WO1994017985A1 - Process of making microporous pps membranes - Google Patents

Abstract

The invention relates to a process for preparing a microporous membrane from an unsulfonated poly(phenylene sulfide) polymer by forming a mixture of an unsulfonated poly(phenylene sulfide) polymer, an amorphous polymer, and optionally a plasticizer, heating the resulting mixture, extruding or optionally casting the mixture into a membrane, controlled cooling (quenching) or coagulating the membrane, and leaching the membrane, while optionally drawing the membrane before, during, and/or after leaching.

Description

PROCESS OF MAKING MICRPOROUS PPS MEMBRANES

5 CROSS REFERENCE TO U.S. PATENT APPLICATIONS

The U.S. application is a continuation-in-part of U.S. Patent application Serial N

746,756, filed August 19, 1991 , now U.S. Patent 5,246,647, issued September 2

1 993, which in turn is a continuation-in-part of U.S. Patent Application Serial N

329,666, filed March 28, 1 989, now U.S. Patent No. 5,043, 1 1 2, both of which ar

10 incorporated herein by reference in their entirety.

BACKGROUND OF THE INVENTION Field of Invention

The present invention relates to a process for preparing microporous membrane from a blend containing an unsulfonated polyiphenylene sulfide) (PPS) polymer, a 15 amorphous polymer, and optionally a solvent and/or optional non-solvent. Suc membranes are useful in the treatment of liquids by the membrane separation processe of ultrafiltration, microfiltration, depth filtration, macrofiltration, membrane distillation, an membrane stripping. The membranes of this invention are also useful as microporou supports for composite liquid and/or gas separation membranes. 20 Description of Related Art

In the past, microporous membranes have been fabricated from polyolefins suc as polyethylene and polypropylene. One typical method of preparing such polyolefi membranes is by an extrusion process which involves dissolving the polyolefin in solvent or a mixture of solvent and non-solvent, extruding the polyolefin/solvent/no

25 solvent mixture into membranes, and immersing the membranes into a leach bat

Another method of preparing such polyolefin membranes is by a melt-extrusion proces which involves extruding the membranes from the molten polyolefin, followed by col drawing the membranes. However, polyolefins, while inexpensive and easy to proces exhibit relatively low heat distortion temperatures. . 30 Poly(phenylene sulfide) polymers are high performance thermoplastics whic possess high glass transition temperatures, high crystalline melting points, high therm

» stability, and high solvent resistance. Such properties make polyiphenylene sulfid polymers useful for membranes employed in liquid separations, particularly membran separation processes which involve treatment of organic, acidic, or basic liquids

35 elevated temperatures.

The very properties which make polyiphenylene sulfide) polymers desirabl materials for use in applications which require high temperature and/or solvent resistance also render such polymers very difficult to process into membranes, particularly since polyiphenylene sulfide) polymers exhibit relatively low solution viscosities at the high membrane fabrication temperatures, in excess of about 250°C, frequently required to fabricate membranes. The low solution viscosities exhibited by polyiphenylene sulfide) polymers are particularly problematic with extrusion or casting blends containing less than about the 40 weight percent polymer required to produce high flux microporous membranes. Such low solution viscosities also render extrusion of hollow fiber microporous membranes from polyiphenylene sulfide) polymers especially difficult. Furthermore, polyiphenylene sulfide) polymers are extremely solvent resistant and are therefore considered to be insoluble in all common solvents. Therefore, to form membranes, PPS, for example, is expected to be dissolved in very strong acids such as concentrated sulfuric acid to sulfonate the polyiphenylene sulfide), which renders the sulfonated polyiphenylene sulfide) soluble in common solvents such as dimethylformamide and dimethylacetamide. The problem associated with such a process is that the fabricated membrane comprises not polyiphenylene sulfide), but rather sulfonated polyiphenylene sulfide), which is soluble in common solvents. Thus the high solvent resistance of polyiphenylene sulfide) is lost.

What is. needed is a process of preparing microporous membranes from unsulfonated polyiphenylene sulfide) polymers using plasticizers, that is, solvents and optional non-solvents, which do not chemically modify or degrade the unsulfonated polyiphenylene sulfide) polymer during fabrication so that the high strength, temperature resistance, and solvent resistance of the unsulfonated polyiphenylene sulfide) polymer is retained by the fabricated membranes. What is further needed is a method of increasing the solution viscosities of the polyiphenylene sulfide) polymers, so that membranes can be more easily fabricated at the high temperatures required to fabricate membranes from such polymers, while retaining the high temperature and solvent resistance of the unsulfonated polyiphenylene sulfide) polymer. What is especially needed is a process for preparing microporous membranes having high flux from unsulfonated polyiphenylene sulfide) polymers.

The membranes of the present invention accomplish these objectives and exhibit excellent solvent and temperature resistance. The membranes also possess high tensile strength. The membranes are useful as microporous membranes for liquid separations such as ultrafiltration, microfiltration, depth filtration, macrofiltration, membrane stripping, and membrane distillation and as microporous supports for composite liquid or gas separation membranes.

SUMMARY OF THE INVENTION In one aspect the present invention relates to a process for preparing microporous membrane from a polyiphenylene sulfide) polymer comprising the steps of A. forming a mixture comprising:

(i) at least one polyiphenylene sulfide) polymer,

(ii) at least one amorphous polymer which is substantially stable a elevated temperatures, which possesses a glass transitio temperature of at least about -100°C, and wherein the amorphou polymer is at least partially immiscible in the polyiphenylene sulfide polymer at ambient conditions; and (iii) optionally a plasticizer comprising at least one organic compoun capable of dissolving at least about 10 weight percent of th polyiphenylene sulfide) polymer at the extrusion or castin temperature;

B. heating the mixture to a temperature at which the mixture becomes, a fluid

C. extruding or casting the fluid under conditions such that a membrane i formed;

D. subjecting the membrane to controlled cooling or coagulation by passin the membrane through at least one zone under conditions such that th membrane solidifies;

E. leaching the membrane by passing the membrane through at least one zon under conditions such that at least a portion of the optional plasticizer fo the polyiphenylene sulfide) polymer, at least a portion of said amorphou polymer, or a combination thereof, is removed from the membrane; and

F. producing a final microporous membrane.

In another embodiment, the present invention comprises the additional step of:

G. before leaching, during leaching, after leaching, or a combination thereof drawing the membrane to increase the flux of fluid through the membrane while the membrane is at a temperature above about 25 °C and below th melting point of the polyiphenylene sulfide) polymer and amorphou polymer or the polyiphenylene sulfide), amorphous polymer and plasticize mixture before and during leaching and for polyiphenylene sulfide) afte leaching. In yet another embodiment the present invention further comprises the additiona step of: H. before leaching, after leaching, before drawing, after drawing, or a combination thereof, annealing the membrane by exposing the membrane to a temperature above the glass transition temperature of the polyiphenylene sulfide) polymer, the polyiphenylene sulfide) and amorphous polymer mixture, or the polyiphenylene sulfide) amorphous polymer and plasticizer mixture and about 10°C below the melting point of the polyiphenylene sulfide) polymer or the depressed melting point of the polyiphenylene sulfide) and amorphous polymer mixture, or the polyiphenylene sulfide) polymer, amorphous polymer and plasticizer mixture for a period of time between about 30 seconds and about 24 hours.

The present invention also relates to the microporous membrane wherein said polyiphenylene sulfide) polymer has a degree of crystallinity of at least about 10 percent and a melting point of at least about 1 90°C.

In another aspect, the present invention relates to the process of the undrawn membrane and further comprises the additional step of:

I. before leaching, after leaching, or a combination thereof, annealing the membrane by exposing the membrane to a temperature above the glass transition temperature of the polyiphenylene sulfide) polymer or the polyiphenylene sulfide) polymer and plasticizer mixture and about 10°C below the melting point of the polyiphenylene sulfide) polymer or the depressed melting point of the polyiphenylene sulfide) polymer and plasticizer mixture for a period of time between about 30 seconds and about 24 hours. In another aspect, the invention relates to the undrawn membrane wherein the polyiphenylene sulfide) polymer has a degree of crystallinity of at least about 1 0 percent and a melting point of at least about 1 90°C. Brief Description of the Drawing

Figure 1 illustrates a composite of temperatures at ambient pressure at which a specific weight percent of PPS will dissolve in the solvents: m-terphenyl, 4-phenylphenol, and diphenylsulfone.

DETAILED DESCRIPTION OF THE INVENTION AND PREFERRED EMBODIMENTS Definitions: As used herein: "Amorphous polymer" refers to amorphous polymers in general, and preferably to polymers independently selected from the group consisting of polysulfones; polyarylsulfones; polyethersulfones; styrene copolymers; polyetherimides, polyetherimide copolymers; ethylene copolymers; amorphous polyesters; amorphous cellulose esters polycarbonates; polystyrenes; polysiloxanes; polyacrylates; polymethacrylates; poly(vinylacetates); polybenzimidazoies; and polyacrylamides. "Plasticizer" refers generally to at least one solvent consisting predominantly o carbon and hydrogen and optionally oxygen, nitrogen, sulfur, halogen, and mixtures thereof, wherein said solvent has a molecular weight of between about 1 60 and abou 650, contains at least one 5,6 or 7-membered ring structure, and possesses a boiling point of between about 1 50°C and about 480°C. "Plasticizer" also preferably refers to at least one solvent independently selected from the group consisting of 4,4'-dibromobiphenyl; 1 -phenylnaphthalene; phenothiazine; 2,5-biphenyl-1 ,3,4-oxadiazole; 2,5-diphenyloxazole; triphenylmethanol; N,N- diphenylformamide; m-terphenyl; benzil; anthracene; 4-benzoylbiphenyl; dibenzoylmethane; 2-biphenylcarboxylic acid; dibenzothiophene; pentachlorophenol; benzophenone; 1 -benzyl-2-pyrrolidinone; 9-fluorenone; 2-benzoylnaphthalene; 1 - bromonphthalene; diphenyl sulfide; 1 ,3-diphenoxybenzene; fiuorene;tetraphenylmethane; p-quaterphenyl; 1 -phenyl-2-pyrrolidinone; 1 -methoxynaphthalene; hydrogenated and partially hydrogenated terphenyl; 1 -ethoxynaphthalene; 1 ,3-diphenylacetone; 1 ,4- dibenzoylbutane; phenanthrene; 4-benzoylbiphenyl; o-terphenyl; 1 ,1 -diphenylacetone; o,o'-biphenol; 2,6-diphenylphenol; 1 ,2,3,-triphenylbenzene; triphenylene; 4- bromobiphenyl; 2-phenylphenol; thianthrene; 4,4'-diphenylbenzophenone; 3- phenoxybenzyl alcohol; 4-phenylphenol; 9,10-dichloroanthracene; p-terphenyl; 2- phenoxybiphenyl; triphenylmethane; 4,4'-dimethoxybenzophenone; 9, 1 0- diphenylanthracene; fluoranthene; diphenyl sulfone; diphenyl phthalate; diphenyl terephthalate; diphenyl isophthalate; diphenyl carbonate; 2,6-dimethoxynaphthalene; 2,7- dimethoxynaphthalene; 4-bromodiphenyl ether; pyrene; 9,9'-bifluorene; 4,4'- isopropylidenediphenol; 2,4,6-trichlorophenol; epsilon-caprolactam; 1 -cyclohexyl-2- pyrrolidinone; and mixtures of these compounds.

"Plasticizer" may optionally also further include at least one non-solvent consisting predominantly of carbon and hydrogen and optionally oxygen, phosphorus, silicon, nitrogen, sulfur, halogen, and mixtures thereof, wherein the non-solvent has a molecula weight of between about 1 20 and about 650 and possesses a boiling point of between about 1 50°C and about 480°C.

"Plasticizer" preferably optionally further comprises at least one non-solven selected from the group consisting of 1 ,3,5-triphenylbenzene, tetraphenylsilane, diphenyl sulfoxide, diphenic acid, 4-acetylbiphenyl, bibenzyl, diphenyl methyl phosphate, triphenyl phosphate, cyclohexyl phenyl ketone, mineral oil, butyl stearate, phenyl benzoate, 1 - phenyldecane, 1 ,3-diphenoxybenzene, 1 ,8-dichloroanthraquinone, polyphosphoric acid, dioctyl phthalate, 5-chlorobenzoxazolone, bis-(4-chlorophenol sulfone), diphenyl chlorophosphate, sulfolane, methyl myristate, methyl stearate, hexadecane, dimethyl phthalate, tetraethylene glycol dimethyl ether, diethylene glycol dibutyl ether, docosane, dotriacontane, tetraphenylene, pentafluorophenol, paraffin oil, 1 -methyl-2-pyrrolidinone, and 4,4'-dihydroxybenzophenone.

"Polyiphenylene sulfide)" or "PPS" refers to a polymeric material which comprises polyiphenylene sulfide). Usually this polymer is prepared from p-dichlorobenzene and sodium sulfide or obtained from Phillips Petroleum Co. Bartlesville, Oklahoma or Aldrich Chemical Company (or as is described below).

The PPS designated lot #1 72CJ from Aldrich Chemical Company was used as received for solubility determinations. Most of the organic compounds examined as high temperature solvents are obtained from Aldrich Chemical Company and are used as received. Other organic chemicals are obtained from suppliers as listed in Chemical Sources U.S.A., published by Directories Pub. Inc., Boca Ratan, Florida.

The polyiphenylene sulfide) polymers useful in this invention are unsulfonated. The PPS polymers from which the membranes are fabricated preferably possess a degree of crystallinity of at least about 10 percent, more preferably of at least about 20 percent, even more preferably of at least about 30 percent, and a melting point of at least about 1 90°C, more preferably of at least about 250°C.

Commercially available PPS, for example, FORTRON^® Grade 300 BO (^® trademark of Hoescht Celanese, Inc.), possesses a glass transition temperature of about 90°C and a melting point of about 285-300°C. Such commercially available PPS possesses a tensile strength of about 1 2,500 psi (86.2 x 10⁶ Pa) (ASTM Test Method D638), and an elongation of 3-6% at about 23°C (and test speed cf about 0.2 in./min. (0.5 cm/min), a flexural strength of about 21 ,000 psi (144.8 x 10⁶ Pa) (ASTM Test Method D-790 at 5% deflection), and a flexural modulus of about 0.6 x 10⁶ psi (4.14 x 10⁹ Pa) (ASTM Method D-790). The synthesis of such PPS polymers is known in the art. See U.S. patents 3,354, 1 29 and 3,524,835, wherein the relevant portions are incorporated herein by reference. Amorphous Polymers

The amorphous polymers useful in this invention are at least partially immiscible at ambient (room) temperature with the polyiphenylene sulfide) polymer in the presence or absence of a plasticizer. In the art generally, some binary and ternary systems containing two polymers and a plasticizer comprising a solvent and optional non-solvent may form a single phase or two coexisting phases, depending upon the relativ proportions of the components in the system. The term compatibility is often used in th art in a thermodynamic sense to be synonymous with miscibility. Solution methods ar commonly used to determine the miscibility of mixtures of two polymers in a solvent an optional non-solvent. One method of determining miscibility is to mix two polymers an a solvent and optional non-solvent. On standing for a few days, the polymers ar considered miscible if phase separation does not occur; if phase separation does occu the two polymers are said to be immiscible. In the present invention, the relativ concentrations of the polyiphenylene sulfide) polymer, the amorphous polymer, an optional plasticizer comprising solvent and optional non-solvent in the mixture must b such that the resulting binary or ternary mixture is immiscible, that is, physically multiphase system at ambient (room) temperature up to about 50°C below the membran fabrication temperature. See C. Olabisi, "Polyblends," Encyl. of Chem. Tech., 3rd Ed. Interscience, New York, New York, Vol. 18, P. 443 (1 982); H. Tompa, "Polyme Solutions," Academic Press, New York, New York, pp. 200-201 (1 959); J. Hildebran et al., "The Solubility of Non-Electrolytes," 3rd Ed., Rheinhold Publishing, New York, Ne York, pp. 382-383 (1 950); D. R. Paul, "Interfacial Agents (Compatibilizers) For Polyme Blends," Polymer Blends, Vol. 2, Academic Press, New York, New York, pp. 35-3 (1978); P.J. Flory, "Principals of Polymer Chemistry," Cornell University Press, Ithaca New York, pp. 554-559 (1953); H. Morawetz, "Macromolecules in Solution," Interscienc Publishing, New York, New York, pp. 85-88 (1 965); the relevant portions ar incorporated herein by reference.

The amorphous polymers useful in this invention are stable at the elevate temperatures required for fabricating the membrane. The amorphous polymers are stabl at temperatures preferably above about 1 50°C, more preferably above about 200°C even more preferably above about 250°C. Stable at elevated temperatures means tha the amorphous polymers do no undergo substantial degradation at the membran fabrication temperature. The amorphous polymers useful in this invention preferabl possess a glass transition temperature of at least about -100°C, more preferably of a least about -80°C, even more preferably of at least about -60°C. The amorphou polymers useful in this invention possess a molecular weight preferably of at least abou 500, more preferably of at least about 1 ,000. The amorphous polymers useful in thi invention possess a molecular weight preferably of less than about 4 X 10⁶, mor preferably of less than about 3 X 10⁶, even more preferably of less than about 1 X 10⁶ Preferred amorphous polymers for use in this invention include polysulfones polyethersulfones; styrene copolymers, such as styrene-acrylonitrile copolymer an styrene-maleic anhydride copolymer; amorphous cellulose esters such as cellulose acetate butyrate and cellulose acetate propionate; amorphous ethylene copolymers; amorphous polyesters; amorphous cellulose ethers such as ETHOCEL^® ethyl cellulose resin and METHOCEL® methyl cellulose resin(® trademarks of The Dow Chemical Company); polycarbonates; polystyrenes; poiysiloxanes; polyacrylates; polymethacrylates; poly(vinylacetates); and polyacrylamides. More preferred amorphous polymers include polysulfones, polyethersulfones, amorphous polyesters, and polycarbonates. Plasticizers

The plasticizers useful in this invention comprise at least one organic compound preferably capable of dissolving at least about 10 weight percent of the poly(phenylene sulfide) polymer present at the membrane fabrication temperature. The plasticizer more preferably dissolves at the fabrication temperature at least about 25 weight percent of the polyiphenylene sulfide) polymer and even more preferably about 50 weight percent of the polyiphenylene sulfide) polymer. The plasticizer may be comprised of a solvent for the polyiphenylene sulfide) polymer or a mixture of a solvent and non-solvent for the polyiphenylene sulfide) polymer, provided the solvent and non-solvent mixture itself is capable of dissolving at least about 10 weight percent of the poly(phenylene sulfide) polymer at the membrane fabrication temperature. A solvent for the poly(phenylene sulfide) polymer dissolves at least about 10 weight percent poly(phenylene sulfide) polymer at the membrane fabrication temperature. A non-solvent for the poly(phenylene sulfide) polymer dissolves less than about 1 0 weight percent of the poly(phenylene sulfide) polymers at the membrane fabrication temperature.

A preferred class of plasticizers (solvents) useful in this invention are organic compounds consisting predominantly of carbon and hydrogen and optionally oxygen, nitrogen, sulfur, halogen, and mixtures thereof, wherein the organic compound has a molecular weight of between about 1 60 and about 650, contains at least one 5, 6 or 7 membered ring structure, and possesses a boiling point of between about 1 50°C and about 480°C. In one aspect, aromatic 6-membered rings are preferred. Preferable solvents are described above. Non-solvents

A preferred class of non-solvents useful in this invention are organic compounds consisting predominantly of carbon and hydrogen and optionally oxygen, phosphorus, silicon, nitrogen, sulfur, halogen, and mixtures thereof, wherein the organic compound has a molecular weight of between about 1 20 and 650, and possesses a boiling point of between about 1 50°C and about 480°C. The non-solvents more preferably have a boiling point of between about 280°C and about 480°C, even more preferably between 300°C and about 480°C. The non-solvents preferably are soluble in the solvent used a elevated temperatures. Preferred non-solvents are described above.

The concentrations of the components in the mixture may vary and are dependen upon the desired membrane characteristics, such as porosity and pore size, and th fabrication method. The concentrations of PPS polymer, the amorphous polymer, and th plasticizer in the mixture is that which result in a mixture with a suitable viscosity fo extrusion or casting at the membrane fabrication temperature. The viscosity of th mixture must not be so high that the fluid is too viscous to fabricate; the viscosity mus not be so low that the fluid lacks the physical integrity required to form a membrane Extrusion mixtures of PPS polymers, amorphous polymers, and plasticizers generall possess non-Newtonian viscosity behavior; therefore, such mixtures exhibit a shear rat dependence upon viscosity. The mixture preferably has a viscosity at extrusio temperatures of between about 100 and about 10,000 poise at a shear rate of fro about 10 to about 10,000 sec^"1. The concentration of PPS polymer in the mixture is preferably from about 1 weight percent to about 90 weight percent, more preferably from about 20 weigh percent to about 80 weight percent, even more preferably from about 25 weight percen to about 75 weight percent.

The concentration of amorphous polymer in the mixture is preferably from abou 3 weight percent to about 80 weight percent, more preferably from about 3 weigh percent to about 70 weight percent, even more preferably from about 3 weight percen to about 65 weight percent. Fabrication

The membranes of this invention may be prepared by casting or extrusion. In th casting process, the polymers are contacted with the plasticizer comprising at least on solvent and optionally at least one non-solvent for the poly(phenylene sulfide) polymer a elevated temperatures. The elevated temperature at which the mixture is contacted is tha temperature at which the mixture is a fluid, and below that temperature at which th polymers undergo substantial degradation and below that temperature at which th plasticizer comprising solvent and optional non-solvent boils. The upper temperature limi is preferably below about 400°C, more preferably below about 380°C, even mor preferably below about 370°C. The minimum temperature limit is preferably at leas about 25°C. The contacting preferably takes place with adequate mixing or agitation.

In the case of casting, a membrane may be cast into flat sheet form by pouring th mixture onto a smooth support surface and drawing down the mixture to an appropriat thickness with a suitable tool such as a doctor blade or casting bar. Alternately, th mixture may be cast in a continuous process by casting the mixture onto endless belt or rotating drums. The casting surface may be such that the membrane may thereafte be readily separated from the surface. For example, the membrane may be cast onto a support having a low surface energy, such as silicone, coated glass, TEFLON®, or coated metal, or a surface to which the membrane will not adhere. Alternately, the mixture may be cast onto a support surface which may thereafter be dissolved away from the finished membrane. The mixture may also be cast onto a porous support surface. The cast membrane is thereafter subsequently quenched or coagulated, leached, and optionally drawn as described hereinafter for membranes formed by the extrusion process. Membranes may be extruded from the poly(phenylene sulfide) polymer mixtures hereinbefore described. The components of the extrusion mixture may be combined prior to extrusion by mixing in any convenient manner with conventional mixing equipment, as for example, in a Hobart brand mixer. The extrusion blend may also be combined and mixed under heating in a resin kettle. Alternately, the extrusion mixture may be combined by extruding the mixture through a twin screw extruder, cooling the extrudate, and grinding or pelletizing the extrudate to a particle size readily fed to a single or twin screw extruder. Alternately, the components of the extrusion composition may be combined directly in a melt-pot or twin screw extruder and extruded into membranes in a single step. The use of static mixers helps to ensure adequate mixing of the components. The mixture is heated to a temperature which results in a fluid possessing a viscosity suitable for extrusion. The temperature should not be so high or the exposure time so long as to cause significant degradation of the poly(phenylene sulfide) polymer, the amorphous polymer, and/or the plasticizer. The temperature should not be so low as to render the fluid too viscous to extrude. The extrusion temperature is preferably between about 100°C and about 400°C, more preferably between about 1 10°C and about 380°C, even more preferably between about 1 20°C and about 370°C.

The mixture of polymers and plasticizer is extruded through a film, tube, or hollow fiber die (spinnerette). Hollow fiber spinnerettes typically are multi-holed and thus produce a tow of multiple fibers. The hollow fiber spinnerettes include a means for supplying fluid to the core of the extrudate. The core fluid is used to prevent the collapsing of the hollow fibers as they exit the spinnerette. The core fluid may be a gas such as nitrogen, air, carbon dioxide, or other inert gas or a liquid which is a non-solvent for the polymers. Examples of suitable core liquids include dioctylphthalate, methyl stearate, polyglycol, mineral oil, paraffin oil, petroleum oil, for example, MOBILTHEM^® 600, 603, and 605 heat transfer oils (^®trademarks of Mobil Oil Corporation), and silicone oil, for example, DC-704^® and DC-710^® silicone oil (^®trademarks of Dow-Corning Corporation). Use of a liquid non-solvent as the core fluid may result in a microporous membrane with an inside skin. A solvent and non-solvent core liquid mixture may be used to control the inside ski morphology. A non-solvent fluid may optionally be used on the outside of the hollow fibe membrane to produce an outside skin. The extrudate exiting the die enters one or more controlled cooling (quench) o coagulation zones. The environment of the quench or coagulation zone may be a gas o a liquid. Within the quench or coagulation zone, the extrudate is subjected to coolin and/or coagulation to cause solidification of the membrane with the optional simultaneous removal of a portion of the plasticizer. In a preferred embodiment, the membrane is initially quenched in a gaseous environment such as air, nitrogen, or other inert gas. In a preferred embodiment, the membrane is slowly quenched or cooled, so as to permit sufficient time for phase separation to occur. With slow quenching or cooling, relatively low concentrations of amorphous polymer, that is, less than about 1 5 weight percent, may be used while still obtaining a membrane with a high flux. The temperature of the gaseous quench zone is that temperature at which solidification occurs at a reasonable rate. The temperature of the gaseous quench zone is preferably in the range of from about 0°C to about 275 °C, more preferably in the range of from about 5°C to about 270°C, even more preferably in the range of from about 25 °C to about 200°C. The residence time in the gaseous quench zone is that which is sufficient to solidify the membrane. The residence time in the gaseous quench zone is preferably at least about 0.01 seconds, more preferably at least about 0.5 seconds, even more preferably at least about 2 seconds. The residence time in the gaseous quench zone is preferably less than about 300 seconds, more preferably less than about 1 20 seconds, even more preferably less than about 90 seconds. Shrouds may be used to help control gaseous flow rates and temperatures within the gaseous quench zone. Following or instead of the gaseous quench, the membrane may optionally be quenched or coagulated in a liquid environment which is substantially a non-solvent for the poly(phenylene sulfide) polymer, such as water, ethylene glycol, or glycerol, and which optionally contains an effective amount of a swelling agent. The temperature of the quench liquid is that temperature at which the membrane is not adversely affected and at which solidification occurs at a reasonable rate. The liquid quench temperature is preferably between about 0°C and about 275°C, more preferably between about 5°C and about 250°C, even more preferably between about 10°C and about 225°C. The residence time in the liquid quench zone is that which is sufficient to solidify the membrane. The residence time in the liquid quench zone is preferably at least about 0.01 seconds, more preferably at least about 0.5 seconds, and even more preferably at least about 2 sec. The residence time in the liquid quench zone is preferably less than about 300 sec, more preferably less than about 1 20 sec, and even more preferably less than about 90 sec.

Following quenching and/or coagulation, the membrane may be passed through one or more leach zones to remove at least a portion of the plasticizer, at least a portion of the amorphous polymer, or a combination thereof. The leach zone need not remove all of the plasticizer and/or amorphous polymer from the membrane. The leach zone preferably removes a substantial portion of the plasticizer and amorphous polymer from the membrane. Preferably, the leach zone removes the plasticizer to a level of less than about 5.0 weight percent in the leached membrane, more preferably of less than about 2.0 weight percent in the leached membrane, even more preferably of less than about 0.5 weight percent in the leached membrane. Preferably, the leach zone removes the amorphous polymer to a level of less than about 5.0 weight percent in the leached membrane, more preferably of less than about 2.0 weight percent in the leached membrane, even more preferably of less than about 0.5 weight percent in the leached membrane.

The leach zone is comprised of a liquid which is a non-solvent for the poly(phenylene sulfide) polymer and which is a solvent for the plasticizer and/or amorphous polymer. Preferred leach liquids include toluene, xylene, acetone, methyl ethyl ketone, N-methyl-pyrrolidinone, water, and chlorinated hydrocarbons such as methylene chloride, carbon tetrachloride, trichloroethylene, and 1 , 1 ,1 -trichloroethane. The leach liquid may also comprise an acid or alkali aqueous solution if an acid or alkali soluble solvent and optional non-solvent for the poly(phenylene sulfide) polymer are used in the extrusion or casting mixture. The maximum temperature of the leach bath is that temperature at which the membrane is not adversely affected. The minimum temperature of the leach bath is that temperature at which plasticizer and/or amorphous polymer removal from the membrane occurs at a reasonable rate. The temperature of the leach bath is preferably between about 0°C and about 250°C, more preferably between about 5°C and about 200°C, even more preferably, between about 10°C and about 1 50°C. The residence time in the leach bath is preferably long enough to remove at least a portion of the plasticizer and/or amorphous polymer. The residence time in the leach bath is preferably less than about 14 hours, more preferably less than about 2 hours. The residence time in the leach bath is preferably more than about 1 sec, even more preferably more than about 30 sec. The organic compounds described herein as solvents (or plasticizers) or non solvents may need to be used in large quantities when commercial membranes are fabricated. Thus it is expected that environmentally acceptable compounds (e.g. thos not containing any halogen-atoms) will be preferred. Similarly, the preferred leaching o quenching organic compounds used for commercial scale will also be environmentall acceptable. Following leaching, the membrane may optionally be dried. Prior to drying, th leach liquid remaining in the membrane may optionally be exchanged with a more volatile non-polar drying agent which possesses a low surface tension and is a solvent for th leach liquid and which is a non-solvent for the polyiphenylene sulfide) polymer in orde to reduce the possibility of pore collapse during drying. Preferred drying agents includ chlorofluorocarbons, for example, FREON 1 13^® chlorofluorocarbon (^®trademark of E.I Dupont de Nemours), isopropanol, or isooctane. The exchange may be carried out a temperatures which do not adversely affect the membrane, preferably between about 0° and about 100°C. The membrane may be dried in air or an inert gas such as nitrogen Drying may also be done under vacuum. The membrane may be dried at temperatures a which drying takes place at a reasonable rate and which do not adversely affect th membrane. The drying temperature is preferably between about 0°C and about 1 80°C more preferably between about 10°C and 1 50°C, even more preferably between abou 1 5 °C and about 1 20°C. The drying time is preferably less than about 24 hours, mor preferably less than about 6 hours. The drying time is preferably at least about 3 seconds, more preferably at least about 60 seconds.

The membrane may optionally be drawn or stretched subsequent to the quenchin or coagulation step using conventional equipment such as godets to improve the flux an strength of the membrane. Drawing may occur before leaching, during leaching, afte leaching, before drying, during drying, after drying, or a combination thereof. The dra temperature is dependent upon whether the membrane contains plasticizer at the time o drawing. For substantially plasticizer-free membranes, the membrane is drawn at temperature which is above the glass transition temperature and below the crystallin melting point of the polyiphenylene sulfide) polymer; the minimum temperature at whic the PPS membrane is drawn is preferably at least about 90°C, more preferably at leas about 100°C. The maximum temperature at which the membrane is drawn is preferabl less than about 270°C, more preferably less than about 260°C. For membrane containing plasticizer, the membrane is drawn at a temperature between ambien temperature and the melting point of the polyiphenylene sulfide) polymer or the depresse melting point of the polyiphenylene sulfide) polymer and plasticizer mixture; preferre lower draw temperatures are above about 25 °C; preferred upper draw temperatures ar less than about 10°C below the depressed melting point. The membranes are drawn b stretching the membranes under tension. The membranes are drawn to a ratio of between about 1 .1 and about 40, more preferably of between about 1 .5 and about 30. The draw ratio refers to the ratio of the original length of the membrane before drawing to the final length of the membrane after drawing. The degree of draw may also be expressed as percent elongation, which is calculated by

I ^L' ^{" L|} ) X 100,

wherein L_f is the final length of the membrane after drawing and L; is the initial length of the membrane before drawing. Drawing may be carried out in a single step or in a series of steps using the same or different draw ratios in each step.

Line speeds for drawing are not critical and may vary significantly. Practical preferred line speeds range from about 10 feet per minute (3 meters per minute) to about 2,000 feet per minute (610 meters per minute). In the case of hollow fibers, the fibers preferably possess an outside diameter of from about 10 to about 7,000 microns, more preferably of from about 50 to about 5,000 microns, even more preferably of from about 100 to about 4,000 microns with a wall thickness preferably of from about 10 to about 700 microns, more preferably of from about 25 to about 500 microns. In the case of films, the films preferably possess a thickness of from about 10 to about 800 microns, more preferably of from about 25 to about 600 microns. The films may optionally be supported by a permeable cloth or screen.

Optionally, before leaching, after leaching, before drawing, after drawing, or a combination thereof, the membrane may be annealed by exposing the membrane to elevated temperatures. The membrane may be annealed at temperatures above the glass transition temperature (Tg) of the polymer or polymer and plasticizer mixture and about 10°C below the melting point of the PPS polymer or depressed melting point of the PPS polymer and plasticizer mixture for a period of time between about 30 seconds and about 24 hours.

The membranes of this invention may be isotropic or anisotropic. Isotropic microporous membranes possess a morphology in which the pore size within the membrane is substantially uniform throughout the membrane. Anisotropic (asymmetric) microporous membranes possess a morphology in which a pore size gradient exists across the membrane; that is, the membrane morphology varies from highly porous, larger pores at one membrane surface to less porous, smaller pores at the other membrane surface. Such anisotropic membranes thus possess a microporous "skin" of smaller pores. In hollow fiber anisotropic membranes, the "skin" may be on the inside or outside surface of the hollow fiber. The term "asymmetric" is often used interchangeably with the term "anisotropic."

In a preferred embodiment of this invention, the microporous membranes are usefu in the treatment of liquids by the membrane separation processes of microfiltration ultrafiltration, macrofiltration, depth filtration, membrane stripping, and membran distillation. Such membranes may also be used as porous supports for composite gas o liquid separation membranes. In a preferred embodiment, the microporous membranes ar useful for ultrafiltration or microfiltration. Ultrafiltration and microfiltration are pressur driven filtration processes using microporous membranes in which particles or solutes ar separated from solutions. Separation is achieved on the basis of differences in particl size or molecular weight. Macrofiltration is a pressure driven filtration process usin microporous membranes to separate particles or solutes having a size greater than abou 10 microns from solution.

Ultrafiltration and microfiltration membranes may be characterized in a variety o ways, including porosity, mean pore size, maximum pore size, bubble point, gas flux water flux, Scanning Electron Microscopy (SEM), and molecular weight cut off. Suc techniques are well known in the art for characterizing microporous membranes. Se Robert Kesting, Synthetic Polymer Membranes, 2nd edition, John Wiley & Sons, Ne York, New York, 1 985, pp. 43-64; Channing R. Robertson (Stanford University) Molecular and Macromolecular Sieving by Asymmetric Ultrafiltration Membranes. OWR Report, NTIS No. PB85-1577661 EAR, September 1 984; and ASTM Test Method F31 6-86 and F31 7-72 (1982); the relevant portions of which are incorporated herein b reference.

Porosity refers to the volumetric void volume of the membrane. The membrane must possess porosities permitting sufficient flux through the membrane while retainin sufficient mechanical strength under use conditions. The membranes of this inventio preferably have a porosity of at least about 10 percent, more preferably of at least abou 20 percent, even more preferably of at least about 25 percent. The membranes of thi invention preferably have a porosity of less than about 90 percent, more preferably o less than about 80 percent, even more preferably of less than about 75 percent. Pore size of the membrane may be estimated by several techniques includin

Scanning Electron Microscopy (SEM), and/or measurements of bubble point, gas flux water flux, and molecular weight cut off. The pore size of any given membrane i distributed over a range of pore sizes, which may be narrow or broad.

The bubble point pressure of a membrane is measured by mounting the membran in a pressure cell with liquid in the pores of the membrane. The pressure of the cell i gradually increased until air bubbles permeate the membrane. Because larger pore become permeable at lower pressures, the first appearance of bubbles is indicative of the maximum pore size of the membrane. If the number of pores which are permeable to air increases substantially with a small increase in pressure, a narrow pore size distribution is indicated. If the number of air-permeable pores increases gradually with increasing pressure, a broad pore size distribution is indicated. The relationship between pore size and bubble point pressure can be calculated from the equation r = 2G P wherein r is the pore radius,

G is the surface tension of the liquid in the membrane pores, and

P is the pressure.

The mean pore size of the membranes of this invention useful for ultrafiltration is preferably between about 5 Angstroms and about 1 ,000 Angstroms, more preferably between about 10 Angstroms and about 500 Angstroms. The maximum pore size of such membranes is preferably less than about 1 ,000 Angstroms, more preferably less than about 800 Angstroms. The mean pore size of the membranes of this invention useful for microfiltration is preferably between about 0.02 micron and about 10 microns, more preferably between about 0.05 micron and about 5 microns; the maximum pore size of such membranes is preferably less than about 10 microns, more preferably less than about 8 microns. The mean pore size of membranes of this invention useful for macrofiltration is preferably between about 10 microns and about 50 microns.

Gas flux is defined as:

F = (amount of gas passing through the membrane) (membrane area)(time)(driving force across the membrane).

A standard gas flux unit is

(centimeter)³(STP) (centimeter)²(second)(centimeter Hg) abbreviated hereinafter as cm³(STP) , cm² sec cmhg where STP stands for standard temperature and pressure.

The membranes of this invention preferably have a gas flux for nitrogen of at least about

10^"6 cm³(STP) , cm² sec cmHg more preferably of at least about

10^"5 cm³(STP) , cm² sec cmHg even more preferably of at least about

10^"4 cm³(STP) , cm² sec cmHg

Water flux is defined as

W = (amount of water passing through the membrane), (membrane area)(time) under given conditions of temperature and pressure.

The membranes of this invention preferably exhibit a water flux of at least about

1 ml , m hr cmHg more preferably of at least about ml m² hr cmHg even more preferably of at least about

10 ml , m² hr cmHg

The membranes are fabricated into flat sheet, spiral wound, tubular, or hollow fiber devices by methods described in the art. Spiral wound, tubular, and hollow fiber devices are preferred. Tubesheets may be affixed to the membranes by techniques known in the art. Preferred tubesheet materials include thermoset and thermoplastic polymers. The membrane is sealingly mounted in a pressure vessel in such a manner that the membrane separates the vessel into two fluid regions wherein fluid flow between the two regions is accomplished by fluid permeating through the membrane. Conventional membrane devices and fabrication procedures are well known in the art.

Ultrafiltration, microfiltration, and macrofiltration are pressure driven filtration processes using microporous membranes to recover or isolate solutes or particles from solutions. The membrane divides the separation chamber into two regions, a higher pressure side into which the feed solution is introduced and a lower pressure side. One side of the membrane is contacted with the feed solution under pressure, while a pressure differential is maintained across the membrane. To be useful, a least one of the particles or solutes of the solution is selectively retained on the high pressure side of the membrane while the remainder of the solution selectively passes through the membrane. Thus, the membrane selectively "rejects" at least one type of the particles or solutes in the solution, resulting in a retentate stream being withdrawn from the high pressure side of the membrane which is enriched or concentrated in the selectively rejected particle(s) or solute(s) and a filtrate stream being withdrawn from the low pressure side of the membrane which is depleted in the selectively rejected particle(s) or solute(s).

The separation process should be carried out at pressures which do not adversely affect the membrane, that is, pressures which do not cause the membrane to mechanically fail. The pressure differential across the membrane is dependent upon the membrane characteristics, including pore size and porosity. For the membranes of this invention useful for ultrafiltration or microfiltration, the pressure differential across the membrane is preferably between about 2 psig (1 3.8 x 10³ Pa) and about 500 psig (3.4 x 10⁶ Pa), more preferably between about 2 psig ( 1 3.8 x 10³ Pa) and about 300 psig (2 x 10⁶ Pa), even more preferably between about 2 psig ( 1 3.8 x 10³ Pa) and about 1 50 psig ( 1 x 10⁶ Pa). Ultrafiltration is commonly performed between about 10 and 1 00 psig (68.9 and 689 x 10³ Pa). Microfiltration in commonly performed at between about 2 (1 3.8 x 10³ Pa) and 50 psig (3.4 x 10⁵ Pa). Macrofiltration is commonly performed at between about 0.5 and 5 psig (3.4 and 34 x 10³ Pa). For the membranes of this invention useful as composite supports for gas or liquid separation membranes, the pressure differential across the membrane is preferably between about 5 psig (3.4 and 34 x 10³ Pa) and about 1 ,500 psig (1 .03 x 10⁶ Pa). The separation process should be carried out at temperatures which do not adversely affect membrane integrity. Under continuous operation, the operating temperature is preferably between about 0°C and about 300°C, more preferably between about 1 5°C and about 250°C, even more preferably between about 20°C and about 175°C.

In specific embodiments, the amount of polyiphenylene sulfide) polymer in the polymer-plasticizer mixture is between about 10 weight percent and about 90 weight percent. In specific embodiments, the membrane is drawn in Step G at a temperature of between about 25 °C and about 273 °C.

In specific embodiments, the membrane is drawn to a draw ratio of between about 1 .1 and about 40. In specific embodiments, the fluid polymer is extruded at a temperature of betwee about 1 00°C and about 400°C.

In specific embodiments, the membrane is subjected to controlled cooling o coagulation at a temperature of between about 0°C and about 275 °C. In specific embodiments, the controlled cooling zone comprises a gaseou environment.

In specific embodiments, the membrane is leached at a temperature of betwee about 0°C and about 275 °C.

In specific embodiments, the leach zone comprises a liquid selected from the grou consisting of toluene, xylene, acetone, methyl ethyl ketone, N-methylpyrrolidinone, water an acid or alkali aqueous solution, and chlorinated hydrocarbons.

In specific embodiments, the final membrane is useful for ultrafiltration microfiltration, or macrofiltration, or as a composite membrane support.

In specific embodiments, the final membrane possesses a porosity in the range o about 1 0 percent to about 90 percent.

In specific embodiments, the mean pore size of the membrane is in the range o about 5 Angstroms to about 1 ,000 Angstroms for ultrafiltration, about 0.02 micron t about 10 microns for micro-filtration, and about 10 microns to about 50 microns fo macrofiltration. In specific embodiments, the said membrane possesses a nitrogen flux of at leas about

10^"4 cm³(STP). cm² sec cmHg In specific embodiments, the said membrane possesses a water flux of at leas about

10 ml . m² hr cmHg In specific embodiments of Claims 2 to 20, and 21 to 40, only a binary system o PPS and one or more amorphous polymers is present. In specific embodiments of Claims 2 to 20, and 21 to 40, a ternary system of PPS, one or more amorphous polymers, one or more solvents (plasticizers) and optionally on or more non-solvents is present.

The following Examples are presented for illustrative purposes only and are no intended to limit the scope of the invention or claims.

EXAMPLE A - Solvents and Non-Solvents for Polv(phenylene sulfide) (PPS) Poly(phenylene sulfide) (PPS), designated as catalogue no. 18,235-4, Lot # 1 72CJ, was obtained commercially from Aldrich Chemical Co. The PPS was dried at abou 1 50°C for 1 6 hours in an air-circulating oven and was stored in a desiccator ove Drierite^®. Large commercial quantities of PPS were obtained as PPS Grade 300BO fro Hoechst Celanese, Inc. One hundred seven organic compounds were evaluated for thei solvent effect on PPS. Most of the organic compounds were obtained from Aldric Chemical Company and used as received. Other organic chemicals were obtained from suppliers as listed in Chemical Sources U.S.A., published annually by Directorie Publishing Co., Inc., of Boca Ratan, Florida.

Mixtures of PPS and a solvent and/or a non-solvent, a total weight of less than about 2 grams, were prepared by weighing PPS and solvent at a precision of + 0.001 in a 1 to 4 dram size glass vial. The resulting air space in each vial, which varied considerably due to the large differences in the bulk densities of the compounds, was purged with nitrogen. The vials were sealed with screw caps containing aluminum foil liners. Solubility was usually determined at about 10 weight percent polymer, followed by additional determinations at about 25 and about 50 weight percent if necessary. Table 1 below lists the organic compounds examined for their solvent effect with

PPS. The approximate solubility of each the polymer is shown at the indicated temperature(s). The organic compounds were assigned a number (beginning with 200) for easy reference.

Also, listed in Table 1 is an approximate molecular weight, melting point, and boiling point, if these physical properties were available.

In the Tables, "g" in the solubility column means "greater than" ( > ), s means "smaller than" ( < ), and = means "equal to. " TABLE 1

RELATIVE SOLUBILITY OF POLY(PHEN YLENE SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS

Approximate

Ref. Molec. Melting Boiling Solub. Temp.

No. Compound Weight Point Point (g= ;s=<) (°c)

200 Triphenylmethanol 260 161 360 g 50.1%? 349

201 Triphenyl ethane 244 93 359 g 50.0% 349

202 Triphenylene 228 196 438 g 49.9% 350

2031,2,3-Triphenylbenzene 306 158 - g 49.9% 349

2041,3,5-Triphenylbenzene 306 173 460 s 10.4% 349

205 Tetraphenylmethane 320 281 431 s 25.2% 349

205 Tetraphenylmethane 320 281 431 =s 50.3%? 349

206 Tetraphenylsilane 337 236 422 s 9.9% 349

207 Diphenyl sulfoxide 202 70 350 s 10.4%a 349

208 Diphenyl sulfone 218 124 379 g 50.0% 349

2092,5-Diphenyloxazole 221 72 360 g 50.1% 349

210 Diphenic acid 242 228 - s 10.1%a 349

2111,1-Diphenylacetone 210 60 - g 49.9% 302

2121,3-Diphenylacetone 210 33 330 g 49.8% 302

2134-Acetylbiphenyl 196 117 - •=s 8.6% 302

2142-Biphenylcarboxylic 198 109 349 g 50.2% 349 acid

2154-Biphenylcarboxylic 198 225 - =s 25.7%? 349 acid

216 m-Terphenyl 230 83 379 g 50.2% 302

2174-Benzoylbiphenyl 258 100 419 g 50.2% 349 TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF P0LY(PHEN YLENE

SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS ■ Approximate

5 Ref. Molec. Melting Boiling Solub. Tem

No. Compound Weight Point Point (g=>;s=<) (°C

2174-Benzoylbiphenyl 258 100 419 s 49.2% 302

2184,4'-Diphenyl- 334 - g 50.0% 302 benzophenone

10 219 l-Benzoyl-4-piperidone 203 56 399 g 10.2%? 349

, 2202-Benzoylnaphthalene 232 81 383 g 50.5% 349

221 Diphenyl carbonate 214 79 301 g 24.9% 302

221 Diphenyl carbonate 214 79 301 g 50.0%?a 302

222 Bibenzyl 182 51 284 s 10.1% 274

15 223 Diphenyl methyl 264 - 389 s 10.2%a 349 phosphate

2241-Bromonaphthalene 207 -1 280 g 50.6% 274

225 N,N-Diphenylformamide 197 71 337 g 50.2% 302

2263-Phenoxybenzyl 200 - 329 g 50.0% 302 0 alcohol

227 Fluoranthene 202 108 384 g 50.0% 349

2282-Phenoxybiphenyl 246 49 342 g 50.0% 302

229 Triphenyl phosphate 326 51 281 s 10.3% 274

230 Cyclohexyl phenyl 188 56 - =s 10.0% 302 5 ketone

2312,5-Diphenyl-l,3,4- 222 139 382 g 50.1% 349 oxadiazole

2321,4-Dibenzoylbutane 266 107 - g 49.8% 302

TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POLY(PHEN YLENE SULFIDE). (PPS). IN VARIOUS ORGANIC COMPOUNDS

Approximate

Ref. Molec. Melting Bo riilning Solub. Temp.

No. Compound Weight Point Point fg^«-*;s^»<) lici

2339-Fluorenone 180 83 342 g 50.4% 302

2341,2 Dibenzoyl 286 146 s 50.2%a 349 benzene

10 235 Dibenzoylmethane 224 78 360 g 50.2% 349 2362,4,6-Trichlorophenol 197 65 246 g 25.0% 242

2362,4,6-Trichlorophenol 197 65 246 s 50.1% 247

237 Benzil 210 94 347 g 50.2% 302

238 p-Terphenyl 230 212 389 g 50.0% 302 15 239 Anthracene 178 216 340 g 50.2% 302

240 Mineral oil 360 s 10.0% 349

241 Butyl stearate 341 343 s 7.1% 302

2429-Phenylanthracene 254 151 417 g 10.0%?a 349

2431-Phenylnaphthalene 204 324 g 50.1% 302 20 2444-Phenylphenol 170 166 321 g 50.0% 302

2452-Phenylphenol 170 59 282 g 50.0% 274

2461-Ethoxynaphthalene 172 280 g 49.8% 274 TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POLY(PHENYLENE SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS

Approximate

Ref. Molec. Melting Boiling Solub. Temp.

No. Compound Weight Point Point (g=->;s=<) (°c)

247 Phenyl benzoate 198 69 298 s 9.8% 274

2481-Phenyldecane 218 - 293 s 10.4% 274

2491-Methoxynaphthalene 158 - 269 g 48.9% 247 10 2502-Methoxynaphthalene 158 74 274 g 24.8% 242

2502-Methoxynaphthalene 158 74 274 s 50.0% 247

251 Sulfuric acid, 98 11 340 0.0% 25 concentrated

2524-Bromobiphenyl 233 86 310 g 50.0% 258 15 2524-Bromobiphenyl 233 86 310 g 11.3% 234

2524-Bromobiphenyl 233 86 310 g 26.9% 240

2534-Bromodiphenyl ether 249 18 305 g 24.7% 243

2534-Bromodiphenyl ether 249 18 305 g 50.1% 274

2541,3-Diphenoxybenzene 262 60 - s 11.3% 255 20 2541,3-Diphenoxybenzene 262 60 - =s 50.0% 274

2551,8-Dichloroan- 277 202 - s 11.5% 254 thraquinone

2551,8-Dichloroan- 277 202 - =s 9.7%a 274 thraquinone

25 2569,10-Dichloroanthracene 247 214 - g 11.4% 252

2569,10-Dichloroanthracene 247 214 - g 50.0% 302

2574,4'-Dibromobiphenyl 312 170 355 g 11.4% 234 2574,4'-Dibromobiphenyl 312 170 355 g 50.1% 302 2574,4'-Dibromobiphenyl 312 170 355 s 24.8% 242 TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POL Y (PHENYLENE SULFIDE). (PPS). IN VARIOUS ORGANIC COMPOUNDS

Approximate Ref. Molec. Melting Boiling Solub. Temp.

No. Compound Weight Point Point (g=>;s=<) (°c)

258 Benzophenone 182 50 305 g 50.4% 274

259 Polyphosphoric acid - - - s 4.4%a 302

2601-Chloronaphthalene 162 -20 258 s 10.0% 203 2601-Chloronaphthalene 162 -20 258 g 24.3% 236

2601-Chloronaphthalene 162 -20 258 s 49.8% 237

261 Diphenyl ether 170 27 259 =s 9.7% 247

262 l-Cyclohexyl-2- 167 - 302 s 9.5% 203 pyrrolidinone 262 l-Cyclohexyl-2- 167 - 302 g 24.6% 236 pyrrolidinone

262 l-Cyclohexyl-2- 167 - 302 s 50.0% 237 pyrrolidinone

262 l-Cyclohexyl-2- 167 - 302 g 50.2% 302 pyrrolidinone

263 l-Benzyl-2- 175 - - s 10.2% 233 pyrrolidinone

263 l-Benzyl-2- 175 - g 50.4% 302 pyrrolidinone 264 o.o'-Biphenol 186 109 315 g 49.9% 302

265 HB-40 (hydrogenated 244 - 325 g 49.4% 302 terphenyl) (Monsanto Co.) TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POLY(PHENYLENE SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS

Approximate Ref. Molec. Melting Boiling Solub. Temp.

No. Compound Weight Point Point (g=>;s=<) (°c)

266 Dioctyl phthalate 391 -50 384 s 10.0% 349

2675-Chloro-2- 170 191 - s 10.2%a 349 benzoxazolone 268 Dibenzothiophene 184 98 332 g 50.3% 302

269 Bis(4-chlorophenyl 287 146 412 s 9.9%a 349 sulfone)

270 Diphenyl phthalate 318 75 - g 24.8% 349 270 Diphenyl phthalate 318 75 - g 50.0%? 349 2712,6-Diphenylphenol 246 101 - g 49.9% 349

272 Diphenyl sulfide 186 -40 296 =s 49.4% 274

273 Diphenyl chlorophosphate 2 26699 - 360 s 10.0%a 349

274 Fluorene 166 113 298 =s 50.1% 274

275 Phenanthrene 178 100 340 g 49.9% 302 276 Sulfolane 120 27 285 s 10.0% 274

277 Methyl myristate 242 18 323 s 7.4% 302

278 Methyl stearate 299 38 358 s 10.1% 349

279 Phenothiazine 199 182 371 g 50.1% 349

280 Hexadecane 226 19 288 s 10.0% 274 281 Dimethyl phthalate 194 2 282 s 9.6% 274

282 Tetraethylene glycol 222 -30 275 s 9.8% 242 dimethyl ether

283 Diethylene glycol 218 -60 256 s 9.8% 242 dibutyl ether TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POLY(PHEN YLENE SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS

Ref. Molec. Melting Boiling Solub. Tem

No. Compound Weight Point Point (g=>;s=<) (°c

284 Docosane 311 44 369 s 5.2% 349

286 Dotriacontane 451 70 476 s 10.1% 349

2872,7-Dimethoxy- 188 138 - g 50.1% 274 naphthalene

2882,6-Dimethoxy- 188 153 g 50.1% 274 naphthalene

289 o-Terphenyl 230 58 337 g 49.9% 302

2904,4'-Dimethoxy- 242 142 g 50.0% 349 benzophenone

2919,10-Diphenyl- 330 246 g 50.0% 349 anthracene

2921,1-Diphenylethylene 180 6 270 =s 25.1% 243

2921,1-Diphenylethylene 180 6 270 s 48.8% 247 293 epsilon-Caprolactam 113 71 271 g 25.1% 242

293 epsilon-Caprolactam 113 71 271 s 50.1% 247

294 Tetraphenylethylene 332 223 420 s 9.8% 302

295 Pentafluorophenol 184 35 143 s 4.6% 141

296 Thianthrene 216 158 365 g 50.0% 302 297 l-Methyl-2- 99 -24 202 s 10.0% 203 pyrrolidinone

298 Pentachlorophenol 266 189 310 g 50.3%?a 302

299 Pyrene 202 150 404 g 50.0% 273

300 Benzanthrone 230 169 - s 50.0%ab 323 3019,9'-Bifluorene 330 247 - g 50.1% 275

302 Santowax R (Monsanto) - 145 364 g 50.0% 273

TABLE 1 (CONTINUED)

RELATIVE SOLUBILITY OF POLY(PHE YLENE SULFIDE), (PPS), IN VARIOUS ORGANIC COMPOUNDS Approximate Ref. Molec. Melting Boiling Solub. Temp.

No. Compound Weight Point Point (g=>;s= ) (°C)

303 Therminol 66 240 - 340 g 50. OX 273

(Monsanto Co.)

304 Therminol 75 - 70 385 g 50.02 273 (Monsanto Co.)

305 l-Phenyl-2- 161 68 345 g 50.0% 273 pyrrolidinone

3064,4'-Isopropyli- 228 156 402 s 50.02.ab 323 denediphenol 3064,4'-Isopropyli- 228 156 402 g 24.9%b 275 denediphenol

3074,4'-Dihydroxybenzo- 214 214 - s 10.3% 319 phenone a = Black or very dark color b ^•= reacts?

Table 2 below illustrates those organic compounds which dissolve at least 50 weight percent PPS. In Table 2, in the approximate solubility column, "g" represents "greater than" (>), "s" represents "less than" (<), and = represents "equal to". TABLE 2

ORGANIC COMPOUNDS WHICH DISSOLVE AT LEAST 50 WEIGHT PERCENT OF PPS

Ref. Approximate

No. Compound Solub. (g=^> s^=<) Temperature °C

2491-Methoxynaphthalene g 48.9% 247

265 HB-40 (hydrogenated g 49.4% 302 terphenyl)

2461-Ethoxynaphthalene g 49.8% 274

2121,3-Diphenylacetone g 49.8% 302

2321,4-Dibenzoylbutane g 49.8% 302

275 Phenanthrene g 49.9% 302

2534-Bromodiphenyl ether g 49.9% 302

2174-Benzoylbiphenyl g 49.9% 302

289 o-Terphenyl g 49.9% 302

2111,1-Diphenylacetone g 49.9% 302

264 o.o'-Biphenol g 49.9% 302

2712,6-Diphenylphenol g 49.9% 349

2031,2,3-Triphenylbenzene g 49.9% 349

202 Triphenylene g 49,9% 350

2524-Bromobiphenyl g 50.0% 258

2452-Phenylphenol g 50.0% 274

296 Thianthrene g 50.0% 302

2184,4'-Diphenyl g 50.0% 302 benzophenone

2263-Phenoxybenzyl alcohol g 50.0% 302 TABLE 2 CONTINUED

ORGANIC COMPOUNDS i WHICH DISSOLVE AT LEAST 50 WEIGHT PERCENT OF PPS

Ref, Approximate No. Compound (Solub. g^=> s=<) Tern perature °C

2444-Phenylphenol g 50.0% 302

256 9 , 10- Dichloroanthracene g 50.0% 302

238 p-Terphenyl g 50.0% 302

2282-Phenoxybiphenyl g 50.0% 302

201 Triphenylmethane g 50.0% 349

2904,4'-dimethoxybenzo- 9 50.0% 349 phenone

291 9 ,10-Diphenylanthracene g 50.0% 349

227 Fluoroanthene g 50.0% 349

208 Diphenyl sulfone g 50.0% 349

270 Diphenyl phthalate g 50.0% 349

221 Diphenyl carbonate g 50.0%?a 302

288 2, 6-Dimethoxy naphthalene g 50.0% 274

287 2, 7-Dimethoxy naphthalene g 50.0% 274

2534-Bromodiphenyl ether g 50.1% 274 TABLE 2 CONTINUED

ORGANIC COMPOUNDS WHICH DISSOLVE AT LEAST 50 WEIGHT PERCENT OF PPS

Ref. Approximate No. Compound Solub. (g=^>;s=^<) Temperature °C

2574,4'-Dibromobiphenyl g 50.1% 302

243 1-Phenylnaphthalene g 50.1% 302

279 Phenothiazine g 50.1% 349

231 2,5-Diphenyl-l,3,4- g 50.1% 349 oxadiazole

2092,5-Diphenyloxazole g 50.1% 349

200 Triphenylmethanol g 50.1%? 349

262 l-Cyclohexyl-2-pyrrolidinone g 50.2% 302

225 N,N-Diphenylformamide g 50.2% 302 216 m-Terphenyl g 50.2% 302

237 Benzil g 50.2% 302

239 Anthracene g 50.2% 302

2574,4'-Dibromobiphenyl g 50.2% 349 2174-Benzoylbiphenyl g 50.2% 349 235 Dibenzoylmethane g 50.2% 349

214 2-Biphenylcarboxylic acid g 50.2% 349 268 Dibenzothiophene g 50.3% 302 298 Pentachlorophenol g 50.3%?a 302

258 Benzophenone g 50.4% 274 263 l-Benzyl-2-pyrroTidinone g 50.4% 302

233 9-Fluorenone g 50.4% 302 TABLE 2 CONTINUED

ORGANIC COMPOUNDS WHICH DISSOLVE AT LEAST 50 WEIGHT PERCENT OF PPS

Ref. Approximate No. Compound Solub. g=^>;s=^< Temperature °C

2202-Benzoylnaρhthalene g 50.5% 349

2241-Bromonaphthalene g 50.6% 274

272 Diphenyl sulfide =s 49.4% 274

2541,3-Diphenoxybenzene =s 50.0% 274 274 Fluorene -s 50.1% 274

205 Tetraphenylmethane =s 50.3%? 349

299 Pyrene g 50.0% 273

301 9,9'-Bifluorene g 50.1% 275

305 l-Phenyl-2-pyrrolidinone g 50.0% 273 02 Santowax • g 50.0% 273

(Monsanto Co.)

(Chem. Abstracts # 26140-60-3) 03 Therminol 66 g 50.0% 273 (Monsanto Co.) (Chem. Abstracts # 61788-32-7) 04 Therminol 75 g 50.0% 273 (Monsanto Co.) (Chem. Abstracts # 26140-60-3 and 217-59-4 mixture) Polv(phenylene Sulfide) -- The polyiphenylene sulfide) (CAS No. 261 25-40-6) was purchased from Hoechst Celanese, Chatham, New Jersey, under the trade name FORTRON^®. The grade was either 0300 BO (powder), or 0300 PO (pellet). The manufacturer's literature indicates a melting point of 285-300°C. The melt flow was determined using a Tinius Olsen Extrusion Plastometer at 31 5°C, a weight of 21 60 g, and an orifice of 0.0825 in. (0.216 cm) wide, and a length of 0.31 5 in. (0.8 cm). The melt flow rate was 1 6.1 g/10 min. Amorphous Polymers

Polystyrene — The polystyrenes used were of two different grades. Polystyrene SYTRON^® Grade 685D is a general purpose polystyrene obtained from

Dow Chemical U.S.A., Midland, Michigan. This grade has a melt flow rate of 1 .6 gram per 10 minutes as measured by ASTM D-1 238 (Condition G), and a Vicat softening point of 108°C as measured by ASTM-1 525 (Rate B).

Polystryene STYRON^® Grade 666D is a general purpose polystyrene obtained from Dow Chemical U.S.A., Midland, Michigan. This grade has a melt flow rate of 8.0 gram per 10 min as measured by ASTM D-1 238 (Condition G), and a Vicat softening point of 99°C as measured by ASTM D-1 525 (Rate B).

Polysulfone is commercially available as UDEL™, from Amoco Chemical co., Grade 1700 and has a. melt index of 6.5 g/min at 660°F and 44 psi. Grade 3500 has a melt index of 3.5g/min at 660°F and 44 psi. Grade 3703 does not have a published melt index.

Poly(etherimide) is commercially available as ULTEM™, Grade 1000 from the General Electric Co.

EXAMPLE 1 PPS/DPS/POLYSTYRENE FILM

A mixture of 50 wt% poly(phenylene sulfide) (PPS) (Celanese FORTRON^® 300 Powder) and the solvent diphenyl sulfone (DPS) were compounded in a Welding Engineer twin screw extruder at approximately 290°C. The cooled polymer-solvent mixture was then ground to pellet size particles. The polymer-solvent mixture was mixed with the amorphous polymer polystyrene (Dow STYRON^® 685D) to produce a final (composition of 40wt% PPS/ 40wt% DPS/20 wt% STYRON. On the front of the extruder was a 2 in. (5.1 cm) long, 0.5 in. (1 .3 cm) diameter element KOCH™ mixing section and a 2.25 in. (5.7 cm) film die set at a gap thickness of approximately 25 mil (0.06 cm). The film die temperature was approximately 250°C. The extruded film was taken up and cooled on a 7.625 in. (1 9.4 cm) diameter roll running at 8 ft/min (2.4 m/min). The thickness of the film membrane after extrusion was 2 mil (0.005 cm). The film was soaked in methylene chloride for approximately 2 hrs. and dried. The properties of the porous film membrane produced were: N₂ flux = 6 x 10^"' cc/cm² sec cmHg

H₂0 flux = 1 .5 x 10⁵ ml/m² hr cmHg The pore size of the membrane was evaluated by a modified version of ASTM F-

31 6-86. The results were:

Mean pore size: 1 .7 micron

Max. pore size 4.6 micron

Examination of the membrane surface by scanning electron microscopy revealed that the surface of the membrane appeared to have pores of approximately 40 micron diameter.

Actual composition of the tertiary blend after the second extrusion was found to be 39.5/39.2/20.3 by Thermal Gravimetric Analysis (TGA).

BINARY FORMULATIONS A number of microporous membranes were produced using no organic compound solvent. The reaction conditions were described below in Examples 1 A to 1 D. Some results are summarized on Table 3 below.

EXAMPLE 1 A BINARY PPS/PS AMORPHOUS MICROPOROUS MEMBRANE Poly(phenylene sulfide) PPS and the amorphous polymer atactic polystyrene (PS) were used to prepare a porous film membrane. A mixture of 70 percent (by weight) of poly(phenylene sulfide) (Hoechst-Celanese, FORTON 300 PO) and 30 percent polystyrene (DOW Chemical, Styron 666) was prepared by combining pellets of the two polymers. The mixture of pellets was fed to a twin screw extruder, equipped with a static mixing element (Koch™, 2 in. (5.1 cm) long by 0.5 (1 .3 cm) in diameter), at 300°C and extruded into film form using a 2 in. (5.1 cm) film die. The film was taken up on a godet roll. The film was subsequently leached in methylene chloride and air dried to give a porous film membrane possessing a nitrogen flux of 0.036 cm³/cm² sec cmHg. The membrane has a water flux of 1 .6 x 1 0⁴ ml m² hr cmHg. Bubble point measurements (ASTM-F31 6-86) indicate a mean pore size of 2.4 microns and a maximum pore size of 9.2 microns. See Table 3, Example 1 A.

EXAMPLES 1 B, 1 C AND 1 D BINARY PPS/AMORPHOUS POLYMER HOLLOW FIBER MEMBRANES Hoechst Celanese FORTRON^R PPS, described previously, was used in it's powder form. Extrudable polymer blends were prepared by combining the PPS with pellets of either polysulphone or polyetherimide, mixing, and then extruding the binary blends through a 0.75 in. ( 1 .9 cm) in single screw extruder at 370°C. The blend was then chipped and reextruded through the single screw extruder with a hollow fiber spinnerette attached to form hollow fibers or tubules. The extrusion was accomplished using nitrogen as a core gas and chilled godet rolls to draw and collect the fiber. Melt pump speeds were maintained in all experiments at 30g/min/spinnerette-hole and a godet speed was maintained at 20ft/min (6 m/min). Hollow fibers were then leached in methylene chloride and tested for their membrane performance. The permeability results are summarized in Table 3 and examples 1 B, 1 C and 1 D. These fibers are useful for microfiltration. Table 3

BINARY PPS/AMORPHOUS POLYMER MICROPOROUS MEMBRANES

Exp PPS Second wt N₂ H₂0 Pore WT % Polymer % FLUX^e FLUX' MAX.

(microns)

1 A^a 70 PS 30 3.6x10 ^** 1 6,000 9.2

1 B^b 60 PEI 40 8x10^"5 5 <0.065

1 C^C 70 PEI 30 1 .7x10^'6 < 1 < 0.065

1 D^d 60 PSF 40 0.8x10^"2 2,054 0.44 (3304)

a. PS = polystyrene, mean pore size 2.4, thin sheet form. b. PEI = polyetherimide, mean pore size not measured, hollow fiber form. c. PEI = polyetherimide, mean pore size not measured, hollow fiber form. d. PSF = polysulfone, mean pore size not measured, hollow fiber form. e. cc/cm² sec cmHg. f. ml/m² hr cmHg.

EXAMPLE 2

PPS/DPS/POLYSTYRENE FILM

The polymer-solvent mixture was formulated in the same manner as described above in Example 1 and then mixed with the amorphous polymer polystyrene (Dow STYRON^® 685D) to give a final composition of 42.5 wt% PPS/ 42.5 wt% DPS/ 1 5 wt% STYRON™. The extrusion conditions for this process were the same as the one in Example 1 . The properties of the porous film membrane produced were: N₂ flux = 1 x 10^"4 cc/cm² sec cmHg

H₂0 flux = unmeasurable

The pore size of the membrane could not be evaluated by present apparatus. 5 The actual composition of the tertiary blend PPS/DPS/STYRON after the second extrusion was determined to be 45.7/41 .7/1 2.6 by TGA.

EXAMPLE 3 PPS/TERP/PS FILM A tertiary blend of 33 wt% poly(phenylene sulfide) (PPS) FORTRON™300 powder), 1 0 37 wt% hydrogenated terphenyl (Monsanto) (HB 40™), and 30 wt% polysulfone (PSF) Amoco UDEL™ 1 700, high molecular weight, pellets) was prepared with a resin kettle blending setup at 260°C. The cooled blend was ground to pellet size particles. This tertiary blend in pellet form was extruded with a Welding Engineer twin screw extruder at approximately 290°C. On the front of the extruder was a 2 in. (5.1 cm) long by 0.5 1 5 in. (1 .3 cm) diameter element KOCH™ mixing section, and a 2.25 in. (5.7 cm) film die set by a gap thickness of approximately 25 mil (0.06 cm). The film die temperature was approximately 270°C. The extruded film was taken up and cooled on a 7.625 in. ( 1 9.4 cm) diameter roll running at 4.5 ft/min (1 .35 m/min).

The film was soaked in methylene chloride for overnight and then vacuum dried. 0 The properties of the porous film membranes produced were: N₂ flux = 3.66 x 10^~1 cc/sec cm² cmHg

H₂0 flux = 5.49 x 1 0⁴ cc/hr m² cmHg

The pore size of the membrane was evaluated by a modified version of ASTM F- 31 6-86. The results were as follows: 25 Mean pore size: 0.49 micron

Max. pore size: 3.08 micron

The thickness of the membrane was 1 .31 6 mm.

EXAMPLE 4

PPS/TERP/PS FILM 0 A tertiary blend of 33 wt% poly(phenylene sulfide) (PPS) (Celanese

FORTRON™300 powder), 37 wt% hydrogenated terphenyl (Monsanto) (HB 40™), and

30 wt% polysulfone (PSF) (Amoco UDEL™ 3500, extrusion grade pellets) was prepared with a resin kettle blending setup at around 260°C. The cooled blend was ground to pellet size particles. This tertiary blend in pellet form was extruded with a Welding

35 Engineer twin screw extruder at approximately 290°C. On the front of the extruder was a 2 in. (5.1 cm) long, 0.5 in. ( 1 .3 cm) diameter element KOCH™ mixing section, and 2.25 in. (5.7 cm) film die set by a gap thickness of approximately 25 mil. The film die temperature was approximately 270°C. The extruded film was taken up and cooled on a 7.625 in. (1 9.4 cm) diameter roll running at 3.6 ft/min (1 .1 m/min).

The film was soaked in methylene chloride overnight and vacuum dried. The 5 properties of the porous film membranes formed were:

N J₂₂ flux = 1 .45 x 10^"2 cc/sec cm² cmHg

H 1₂₂0( flux = 5.03 x 10² cc/hr m² cmHg

The pore size of the membrane was evaluated by a modified version of ASTM F- 31 6-86. The results were: 10 Mean pore size: 0.1 5 micron;

Max. pore size: 0.77 micron.

The thickness of the membrane was 1 .321 mm.

EXAMPLE 5 PPS/TERP/PSF FILM 1 5 (a) A tertiary blend of 33 wt% poly(phenylene sulfide) (PPS) (Celanese

FORTRON^'"300 powder), 37 wt% hydrogenated terphenyl (Monsanto) (HB 40^"), and 30 wt% polysulfone (PSF) (Amoco UDEL~3703, low molecular weight, pellets) was prepared with a resin kettle blending setup at around 260°C. The cooled blend was ground to pellet size particles. This tertiary blend in pellet form was extruded with a Welding 20 Engineer twin screw extruder at approximately 290°C. On the front of the extruder was a 2 in. (5.1 cm) long, 0.5 in. (1 .3 cm) diameter element KOCH™ mixing section, and a 2.25 in. (5.7 cm) film die set by a gap thickness of approximately 25 mil (0.06 cm). The film die temperature was approximately 270°C. The extruded film was taken up and cooled on a 7.625 in. (19.4 cm) diameter roll running at 3 ft/min (0.9 m/min). 25 The film was soaked in methylene chloride for overnight and then vacuum dried.

The properties of the porous film membranes formed were: N2 flux = 5.8 x 10^"1 cc/sec cm² cmHg H₂0 flux = 1 .20 x 10⁵ cc/hr m² cmHg

The pore size of the membrane was evaluated by a modified version of ASTM F- 30 31 6-86. The results were:

Mean pore size: 0.67 micron;

Max. pore size: 3.08 micron.

The thickness of the membrane is 1 .496 mm.

EXAMPLE 6 35 PPS/TERP/PSF FILM

(a) A tertiary blend of 33 wt% poly(phenylene sulfide) (PPS) (Celanese FORTRON^"300 powder), 47 wt% hydrogenated terphenyl (Monsanto) (HB40^™, and 20 wt% polysulfone (PSF)(Amoco UDEL^" 1 700, high molecular weight, pellets) was prepared with a resin kettle blending setup at about 260°C. The cooled blend was ground to pellet size particles. This tertiary blend in pellet form was extruded with a Welding Engineer 5 twin screw extruder at approximately 290°C. On the front of the extruder was a 2 in. (5.1 cm) long, 0.5 in. ( 1 .3 cm) diameter element KOCH™ mixing section, and a 2.25 in. (5.7 cm) film die set by a gap thickness of approximately 25 mil (0.06 cm). The film die temperature was approximately 270°C. The extruded film was taken up and cooled on a 7.625 in. ( 1 9.4 cm) diameter roll running at 10 ft/min (3 m/min). 10 The film was soaked in methylene chloride overnight and then vacuum dried. The properties of the porous film membranes formed when the roller was running at 10 ft/min. were:

N₂ flux = 3.67 x 10^"3 cc/sec cm² cmHg

H₂0 flux = 3.35 x 10² cc/hr m² cmHg

1 5 The pore size of the membrane was evaluated by a modified version of ASTM F-31 6-86. The results were:

Mean pore size: < 0.1 micron

Max. pore size: 0.26 micron

The membrane had a thickness of 0.582 mm. 20 (b) Example 6 (a) was repeated except that the roller speed was 1 6 ft/min. The membrane had the following properties:

N₂ flux = 4.62 x 1 0^"3 cc/cm² sec cmHg

H₂0 flux = 4.92 x 10² cc/hr m² cmHg

The pore size of the membrane was evaluated by a modified version of ASTM F- 25 31 6-86. The results were:

Mean pore size: < 0.1 micron

Max. pore size: 0.23 micron

The membrane had a thickness of 0.405 mm.

(c) Example 6(a) was repeated except that the roller speed was 20 ft/min (6 30 m/min).

The membrane had the following properties:

N₂ flux = 5.94 x 10^"3 cc/sec cm² cmHg

H₂0 flux = 6.37 x 10² cc/hr m² cmHg.

The pore size of the membrane was evaluated by a modified version of ASTM F- 35 31 6-8. The results were:

Mean pore size: < 0.1 micron Max. pore size: 0.27 micron

The thickness of the membrane was 0.396 mm.

EXAMPLE 7 PPS/DPIP-DPTP/PSF FIBER 40% PPS, 40% diphenyl isophthalate/diphenyl terephthalate (75/25 w/w), 20% polysulphone. The spin rate 80 ft/min (24.1 m/min), quench room temperature water 10 in. (25.4 cm) from spinnerette face, ID = 550 micrometers, initial weight of sample = 1 .48 g; weight post methylene chloride leach = 0.61 g = 41 % PPS. N₂ flux = 0.24 cc/cm² sec cmHg H₂0 flux = 90,000 cc/m² hr cmHg bubble point = 8 psi (55 x 10³ Pa)

Max. pore size = 1 .1 micrometer.

EXAMPLE 8 PPS/CLTM/PS FIBER 40% PPS, 40% caprolactam, 20% polysulphone. The spin rate 1 20 ft/min. (36 m/min), quench room temperature water 1 5 in. (38 cm) from spinnerette face initial weight of sample - 2.36 g, final weight - 1 .05 g = 44% PPS fiber. N₂ flux = 0.10 cc/cm² sec cmHg

H₂0 flux = 42,500 cc/m² hr cmHg bubble point = 12 psi (83 x 10³ Pa)

Max. pore size = 0.75 micrometer.

EXAMPLE 9 PPS/CLTM/PS FIBER 35% PPS, 45% epsilon caprolactam, 20% polysulphone . The spin rate 140 ft/min (42 m/min), quench room temperature water 1 5 in. (38 cm) from spinnerette face. Initial weight of sample = 1.60 grams; final weight = 0.69_g = 43% PPS. N₂ flux = 0.012 cc/cm² sec cmHg

Bubble point = 19 psi (13.1 x 10⁴ Pa)

Max pore size = 0.5 micrometers. EXAMPLE 10

PPS/HB-40/PS FIBER 40% PPS, 40% Monsanto^® HB-40 heat transfer fluid, 20% polysulphone. The spin rate 90 ft/min (27 m/min), room temperature water quench 20 in. 50.8 cm) from face. The initial sample weight = 4.26 g, final weight = 1 .84 g = 43% PPS, fiber 500 micrometer ID.

N₂ flux = 0.0010 cc/cm² sec cmHg Bubble point = > 1 00 psi (6.9 x 1 0⁵ Pa)

Max pore size = < 0.09 micrometers.

EXAMPLE 1 1 PPS/PS HB-40/IRGANOX HOLLOW FIBER MEMBRANE 33% PPS, 30% polysulphone, 37% HB-40, 0.2% lrganox^R (antioxidant), spin rate

= 1 50 ft/min (45 m/min), water quench 1 5 in. (38 cm) from spinnerette face 300 micrometer ID. 35% . PPS following methylene chloride leach =

N₂ flux = 3.5 x 10^"2 cc/cm² sec cmHg

H²0 flux = 1 5,000 cc/m² hr cmHg Bubble point = 1 8 psi ( 1 .2 x 10⁵ Pa)

Max. pore size = 0.5 micrometer.

EXAMPLE 1 2 PPS/HB 40/PEI HOLLOW FIBER MEMBRANE 40% PPS, 40% HB-40, 20% poly(ethermide)(PEI) was spun at a spin rate 140 ft/min (42 m/min). No quench bath. Draw zone 1 5 in. (38 cm), ID-350 micron. Initial weight = 5.61 g, final weight = 2.47g, 44%PPS methylene chloride leach. N₂ flux = 0.007 cc/cm² sec cmHg

H₂0 flux = Not available

Bubble point = 75 psi (5.2 x 10⁵ Pa) Max pore size = 0.1 2 micron

EXAMPLE 1 3 PPS/HB 40/PEI HOLLOW FIBER MEMBRANE 33 % PPS, 42% HB-40, 25 % PEI. The spin = rate 1 60 ft/min (48 m/min). No quench bath. Draw zone = 1 5 in. (38 cm), 200 micron ID, methylene chloride leach bath, 36% PPS.

N₂ flux = 0.021 cc/cm² sec cmHg

H₂0 flux = 3000 cc/m² hr cmHg

Bubble point = 77 psi (5.3 x 10⁵ Pa)

Max. pore size = 0.1 2 micron EXAMPLE 14

PPS/HB 40/PEI HOLLOW FIBER MEMBRANE 28% PPS, 25% PEI, 47% HB-40; 60ft/min (1 8 m/min) draw zone = 24 in. (60.1 cm), ID = 500 micrometers. No quench bath, 31 % PPS after methylene chloride leach. N₂ flux = 0.034 cc/cm² sec cmHg H₂0 flux = 3,000 cc/m² hr cmHg

Bubble point = 1 8 psi (1 .2 x 10⁵ Pa) Max. pore size = 0.5 micron

While only a few embodiments of the invention have been shown and described herein, it will become apparent to those skilled in the art that various modifications and changes can be made in the fabrication of microporous poly (phenylene sulfide) polymers for use as membranes in the separation of components of a fluid mixture without departing from the spirit and scope of the present invention. All such modifications and changes coming within the scope of the appended claims are intended to be carried out thereby.

Claims

WE CLAIM:

1 . A process for preparing a microporous membrane from a poly(phenylene sulfide) polymer comprising the steps of:

A. forming a mixture comprising:

(i) at least one polyiphenylene sulfide) polymer, (ii) at least one amorphous polymer which is substantially stable at elevated temperatures, which possesses a glass transition temperature of at least about -1 00°C, and wherein said amorphous polymer is at least partially immiscible in said poly(phenylene sulfide) polymer at ambient conditions; and (iii) optionally a plasticizer comprising at least one organic compound capable of dissolving at least about 10 weight percent of said polyiphenylene sulfide) polymer at the extrusion or casting temperature;

B. heating the mixture to a temperature at which said mixture becomes a fluid;

C. extruding or casting said fluid under conditions such that a membrane is formed;

D. subjecting said membrane to controlled cooling or coagulation by passing said membrane through at least one zone under conditions such that said membrane solidifies;

E. leaching said membrane by passing said membrane through at least one zone under conditions such that at least a portion of said optional plasticizer for said poly(phenylene sulfide) polymer, at least a portion of said amorphous polymer, or a combination thereof, is removed from said membrane; and

F. producing a final microporous membrane.

2. The process of Claim 1 which comprises the additional step of:

G. before leaching, during leaching, after leaching, or a combination thereof, drawing said membrane to increase the flux of fluid through said membrane, while said membrane is at a temperature above about 25 °C and below the melting point of said polyfphenylene sulfide) polymer, or poly(phenylene sulfide) and amorphous polymer mixture, or polyfphenylene sulfide), amorphous polymer, and plasticizer mixture before and during leaching and for polyfphenylene sulfide) after leaching.

3. The process of Claim 2 wherein said amorphous polymer is selected from the group consisting of polysulfones; polyarylsulfones; polyethersulfones; styrene copolymers; polyetherimides, polyetherimide copolymers; ethylene copolymers; amorphous polyesters; amorphous cellulose esters; polycarbonates; polystyrenes; polysiloxanes; polyacrylates; polymethacrylates; poly(vinylacetates); polybenzimidazoles; and polyacrylamides.

4. The process of Claim 3 wherein said plasticizer is present and comprises at least one solvent consisting predominantly of carbon and hydrogen and optionally oxygen, nitrogen, sulfur, halogen, and mixtures thereof, wherein said solvent has a molecular weight of between about 1 60 and about 650, contains at least one 5, 6 or 7- membered ring structure, and possesses a boiling point of between about 1 50°C and about 480°C.

5. The process of Claim 4 wherein said plasticizer comprises at least one solvent selected from the group consisting of 4,4'-dibromobiphenyl; 1 - phenylnaphthalene; phenothiazine; 2,5-biphenyl-1 ,3,4-oxadiazole; 2,5-diphenyloxazole; triphenylmethanol; N,N-diphenylformamide; m-terphenyl; benzil; anthracene; 4- benzoylbiphenyl; dibenzoylmethane; 2-biphenylcarboxylic acid; dibenzothiophene; pentachlorophenol; benzophenone; 1 -benzyl-2-pyrrolidinone; 9-fluorenone; 2- benzoylnaphthalene; 1 -bromomaphthalene; diphenyl sulfide; 1 ,3 diphenoxybenzene; fluorene; tetraphenylmethane; p-quaterphenyl; 1 -phenyl-2-pyrrolidinone; 1 - methoxynaphthalene; hydrogenated and partially hydrogenated terphenyl; 1 - ethoxynaphthalene; 1 ,3-diphenylacetone; 1 ,4-dibenzoylbutane; phenanthrene; 4- benzoylbiphenyl; o-terphenyl; 1 ,1 -diphenylacetone; o,o'-biphenol; 2,6-diphenylphenol;

1 ,2,3,-triphenylbenzene; triphenylene; 4-bromobiphenyl; 2-phenylphenol; thianthrene;

4,4'-diphenylbenzophenone; 3-phenoxybenzyl alcohol; 4-phenylphenol; 9, 10- dichloroanthracene; p-terphenyl; 2-phenoxybiphenyl; triphenylmethane; 4,4'- dimethoxybenzophenone; 9,10-diphenylanthracene; fluoranthene; diphenyl sulfone; diphenyl phthalate, diphenyl terephthalate; diphenyl isophthalate; diphenyl carbonate;

2,6-dimethoxynaphthalene; 2,7-dimethoxynaphthalene; 4-bromodiphenyl ether; pyrene;

9,9'-bifluorene; 4,4'-isopropylidenediphenol; 2,4,6-trichlorophenol; epsilon-caprolactam;

1 -cyclohexyl-2-pyrrolidinone; and mixtures of these compounds.

6. The process of Claim 5 wherein said plasticizer further comprises at least one non-solvent consisting predominantly of carbon and hydrogen and optionally oxygen, phosphorus, silicon, nitrogen, sulfur, halogen, and mixtures thereof, wherein said non- solvent has a molecular weight of between about 1 20 and about 650 and possesses a boiling point of between about 150°C and about 480°C.

7. The process of Claim 6 wherein said plasticizer comprises at least one non- solvent selected from the group consisting of 1 ,3,5-triphenylbenzene, tetraphenylsilane, diphenyl sulfoxide, diphenic acid, 4-acetylbiphenyl, bibenzyl, diphenyl methyl phosphate, triphenyl phosphate, cyclohexyl phenyl ketone, mineral oil, butyl stearate, phenyl benzoate, 1 -phenyldecane, 1 ,3-diphenoxybenzene, 1 ,8-dichloroanthraquinone, polyphosphoric acid, dioctyl phthalate, 5-chlorobenzoxazolone, bis-(4-chlorophenol sulfone), diphenyl chlorophosphate, sulfolane, methyl myristate, methyl stearate, hexadecane, dimethyl phthalate, tetraethylene glycol dimethyl ether, diethylene glycol dibutyl ether, docosane, dotriacontane, tetraphenylene, pentafluorophenol, paraffin oil, 1 -methyl-2-pyrrolidinone, and 4,4'-dihydroxybenzophenone.

8. The process of Claim 7 wherein the amount of poly(phenylene sulfide) polymer in the polymer-plasticizer mixture is between about 1 0 weight percent and about 90 weight percent.

9. The process of Claim 8 wherein the membrane is drawn in Step G at a temperature of between about 25 °C and about 273 °C.

10. The process of Claim 9 wherein said membrane is drawn to a draw ratio of between about 1 .1 and about 40.

1 1 . The process of Claim 9 wherein said fluid is extruded at a temperature of between about 100°C and about 400°C.

1 2. The process of Claim 1 1 wherein said membrane is subjected to controlled cooling or coagulation at a temperature of between about 0°C and about 275 °C.

1 3. The process of Claim 1 2 wherein said controlled cooling zone comprises a gaseous environment.

14. The process of Claim 1 3 wherein said membrane is leached at a temperature of between about 0°C and about 275 °C.

1 5. The process of Claim 14 wherein said leach zone comprises a liquid selected from the group consisting of toluene, xylene, acetone, methyl ethyl ketone, N- methylpyrrolidinone, water, an acid or alkali aqueous solution, and chlorinated hydrocarbons.

1 6. The process of Claim 8 wherein said final membrane is useful for ultrafiltration, microfiltration, or macrofiltration, or as a composite membrane support.

1 7. The process of Claim 1 6 wherein said final membrane possesses a porosity in the range of about 10 percent to about 90 percent.

1 8. The process of Claim 1 7 wherein the mean pore size of said membrane is in the range of about 5 Angstroms to about 1 ,000 Angstroms for ultrafiltration, about 0.02 micron to about 1 0 microns for micro-filtration, and about 10 microns to about 50 microns for macrofiltration.

1 9. The process of Claim 1 8 wherein said membrane possesses a nitrogen flux of at least about

10^"4 cm³(STP). cm² sec cmHg

20. The process of Claim 18 wherein said membrane possesses a water flux of at least about

10 ml m² hr cmHg

21 . The process of Claim 2 which further comprises the additional step of: H. before leaching, after leaching, before drawing, after drawing, or a combination thereof, annealing said membrane by exposing said membrane to a temperature above the glass transition temperature of the poly(phenylene sulfide) polymer or the poly(phenylene sulfide) polymer and plasticizer mixture and about 10°C below the melting point of the poly(phenylene sulfide) polymer or depressed melting point of the polyfphenylene sulfide) polymer and plasticizer mixture for a period of time between about 30 seconds and about 24 hours.

22. The membrane of Claim 8 wherein said poly(phenylene sulfide) polymer has a degree of crystallinity of at least about 10 percent and a melting point of at least about 1 90°C.

23. The process of Claim 1 wherein said amorphous polymer is selected from the group consisting of polysulfones; polyarylsulfones; polyethersulfones; styrene copolymers; polyetherimides, polyetherimide co-polymers; ethylene copolymers; amorphous polyesters; amorphous cellulose esters; polycarbonates; polystyrenes; polysiloxanes; polyacrylates; polymethacrylates; poly(vinylacetates); polybenzimidazoles; and polyacrylamides.

24. The process of Claim 23 wherein said plasticizer is present and comprises at least one solvent consisting predominantly of carbon and hydrogen and optionally oxygen, nitrogen, sulfur, halogen, and mixtures thereof, wherein said solvent has a molecular weight of between about 1 60 and about 650, contains at least one 5,6 or 7- membered ring structure, and possesses a boiling point of between about 1 50°C and about 480°C.

25. The process of Claim 24 wherein said plasticizer comprises at least one solvent selected from the group consisting of 4,4'-dibromobiphenyl; 1 -phenylnaphthalene; phenothiazine; 2,5-piphenyl-1 ,3,4-oxadiazole; 2,5-diphenyloxazole; triphenylmethanol; N,N-diphenylformamide; m-terphenyl; benzil; anthracene; 4-benzoylbiphenyl; dibenzoylmethane; 2-biphenylcarboxylic acid; dibenzothiophene; pentachlorophenol; benzophenone; 1 -benzyl-2-pyrrolidinone; 9-fluorenone; 2-benzoylnaphthalene; 1 - bromomaphtha lene ; diphenyl sulfide; 1 , 3-d iphenoxybenzene ; fluorene; tetraphenylmethane; p-quaterphenyl; 1 -phenyl-2-pyrrolidinone; 1 -methoxynaphthalene; hydrogenated and partially hydrogenated terphenyl; 1 -ethoxynaphthalene; 1 ,3- diphenylacetone; 1 ,4-dibenzoylbutane;phenanthrene;4-benzoylbiphenyl; o-terphenyl; 1 , 1 - diphenylacetone; o,o'-biphenol; 2,6-diphenylphenol; 1 ,2,3,-triphenylbenzene; triphenylene; 4-bromobiphenyl; 2-phenylphenol; thianthrene; 4,4' diphenylbenzophenone; 3- phenoxybenzyl alcohol; 4-phenylphenol; 9, 10-dichloroanthracene; p-terphenyl; 2- phenoxybiphenyl ; triphenylmethane ; 4,4'-dimethoxybenzophenone; 9 , 1 0- diphenylanthracene; fluoranthene; diphenyl sulfone; diphenyl phthalate; diphenyl terephthalate; diphenyl isophthalate; diphenyl carbonate; 2,6-dimethoxynaphthalene; 2,7- dimethoxynaphthalene; 4-bromodiphenyl ether; pyrene; 9,9'-bifluorene; 4,4'- isopropylidenediphenol; 2,4,6-trichlorophenol; epsilon-caprolactam; 1 -cyclohexyl-2- pyrrolidinone; and mixtures of these compounds.

26. The process of Claim 25 wherein said plasticizer further comprises at least one non-solvent consisting predominantly of carbon and hydrogen and optionally oxygen, phosphorus, silicon, nitrogen, sulfur, halogen, and mixtures thereof, wherein said non- solvent has a molecular weight of between about 1 20 and about 650 and possesses a boiling point of between about 1 50°C and about 480°C.

27. The process of Claim 26 wherein said plasticizer comprises at least one non-solvent selected from the group consisting of 1 ,3,5-triphenylbenzene, tetraphenylsilane, diphenyl sulfoxide, diphenic acid, 4-acetylbiphenyl, bibenzyl, diphenyl methyl phosphate, triphenyl phosphate, cyclohexyl phenyl ketone, mineral oil, butyl stearate, phenyl benzoate, 1 -phenyldecane, 1 ,3-diphenoxybenzene, 1 ,8- dichloroanthraquinone, polyphosphoric acid, dioctyl phthalate, 5-chlorobenzoxazolone, bis- (4-chlorophenol sulfone), diphenyl chlorophosphate, sulfolane, methyl myristate, methyl stearate, hexadecane, dimethyl phthalate, tetraethylene glycol dimethyl ether, diethylene glycol dibutyl ether, docosane, dotriacontane, tetraphenylene, pentafluorophenol, paraffin oil, 1 -methyl-2-pyrrolidinone, and 4,4'-dihydroxybenzophenone.

28. The process of Claim 27 wherein the amount of poly(phenylene sulfide) polymer in the polymer-plasticizer mixture is between about 10 weight percent and about 90 weight percent.

29. The process of Claim 28 wherein said fluid is extruded at a temperature of between about 100°C and about 400°C.

30. The process of Claim 29 wherein said membrane is subjected to controlled cooling or coagulation at a temperature of between about 0°C and about 275 °C.

31 . The process of Claim 30 wherein said controlled cooling zone comprises a gaseous environment.

32. The process of Claim 31 wherein said membrane is leached at a temperature of between about 0°C and about 275 °C.

33. The process of Claim 32 wherein said leach zone comprises a liquid selected from the group consisting of toluene, xylene, acetone, methyl ethyl ketone, N- methylpyrrolidinone, water, an acid or alkali aqueous solution, and chlorinated hydrocarbons.

34. The process of Claim 28 wherein said final membrane is useful for ultrafiltration, microfiltration, or macrofiltration, or composite membrane support.

35. The process of Claim 34 wherein said final membrane possesses a porosity in the range of about 10 percent to about 90 percent.

36. The process of Claim 35 wherein the mean pore size of said membrane is in the range of about 5 Angstroms to about 1 ,000 Angstroms for ultrafiltration, about 0.02 micron to about 10 microns for micro-filtration, and about 10 microns to about 50 microns for macrofiltration.

37. The process of Claim 36 wherein said membrane possesses a nitrogen flux of at least about

10^"4 cm³(STP). cm² sec cmHg

38. The process of Claim 36 wherein said membrane possesses a water flux of at least about

10 ml . m² hr cmHg

39. The process of Claim 23 which further comprises the additional step of: I. before leaching, after leaching, or a combination thereof, annealing said membrane by exposing said membrane to a temperature above the glass transition temperature of the poly(phenylene sulfide) polymer, or the poly(phenylene sulfide) polymer and plasticizer mixture and about 10°C below the melting point of the poly(phenylene sulfide) polymer or the depressed melting point of the poly(phenylene sulfide) polymer and plasticizer mixture for a period of time between about 30 seconds and about 24 hours.

40. The membrane of Claim 23 wherein said poly(phenylene sulfide) polymer has a degree of crystallinity of at least about 10 percent and a melting point of at least about 1 90°C.