preparing a microporous membrane, for example, by quenching a solution of a film forming polymer in a non-solvent system for the polymer.
• European Patent Application 0 005 536 (1979) and U.S. Patent No. 4,340,479 both to Pall describe a similar process.
• microporous membranes for example, made of nylon, are available from Pall Corporation, Glen Cove, New York under the trademark ULTIPOR N 66 .
• Another commercially significant membrane made of polyvinylidene fluoride is available from Millipore Corp., Bedford, Massachusetts under the trademark DURAPORE. This membrane is probably produced by the aforementioned Grandine,II patents. Such membranes are advertised as useful for the sterile filtration of pharmaceuticals, e.g. removal of microorganisms.
• a tighter filter i.e. one with a sufficiently small effective pore dimension to enable the capture of the fine particulate, e.g., microorganisms, by mechanical sieving.
• Such filter structures in the form of microporous membranes of 0.1 micrometer rating or less, may be readily prepared. The flow rate, however, exhibited by such structures at conventional pressure drops is low. Thus such modification of the internal geometry, i.e. pore size, of the microporous membrane is not an economical solution to the problem of bacterial breakthrough.
• Cationically charged membranes which are used for the filtration of anionic particulate contaminants are also known in the art.
• Example charge modified filter membranes are disclosed in the Assignee's Japanese Patent No. 923649 and French Patent No. 7415733.
• an isotropic cellulose mixed ester membrane was treated with a cationic colloidal melamine formaldehyde resin to provide charge functionality.
• the membrane acheived only marginal charge modification.
• the membrane was discolored and embrittled by the treatment, extractables exceeded desirable limits for certain critical applications, and the membrane was not thermally sanitizable or sterilizable.
• Treatment of the nylon membranes prepared by the methods described in U.S. Patent No. 2,783,894 to Lovell (1957) and U.S. Patent No. 3,408,315 to Paine (1968) is suggested.
• Nylon membranes so treated also demonstrate marginal charge modification, high extractables and/or are not thermally sanitizable or sterilizable.
• Cationic charge modified nylon membranes covered by these inventions are now being sold by AMF CUNO Division under the trademark ZETAPOR. Pall Corp., Glen Cove, New York is also selling a cationic charge modified nylon membrane under trademark N 66 POSIDYNE.
• Patents: 4,214,020 to Ward et al (1980) is directed to coating the exteriors of hollow fiber semipermeable membranes.
• the coatings provide the desired selective separation and/or desirable flux.
• the process described in Ward et al involves immersing a bundle of hollow fibers in a coating liquid containing materials suitable for forming the coating and providing a sufficient pressure drop from the exterior of the hollow fiber.
• Material suitable for forming the coating should have a sufficiently large molecular size or particle size so that the material does not readily pass through the pores in the walls of the hollow fibers when subjected to the pressure drop used in the process.
• the pores in the hollow fibers are said to have an average crosssectional diameter less than about 20,000 angstroms, and preferably less than about 1000 to 5000 angstroms.
• Nylon is a material of choice for the hollow fibers.
• the depositable material may be a poly (alkyl acrylates) and poly (alkyl methacrylates) wherein the alkyl groups have,
• 4,250,029 to Kiser et al (1981) is directed to coated membranes having two or more coatings of polyelectrolytes with oppositely charged adjacent pairs separated by a layer of material which substantially prevents charge neutralization.
• the membranes coated are ultrafiltration, reverse osmosis and electrodialysis filtration membranes.
• Preferred membranes are said to be aliphatic and aromatic nylons.
• the anionics useful are said to be polymeric anionic polyelectrolytes of relatively high molecular weight, i.e. above 50,000 preferably above 500,000.
• Kiser et al states that since the anionics are preferably applied as a final coating, after the cationic and on the same side of the membrane as the coatings, there is no essential requirement that the anionic be substantive to the membrane, i.e., the opposite charge of the previously applied cationic coating is sufficient to bind the anionic polyelectrolyte.
• both the cationic and anionic polyelectrolyte coatings are to be applied to the same side of a membrane they may be separated by a nonionic or neutral layer which may be deposited in the same manner as the polyelectrolytes. This neutral layer separates the oppositely charged polyelectrolyte coating preventing neutralization of the charges.
• polyelectrolytes having an anionic charge is poly (acrylic) acid. It is stated, however, that when a coating of cationic material is followed by an anionic layer with little or no neutral layer between the charged layers, the permeation properties of a hollow fiber membrane seems to decrease, as compared to a single layer coating.
• microporous membranes in the form of hollow tubes or fibers capable of capturing charged particulate contaminant of a size smaller than the effective pore size of the membrane.
• the tubes are comprised of a hydrophilic organic polymeric microporous membrane having a microstructure throughout the membrane and a charge modifying amount of a charge modifying agent bonded to substantially all of the membrane microstructure without substantial pore size reduction or pore blockage.
• the preferred microporous filter membrane is nylon.
• the charge modified microporous hollow tube membrane of this invention may be used for the filtration of fluids, particularly parenteral or biological liquids and for cross-flow filtration, e.g. plasmapheresis.
• Figure 1 is a schematic of the system employed in Example
• Figure 2 is a summary plot of the five membranes evaluated in Example IV.
• Figure 3 is a schematic of the system employed in Example
• Figure 4-7 are summary plots for Example V herein.
• the anionic charge modified microporous hollow tube membranes of this invention are produced from organic polymeric microporous membrane. Such membranes are well known in the art.
• microporous filter membrane an asymmetric or symmetric, microporous membrane having a pore size of at least .05 microns or larger, or an initial bubble point (IBP), as that term is used herein, in water of less than 120 psi.
• IBP initial bubble point
• a maximum pore size useful for this invention is about 1.2 micron or an IBP of greater than about 10 psi.
• the membrane has a fine microstructure throughout the membrane.
• symmetrical it is meant that the pore structure is substantially the same on both sides and throughout the membrane.
• asymmetric it is meant that the pore size differs from one surface to the other.
• microporous filter membrane A number of commercially available membranes not encompassed by the term “microporous filter membrane” are those having one side formed with a thin skin which is supported by a much more porous open structure which are typically used for reverse osmosis, ultrafiltration and dialysis. Thus by the use of the term “microporous filter membrane” it is meant membranes suitable for the removal of suspended solids and particulates from fluids which permit dissolved solids to pass therethrough. These membranes, however, may have other uses both known and unknown.
• hydrophilic in describing the preformed and the charge modified microporous membrane of this invention, it is meant a membrane which adsorbs or absorbs water. Generally, such hydrophilicity is produced by a sufficient amount of hydroxyl (OH-), carboxyl (-COOH), amino (-NH 2 ) and/or similar functional groups on the surface of the membrane. Such groups assist in the adsorption and/or absorption of water onto the membrane.
• Such hydrophilicity of the membrane and internal microstructure (which may be obtained or enhanced by treatment of the preformed membrane) is a necessary element for the preformed membrane which is treated in order to provide the adequate inclusion of the charge modifying agent to the microporous membrane internal microstructure. Such hydrophilicity of the membrane of this invention is necessary in order to render the membrane more useful for the filtration of aqueous fluids.
• a preferred microporous filter membrane is one produced from nylon.
• nylon is intended to embrace film forming polyamide resins including copolymers and terpolymers which include the recurring amido grouping. While, generally, the various nylon or polyamide resins are all copolymers of a diamine and a dicarboxylic acid, or homopolymers of a lactam or an amino acid, they vary widely in crystallinity or solid structure, melting point, and other physical properties.
• Preferred nylons for use in this invention are copolymers of hexamethylene diamine and adipic acid and homopolymers of polyo-caprolactam.
• these preferred polyamide resins have a ratio of methylene (CH 2 ) to amide (NHCO) groups within the range about 5:1 to about 8:1, most preferably about 5:1 to about 7:1.
• the preferred nylon 6 and nylon 66 each have a ratio of 6:1, whereas nylon 610 has a ratio of 8:1.
• nylon polymers are available in a wide variety of grades, which vary appreciably with respect to molecular weight, within the range from about 15,000 to about 42,000 and in other characteristics.
• the highly preferred species of the units comprising the polymer chain is polyhexamethylene adipamide, ue. nylon 66, and molecular weights in the range above about 30,000 are preferred. Polymers free of additives are generally preferred, but the addition of antioxidants or similar additives may have benefit under some conditions.
• the preferred membrane substrates are produced by the method disclosed in U.S. Patent No. 3,876,738 to Marinaccio et al. Another similar method of producing such membranes is described in European Patent Application No. 0 005 536 and U.S. Patent No. 4,340,479 to Pall. The entire disclosures of all of these references are incorporated herein by reference.
• Marinaccio et al produces microporous films by casting or extruding a solution of a film-forming polymer in a solvent system into a quenching bath comprised of a non- solvent system for the polymer.
• the non-solvent system may comprise only a non-solvent, the solvent system may consist of any combination of materials provided the resultant non-solvent system is capable of setting a film and is not deleterious to the formed film.
• the non-solvent system may consist of materials such as water/salt, alcohol/salt or other solvent-chemical mixtures.
• the Marinaccio et al process is especially effective for producing nylon microporous hollow tubes. More specifically, the general steps of the process involve first forming a solution of the film-forming polymer, casting the solution to form a hollow tube and quenching the tube in a bath which includes a non-solvent for the polymer.
• nylon solutions which can be used in the Marinaccio et al process include solutions of certain nylons in various solvents, such as lower alkanols, e.g., methanol, ethanol and butanol, including mixtures thereof. It is known that other nylons will dissolve in solutions of acids in which it behaves as a polyelectrolyte and such solutions are useful.
• Representative acids include, for example, formic acid, citric acid, acetic acid, maleic acid and similar acids which react with nylons through protonation of nitrogen in the amide group characteristic of nylon.
• the nylon solutions are diluted with non-solvent for nylon, the non-solvent employed being miscible with the nylon solution. Dilution with non-solvent may, according to Marinaccio et al, be effected up to the point of incipient precipitation of the nylon.
• the non-solvents are selected on the basis of the nylon solvent utilized. For example, when water-miscible nylon solvents are employed, water can be employed. Generally, the non-solvents can be methyl formate, aqueous lower alcohols, such as methanol and ethanol, polyols such as glycerol, gycols, polyglycols, and ethers and esters thereof, water and mixtures of such compounds. Moreover, salts can also be used to control solution properties.
• the quenching bath may or may not be comprised of the same non-solvent selected for preparation of the nylon solution and may also contain small amounts of the solvent employed in the nylon solution. However, the ratio of solvent to non-solvent is lower in the quenching bath than in the polymer solution in order that the desired result be obtained.
• the quenching bath may also include other nonsolvents, e.g., water.
• the formation of the polymer hollow tubes can be accomplished by any of the recognized methods familiar to the art.
• hollow tubes are formed by extrusion over a fluid core and quenching in an appropriate bath using appropriately designed and shaped nozzles.
• the wall thickness will be cast at thickness in the range of from about 1 mil. to about 20 mils., preferably from about 1 to about 10 mils.
• the polymer solution is cast and simultaneously quenched, although it may be desirable to pass the cast tube through a short air evaporation zone prior to the quench bath. This latter technique is, however, not preferred.
• the tube is removed from the quench bath and preferably washed free of solvent and or non-solvent. Subsequently the tube can be at least partially dried and then charged modified.
• Pall's aforementioned European Patent Application No. 0 005 536 and U.S. Patent No. 4,340,479 describe a similar method for the conversion of polymer into microporous membrane. This process may be appropriately modified to produce hollow tubes.
• Pall provides a process for preparing skinless hydrophilic alcohol-insoluble polyamide membranes by preparing a solution of an alcohol-insoluble polyamide resin in a polyamide solvent. Nucleation of the solution is induced by the controlled addition to the solution of a non-solvent for the polyamide resin, under controlled conditions of concentration, temperature, addition rate, and degree of agitation to obtain a visible precipitate of polyamide resin particles (which may or may not partially or completely redissolve) thereby forming a casting solution.
• the casting solution is cast and then contacted and diluted with a mixture of solvent and non-solvent liquids containing a substantial proportion of the solvent liquid, but less than the proportion in the casting solution, thereby precipitating polyamide resin from the casting solution in the form of a thin skinless hydrophilic membrane.
• the resulting membrane is then washed and dried.
• the solvent for the polyamide resin solution is formic acid and the non-solvent is water.
• the polyamide resin solution film is contacted with the nonsolvent by immersing the film, carried on the substrate, in a bath of non-solvent comprising of water containing a substantial proportion of formic acid.
• nylon membranes i.e. described in Marinaccio et al and Pall, are characterized by a hydrophilic, isotropic structure, having a high effective surface area and a fine internal microstructure of controlled pore dimensions with narrow pore size distribution and adequate pore volume throughout the membrane structure.
• a representative 0.22 micrometer rated nylon 66 membrane polyhexamethylene adipamide
• FOP foam all over point
• FOP foam all over point
• the charge modifying agent i.e. anionic or cationic charge modifying agent
• bound it is meant that the charge modifying agent is sufficiently attached to or incorporated into the membrane so that it will not significantly extract under the intended conditions of use.
• substantially all of the internal microstructure as used herein it is meant substantially all of the external surface and internal pore surfaces. Typically this is meant the surfaces which are wetted by a fluid, e.g., water, passing through the membrane or in which the membrane is immersed.
• charge modifying agent a compound or composition that when bound to the microporous filter membrane alters the "zeta potential" of the membrane (see Knight et al, “Measuring the Electrokinetic Properties of Charged Filter Media,” Filtration and Separation, pp30-34, Jan./Feb. 1981).
• the charge modifying agent can be part of the solvent-non-solvent casting system and/or quench bath or a subsequent treatment to the formed membrane.
• the anionic or cationic charge modifying agent is a compound or composition which is capable of bonding to the membrane microstructure without substantial pore size reduction or pore blockage and provides an anionic or cationic charge or negative or positive zeta potential to the membrane microstructure.
• anionic or cationic charge modifier is a water soluble compound having substituents capable of binding to the membrane and substituents which are capable of producing a more negative or more positive "zeta potential" in the use environment (e.g. aqueous) or anionic functional groups.
• Preferred anionic functional groups may be carboxyl, phosphonous, phosphonic and sulfonic.
• the anionic charge modifying agent may be a water soluble organic polymer having a molecular weight greater than about 2,000 and less than about 500,000 and capable of of becoming a non-extractable constituent of the membrane.
• the anionic charge modifying agent can also be crosslinked to the membrane through a cross-linking agent, for example, an aliphatic polyepoxide having a molecular weight of less than about 500 and preferably methylated urea formaldehyde resin and melamine formaldehyde.
• a cross-linking agent for example, an aliphatic polyepoxide having a molecular weight of less than about 500 and preferably methylated urea formaldehyde resin and melamine formaldehyde.
• the anionic charge modifying agents which may be used in this invention are polymeric anionic polyelectrolytes. Generally, these polyelectrolytes have relatively low molecular weight, e.g. less than 500,000, and are water or other solvent soluble at the desired levels of application. If the anionic agents are applied directly to the membrane it is necessary that they be capable of binding thereto. If they are applied to a cationically charge modified membrane (discussed below), they need only bond to the cationic charge on the membrane.
• the anionic charge modifying agent may have either a high or low charge density, or anything between these extremes, however, high charge density is preferred.
• Specific preferred anionic charge modifying agents useful herein are poly (styrene sulfonic) acid, poly (toluene sulfonic) acid, poly (vinyl sulfonic) acid and poly (acrylic) acid.
• Other anionic charge modifying agents are poly (methacrylic acid), poly (itaconic acid), hydrolyzed poly (styrene/maleic anhydride) and poly (vinyl phosphonic acid). Additionally, the alkali and alkaline earth metal salts of all of the foregoing may be utilized.
• Highly preferred anionic charge modifying agents are poly (styrene sulfonic) acids:
• the anionic charge modifying agent may also be crosslinked to the microporous membrane structure through an aliphatic polyepoxide cross-linking agent having a molecular weight of less than about 500.
• the polyepoxide is a di- or tri-epoxide having a molecular weight of from about 146 to about 300.
• Such polyepoxides have viscosities (undiluted) of less than about 200 centipoise at 25C.
• R is an alkly of 1 to 6 carbon atoms and n is from 2 to 3.
• the limitation that the number of carbon atoms in the non-epoxide portion — (R) — be less than 6 is so that the polyepoxide will be soluble in water or ethanol-water mixtures, e.g. up to 20% ethanol. While higher carbon content materials are functionally suitable, their application would involve the use of polar organic solvents with resulting problems in toxicity, flammability and vapor emissions.
• Triglycidyl ethers i.e. tri-epoxides may also be utilized as the polyepoxide cross-linking agent.
• the triglycidyl ether of glycerol may be utilized.
• These tri-epoxides have the following formula: The triglycidyl ether of glycerol is available from Shell, Inc. as Epon
• Another preferred cross-linking agent is methylated urea formaldehyde resin, commercially available from American Cyanamid; for example, Beetle 65, and melamine formaldehyde, e.g., Cymel 303 from American Cyanamide.
• the anionic charge modifying agent may be applied to a membrane which has been previously treated to produce a hydrophilic cationic charge modified membrane.
• a membrane which has been previously treated to produce a hydrophilic cationic charge modified membrane.
• Preferred membranes and methods of producing such cationic charge modified membranes are described in Assignees aforementioned applications and European publications to Barnes et al (USSN 268,543 and EPC 066814) and Ostreicher et al (USSN 314,307 and EPC 0050 864). The entire disclosures of these applications and publications are incorporated herein by reference.
• Treating a cationically charge modified membrane in accordance with this invention enhances the bonding of the anionic charge modifier to the membrane and/or reduces the requirements for a cross-linking agent.
• the process for anionically charge modifying a hydrophilic organic polymeric microporous membrane, e.g. nylon comprises applying and binding to substantially all of the membrane microstructure, without substantial pore size reduction or pore blockage, a charge modifying amount of the anionic charge modifying agent.
• the process comprises (a) contacting the membrane, i.e. hollow tubes with an aqueous solution of the anionic charge modifying agent; and (optionally) (b) contacting the membrane with an aqueous solution of the cross-linking agent.
• the contacting steps may be performed in any order, i.e. step (a) followed by step (b), vice versa or simultaneously. It is preferred, to perform steps (a) and
• the aqueous solution of anionic charge modifying agent that the membrane is contacted with contain at least about .5% by weight charge modifying agent in the aqueous solution.
• the upper range is limited by economic and solubility limitations. For example, an excess of charge modifying agent which is not bonded to the microporous membrane will not be economically utilized and will constitute an undesirable extractive from the membrane. It has been found that the amount of charge modifying agent in the aqueous solution should not exceed about 10% by weight of the solution.
• the amount of cross-linking agent used in the aqueous solution is highly dependent on the specific cross-linking agent and the amount and type anionic charge modifying agent used, and the crosslinking mechanism between these compounds to provide the bonding of such charge modifying agent to the microporous membrane.
• a weight ratio of anionic charge modifying agent to cross-linking agent of from about 1:1 to about 500:1, preferably from about 1:1 to about 20:1 in the aqueous solutions contacted with the membrane, is generally sufficient to provide the binding of the anionic charge modifying agent to the membrane.
• the aqueous solution containing the cross-linking agent contains at least about .1% cross-linking agent by weight of the solution, up to a maximum of about 5% weight of the solution when used in conjunction with the aforementioned aqueous solution of anionic charge modifying agent, that adequate bonding of the charge modifying agent to the microporous membrane is obtained.
• Both the anionic charge modifying agent and the crosslinking agent may be contacted with the membranes hollow tube by dipping the tubes in the aqueous solutions of these compounds for a period of time sufficient to effect the desired degree of pick-up.
• the agents may be applied by spraying or contacting a wick or roll along the surface of the microporous membrane which almost immediately adsorbs and/or absorbs the aqueous solution due to the membrane's hydrophilicity.
• the preferred cationic charges membranes used in this invention are described in the aforementioned Barnes et al and Ostreicher et al publications and applications.
• the preferred charge modifying agent described in Ostreicher et al is a water-soluble organic polymer having a molecular weight greater than about 1,000, wherein the monomer has at least one epoxide substituent capable of bonding to the surface of the membrane and at least one tertiary amine or quaternary ammonium grbup capable of providing a cationic charge site.
• this charge modifier is a polyamido-polyamine epichlorohydrin cationic resin, in particular, those described in the following U.S. patents:
• the preferred polyamido-polyamine epichlorohydrin cationic resins are available commercially as Polycup 172, 1884, 2002 or S 2064 (Hercules); Cascamide Resin pR-420 (Borden); or Nopcobond 35 (Nopco).
• the polyamido-polyamine epichlorohydrin resin is Hercules R 4308, wherein the charged nitrogen atom forms part of a heterocyclic grouping, and is bonded through a methyiene moiety to a depending, reactive epoxide group.
• a secondary charge modifying agent can be used to enhance the cationic modifying agent and/or enhance the bonding of the primary charge modifying agent to the microporous surface and/or itself.
• the secondary charge modifying agent used in this invention is selected from the group consisting of:
• the secondary charge modifying agent is a polyamine having the formula:
• R 1 and R 2 are alkyl of 1 to 4 carbon atoms and x is an integer from 0 to 4.
• R 1 and R 2 are both ethyl.
• Preferred polyamines are: Ethylene diamine H 2 N-(CH 2 ) 2 -NH 2
• the highly preferred polyamine is tetraethylene pentamine.
• aliphatic amines used in this invention may have at least one secondary amine moiety and a carboxyl or hydroxyl substituent.
• exemplary of such aliphatic amines are gamma aminobutyric acid (H 2 NCH 2 CH 2 CH 2 COOH) and 2-aminoethanol
• the secondary charge modifying agent is bonded to the microporous membrane by bonding to a portion of the epoxide substituents of the polymeric primary charge modifying agent.
• the amount of primary and secondary cationic charge modifying agent utilized is an amount sufficient to enhance the electropositive capture potential of the microporous membrane. Such an amount is highly dependent on the specific charge modifying agents utilized.
• the foregoing primary and secondary cationically charge modifying agents are bonded to a hydrophilic organic polymeric microporous membrane, e.g., nylon, by applying to the membrane a charge modifying amount of the primary cationic charge modifying agent bonded to the membrane structure through the epoxide substituent.
• the process comprises (a) contacting the membrane i.e., hollow tube, with an aqueous solution of the primary cationic charge modifying agent and (b) contacting the membrane with an aqueous solution of the secondary charge modifying agent.
• the contacting steps may be performed in any order, i.e., step (a) prior to step (b) or vice-versa. It is preferred, however, for optimum (minimum) extractables to first contact the membrane with an aqueous solution of the primary cationic charge modifying and then subsequently contact the so treated membrane with the aqueous solution of the secondary charge modifying agent.
• the foregoing secondary charge modifying agent can be used as the charge modifying agent provided it is bonded to the microporous membrane structure through the af oredescribed aliphatic poly-epoxide crosslinking agents used to produce the aforedescribed anionically modified membrane.
• the aliphatic polyamine charge modifying agent can be bonded to the microporous membrane by (a) contacting the membrane with an aqueous solution of the cationic charge modifying agent and (b) contacting the membrane with an aqueous solution of the polyepoxide crosslinking agent.
• the contacting steps may be performed in any order, i.e., step (a) prior to step (b) or vice-versa.
• Such contacting steps also include contacting the membrane with an aqueous solution of a mixture of the charge modifying agent and the polyepoxide crosslinking agent.
• the membrane is drained for a period of time sufficient to remove most of the water and chemical compound(s) not absorbed or adsorbed onto the surface of the membrane.
• the membrane may be transferred directly from the first contacting step to a subsequent contacting step, although this is less preferred.
• microporous membrane After the microporous membrane has been contacted with the aqueous solution(s), it may then be washed, dried and cured.
• the final drying and curing temperature for the filtration membrane should be sufficient to dry and cure the membranes. Preferably this temperature is from about 120oC to 140oC for minimization of drying time without embrittlement or other detrimental effects to the membranes.
• the total thickness of the filtration membrane is preferably from about 3 mils to about 30 mils and most preferably about 3 to 15 mils thick (dry thickness).
• the filtration membrane i.e. hollow tubes may then be rolled and stored under ambient conditions for further processing into the usual commercial forms, for example, cartridges by methods well known to the art.
• the present invention provides an charge modified microporous hollow tubes having integral, coherent hydrophilic microporous membrane wall of retained internal pore geometry.
• the charge modified membrane has an improved effective filtration rating relative to the untreated micro-reticulate polymer oppositely charged structure for cationic submicronic particulate contaminants and has a decreased adsorptive capacity for like charged submicronic particulate, such particulates often being desirably retained in the liquid to be filtered, as for example, in cross-flow filtration a contaminant particulate that can cause pore blockage of the membrane.
• These properties are brought about by charge sites or regions attached to, bonded to or populating the microstructure or pore surfaces throughout the membrane.
• charge sites are effective over a broad range of pH's in enhancing filtration performance through eletrokinetic effects.
• the choice of charge modifying agent, cross-linking agent and process conditions assures that the foregoing is accomplished without substantial pore size reduction or pore blockage.
• the resulting charge modified membrane offers improved micrometer rating, for oppositely charged submicronic particulate, at equivalent flow and capacity with retention of membrane structure, yet without evidence of significant resin extractables, and improved cross-flow filtration effectiveness, particularly in plasmapheresis.
• the effective micrometer rating for oppositely charged contaminant particles is less than the effective micrometer rating of the microreticulate membrane structure, but not for similarly charged particulate. Adsorption of critical or required anionic particulate or consistituents is minimized or eliminated.
• effective micrometer rating for contaminant particles it is meant the actual size of the particles that the membrane will quantitatively remove from the fluid being filtered.
• effective micrometer rating of the microreticulate membrane structure it is meant the size of the particulate that would pass through the membrane if all adsorptive effects of the membrane were eliminated.
• the filter is sanitized or sterilized by autoclaving or hot water flushing.
• Preparation for use in sterile filtration requires that the membrane be sterilized as by treatment in an autoclave at 121oC under 15 psig. for 1 hour. Accordingly, the charge modified membrane must be resistant to this type treatment, and must retain its integrity in use. Any modification to the filter structure, especially brought about by chemical agents which may be unstable under conditions of treatment and use, must be scrutinized with care to minimize the prospect of extractables contaminating the filtrate, interfering with analysed and potentially introducing harmful toxins to a patient.
• any such filter must meet the test standards in the industry, e.g. ASTM D 3861-79 (incorporated herein by reference), and generally have less than 5 mg. of extractables in 250 ml solvent (water at 80°C.; 35% ethanol at room temperature) for a 293 mm diameter disc.
• the membrane and process of this invention insures low extraction levels.
• the resulting charge modified membrane is characterized by retention of internal microstructure, thus offering essentially the same flow characteristics as the untreated membrane.
• the charge modified microporous hollow tube membranes additionally are to handle and readily formed into cartridges. By reason of its retained flow characteristics, it may be employed directly into existing installations without pumping modifications. These favorable properties are secured without sacrifice to other characteristics.
• the membrane may also be constructed to meet or exceed extractable requirements.
• Biological liquids as that term is employed in the specification and claims, is a liquid system which is derived from or amenable to use with living organisms. Such liquids are ordinarily handled and processed under sanitary or sterile conditions and therefore require sanitized or sterilized media for filtration. Included within such term are isotonic solutions for intermuscular (im) or intravenous (iv) administration, solutions designed for administration per os, as well as solutions for topical use, biological wastes or other biological fluids which may contain cationic impurities, e.g., asbestos, alkali metal hydroxides or other cationic contaminants which are desirably isolated or separated for examination or disposal by immobilization or fixation upon or entrapment within a filter media. This can be accomplished with a minimum of removal or adsorption of desirable anionic particulates.
• isotonic solutions for intermuscular (im) or intravenous (iv) administration solutions designed for administration per os, as well as solutions for topical use
• Hollow tube filter membranes in accordance with this invention may be employed alone or in combination with other filter media to treat pharmaceuticals such as antibodies, saline solutions, dextrose solutions, vaccines, blood plasma, serums, sterile water or eye washes; beverages, such as cordials, gin, vodka, beer, scotch, whisky, sweet and dry wines, champagne or brandy; cosmetics such as mouthwash, perfume, shampoo, hair tonic, face cream or shaving lotion; food products such as vinegar, vegetable oils; chemicals such as antiseptics, insecticides, photographic solutions, electroplating solutions, cleaning compounds, solvent purification and lubrication oils, and the like.
• the hollow microporous tubes are also suitable for plasmapheresis, amd more broadly for cross-flow filtration.
• cross-flow filtration it is meant the separation of undissolved particulate and suspended solids from a fluid, e.g., liquid, blood, mixture by passing or circulating, parallel or tangential to the surface of the membrane the fluid mixture producing a circulating effluent of concentrated particles or solids continuing to flow tangential to the membrane.
• a fluid e.g., liquid, blood
• Such techniques are well known in the art, particularly for plasmapheresis. It is believed that the charge on the membrane prevents the similarly charged particulate or suspended solids in the fluid from clogging of blocking the pores by preventing excessive adsorption thereof, thus enhancing the efficiency and effectiveness of filtration.
• Thickness The dry membrane thickness was measured with a 1 inch (1.27 cm) diameter platen dial thickness gauge. Gauge accuracy was +0.00005 inches (+.05 mils).
• IBP Initial Bubble Point
• FAOP Foam-All-Over Point
• a 47 mm diameter disc of the membrane sample is placed in a special test holder which seals the edge of the disc.
• a perforated stainless steel support screen Above the membrane and directly in contact with its upper face, is a perforated stainless steel support screen which prevents the membrane from deforming or rupturing when air pressure is applied to its bottom face.
• the holder Above the membrane and support screen, the holder provides an inch deep capacity into which distilled water is introduced.
• a regulated air pressure is increased until a first stream of air bubbles is emitted by the water wetted membrane into the quiescent pool of water.
• the air pressure at which this first stream of air bubbles is emitted is called the Initial Bubble Point (IBP) of the largest pore in that membrane sample - see ASTM F-316-70 which is incorporated herein by reference.
• IBP Initial Bubble Point
• the air pressure is further increased until the air flow through the wetted membrane sample, as measured by a flow meter in the line between the regulator and the sample holder, reaches 1000 cc/min.
• the air pressure at this flow rate is called the Foam-AllOver-Point (FAOP), and is directly proportional to the mean pore diameter of the sample membrane.
• FAOP Foam-AllOver-Point
• a 47 mm diameter disc of the membrane sample is placed in a test housing which allows pressurized water to flow through the membrane. Prefiltered water is passed through the membrane sample at a pressure differential of 5 psid. A graduated cylinder is used to measure the volume of water passed by the membrane sample in a one minute period. In this series of tests this parameter is used in conjunction with the IBP and FAOP to determine if any reduction in pore size or pore blockage has occurred as a result of the anionic charge modifying process utilized.
• a 47 mm diameter disc of the membrane sample is placed in a test housing which allows pressurized water to flow thru the membrane.
• the challenge solution consists of distilled water at a pH of 7.0, and methyiene blue dye.
• the dye inlet concentration is adjusted to produce a 34 percent transmittance at a wavelength of 660 nm, as measured on a Bausch & Lomb Spectronic 710 Spectrophotometer.
• a peristaltic pump the challenge solution is flowed thru the membrane sample at a flow rate of 28 ml/min.
• the transmittance of the effluent is measured by passing it thru a constant flow cell in the aforementioned spectrophotometer.
• the effluent transmittance and pressure drop across the membrane is measured and recorded as a function of time.
• the test is terminated when the effluent transmittance increases to 45 percent of the inlet transmittance.
• the length of time that it takes to reach the 45 percent transmittance in the effluent is called the "breakthru" time. Since methyiene blue is a low molecular weight cationic dye incapable of being mechanically removed (filtered) by the membrane, this breakthru time is proportional to the anionic adsorptive capacity of the membrane sample. This test is therefore used to determine the effectiveness of the charge modification technique.
• Extractables are determined by ASTM D-3861-79.
• the quantity of water-soluble extractables present in membrane filters is determined by immersing a preweighed membrane in boiling reagent grade water for an extended time and then drying and reweighing the membrane.
• a control membrane is employed to eliminate weighing errors caused by balance changes or changing moisture content of the membrane in the weighing procedures. Weight changes of the control membrane are applied as a correction factor to the weight change of the test membrane filters.
• a representative nylon 66 membrane of 0.22 micrometer nominal rating, having a nominal surface area of about 13 m 2 /g, an Initial Bubble Point of about 47 psi, a Foam-All-Over-Point of about 52 psi was prepared by the method of Marinaccio et al, U.S. Patent 3,876,738, utilizing a dope composition of 16 percent by weight nylon 66 (Monsanto Vydyne 66B), 7.1% methanol and 76.9% formic acid, a quench bath composition of 25% methanol, 75% water by volume (regenerated as required by the method of Knight et al, U.S.
• Patent 3,928,5157 a casting speed of 24 inches/minute (61 cm/min.), and a quench bath temperature of 20oC.
• the membrane was cast just under the surface of the quench bath by application to a casting drum rotating in the bath (9 to 10 mils as cast wet, to obtain 4.5 to 5.5 mils dry) and allowed to separate from the drum about 90° of arc from the point of application.
• a portion of the uniform opaque film was dried (in restrained condition to resist shrinkage) in a forced air oven at 8090oC for 30 minutes.
• the casting solution was twenty-six percent solids and had a viscosity of about 90,000 cp.
• the casting solution was made by combining 40 gm methanol (99.5% Dupont Technical Grade) with 2180 gm formic acid (98% Union Carbide, glacial) in a one gallon glass jar which was allowed to stand at least two hours at room temperature.
• the standard quench system consisted of 25 percent methanol in 75 percent D.L water, by volume. The same quench fluid was used inside as well as outside the hollow fiber. The quench fluid was recirculated at about two gallons per minute by a 316 stainless steel centrifugal pump and was filtered through a five micron polypropylene Microwynd cartridge (AMF Cuno). III Fiber Casting
• the casting operation was done at four to six feet per minute with the extrusion die oriented vertically downward. Dwell time in the quench bath was at least 20 to 30 seconds.
• the die plate was 316 stainless steel with an orifice of 40 mils and a land length of about 0.125 inch.
• Quench fluid was delivered at a rate of about 0.2 ml/min to the center of the hollow fiber by means of a number 26 hypodermic needle (18 mils OD x 10 mils ID) positioned so that the end of the needle was flush with the outer face of the die plate.
• dope to the extrusion die was accomplished from a stainless steel reservoir of 500 ml capacity, pressurized to about 80 psi. Another reservoir was used for the center quench fluid and was pressurized to 20 to 60 psi. Control of the dope flow was achieved by changing reservoir pressure, while the center quench flow was controlled by a rotameter equipped with a vernier valve. The center quench fluid was filtered through a five micron polypropylene MICROWYND cartridge. The casting solution was not filtered.
• the porous hollow fiber was wound on a 3.5 inch OD PVC core four inches long.
• a level wind apparatus distributed the fiber uniformly over the core surface and left a relatively open winding pattern which enhanced wash fluid circulation in a subsequent step.
• the windup was capable of handling fiber production of up to 25 feet per minute.
• a constant speed nip roll positioned just before the windup further improved the windup system.
• Washing was accomplished by putting the fiber wound on take-up spools into a laboratory pipette washer connected to a source of room temperature D.L water.
• a typical wash cycle entailed a total of 20 fill and empty cycles over a period of about 60 minutes and used a total of about 80 gallons of wash water.
• Fiber IBP and FAOP were measured by potting one end of a dry fiber about four inches long into a 3/8 inch OD polyolefin tubing, using one of several available polyur ethane potting compounds. After the urethane was cured, the potted section was sliced through with a knife blade and the fiber OD and ID were measured under a 40 power microscope fitted with an eyepiece scale. The other end of the fiber was closed off with a blob of hot melt adhesive and the potted tubing end was fitted to a source of pressurized air and a pressure gauge. The porous fiber was immersed in water and the IBP and FAOP was noted as the air pressure applied to the potted tube end was slowly increased.
• a similar test module was used for measuring flow through the fiber walls, only in this case ten or twenty fibers each about six inches long were bundled together.
• a Masterflex pump was used to pump D.I. water through the fiber walls, with pressure and flow measured by a mercury manometer and rotameter, respectively.
• the characteristic, K, of the fibers was then calculated from the relationship:
• the first cartridge had 600 fibers with an LD. of 19.6 mils, O.D. of 30 mils and length of 7.68 inches. Approximate pore size was 0.6 microns.
• the measured flow rate of the cartridge was 637 ml/min with 0.5 psi outside pressure. This is equal to a flow of 1.7 gpm for a 5 ft 2 unit (about 1500 fibers).
• the second cartridge had about 1062 fibers of 17.5 mil LD., 31 mil O.D., 7.68 inches in length. Approximate pore size of 0.2u with flow rate of 730 ml/min at 0.6 psi external pressure. This is equivalent to a flow of 1.8 gpm for a 5 ft 2 cartridge at 3.6 psi applied pressure.
• MICROPOROUS FIBER CARTRIDGE (8105-50 - Untreated) A. Fiber Characterists
• the double layer of membrane was introduced into a 1.25% by weight solution of Hercules R4308.
• the pH of the bath was 10.5
• This bath was produced by diluting 38lbs. (17.17 Kg.) of Hercules R4308 resin from its initial 20% by weight concentration to 5%. Five normal (5N) sodium hydroxide solution was then added to raise the pH to 10.5. The solution was then diluted with D.I. water having greater than 150,000 ohm-cm resistivity in a ratio (volume) 2.5:1. The total volume of bath solution was 60 gallons.
• the membrane Upon exiting this bath, the membrane was wiped on the bottom surface to remove excess water. A 3 minute air soak with cool air movement was used before the membrane entered the secondary charge modifying agent bath.
• This bath was produced by adding 0.023% tetraethylene pentamine by weight or .113 lbs. (.0513 kg) to 60 gallons (227. liters) of D.I. water (at least 150,000 ohm -cm resistivity). The pH was about 9. The immersion conditions are identical to the first bath of primary charge modifying agent. The membrane was then wrapped around a take up roll.
• the membrane was then washed in a subsequent operation and checked for extraction levels.
• nylon membrane including hollow tubes, was treated with a water solution of charge modifying agent and, where indicated, a cross-linking agent. Since solubility of some cross-linking agents in water is limited, the agent was first diluted in alcohol and then mixed with the aqueous solution of anionic charge modifying agent. The membrane was drained, washed and dried in an oven at from 100oC to 125oC for 15-20 minutes. The membrane was then washed. The treatments and test results are tabulated on the attached Table 1.
• PSSA polystyrene sulfonic acid
• EGDGE is ethylene glycol diglycidyl ether (POLYSCIENCE).
• PAA polyacrylic acid (GOOD-RITE K702, 722, 732, 752, GOODRICH):
• Pluronic is a polyol (BASF WYANDOTTE).
• 4308 is polyamido - polyamine epichlorohydrin resin (POLYCUP, HERCULES).
• TEPA is tetraethylene pentamine (UNION CARBIDE): H 2 N(CH 2 ) 2 NH(CH 2 ) 2 NH(CH 2 ) 2 NH(CH 2 ) 2 NH 2 9.
• C-303 is hexa methoxy-methyl melamine resin (CYMEL 303, AMERICAN CYANAMID).
• C-35201 is water borne epoxy resin (CMD 35201, CELANESE).
• B-65 is methylated urea formaldehyde resin (BEETLE 65,
• Example 24 0.45 micron anionic (Sample 24) or 0.45 micron cationic (Example II) and 0.2 micron untreated (Example I), were evaluated for the separation of plasma and cellular components of blood.
• the test criteria is the rate of hemoglobin appearance into the plasma phase vs. the filtration rate.
• the test procedure and results are described below.
• the 0.2 micron untreated membrane gave the best results, however, the charged modified 0.45 micron membranes performed better than the untreated 0.45 micron membrane.
• Four membranes (0.45 micron untreated, 0.45 micron anionic, 0.45 micron cationic, and 0.2 micron untreated) were presented for comparison with the membrane employed most frequently in prior studies with this system, SARTORIUS 0.45 micron cellulose nitrate.
• a modified SARTORIUS membrane cell is assembled with three 16 x
• Plasma 250 ml is circulated over the membranes as a pretreatment. Approximately 300 ml of whole human blood (drawn no more than 3 hours prior to the run) is added to a beaker containing 500 IU of heparin. The blood pump is started and set to read "10" on the speed meter (about 38 ml/min).
• the filtration rate is measured by diverting the filtrate into a graduated cylinder and samples of filtrate and blood are taken for analysis.
• the blood pump speed meter reading is incremental by 5 and the procedure is repeated until two obviously pink/red samples have been obtained.
• Filtrate samples are analyzed for hemoglobin (Hgb) by spectrophotometric techniques. Blood samples are analyzed for hematocrit, and plasma and total Hgb by a Coulter counter. One sample each of blood and filtrate is selected for protein electrophoresis.
• Hgb hemoglobin
• the optimally functioning primary separation unit of a plasmapheresis system must be capable of producing the greatest flow of plasma with the least damage to the cellular blood components.
• Q F must be maximized while holding D to some arbitrarily acceptable value.
• the evaluation of the five membranes tested can most readily be peformed in this manner from a plot of the Hgb appearance rate, D, as a function of the filtrate rate, Q, shown in Figure 2. The curve furthest to the lower right will specify the membrane of choice, based on the above stated criteria. Clearly, the 0.2u untreated membrane gave the best results. At the Hgb appearance rate 1.5 mg/min, this test produced 9.3 ml/min of filtrate.
• the second best performer the 0.45u negative gave 74 percent (6.9 ml/min) of this value for the same criterion.
• the control membrane (Satorius 0.45u cellulose nitrate) produced only 4.6 ml/min or 49 percent as much filtrate as did the 0.2u.
• the present evaluation involves six hollow fiber modules: two each of the unmodified fiber, anionic (negative) surface modified, and cationic (positive) surface modified.
• the anionic fibers were prepared pursuant to Sample 29 (C8-30-2).
• the cationic fibers were treated in a manner similar to Example H (C-8-31-1)
• FIG. 3 The system employed in these studies is shown in Figure 3. It consists of a Travenol Laboratories roller-type blood pump (used on the Travenol RSP hemodialyzer), clot filter, 0-760 mm Hg pressure gauge, Swagelok fittings for connection to the hollow fiber module,
• Manostat Calcuflow flow meter and fluid reservoir with stirrer.
• the apparatus is assembled with the desired test module oriented vertically (with flow from top to bottom) and 250 ml of human plasma is added to the reservoir beaker.
• the plasma is circulated through the system for 15 minutes at approximately 100 ml/min. This allows for leak checks and for deposition of plasma proteins on rough or otherwise biologically reactive surfaces.
• Pretreatment of the system in this manner has been shown to decrease the degree of hemolysis that occurs on the initial contact of the blood with the membrane.
• the pump is stopped and the pump inlet line is transferred to a second reservoir beaker containing 250-300 ml of fresh human blood and 500 IU of heparin.
• An initial blood sample is taken from the beaker.
• the pump is restarted and the module and filtrate outlet lines are moved to the blood beaker when the first evidence of blood leaving the module is noted. Timing of the run begins at this point.
• the remainder of the test is divided into intervals of ten minutes each. At the midpoint of each interval, the inlet pressure and filtration rate are recorded. At the end of each interval, a filtrate sample is taken for analysis. Each sample is immediately centrifuged and the plasma is separated from any cells or fragments that are present. This will lessen the likelihood of falsely high plasma hemoglobin values. The pump is incremented and the next interval begins. At the end of the test, a blood sample is taken from the beaker to provide a check on the mass balance.
• Hgb appearance rate D has been corrected for the hemolysis effects of the blood pump and other hardware and represent only the effects produced by the test module. It should be noted that blood leaks into the filtrate were a significant problem with three of the surface modified fiber modules: 8207-2 (anionic), 8207-5 (cationic) and 8207-6 (cationic). In the test of module 8207-2 (anionic) the leak was so severe that it was difficult to distinguish between the fluid in the filtrate and blood outlet lines until the samples had been centrifuged. Normally, the filtrate has the appearance of plasma with slight brown or pink coloration. The extent to which this leakage affected the results is unknown.
• Figure 4 presents the filtration rate for each module as a function of the blood inflow rate.
• the surface modified fibers produced greater filtration rates for a given blood flow rate than did the unmodified fibers.
• the modified fiber modules averaged about 29 percent more filtrate than the untreated fiber modules.
• Figure 5-7 present the rate of hemoglobin appearance, D, as a function of the filtration rate Q F , for the various modules.
• Figure 5 shows the performance of the unmodified fibers. Both modules exhibited relatively high initial hemolysis rates which declined sharply as the filtration rate increased. After reaching a minimum rate of hemolysis, corresponding to filtration rates of 40-45 ml/min, hemolysis increased with further increases in filtration rate. The minimum hemolysis rates for both modules were below the arbitrary standard of 1.5 mg/min. (By this standard, a patient with a plasma volume of 3 liters could be treated for 6 hours and have the plasma Hgb increase by 15 mg/dl.
• FIG. 6 presents the results for the modules with the cationic modified fibers.
• Module 8207-5 performed similarly to the unmodified units, although the minimum hemolysis rate was not as low.
• Polysulfone was solubilized in 1, 2-dichloroethane (DCE) and reacted with chlorosulfonic acid, washed throughly in DCE and redissolved in dimethylformamide (DFM).
• DCE 1, 2-dichloroethane
• DFM dimethylformamide
• the sulfonated polysulfone is not soluble in DCE as was the base polymer. At this point the sulfonated polymer is relatively free of chlorosulfonic acid and therefore could easily be handled in aqueous media.
• Nylon microporous membranes have been charge modified with dilute solutions of the sulfonated polysulfone polymer (SPS). Such treatment should produce a membrane that is compatible with blood since red blood cells are negatively charged.
• SPS sulfonated polysulfone polymer
• Untreated nylon microporous membrane (217-E13-0102) made pursuant to Example I was charge modified using the sulfonated polysulfone polymer solution produced above.
• the polymer solution was further diluted to 1:2, 1:5, and 1:8 in dimethyl formamide (DMF).
• Microporous nylon membranes were equilibrated in the diluted polymer solutions, air dried and then challenged with a dilute solution (0.02 ppm) of methyiene blue.
• Methyiene blue is a cationic dye, i.e., a dye with an immobilized positive charge.
• the treated membranes exhibited a negative charge when challenged with the methyiene blue dye solution, as shown in Table XIV below.
• the nylon membrane has been coated with a polymer containing an immobilized negative charge, i.e., SO 3 -.
• SO 3 - an immobilized negative charge
• the methyiene blue as mentioned before, possesses a positive charge, i.e., CH 3 +.
• the methyiene blue is adsorbed to the SPS coated nylon membrane through the SO 3 - group on the sulfonated polysulfone.

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• 1984
  • 1984-12-21 EP EP19850900441 patent/EP0167573A4/de not_active Withdrawn
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