Title of Invention

A PROCESS FOR PRODUCING AN INTEGRALLY ASYMMETRICAL HYDROPHOBIC MEMBRANE AND THE MEMBRANE PREPARED THEREBY

Abstract

The invention relates to a method for producing an integrally asymmetrical hydrophobic polyolefinic membrane with a sponge-like, open-pored microporous support structure and an separating layer with a structure which is denser than the support structure, by means of a thermally induced liquid-liquid phase separation process. A solution of at least one polyolefin in a solvent system consisting of a compound A and a compound B, is extruded to obtain a shaped body. Compound A is a weak solvent and compound B is a non-solvent for the polymer. After leaving the moulding tool, the shaped body is cooled using a solid or liquid cooling medium which will not dissolve the polymer at temperatures up to the temperature of the tool and which will not chemically react with the polymer, until phase separation occurs and the polymer-rich phase hardens.

Full Text

Integrally asymmetrical polyolefin membrane Description: The invention relates to a process for producing a hydrophobic membrane using a thermally induced phase separation process in accordance with the preamble of Claim 1, the membrane having a sponge-like, open-pored, microporous structure. The invention relates further to a hydrophobic integrally asymmetrical membrane that is suited in particular for gas exchange and is composed primarily of at least one polymer selected from the group of polyolefins and has first and second surfaces, the membrane having a support layer with a sponge-like, open-pored, microporous structure and adjacent to this support layer on at least one of the surfaces a separa-tioh layer with denser structure, and to the use of such a membrane for blood oxygenation. In a multitude oT applications in the fields of chemistry, biochemistry, or medicine, the problem arises of separating gaseous components from liquids or adding such components to the liquids. For such gas exchange processes, there is increasing use of membranes that serve as a separation membrane between the respective liquid, irom wnich a gaseous component is to be separated or to which a gaseous component IS to be added, and a fluid that serves to absorb or release this gaseous component. The fluid in this case can be either a gas or a liquid containing the gas com-poneni to be exchanged or capable of absorbing it. Using such membranes, a large exchange surface can be provided for gas exchange and, if required, direct contact between the liquid and fluid can be avoided. An important application of membrane-based gas exchange processes in the medical field is for oxygenators, also called artificial lungs. In these oxygenators, which are used in open-heart operations, for example, oxygenation of blood and removal of carbon dioxide from the blood take place. Generally, bundles of hollow-fiber membranes are used for such oxygenators. Venous blood flows in this case in the exterior space around the hollow-fiber membranes, while air, oxygen-enriched air, or even pure oxygen, i.e., a gas, is passed through the lumen of the hollow-fiber membranes. Via the membranes, there is contact between the blood and the gas, enabling transport of oxygen into the blood and simultaneously transport of carbon dioxide from the blood into the gas. In order to provide the blood with sufficient oxygen and at the same time to remove carbon dioxide from the blood to a sufficient extent, the membranes must ensure a high degree of gas transport: a sufficient amount of oxygen must be transferred from the gas side of the membrane to the blood side and, conversely, a sufficient amount of carbon dioxide from the blood side of the membrane to the gas side, i.e., the gas flow or gas transfer rates, expressed as the gas volume transported per unit of time and membrane surface area from one membrane side to the other, must be high. A decisive influence on the transfer rates is exerted by the porosity of the membrane, since only in the case of sufficiently high porosity can adequate transfer rates be attained. A number of oxygenators are in use that contain hollow-fiber membranes with open-pored, microporous structure. One way to produce this type of membrane for gas exchange, such as for oxygenation, is described in DE-A-28 33 493. Using the process in accordance with this specification, membranes can be produced from meltable thermoplastic polymers with up to 90% by volume of interconnected pores. The process is based on a thermally induced phase separation process with liquid-liquid phase separation. In this process, a homogeneous single-phase melt mixture is first formed from the thermoplastic polymer and a compatible component that forms a binary system with the polymer, the system in the liquid state of aggregation having a range of full miscibility and a range with a miscibility gap, and this melt mixture is then extnjded into a bath that is substantially inert with respect to, i.e., does not substantially react chemically with, the polymer and has a temperature lower than the demixing temperature. In this way, a liquid-liquid phase separation is initiated and, on further cooling, the thermoplastic polymer solidified to form the membrane structure. An improved process for producing such membranes, which permits specific adjustment of the pore volume, size, and wall, is disclosed in DE-A-32 05 289. In this process, 5-90% by weight of a polymer is dissolved, by heating to above the critical demixing temperature, in 10-95% by weight of a solvent system of first and second compounds, which are liquid and miscible with each other at the dissolving temperature, to form a homogeneous solution, whereby the employed mixture of polymer and the cited compounds has a miscibility gap in the liquid state of aggregation below the critical demixing temperature, the first compound is a solvent for the polymer, and the second compound increases the phase separation temperature of a solution consisting of the polymer and the first compound. The solution is then given shape and, by cooling in a cooling medium consisting of the first compound or the employed solvent system, is brought to demixing and solidifying of the high-polymer-content phase, and the cited compounds are subsequently extracted. The membranes disclosed in accordance with DE-A-28 33 493 or DE-A-32 05 289 have an open-pored, microporous structure and also open-pored, microporous surfaces. On the one hand, this has the result that gaseous substances, such as oxygen (O2) or carbon dioxide (CO2), can pass through the membrane relatively unrestricted and the transport of a gas then takes place as a Knudsen flow, combined with relatively high transfer rates for gases or high gas flow rates through the membrane. Such membranes with gas flow rates for CO2 exceeding 5 ml/{ cm^*min*bar) and for O2 at approximately the same level have gas flow rates that are sufficiently high for oxygenation of blood. On the other hand, however, in extended-duration use of these membranes in blood oxygenation or generally in gas exchange processes with aqueous liquids, blood plasma or a portion of the liquid can penetrate into the membrane and, in the extreme case, exit on the gas side of the membrane, even if in these cases the membranes are produced from hydrophobic polymers, in particular polyolefins. This results in a drasfic decrease in gas transfer rates. In the medical area of blood oxygenation, this is termed plasma breakthrough. The plasma breakthrough time of such membranes, as producible in accordance with DE-A-28 33 493 or DE-A-32 05 289, is sufficient in most cases of conventional blood oxygenation to oxygenate a patient in a normal open-heart operation. However, the desire exists for membranes with higher plasma breakthrough times in order to attain higher levels of safety in extended-duration heart operations and to rule out the possibility of a plasma breakthrough that would require immediate replacement of the oxygenator. The aim, however, is also to be able to oxygenate premature infants or in general patients with temporarily restricted lung function long enough until the lung function is restored, i.e., to be able to conduct extended-duration oxygenation. A prerequisite for this is appropriately long plasma breakthrough times. A frequently demanded minimum value for the plasma breakthrough time in this connection is 20 hours. From EP-A-299 381, hollow-fiber membranes for oxygenation are known that have plasma breakthrough times of more than 20 hours, i.e., there is no plasma breakthrough even under extended use. With the otherwise porous membrane, this is attained by a barrier layer that has an average thickness, calculated from the oxygen and nitrogen flow, not exceeding 2 pm and is substantially impermeable to ethanol. The membrane is substantially free of open pores, i.e., pores that are open both to the outside and to the inside of the hollow-fiber membrane. According to the disclosed examples, the membranes in accordance with EP-A-299 381 have a porosity of at most 31 % by volume, since at higher porosity values the pores are interconnected and communication occurs between the sides of the hollow-fiber membranes, resulting in plasma breakthrough. In the barrier layer, the transport of gases to be exchanged occurs by solution diffusion. The production of these membranes is conducted via a melt-drawing process, i.e., the polymer is first melt-extruded to form a hollow fiber and then hot- and cold-drawn. In this case, only relatively low porosity values are obtained, which means that, in conjunction with the transport occurring in the barrier layer via solution diffusion, the attainable transfer rates for oxygen and carbon dioxide remain relatively low. Moreover, while the hollow-fiber membranes in accordance with EP-A-299 381 exhibit sufficient tensile strength as a result of the pronounced drawing in conjunction with manufacture, they have only a small elongation at break. In subsequent textile processing steps, such as producing hollow-fiber mats, which have proven excellent in the production of oxygenators with good exchange capacity and as are described in EP-A-285 812, for example, these hollow-fiber membranes are therefore difficult to process. Typically, in melt-drawing processes, membranes are formed with slit-shaped pores with pronounced anisotropy, the first main extension of which is perpendicular to the drawing direction and the second main extension perpendicular to the membrane surface, i.e., in the case of hollow-fiber membranes runs between the exterior and interior surfaces of the membrane, so that the channels formed by the pores run in a relatively straight line between the surfaces. In the case in which, for example, mechanical damage in the spinning process causes leaks in the barrier layer, a preferred direction then exists for the flow of a liquid between the interior and exterior surfaces or vice-versa, thereby promoting plasma breakthrough. It is therefore an object of the invention to provide a process with a wide variety of applications and with which integrally asymmetrical membranes with a microporous support structure and a separation layer with denser stnjcture can be produced that are suited for gas exchange and that exhibit at least to a reduced extent the disadvantages of the prior art membranes, permit high gas exchange capacity, are impervious at least over extended periods of time to a breakthrough of hydrophilic liquids, in particular blood plasma, i.e., are suited in particular to extended-duration oxygenation, and have good qualities for further processing. It is a further object of the invention to provide membranes in particular for gas ex-ch$inge in which the disadvantages of the prior art membranes are at least reduced, that have a high capacity for gas exchange and sufficiently high gas flow rates for blood oxygenation, are resistant at least over extended periods of time to the breakthrough of hydrophilic liquids, in particular blood plasma, and exhibit good qualities for further processing. The object is met by a process for producing an integrally asymmetrical hydrophobic membrane having a sponge-like, open-pored, microporous support structure and a separation layer with a denser structure compared to the support structure, the process comprising at least the steps of: a) preparing a homogeneous solution of 20-90% by weight of a polymer component consisting of at least one polymer, selected from the group of polyolefins, in 80-10% by weight of a solvent system containing a compound A and a compound B that are liquid and miscible with each other at the dissolving temperature, whereby the employed mixture of the polymer component and compounds A and B has a critical demixing temperature and a solidification temperature and has a miscibility gap in the liquid state of aggregation below the critical demixing temperature, and whereby a solvent for the polymer component is selected for compound A, and compound B raises the demixing temperature of a solution consisting of the polymer component and compound A, b) rendering the solution to form a shaped object, with first and second surfaces, in a die having a temperature above the critical demixing temperature, c) cooling of the shaped object using a cooling medium, tempered to a cooling temperature below the solidification temperature, at such a rate that a thermodynamic non-equilibrium liquid-liquid phase separation into a high-polymer-content phase and a low-polymer content phase takes place and solidification of the high-polymer-content phase subsequently occurs when the temperature falls below the solidification temperature, d) possibly removing compounds A and B from the shaped object, characterized in that a strong solvent for the polymer component is selected for compound A, for which the demixing temperature of a solution of 25% by weight of the polymer component in this solvent is at least 10% below the melting point of the pure polymer component, that a weak non-solvent for the polymer component is se lected for compound B, which does not dissolve the polymer component to form a homogeneous solution when heated to the boiling point of compound B and for which the demixing temperature of a system consisting of 25% by weight of the polymer component, 10% by weight of the weak non-solvent, and 65% by weight of cortipound A, used as a solvent, is at most 8% above the demixing temperature of a system consisting of 25% by weight of the polymer component and 75% by weight of compound A, and that, for cooling, the shaped object is brought into contact with a solid or liquid cooling medium that does not dissolve or react chemically with the polymer component at temperatures up to the die temperature. Surprisingly, it has been shown that, by adhering to these process conditions, integrally asymmetrical membranes are obtained in which at least one surface is formed as a separation layer, which has a denser structure compared to the support layer structure and covers the adjacent sponge-like, open-pored, microporous support layer structure. The process according to the invention allows the realization of separation layers with very thin layer thickness, whose structure can be adjusted down to a nanoporous structure with pores at most 100 nm or to a dense structure. At the same time, the support layer of the membranes produced in this manner has a high volume porosity. Preferably, using the process according to the invention, integrally asymmetrical membranes are produced with a dense separation layer. In the context of the present invention, a dense separation layer is understood to be one for which no pores are evident based on an examination by scanning electron microscope at 60000X magnification of the membrane surface having the separation layer. The process according to the invention thus permits the production of integrally asymmetrical membranes with a separation layer that renders the membranes impervious over long periods of time to liquid breakthrough but at the same time gas permeable, and with a support layer with high volume porosity, resulting at the same time in high gas transfer capacity for these membranes in gas transfer processes. The object is therefore further met by a hydrophobic integrally asymmetrical membrane, in particular for gas exchange, that is composed substantially of at least one polymer selected from the group of polyolefins and has first and second surfaces, the membrane having a support layer with a sponge-like, open-pored, microporous structure and adjacent to this support layer on at least one of its surfaces a separation layer with denser structure, characterized in that the pores, if any, in the separation layer have an average diameter and that the membrane has a porosity in the range from greater than 30% to less than 75% by volume and a gas separation factor a(C02/N2) of at least 1. These membranes find excellent application for blood oxygenation, whereby the separation layer of these membranes is responsible for making these membranes impervious over extended periods of time to the breakthrough of blood plasma. Within the context of the present invention, an integrally asymmetrical membrane is understood to be one in which the separation and support layers consist of the same material and have been formed together directly during membrane production and both layers are integrally joined with each other as a result. In the transition from the separation layer to the support layer, there is merely a change with respect to the membrane structure. Contrasting with this are composite membranes, for example, which have a multilayer structure formed by applying, in a separate process step, a dense layer as a separation layer on a porous, often microporous support layer or support membrane. The result is that the materials constituting the support and separation layers also have different properties in the case of composite membranes:. The process according to the invention is based on a thermally induced phase separation process with liquid-liquid phase separation. According to the invention, the polymer component and compounds A and B form a binary system, which in the liquid state of aggregation has a range in which the system is present as a homogeneous solution and a range in which it exhibits a miscibility gap. If such a system is cooled, from the range in which it is present as a homogenous solution, below the critical denriixing or phase separation temperature, liquid-liquid demixing or phase separation into two liquid phases, namely one with a high polymer content and the other with a low polymer content, initially takes place. On further cooling, below the solidification temperature, the high-polymer-content phase solidifies to form a three-dimensional membrane structure. The cooling rate thereby has a substantial influence on the pore structure being created. If the cooling rate is high enough that the liqiiid-liquid phase separation cannot take place under thermodynamic equilibrium conditions but rather under thermodynamic non-equilibrium conditions and on the other hand still relatively slowly, the liquid-iiquid phase separation occurs approximately concurrently with the formation of a large number of droplets of liquid that are of substantially the same size. The resulting polymer object then has a sponge-like cellular and open-pored microstructure. If the cooling rate is significantly higher, the polymer solidifies before most of the droplets of liquid can form. In this case, net-wQrk-like microstructures are formed. The variety of such sponge-like microporous structures formed via processes with thermally induced liquid-liquid phase separation are described in detail in DE-A-27 37 745, to the disclosure of which reference is hereby explicitly made, and depicted for example in R.E. Kesting, "Synthetic Polymeric Membranes", John Wiley & Sons, 1985, pp. 261-264. The employed combinations of the polymer component, compound A. and compound B, whereby compounds A and B together form the solvent system, must be convertible jointly into a single homogeneous liquid phase and have a critical demix-ing temperature below which a phase separation into two liquid phases occurs. This is higher, however, than the demixing temperature of a solution containing equal parts of polymer but only compound A as a solvent system. In polymer/compound A systems with a miscibility gap in the liquid state of aggregation, the addition of compound B therefore raises the critical demixing temperature. Adding compound B enables selective control of pore size and pore volume in the porous structures obtained. For compound A, compounds are to be used that are solvents for the polymer component and in which, when heated at most to the boiling point of this compound, this polymer component is dissolved completely to form a homogeneous solution. According to the invention, a solvent must be used as compound A for which the demixing temperature of a solution of 25% by weight of the polymer component in this solvent is at least 10% under the melting point of the pure component consisting of the at least one polymer. Within the scope of the present invention, such a solvent is referred to as a strong solvent. The demixing or phase separation temperature can be determined in a simple manner by initially preparing a homogeneous solution of the polymer component in the solvent to be investigated and then heating this solution to a temperature approximately 20°C above the dissolving temperature. This solution is stirred and maintained at this temperature for about 0.5 hours, in order to achieve sufficient homogeneity. Subsequently, the solution is stirred and cooled at a rate of 1°C/min. The phase separation temperature is determined as the temperature at which clouding becomes visible. On further cooling, the phase with high polymer content solidifies at the solidification temperature. For compound B, according to the invention a compound is selected that is a weak non-solvent for the polymer component. Non-solvent for the polymer component is understood to mean a compound that does not dissolve the polymer component, in a concentration of 1% by weight in the non-solvent, to form a homogeneous solution when heated to at most the boiling point of this non-solvent. In the scope of the present invention, the strength of the non-solvent is assessed on the basis of the difference between the demixing temperature of a system consisting of the polymer component and a strong solvent and the demixing temperature of a corresponding system containing as a solvent system the same solvent and 10% by weight of the non-solvent to be investigated. The polymer concentration in each case is 25% by weight. A weak non-solvent is then understood to be one that leads to an increase in the demixing temperature of at most 8% relative to the demixing temperature of the corresponding system consisting only of solvent and polymer. A strong non-solvent is, by definition, one that leads to an at least 10% increase in the demixing temperature. Compound A can also be blended with one or more liquids, in particular other solvents. Compound B can also be employed as a mixture with one or more other compounds, in particular additional non-solvents. As a result, within the context of the present invention, compound A is understood as not only a single compound but also a mixture of different solvents, for example two strong solvents or a strong with a weak solvent, as long as the overall action as a strong solvent is maintained. Likewise, compound B is also understood to be a mixture of different non-solvents, for example several weak non-solvents, as long as the action as a weak non-solvent is maintained. The fraction of polymer required for membrane production and the ratio of compound A to compound B in the solvent system can be determined by generating phase diagrams in simple experiments. Such phase diagrams can be developed using known methods, such as are described in C.A. Smolders, J J, van Aartsen, A. Steenbergen, Kojloid-Z. und Z, Polymere, 243 (1971), pp. 14-20. As a rule, for a given solvent A, the fraction of compound B, i.e., weak non-solvent, in the mixture of the polymer component, compound A, and compound B depends on the strength of the non-solvent, i.e., compound B. Preferably, the fraction of compound B in the solvent system is 1 to 45% by weight. According to the invention, the polymer component used is at least one polymer selected from the group of polyolefins. In this case, the polymer component can be a single polyolefin or a mixture of several polyolefins, whereby the polyolefins in the present context also include polyolefin copolymers or modified polyolefins. Mixtures of different polyolefins are interesting in that various properties such as permeability or mechanical characteristics can be optimized. For example, by adding just slight amounts of a polyolefin with an ultrahigh molecular weight, for example exceeding 106 daltons, a strong influence can be exerted on the mechanical properties. A prerequisite for this, of course, is that the polyolefins employed together be soluble in the solvent system used. in an advantageous embodiment of the process according to the invention, the at least one polymer in the polymer component is a polyolefin consisting exclusively of carbon and hydrogen. Especially prefenred polyolefins are polypropylene and poly(4-methyl-1-pentene) or mixtures of these polyolefins among themselves or with other polyolefins. Of particular advantage is the use of poly(4-methyl-1-pentene) or a mixture of poly(4-methyl-1-pentene) with polypropylene. High gas transfer rates can be realized thereby, while maintaining good mechanical properties for the membranes. For compounds A and B, which jointly form the solvent system, compounds are to be used that fulfill the stated conditions. In the case of the preferred use of polypropylene as the polymer, dioctyl adipate, isopropyl myristate, or mixtures thereof are preferably used for compound A. Compound B in this case can advantageously be di- ethyl phthalate, glycerin triacetate, castor oil, glycerin diacetate, or mixtures thereof. In the preferred use of poly(4-methyi-1-pentene) as the polymer, compound A is preferably dioctyl adipate, isopropyl myristate, diphenyl ether, dibenzyl ether, or mixtures thereof. Glycerin triacetate, diethyl phthalate, castor oil, N,N-bis{2-hydroxyethyl)tallow amine, soybean oil, or mixtures thereof have proven advantageous as compound B, Especially good results are exhibited when glycerin triacetate is used as compound B. The polymer fraction of the mixture from v\/hich the solution is formed is preferably 30^60% by weight, and the fraction of the solvent system, consisting of compounds A and B, is 70-40% by weight. The polymer fraction is especially preferred to be 35-50% by weight and the fraction of compounds A and B 65-50% by weight. If necessary, additional substances such as antioxidants, nucleating agents, fillers, components to improve biocompatibility, i.e., blood tolerance when using the membrane in oxygenation, such as vitamin E, and similar substances can be employed as additives to the polymer component, compounds A and B, or to the polymer solution. The polymer solution formed from the polymer component and the solvent system is given shape using suitable dies to produce a membrane preferably in the form of a flat or hollow-fiber membrane. Conventional dies such as sheeting dies, casting molds, doctor blades, profiled dies, annular-slit dies, or hollow-fiber dies can be employed. Preferably, hollow-fiber membranes are produced using the process according to the invention. In this case, the polymer solution is extruded through the annular gap of the corresponding hollow-fiber dies to form a shaped object, i.e., a hollow fiber. A fluid is metered through the central bore of the hollow-fiber die that acts as an interior filler that shapes and stabilizes the lumen of the hollow-fiber membrane. The extruded hollow fiber or resulting hollow-fiber membrane then exhibits a surface facing the lumen, the interior surface, and a surface facing away from the lumen, the exterior surface, separated from the interior suri'ace by the wall of the hollow fiber or hollow-fiber membrane. After.shaping, the shaped object is cooled using a solid or liquid cooling medium, so that a thermodynamic non-equilibrium liquid-liquid phase separation occurs in the shaped object, i.e., in the shaped polymer solution, and the polymer structure subsequently solidifies and hardens. In this process, the cooling medium has been tempered to a temperature below the solidification temperature. According to the invention, in order to produce the desired integrally asymmetrical membrane with separation layer, the cooling medium must be one that does not dissolve the polymer component and does not chemically react with it, even when the medium is heated to the die temperature. The use of such a cooling medium is decisive for the formation of a separation layer with denser structure. Such a requirement placed on the cooling medium rules out, for example, the use as a cooling medium of the mixture of compounds A and B employed as the solvent system. Although such a system would not dissolve the polymer component at the cooling temperature, the polymer component forms a homogeneous solution at the die temperature, as previously noted. Itjs advantageous if the exit surface of the die and the surface of the cooling medium are spatially separated by a gap, which is transited by the shaped object prior to contact with the cooling medium. The gap can be an air gap, or it can also be filled with another gaseous atmosphere, and it can also be heated or cooled. The polymer solution, however, can also be brought directly into contact with the cooling medium after exiting from the die. In the production of flat membranes, the cooling medium can be a solid material or a solid surface, for example in the form of a glass or metal plate or an appropriately temperature-controlled or cooled cooling roller, onto which the shaped object is laid. Preferably, the solid cooling medium has a high thermal conductivity and is especially preferred to consist of a metallic material. In an advantageous embodiment of the process according to the invention, however, a liquid cooling medium is used. It is especially preferred for the liquid used as the cooling medium to be a non-solvent for the polymer component, i.e., it does not dissolve the polymer component to form a homogeneous solution when heated to at most the boiling point of the cooling medium. The liquid used as the cooling medium can also contain a component that is a solvent for the polymer component, or it can also be a mixture of different non-solvents, as long as it overall does not dissolve the polymer component at temperatures up to at least the die temperature. It is observed in this case that the degree of non-solvent character of the cooling medium influences the tightness of the separation layer being formed. In an especially preferred embodiment of the process according to the invention, therefore, a liquid is used as a cooling medium that is a strong non-solvent for the polymer component. Concerning the definitions of non-solvent and strong non-solvent, refer to the previous discussion in conjunction with compound B. Preferably, the cooling medium at the cooling temperature is a homogeneous, single-phase liquid. This ensures production of membranes with especially homogeneous surface structures. The liquid cooling medium can be one that is miscible with the solvent system to form a homogeneous solution or one that does not dissolve the compounds forming the solvent system. To initiate a thermodynamic non-equilibrium liquid-liquid phase separation, the temperature of the cooling medium must be significantly below the critical demixing temperature or phase separation temperature of the polymer solution used and furthermore below the solidification temperature in order to solidify the phase with high polymer content. In this case, the formation of the separation layer Is promoted when there is as great a difference as possible between the demixing temperature and the temperature of the cooling medium. The cooling medium preferably has a temperature at least 100°C below the phase separation temperature, and especially preferably a temperature that is at least 1500C below the phase separation temperature. It is particularly advantageous if the temperature of the cooling medium in this case is under 50°C. In individual cases, cooling to temperatures below ambient temperature can be required. It is also possible for cooling to take place in several steps. The liquid cooling medium is preferably in a shaft or spinning tube which the shaped object passes through for cooling purposes. The cooling medium and shaped object are generally fed in the same direction through the shaft or spinning tube. The shaped object and cooling medium can be fed at the same or different linear speeds through the spinning tube, whereby, depending on the requirement, either the shaped object or the cooling medium can have the higher linear speed. Such process variants are described in DE-A-28 33 493 or EP-A-133 882. for example. The interior filler employed in extrusion of hollow filaments can be in gaseous or liquid form. When using a liquid as the interior filler, a liquid must be selected that substantially does not dissolve the polymer component in the shaped polymer solution b0low the critical demixing temperature of the polymer solution. To achieve an open-pored structure on the interior surface, interior fillers are preferably used that are solvents for the at least one polymer used, whereby the previously cited condition must be observed, and/or temperatures of the interior filler are set that are in the vicinity of the polymer solution temperature. In other respects, the same liquids can be used as can also be used as the cooling medium. In this manner, hollow-fiber membranes can be produced that have a separation layer on both their outside and inside, or also hollow-fiber membranes that have a separation layer only on the inside. Preferably, the interior filler is then a non-solvent for the polymer component and especially preferably a strong non-solvent for the polymer component. The interior filler can be miscible with the solvent system, in case the fluid is gaseous, it can be air, a vaporous material, or preferably nitrogen or other inert gases. In a further advantageous embodiment of the process according to the invention, at leaist one of the surfaces of the shaped object leaving the die, i.e. the polymer solution leaving the die in a shaped state, preferably the surface on which the separation layer is to be formed, is subjected prior to cooling to a gaseous atmosphere promoting the evaporation of compound A and/or B, i.e., to an atmosphere in which the evaporation of compound A and/or B is possible. Preferably, air is used to form the gaseous atmosphere. Likewise preferred are nitrogen or other inert gases or also vaporous media. The gaseous atmosphere is advantageously conditioned and generally has a temperature below that of the die. To evaporate a sufficient fraction of compound A and/or B, at least one of the surfaces of the shaped object is preferably subjected to the gaseous atmosphere for at least 0.5 ms. To provide the gaseous atmosphere promoting the evaporation of compound A and/or B, the die and cooling medium can, as previously noted, be spatially sepa- rated such that a gap is formed between them that contains the gaseous atmosphere and through which the shaped object passes. In producing flat membranes, for example, the polymer solution extruded through a sheeting die, for example, can, as a flat sheet, initially be passed through a gap, such as an air gap, before being cooled. In this case, both surfaces of the flat sheet, as well as the edges, are enveloped by the gaseous atmosphere, influencing the formation of a separation layer on both surfaces of the resulting flat membrane. If the extrusion of the flat sheet is performed directly onto a heated carrier, for example in the form of a heating roller, and if the flat sheet on the carrier then passes through a defined zone in a gaseous atmosphere before being cooled by the cooling medium, only one surface of the flat sheet, namely that facing away from the heating roller, comes into contact with the gaseous atmosphere, thus influencing the formation of a separation layer, by evaporation, only on this surface. In the case of producing hollow-fiber membranes, the hollow filament leaving the die can likewise be directed through a gap formed between the die and cooling medium and containing the gaseous atmosphere. In individual cases, the structure of the separation layer can also be influenced by drawing the shaped polymer solution after exiting the die, i.e. particularly in the air gap, whereby the drawing is effected by establishing a difference between the exit speed of the polymer solution from the die and the speed of the first withdrawal device for the cooled shaped object. Aftpr cooling and hardening of the polymer stmcture. compounds A and B are usually removed from the shaped object. Removal can be performed, for example, by extraction. Preferably, extraction agents are used that do not dissolve the polymer or polymers but are miscible with compounds A and B. Subsequent drying at elevated temperatures can be necessary to remove the extraction agent from the membrane. Suitable extraction agents are acetone, methanol, ethanol, and preferably isopropa-nol. In some cases, it can also be practical to retain one or both of the two compounds A and B at least in part in the shaped object and to extract only one or neither of the compounds. Other components added to compounds A and/or B as additives can remain in the membrane structure as well and thus serve as functional active liquids, for example. Various examples of microporous polymers containing functional active liquids are described in DE-A 27 37 745. Before or after the removal of at least a substantial portion of the solvent system, a slight drawing of the membrane can take place in order in particular to modify the properties of the separation layer in a specific manner. For example, in a substantially dense separation layer, drawing can be used to create pores and/or adapt the pore size of the separation layer to the size required by the specific application for the resulting membrane. In producing the membrane of the invention, however, the pores must remain under 100 nm, so that the membrane is suitable for gas exchange or also gas separation, premature breakthrough of liquid can be avoided, and the gas separation factor a(C02/N2) remains at least 1 in accordance with the invention. For this reason, the drawing should generally not exceed 10-15% when producing the membrane of the invention. The drawing can, as required, also be performed in multiple directions and is advantageously performed at elevated temperatures. For example, such drawing can also be conducted during drying of the membrane that might be necessary after extraction. Using the process according to the invention, membranes can, on the one hand, be produced for gas separation tasks in which, for example, a single gas component is selectively separated from a mixture of at least two gases or a single gas component in a mixture of at least two gases is enriched, or for gas transfer tasks, in which a gas dissolved in a liquid is selectively removed from this liquid, and/or a gas from a mixture of gases is dissolved in a liquid. On the other hand, adjustment of the pore size of the separation layer, for example in a downstream drawing step, also permits production of membranes for nanofiltration, such as for separating low-molecular substances preferably from non-aqueous media, or for ultrafiltration, such as for treating fresh water, sewage, or process water, as well as for applications in the food and dairy industries. The process according to the invention is particularly suited to producing the integrally asymmetrical membrane according to the invention. Due to its structure, the membrane of the invention is distinguished by high gas flow rates and high gas transfer rates while maintaining high levels of safety with respect to a breakthrough of the liquid, from which, when using the membrane of the invention for gas transfer, a gaseous component is to be separated or to which a gaseous component is to be added, and also by good mechanical properties. To achieve this, the membrane has a high volume porosity, whereby the latter is determined substantially by the structure of the support layer, and a defined separation layer with a structure denser than that of the support layer and with reduced thickness. The support layer of the membrane of the invention can have the aforementioned various structures. In one embodiment of the membrane of the invention, the support layer.has a sponge-like, cellular and open-pored structure, in which the pores can be described as enveloped microcells that are interconnected by channels, smaller pores, or passages. In another embodiment of the membrane of the invention, the support layer has a non-cellular structure, in which the polymer phase and the pores form interpenetrating network structures. In any case, however, the support layer is free of macrovoids, i.e., free of such pores often referred to in the literature as finger pores or caverns. The pores of the support layer can have any geometry and be, for example, of elongated, cylindrical, rounded shape, or also have a more or less irregular shape. In accordance with the invention, the pores in the support layer are on average substantially isotropic. This is understood to mean that, although the individual pores can also have an elongated shape, the pores on average in all spatial directions have substantially the same extension, whereby deviations of up to 20% can exist between the extensions in the individual spatial directions. With an insufficiently low volume porosity, i.e. an insufficient pore fraction compared to the total volume of the membrane, the attainable gas flow and gas transfer rates are too low. On the other hand, an excessive pore fraction in the membrane leads to deficient mechanical properties, and the membrane cannot be readily processed in subsequent processing steps. For this reason, the membrane of the invention has a volume porosity in the range of greater than 30% to less than 75% by volume, preferably greater than 50% to less than 75% by volume, and especially preferably greater than 50% to less than 65% by volume. The membrane of the invention can have a separation layer on only one of its surfaces, or it can have a separation layer on both surfaces. A preferred embodiment of the membrane of the invention has a separation layer only on one, the first surface, and the second surface on the opposite side of the support layer has an open-pored, network-like structure with approximately circular openfngs. Approximately circular openings are understood to be openings in which the ratio of the major axis to the minor axis does not exceed 2:1. Due to their open-pored structure, such membranes have on their one side a comparatively small resistance to gas flow, for example. In the membranes of the invention, existing pores in the surface exhibited by the separation layer, whose diameters are The separation layer influences on the one hand the gas flow and gas transfer rates but on the other hand the breakthrough time, i.e., the time the membrane is protected from a breakthrough of the liquid from which, when using the membrane of the invention, a gaseous component is to be separated or to which a gaseous component is to be added, or from a breakthrough of components contained in the liquid. It also influences whether and how well various gases in a gas mixture can be separated from one another, i.e., the gas separation factor a(COg/Nj). for example. With a non-porous separation layer, very long breakthrough times are the result, but the transfer rates and gas flow rates are limited in size, since in non-porous membrane layers the gas transfer or gas flow takes place solely via a comparatively slow solution diffusion, in contrast to the considerably greater Knudsen flow in porous structures. In the case of a porous separation layer, on the other hand, the gas transfer rates and gas flow rates are higher than those with a non-porous separation layer, but reduced breakthrough times result due to the pores. The tightness of the separation layer and its suitability in particular for gas transfer can often not be evaluated with sufficient reliability solely on the basis of visual inspection, using a scanning electron microscope for example. In this case, not only the size of existing pores or in general structural defects such as fissures but also their number play a role. However, the absence or presence of pores and/or defects, as well as their number, can be evaluated by examining the gas permeation and gas flow through the membrane as well as the gas separation factors. It is well known that the general principles of gas transport in polymer membranes depend on the pore size in the membrane. In membranes in which the separation layer has pores at most 2-3 nm in size, the gas permeates through this membrane via solution diffusion mechanisms. The permeability coefficient PQ of a gas then depends solely on the polymer material of the membrane and on the gas itself, and the gas flow Qo, i.e.. the permeability coefficient divided by the membrane thickness, depends, for a given gas, only on the thickness of the non-porous membrane. The gas separation factor a. which specifies the ratio of the permeability coefficients or the gas flows Q of two gases in this membrane, therefore depends likewise solely on the polymer material and not, for example, on the thickness of the separation layer. For example, the gas separation factor for CO2 and N2 is then ao(COg/Ns) = Po(C02)/Po(N2). For polymers in general use, resulting ao(C02/N2) values are at least 1 and generally at least 3, In porous membranes with pores between 2 nm and about 10 pm in size, the transport of gases takes place primarily via Knudsen flow. The calculated gas separation factors ai. as the ratio of the measured apparent permeability coefficients, are then inversely proportional to the square root of the ratio of the molecular weights of the gases. For a,(C02/N2), therefore, the result is V28/44 = 0.798, for example. If a gas permeates the membranes of the present invention, which have a micropo-rous support structure and compared with it a denser separation layer with pores not exceeding 100 nm on average, the permeation through the separation layer is the step that determines the rate. If this separation layer has a significant number of pores or defects, on the one hand the apparent permeability coefficients increase, but on the other hand the gas separation factor decreases. For this reason, the presence or absence of pores and/or defects in the separation layer of the membranes of the invention can be determined on the basis of the measured gas separation factors for CO2 and N2, a(C02/N2). If the CO2/N2 gas separation factor a(C02/N2) is less than 1, the membrane has an excessive number of pores or defects in the separation layer. If the number of pores or defects in the separation layer is too high, however, a premature liquid breakthrough or plasma breal The separation layer must not be too thin, since this increases the risk of defects and thus of breakthrough, and the resulting a(C02/N2) values are too low. However, the time to actual breakthrough is still relatively long, since with the membranes of the invention there is no preferred direction for the flow of a liquid; rather, the course of the liquid is tortuous due to the pore structure. Contrasting with this are membranes produced according to the aforementioned melt-drawing process, in which, due to the pronounced anisotropy of the pores, a preferred direction for the flow of the liquids from one surface to the other results. While excessively thin separation layers make the risk of defects too great, an excessive separation layer thickness makes the transfer rates and gas flow rates too low. Preferably, therefore, the thickness of the separation layer lies between 0.01 pm and 5 pm, especially preferably between 0.1 pm and 2 pm. Membranes of the invention with a separation layer thickness between 0.1 pm and 0.6 pm are excellently suited. The thickness of the separation layer can be determined for the membranes of the invention in a simple manner by measuring the layer using fracture images generated by scanning electronic microscopy or by ultrathin-section characterizations using transmission electron microscopy. In conjunction with the high porosity of the membranes, this permits the attainment of a sufficiently high permeability of the membranes for use in blood oxygenation and thus sufficiently high gas flow rates. Preferably, therefore, the membranes of the invention have a gas flow Q for CO2, Q(C02), of at least 5 ml/(cm^*min*bar). An important application of the membranes of the invention is oxygenation of blood. In these applications, as previously noted, the plasma breakthrough time plays a role, i.e., the time in which the membrane is stable against a breakthrough of blood plasma. It must be emphasized that plasma breakthrough is a considerably more complex process than the mere penetration of a hydrophobic membrane by a hydro-philic liquid. According to accepted opinion, plasma breakthrough is induced by the fact that initially proteins and phospholipids in the blood effect a hydrophilation of the pore system of the membrane, and in a subsequent step a sudden penetration of blood plasma into the hydrophilated pore system takes place. The critical variable for a liquid breakthrough is therefore considered to be the plasma breakthrough time. The membranes of the invention preferably exhibit a plasma breakthrough time of at least 20 hours, and especially preferably a plasma breakthrough time of at least 48 hours. In general, in the membranes produced according to the invention and the membranes of the invention, the transition from the porous support layer to the separation layer takes place in a narrow region of the membrane wall. In a preferred embodiment of the membrane of the invention, the membrane structure changes abruptly in the transition from the separation layer to the support layer, i.e., the membrane structure changes substantially transition-free and suddenly from the microporous support structure to the separation layer. Membranes with such a structure have, in comparison to membranes with a gradual transition from the separation layer to the support layer, the advantage of higher permeability of the support layer for gases to be transferred, since the support layer is less compact in its area adjacent to the separation layer. The hydrophobic membrane of the invention consists substantially of at least one polymer selected from the group of polyolefins. The at least one polymer can be a single polyolefin or a mixture of several polyolefins, including poiyolefin copolymers or modified polyolefins. Mixtures of polyolefins with different molecular weights or of various polyolefins are interesfing to the extent that they allow various properties to be optimized, such as gas transfer rates or mechanical properties. For example, by adding just slight amounts of a polyolefin with an ultrahigh molecular weight, exceeding 106 daltons, for example, a strong influence can be exerted on the mechanical properties. Preferably, the membrane is composed of a polyolefin consisting exclusively of carbon and hydrogen. It is especially preferred for the membrane to be made from polypropylene or poly(4-methyl-1-pentene) or mixtures of these polyolefins with other polyolefins. Of particular advantage is the use of poly(4-methyl-1-pentene) or a mixture of poly(4-methyl-1-pentene) with polypropylene. High gas transfer rates can be realized with good mechanical properties for the membranes. If necessary, the at least one polymer can contain additional materials as additives, such as antioxidants, nucleating agents, fillers, components to improve biocompatibility, i.e., blood tolerance when using the membrane in oxygenation, such as vitamin E, and similar substances. In a preferred embodiment, the membrane is a flat membrane. The flat membrane preferably has a thickness between 10 and 300 µm. especially preferably between 30 and 150 µm. The flat membrane can have a separation layer on only one of its surfaces or on both surfaces. In a likewise preferred embodiment, the membrane of the invention is a hollow-fiber membrane. Depending on the embodiment, it can have a separation layer on its interior surface only, i.e. on the surface facing the lumen, or only on its exterior surface, Le. the surface facing away from the lumen, or on both the interior and exterior surfaces. The separation layer is preferably on the exterior surface. The hollow-fiber membrane preferably has an outside diameter between 30 and 3000 µm, especially preferably between 50 and 500 µm. A wall thickness of the hollow-fiber membrane between 5 and 150 µm is advantageous, and a thickness between 10 and 100 |jm is especially advantageous. The membrane of the invention has outstanding mechanical properties, readily enabling processing in subsequent processing steps. When using the hollow-fiber membrane, it has proven beneficial for the hollow-fiber membranes, with respect to the performance characteristics of membrane modules made therefrom, to be initially formed, for example, by appropriate knitting processes into mats of hollow-fiber membranes substantially parallel to each other, which are then fashioned into appropriate bundles. The associated textile processes impose stringent demands on the mechanical properties of the membranes, in particular on the tensile strength and elongation. These requirements are fulfilled by the membrane of the invention. The hollow-fiber membranes of the invention preferably have a breaking force of at least 70 cN and an elongation at break of at least 75%. The membrane of the invention can be used in numerous applications in which a membrane is required with a separation layer with pores at most 100 nm in size. Preferably, the membrane of the invention is suited for applications in the fields of gas separation or gas exchange, in which gaseous components are to be separated from liquids or added to them. Due to their high impermeability for plasma, i.e. to their long plasma breakthrough times, and their high gas transfer capacity for O2 and CO2, the membranes of the invention are excellently suited for use in oxygenators, i.e., for the oxygenation of blood and in particular for the extended-duration oxygenation of blood. The invention will now be described in more detail with reference to the following examples and figures: Fig. 1 shows a scanning electron microscopic (SEM) image of the exterior surface of a hollow-fiber membrane according to example 1 at 60000x magnification. Fig. 2 shows an SEM image of the interior surface of a hollow-fiber membrane according to example 1 at 13500x magnification. Fig. 3 shows an SEM image of the surface of fracture perpendicular to the longitudinal axis of a hollow-fiber membrane according to example 1, in the vicinity of its outer side, at 13500x magnification. Fig. 4 shows an SEM image of the exterior surface of a hollow-fiber mem- brane according to example 2 at 60000x magnification. Fig. 5 shows an SEM image of the interior surface of a hollow-fiber membrane according to example 2 at 13500x magnification. Fig. 6 shows an SEM image of the surface of fracture perpendicular to the longitudinal axis of a hollow-fiber membrane according to example 2, in the vicinity of its outer side, at 13500x magnification. Fig. 7 shows an SEM image of the exterior surface of a hollow-fiber mem- brane according to example 5 at 60000x magnification. Fig. 8 shows an SEM image of the interior surface of a hollow-fiber membrane according to example 5 at 13500x magnification. Fig. 9 shows an SEM image of the surface of fracture perpendicular to the longitudinal axis of a hollow-fiber membrane according to example 5, in the vicinity of its outer side, at 13500x magnification. Fig. 10 shows an SEM image of the exterior surface of a hollow-fiber mem- brane according to example 7 at 60000x magnification. Fig. 11 shows an SEM image of the interior surface of a hollow-fiber membrane according to example 7 at 13500x magnification. Fig, 12 shows an SEM image of the surface of fracture perpendicular to the longitudinal axis of a hollow-fiber membrane according to example 7, in the vicinity of its outer side, at 13500x magnification. Fig. 13 shows an SEM image of the interior surface of a holiow-fiber membrane according to comparative example 1 at 6000x magnification. Fig. 14 shows an SEM image of the exterior surface of a hollow-fiber mem- brane according to comparative example 1 at 27000x magnification. Fig. 15 shows an SEM image of the exterior surface of a hollow-fiber mem- brane according to comparative example 2 at 27000x magnification. Fig. 16 shows an SEM image of the surface of fracture perpendicular to the longitudinal axis of a hollow-fiber membrane according to comparative example 2, in the vicinity of its outer side, at 13500x magnification. Fig. 17 shows an SEM image of a membrane according to comparative exam- ple 4 at 3000x magnification; fracture edge of the membrane between the membrane wall and the surface that was facing the glass side during membrane production. Fig. 18 shows an SEM image of a membrane according to comparative exam- ple 4 at 9000x magnification, showing the membrane surface that was facing the glass side during membrane production. Fig. 19 shows an SEM image of a membrane according to comparative exam- ple 5 at 3000x magnification; fracture edge of the membrane between the membrane wall and the surface that was facing the glass side during membrane production. Fig. 20 shows an SEM image of a membrane according to comparative exam- pie 4 at 900x magnification, showing the membrane surface that was facing the glass side during membrane production. In the examples, the following methods were employed to characterize the membranes obtained: Determination of the plasma breakthrough time: To determine the plasma breakthrough time, a phospholipid solution maintained at 37°C (1.5 g L-a-Phosphatidy-LCholine dissolved in 500 ml physiological saline solution) is directed with a flow of 6 l/(min*2m) at a pressure of 1.0 bar along one surface of a membrane sample. Air is allowed to flow along the other surface of the membrane sample, the air after exiting the membrane sample being fed through a cooling trap. The weight of the liquid accumulated in the cooling trap is measured as a function of time. The time until the occurrence of a significant increase in the weight, i.e., to the first significant accumulation of liquid in the cooling trap, is designated as the plasma breakthrough time. Determination of the volume porositv: A sample of at least 0.5 g of the membrane to be examined is weighed in a dry state. The membrane sample is then placed for 24 hours into a liquid that wets the membrane but does not cause it to swell, such that the liquid penetrates into all pores. This can be detected visually in that the membrane sample is transformed from an opaque to a glassy, transparent state. The membrane sample is then removed from the liquid, liquid adhering to the sample removed by centrifugation at about 1800 g, and the mass of the thus pretreated wet, i.e., liquid-filled, membrane, determined. The volume porosity in % is determined according to the following formula: where Determination of the breaking force and elongation at break: To characterize the membrane with respect to its breaking force and elongation at break, the membrane is elongated at ambient temperature at a constant rate until it breaks, and the force required therefore is determined along with the change in length. Determination of the average diameter of the pores in the separation layer: The determination of the average diameter of the pores in the separation layer is performed using an image-analysis technique. For this purpose, the pores are as-sumed to have a circular cross-section. The average pore diameter is then the arithmetic mean of all visible pores on a membrane surface of approx. 8 pm x 6 |jm at eOOOOx magnification. Example 1: 36.6% by weight poly(4-methyl-1-pentene) (TPX DX845) was dissolved in a nitrogen atmosphere in a container with stirrer at a temperature of 260°C in 63.4% by weight of a solvent system consisting of 70% by weight dioctyl adipate, which acts as a strong solvent for poly(4-methyl-1 -pentene), 20% by weight glycerin triacetate, and 10% by weight castor oil, the latter acting as weak non-solvents for poly(4-methyl-1-pentene). After degassing the clear and homogeneous solution was fed with a gear pump to a hollow-fiber die with an annular-gap outside diameter of 1.2 mm, which had been heated to 248°C and thereby a temperature above the demixing temperature, and extruded to form a hollow fiber. Nitrogen was metered into the lumen of the hollow fiber through the interior bore of the hollow-fiber die. After an air section of 5 mm, the hollow fiber passed through an approx, 1 m long spinning tube, through which glycerin triacetate, tempered to ambient temperature, flowed as a cooling medium. The hollow fiber, solidified as a result of the cooling process in the spinning tube, was drawn off from the spinning tube at a rate of 72 m/min, wound onto a spool, subsequently extracted with isopropanol, and then dried at approx. 120°C. A hoilow-fiber membrane resulted with an outside diameter of 365 pm and a wall thickness of 86 pm, for which no pores were observable on its exterior surface in a scanning-electron-microscopic (SEM) image even at 60000x magnification (Fig. 1), whereas the interior surface facing the lumen had an open-pored, network-like structure with approximately circular openings (Fig. 2). The sponge-like, open-pored, microporous support structure, which is covered by the approx. 0.2 pm thick separation layer, is evident in the fracture image of a surface of fracture perpendicular to the longitudinal axis of the hollow-fiber membrane (Fig. 3). For the membrane according to this example, a volume porosity of 57%, a CO2 flow of 8.16 ml/(cm^*min*bar), an N2 flow of 1.24 ml/(cm^*min*bar), and a gas separation factor a(C02/N2) of 6.6 were determined. The membrane exhibited a plasma breakthrough time of more than 72 hours. After this time, the test was discontinued. With a breaking force of 85 cN and an elongation at break of 129%, the membrane was well suited to further textile processing. Example 2: Poly(4-methyl-1-pentene) was melted in an extruder stepwise at increasing temperatures ranging from 270'*C to 290X and fed continuously to a dynamic mixer using a gear pump. The solvent system, consisting of 70% by weight dioctyl adipate, 15% by weight glycerin triacetate, and 15% by weight castor oil was also fed via a dosing pump to the mixer, in which the polymer and the solvent system were processed together at a temperature of 290°C to a homogeneous solution with a polymer concentration of 35% by weight and a solvent-system concentration of 65% by weight. This solution was fed to a hollow-fiber die with an annular-gap outside diameter of 1.2 mm and extruded above the phase separation temperature at 250°C to form a hollow fiber. Nitrogen was used as the interior filler. After an air section of 5 mm, the hollow fiber passed through an approx. 1 m long spinning tube, through which the cooling medium, tempered to ambient temperature, flowed. Glycerin triacetate was used as the cooling medium. The hollow fiber, solidified as a result of the cooling process in the spinning tube, was drawn off from the spinning tube at a rate of 72 m/min, wound onto a spool, subsequently extracted with isopropanol, and then dried at approx. 120°C. A hollow-fiber membrane was produced with an outside diameter of 411 ym, a wall thickness of 94 pm, and a porosity of 56,5% by volume. The outside of the membrane had a separation layer, whereby no pores were evident according to SEM examination of the exterior surface at a magnification of 60000x. For the membrane according to this example, a CO2 flow of 6.21 ml/(cm^*min*bar). an N2 flow of 0.66 ml/(cm^*min*bar), and a gas separation factor a(C02/N2) of 9.4 were determined. The membrane exhibited a plasma breakthrough time of more than 72 hours. After this time, the test was discontinued. Example 3: A hollow-fiber membrane was produced as in example 2, whereby the solvent system was a mixture of 70% by weight dioctyl adipate. 20% by weight glycerin triacetate, and 10% by weight castor oil, and the cooling medium was a mixture of dioctyl adipate, glycerin triacetate, and castor oil in a ratio of 20:75:5% by weight. The polymer concentration of the solution was 37% by weight, and the die temperature 2470.C A hollow-fiber membrane resulted with an outside diameter of 388 pm and a wall thickness of 97 pm, for which individual pores less than approx, 20 nm in size were observable on its exterior surface in a scanning-electron-microscopic (SEM) exami- nation at 60000x magnification (Fig. 4). The interior surface facing the lumen had an open-pored, network-like structure with approximately circular openings (Fig. 5). A sponge-like, open-pored, microporous support structure, which was covered by a closed, approx. 0.2 pm thick separation layer, was evident in the fracture image of a surface of fracture perpendicular to the longitudinal axis of the hollow-fiber membrane (Fig. 6). For the membrane according to this example, a CO2 flow of 53.41 ml/(cm^*min*bar), an N2 flow of 51.11 ml/(cm^*min*bar), and a gas separation factor a(C02/N2) of 1.05 were determined. The breaking force of the membrane was 92 cN and the elongation at break 132%. The membrane exhibited a plasma breakthrough time of more than 72 hours. After this time, the test was discontinued. Example 4: A hollow-fiber membrane was produced as described in example 2. The solvent system used was a mixture of 70% by weight dioctyl adipate, 15% by weight glycerin triacetate, and 15% by weight castor oil, and the cooling medium used was a mixture of 37.3% by weight dioctyl adipate, 48.2% by weight glycerin triacetate, and 14.5% by weight castor oil. The membrane according to this example, with an outside diameter of 390 pm and a wall thickness of 93.5 pm, had, similar to the membrane of example 1, as evidenced by the SEM images an exterior surface without pores and an interior surface facing the lumen with an open-pored, network-like structure with approximately circular openings. The sponge-like, open-pored, microporous support structure was covered by a closed, approx. 0.4 pm thick separation layer. The membrane had a plasma breakthrough time of 46 hours. Example 5: The procedure as in example 2 was followed. The solvent system used was a mixture of 80% by weight dioctyl adipate and 20% by weight castor oil, and the cooling medium was glycerin triacetate. The die temperature was 240°C. The membrane had on its exterior surface isolated pores with sizes up to approx. 50 nm (Fig. 7). The interior surface facing the lumen had an open-pored, network-like structure with approximately circular openings (Fig. 8). The sponge-like, open-pored, microporous support structure was covered by a closed, approx. 0.2 pm thick sepa- ration layer (Fig. 9). The membrane had an inside diameter of 209 |jm, a wall thickness of 90 |jm, a breaking force of 96 cN, an elongation at break of 123%, a CO2 flow of 42.64 ml/(cm^*min*bar), and a gas separation factor aCCOg/Ns) of 1. The plasma breakthrough time was more than 72 hours. After this time, the test was discontinued. Example 6: The procedure as in example 2 was followed. The solvent system was a mixture of 75% by weight isopropyl myristate, acting as a strong solvent, and 25% by weight castor oil, and the cooling medium was glycerin triacetate. The die temperature was 220X. The membrane had on its exterior surface individual pores with sizes up to approx. 50 nm. The support structure was covered by a closed, approx. 0.2 \im thick separation layer. The plasma breakthrough time exceeded 72 hours. Example 7: The procedure as in example 2 was followed, whereby the solvent system was a mixture of 70% by weight dioctyl adipate, 20% by weight glycerin triacetate, and 10% by weight castor oil, and the cooling medium was a mixture of 65% by weight glycerin and 35% by weight water. In this case, the cooling medium was not miscible with the solvent system. The die temperature was 235X, and the air gap 20 mm. The resulting hollow-fiber membrane had an inside diameter of 203 pm, a wall thickness of 90 pm, and a porosity of 57% by volume. The membrane exhibited a CO2 flow of 13.17 ml/(cm^*min*bar), an N2 flow of 2.98 ml/(cm^*min*bar). and a separation layer on its exterior surface with a gas separation factor a(C02/N2) of 4.42. For the membrane according to this example, in the scanning-electron-microscopic examination, no pores were observable on its exterior surface even at 60000x magnification (Fig. 10), whereas the interior surface facing the lumen had an open-pored, network-like structure with approximately circular openings (Fig. 11). A sponge-like, open-pored, microporous support structure, covered by a very thin, approx. 0.1 pm thick separation layer, was evident in the fracture image of a surface of fracture per- pendicular to the longitudinal axis of the hollow-fiber membrane (Fig. 12). Plasma breakthrough times exceeding 72 hours were determined. Comparative example 1: A membrane was produced as in example 2, whereby the solvent system was a mixture of 80% by weight dioctyl adipate and 20% by weight castor oil. The resulting solution contained 47% by weight poly(4-methyl-1"pentene). The die temperature was 248°C and thereby above the demixing temperature. The cooling medium used was dioctyl adipate tempered to ambient temperature, i.e., the same compound that served as compound A, i.e., as a solvent. The finished membrane had an outside diameter of 390 pm, a wall thickness of 97 pm, and a porosity of 45% by volume. As evidenced by the SEM images, the exterior surface of the membrane was open-pored with numerous pores larger than 0.1 pm (Fig. 14). The interior surface facing the lumen was open-pored with approximately circular pores (Fig. 13). The membrane exhibited a CO2 flow of 17.54 ml/(cm^*min*bar). an N2flow of 20.30 ml/(cm^*min*bar), and a gas separation factor cx(Gp2/N2) of 0.86. Comparative example 2: A membrane was produced as in example 2. whereby the solvent system was a mixture of 90% by weight isopropyl myristate and 10% by weight castor oil. The polymer fraction in the resulting solution was 47% by weight. The die temperature was set at 248°C. The cooling medium was a mixture of 80% by weight dioctyl adipate and 20% by weight castor oil, tempered to ambient temperature, whereby the cooling medium was a solvent with respect to the polymer component poly(4-methyl-1-pentene). The membrane according to this comparative example had an outside diametel- of 390 pm, a wall thickness of 97 pm, and a porosity of approx. 45% by volume. As evidenced by the SEM images, the exterior surface of the membrane was open-pored with numerous pores larger than 100 nm (Fig. 15). The adjacent support: structure had a pronounced particle structure, and sponge-like, porous structures were not evident (Fig. 16). The membrane exhibited a C02flow of 138 ml/(cm^*min*bar), an N2 flow of 150 ml/(cm^*min*bar), and a gas separation factor a(C02/N2) of 0.92. Comparative example 3: A solution was prepared containing 44% by weight polypropylene and 56% by weight of a solvent system consisting of 75% by weight soybean oil as compound A and 25% by weight castor oil as compound B, whereby soybean oil is not classifiable as a strong solvent with respect to polypropylene. The solution was extmded through a hollow-fiber die at 235X, and the extruded hollow fiber, after passing an air gap of 5 mm in length, was directed through a spinning tube containing a cooling medium consisting of 75% by weight soybean oil and 35% by weight castor oil, i.e., the same combination also used as the solvent system. This solution was extruded through a hollow-fiber die with a 0.3 mm wide annular gap to form hollow fibers. Nitrogen was used as the interior filler. The die had a temperature of 235^*0. After an air section of approx. 5 mm, the hollow fibers passed through a 2 m long spinning tube, through which a cooling medium tempered to 40°C flowed. The flow rate of the cooling medium was adapted to the spinning speed and was approx. 90 m/min. As a result of the cooling in the spinning tube, phase separation and solidification of the hollow filaments took place, so that they could be continuously drawn off from the spinning tube. Subsequently, the hollow filaments were extracted for 6 hours at 60°C in isopropanol to remove the solvent system, and the resulting hollow-fiber membranes were then dried for 6 sec. at 120^*0. A drawing of approx. 5% took place during drying. The resulting hollow-fiber membranes according to this comparative example had an outside diameter of 375 pm, a wall thickness of 55 pm, and a volume porosity of 44.5% by volume. The outside of the membranes also had an open-pored stnjcture with numerous pores larger than 0.1 pm in the exterior surface. The membrane exhibited a CO2 flow of 49.25 ml/(cm^*min*bar), an N2 flow of 56.45 ml/(cm^*min*bar), and a gas separation factor a(C02/N2) of 0.87. As a result, the plasma breakthrough tinges of the membranes according to this comparative example are quite low at 3-5 hours, and the membranes are therefore not suitable for extended-duration use. Comparative examples 4 and 5: 25% by weight poly(4-methyl-1-pentene) was dissolved at 255'*C in 75% by weight of a mixture of 90% by weight isopropyl myristate and 10% by weight glycerin mono-acetate, i.e., in accordance with the definition of the present invention, a mixture of a strong solvent and a strong non-solvent. The homogeneous and clear solution, tempered to 255°C, was applied with a doctor blade to a glass plate maintained at ambient temperature, whereby the distance between the doctor blade and the glass plate was set to 250 |jm. The cooled, porous polymer film was extracted with isopropanol and then dried at ambient temperature. The resulting flat membrane had a pronounced compact and in part particle stmcture over its thickness, with intermediate pore channels (Fig. 17) that extend to the surface facing the glass side during production and there form pores in part exceeding 0.1 pm (Fig. 18). No separation layer was evident. When applying the polymer solution with a doctor blade to a glass plate heated to 100°C, open-pored structures resulted in the area of the membrane wall. However, a separation layer is also not evident in the SEM image of the fracture edge, whereby the SEM image depicts the fracture edge between the membrane wall and the surface that was facing the glass side during membrane production (Fig. 19). This surface is clearly open-pored, with pores in the micrometer range (Fig. 20). Claims: 1. Process for producing an integrally asymmetrical hydrophobic membrane having a sponge-like, open-pored, microporous support structure and a separation layer with a denser structure compared to the support structure, the process comprising at least the steps of: a) preparing a homogeneous solution of 20-90% by weight of a polymer component consisting of at least one polymer, selected from the group of polyolefins, in 80-10% by weight of a solvent system containing a compound A and a compound B that are liquid and miscible with each other at the dissolving temperature, whereby the employed mixture of the polymer component and compounds A and B has a critical demixing temperature and a solidification temperature and has a miscibility gap in the liquid state of aggregation below the critical demixing temperature, and whereby a solvent for the polymer component is selected for compound A, and compound B raises the demixing temperature of a solution consisting of the polymer component and compound A, b) rendering the solution to form a shaped object, with first and second surfaces, in a die having a temperature above the critical demixing temperature, c) cooling of the shaped object using a cooling medium, tempered to a cooling temperature below the solidification temperature, at such a rate that a thermodynamic non-equilibrium liquid-liquid phase separation into a high-polymer-content phase and a low-polymer content phase takes place and solidification of the high-polymer-content phase subsequently occurs when the temperature falls below the solidification temperature, d) possibly removing compounds A and B from the shaped object, characterized in that a strong solvent for the polymer component is selected for compound A, for which the demixing temperature of a solution of 25% by weight of the polymer component in this solvent is at least 10% below the melting point of the pure polymer component, that a weak non-solvent for the polymer component is selected for compound B,"which does not dissolve the polymer component to form a homogeneous solution when heated to the boiling point of compound B and for which the demixing temperature of a system consisting of 25% by weight of the polymer component, 10% by weight of the weak non-solvent, and 65% by weight of compound A, used as the solvent, is at most 10% above the demixing temperature of a system consisting of 25% by weight of the polymer component and 75% by weight of compound A, and that, for cooling, the shaped object is brought into contact with a solid or liquid cooling medium that does not dissolve the polymer component or react chemically with it at temperatures up to the die temperature, 2. Process according to Claim 1, characterized in that the cooling medium is a liquid that is a non-solvent for the polymer component and does not dissolve the polymer component to form a homogeneous solution when heated up to the boiling point of the cooling medium. 3. Process according to one or more of Claims 1 or 2, characterized in that the cooling medium is a liquid that is a strong non-solvent for the polymer component, for which the demixing temperature of a system consisting of 25% by weight of the polymer component, 10% by weight of the strong non-solvent, and 65% by weight of compound A, used as a solvent, is at least 10% higher than the demixing temperature of a system consisting of 25% by weight of the polymer component and 75% by weight of compound A. 4. Process according to one or more of Claims 1 to 3, characterized in that the cooling medium is a homogeneous, single-phase liquid at the cooling temperature. 5. Process according to one or more of Claims 1 to 4, characterized in that the cooling medium has a temperature that is at least 100°C below the critical demixing temperature. 6. Process according to one or more of Claims 1 to 5, characterized in that 30-60% by weight of the polymer component is dissolved in 70-40% by weight of the solvent svstem. 7. Process according to one or more of Claims 1 to 6, characterized in that the at least one polymer forming the polymer component is a polyolefin consisting exclusively of carbon and hydrogen. 8. Process according to Claim 7, characterized in that the at least one polyolefin is a poiy(4-methyl-1-pentene). 9. Process according to Claim 7, characterized in that the at least one polyolefin is a polypropylene. 10. Process according to Claim 7, characterized in that the at least one polyolefin is . a mixture of a poly(4-methyl-1-pentene) and a polypropylene, 11. Process according to Claim 8, characterized in that dioctyl adipate, isopropyl myristate, diphenyl ether, dibenzyl ether, or a mixture thereof is used as compound A. 12. Process according to Claim 8. characterized in that glycerin triacetate, diethyl phthalate. castor oil, N,N-bis(2-hydroxyethyl)tallow amine, soybean oil, or a ^ mixture thereof is used as compound B. 13. Process according to Claim 9, characterized in that dioctyl adipate. isopropyl myristate. or a mixture thereof is used as compound A. 14. Process according to Claim 9. characterized in that diethyl phthalate, glycerin triacetate, castor oil. glycerin diacetate, or a mixture thereof is used as compound B. 15. Process according to one or more of Claims 1 to 14 for producing a hollow-fiber membrane. 16. Hydrophobic integrally asymmetrical membrane, in particular for gas exchange, composed substantially of at least one polymer selected from the group of polyolefins and having first and second surfaces, the membrane having a support layer with a sponge-like, open-pored, microporous stnjcture and adjacent to this support layer on at least one of its surfaces a separation layer with denser structure, characterized in that the pores, if any. in the separation layer have an average diameter 100 nm, that the support layer Is free of macrovoids and the pores in the support layer are on average substantially isotropic, and that the membrane has a porosity in the range from greater than 30% to less than 75% by volume and a gas separation factor a(C02/N2) of at least 1. 17. Membrane according to Claim 16, characterized in that the first surface of the membrane has a separation layer and the second surface on the opposite side of the support layer has an open-pored, network-like structure with approximately circular openings. 18. Membrane according to one or more of Claims 16 or 17, characterized in that the membrane structure changes abruptly in the transition from the separation to the support layer. 19. Membrane according to one or more of Claims 16 to 18, characterized in that the gas separation factor a(C02/N2) is at least 2. 20. Membrane according to one or more of Claims 16 to 19, characterized in that the separation layer has a thickness between 0.01 µm and 5 µm. 21. Membrane according to Claim 20, characterized in that the separation layer has a thickness between 0.1 pm and 2 µm. 22. Membrane according to one or more of Claims 16 to 21, characterized in that the porosity is in the range from greater than 50% to less than 75% by volume. 23. Membrane according to one or more of Claims 16 to 22, characterized in that the membrane has a plasma breakthrough time of at least 20 hours. 24. Membrane according to Claim 23, characterized in that the plasma breakthrough time is at least 48 hours. 25. Membrane according to one or more of Claims 16 to 24, characterized in that the at least one polymer is a polyolefin consisting exclusively of carbon and hydrogen. 26. Membrane according to Claim 25, characterized in that the polyolefin is a poly(4-methyl-1 -pentene). 27. Membrane according to Claim 25, characterized in that the polyol,efin is a polypropylene. 28. Membrane according to Claim 25, characterized in that the membrane is composed substantially of a mixture of a poly(4-methyl-1-pentene) and a polypropylene. 29. Membrane according to one or more of Claims 16 to 28, characterized in that the membrane has a gas flow Q(C02) of at least 5 ml/(cm^*min*bar). 30. Membrane according to one or more of Claims 16 to 29, characterized in that the membrane is a hollow-fiber membrane. 31. Membrane according to one or more of Claims 16 to 30, producible using a process according to one or more of Claims 1 to 15. 32. Use of the membrane according to one or mor^of Claims 16 to 31 for gas transfer. 33. Use of the membrane according to one or more of Claims 16 to 31 for oxy genation of blood. 34. A process for producing an integrally asymmetrical hydrophobic membrane substantially as herein described with reference to the accompanying drawings.

Documents:

in-pct-2001-0971-che abstract-duplciate.pdf

in-pct-2001-0971-che claims-duplcaite.pdf

in-pct-2001-0971-che description(complete)-duplicate.pdf

in-pct-2001-0971-che drawings-duplciate.pdf

in-pct-2001-971-che-abstract.pdf

in-pct-2001-971-che-claims filed.pdf

in-pct-2001-971-che-claims granted.pdf

in-pct-2001-971-che-correspondnece-others.pdf

in-pct-2001-971-che-correspondnece-po.pdf

in-pct-2001-971-che-description(complete)filed.pdf

in-pct-2001-971-che-description(complete)granted.pdf

in-pct-2001-971-che-drawings.pdf

in-pct-2001-971-che-form 1.pdf

in-pct-2001-971-che-form 19.pdf

in-pct-2001-971-che-form 26.pdf

in-pct-2001-971-che-form 3.pdf

in-pct-2001-971-che-form 5.pdf

in-pct-2001-971-che-pct.pdf