Hollow fiber membranes for separating plasma from blood

Abstract

The present invention relates to a hollow fiber membrane for separating plasma from blood, comprising a blood contacting layer and a support layer, each having a hydrophobic polymer, a hydrophilic polymer, and vitamin E, and to a method for producing the hollow fiber membrane to provide the hollow fiber membrane, characterized by reduced hemolysis such that the hollow fiber membrane can be advantageously used in plasma exchange processes.

Description

[Technical Field]

[0001] The subject matter of the present invention relates to hollow fiber membranes for separating plasma from blood. Such hollow fiber membranes are used in extracorporeal blood treatment therapy for patients. The present invention also relates to methods for producing such hollow fiber membranes. [Background technology]

[0002] Hollow fiber membranes are used, inter alia, in extracorporeal blood treatment therapy to separate plasma from a patient's blood and process it using a suitable form of treatment. Such hollow fiber membranes are therefore also called plasma membranes. The treatment for separating plasma from blood is called plasma exchange. The term "plasma exchange" refers to a medical procedure in which plasma is extracted from blood.

[0003] A distinction is made between several plasma exchange methods: in nonspecific plasma exchange, whole plasma is separated from cellular blood components. From a therapeutic point of view, nonspecific separation of plasma from blood requires fluid balance, e.g., replacement with a plasma expander during the procedure and / or addition of fresh plasma to the patient.

[0004] Selective plasma exchange is used, for example, in the treatment of autoimmune diseases. For this purpose, selective hollow fiber membranes are used to separate only a portion of the plasma proteins in plasma. Cascade filtration, which is used in therapeutic procedures, should also be mentioned in this context. Here, plasma can first be nonspecifically separated from blood in a first filtration step, and then selectively separated from this separated plasma in a second filtration step.

[0005] Generally, the term "plasma" refers to the non-cellular portion of blood. Human plasma is composed of approximately 90% water and 10% of substances dissolved therein, particularly plasma proteins (e.g., albumin, lipoproteins, immunoglobulins, fibrinogen), which are also contained in colloidal form. Plasma is more viscous than water due to its content of plasma proteins. Plasma viscosity is primarily determined by the high molecular weight proteins immunoglobulins and fibrinogen. The amount of plasma in a blood volume is approximately 55% by volume, and the amount of blood cellular components is correspondingly approximately 45% by volume.

[0006] In the applied plasma exchange procedure, blood is withdrawn from a patient during extracorporeal blood treatment and passed through a hollow fiber membrane filter through an extracorporeal blood circuit. Plasma separation is achieved within the hollow fiber membrane filter on a suitable hollow fiber membrane through filtration. The plasma is transported and separated across the membrane wall of the hollow fiber membrane by convective transport (i.e., by pressure difference). For this purpose, blood is introduced into the hollow fiber membrane filter and typically passes through the lumen of the hollow fiber membrane. The transmembrane pressure difference, regulated by the device, transports the plasma over the membrane wall, thereby retaining the cellular components of the blood by the membrane wall.

[0007] Hollow fiber membranes intended for plasma separation must therefore satisfy certain requirements to enable therapeutic plasma separation, as described herein. The pores of the plasma membrane are such that components of the plasma, i.e., plasma proteins, can pass through the membrane. In particular, certain types of treatments require that high molecular weight plasma proteins, such as "low-density lipoproteins" (LDL), which have a molecular weight of approximately 2.7 MDa, must also be able to pass through the membrane wall of the hollow fiber membrane, while blood cells will be retained due to the pore size. For certain plasma exchange procedures, it may be necessary for not all plasma proteins of the plasma to pass through the membrane wall, but only a portion of the plasma proteins in the lower molecular weight range.

[0008] Hollow fiber membranes for plasma separation from blood therefore differ from known hollow fiber membranes used in hemodialysis by their pore size. In extracorporeal hemodialysis treatment, it is particularly necessary to separate low- and medium-molecular-weight metabolic products from the patient's blood. However, these hollow fiber membranes for extracorporeal blood treatment are such that albumin, with a molecular weight of approximately 66 kDa, is almost completely retained by the hollow fiber membrane. In contrast, plasma separation requires that the pore size of the selective layer of the membrane be as large as possible compared with the cellular components of the blood so that cellular components are excluded from passing through the membrane while plasma proteins can pass through the membrane wall.

[0009] Separation of plasma from blood using hollow fiber membranes is usually accompanied by the harmful occurrence of hemolysis. It is suspected that the membrane structure caused by the large pores of hollow fiber membranes, combined with the transmembrane pressure difference required for filtration, exerts mechanical force on blood cells, causing cell damage and destroying red blood cells. The occurrence of hemolysis during plasma separation is problematic from a therapeutic standpoint. In this case, the separated plasma is contaminated with hemoglobin and cell debris, and therefore cannot be used for further therapeutic steps.

[0010] DE 10 2007 019 051 B3 discloses a two-layer hollow fiber membrane for the separation of plasma from blood produced by coextrusion from two rotating masses. The hollow fiber membrane is characterized by a coarse-mesh selective blood-contacting layer and a porous support layer.

[0011] DE 10 2017 201 630 A1 describes the production of hollow fiber membranes for blood treatment by extrusion of a spun mass, the spun mass containing a certain amount of vitamin E and the internal precipitant containing a certain proportion of a hydrophilic polymer. [Prior art documents] [Patent documents]

[0012] [Patent Document 1] DE 10 2007 019 051 B3 [Patent Document 2] DE 10 2017 201 630 A1 [Patent Document 3] DE 102016224627 A1 [Patent Document 4] DE10211051 Summary of the Invention [Problem to be solved by the invention]

[0013] In view of the above problems, according to a first aspect there is provided a hollow fiber membrane for the separation of plasma from blood which exhibits reduced hemolysis.

[0014] In a second aspect, it is an object to find a method for producing the above-mentioned hollow fiber membranes for plasma separation.

[0015] A third aspect of the underlying problem is to provide a sterile hollow fiber membrane filter for the separation of plasma from blood with low hemolysis so that it can be advantageously used in plasma exchange procedures. [Means for solving the problem]

[0016] In a first aspect of the invention, the underlying problem is solved by a hollow fiber membrane having the features of claim 1. Dependent claims 2 to 9 represent advantageous embodiments.

[0017] In a second aspect of the invention, the underlying problem is solved by a method having the features according to claim 10. Dependent claims 11 to 14 present advantageous embodiments of the process.

[0018] In a third aspect of the invention, the underlying problem is solved by a sterile hollow fiber membrane filter having the features according to claim 15. [Brief explanation of the drawings]

[0019] [Figure 1] FIG. 1 is a schematic diagram of the apparatus. [Figure 2]FIG. 2 is a schematic diagram of the apparatus for measuring the LDL sieving coefficient. [Figure 3] FIG. 3 is a cross section of a comparative hollow fiber membrane subjected to a hemolysis test. [Figure 4] FIG. 4 is a cross section of a hollow fiber membrane prepared according to the example and subjected to a hemolysis test. DETAILED DESCRIPTION OF THE INVENTION

[0020] A first aspect of the present invention relates to a hollow fiber membrane for separating plasma from blood, comprising a blood contact layer and a support layer, each containing a hydrophobic polymer and a hydrophilic polymer, and vitamin E, particularly α-tocopherol or tocotrienol, wherein the vitamin E, particularly α-tocopherol or tocotrienol, is present in an amount of 0.005 to 0.25% by weight based on the total weight of the hollow fiber membrane, and wherein the hollow fiber membrane has a sieving coefficient for albumin determined in accordance with DIN EN ISO 8637-3:2018 of 50 to 100%, or a sieving coefficient for immunoglobulin M determined in accordance with DIN EN ISO 8637-3:2018 of 50 to 100%, or a sieving coefficient for low-density lipoproteins determined in accordance with DIN EN ISO 8637-3:2018 of 80 to 100%.

[0021] The hollow fiber membranes according to the invention advantageously have a lower hemolytic effect and are therefore superior to comparable hollow fiber membranes that do not contain vitamin E. In addition, the hollow fiber membranes according to the invention also exhibit improved characteristics of reduced tendency to blood coagulation and reduced triglyceride concentration and are therefore also superior to comparable hollow fiber membranes without vitamin E. Triglycerides are preferentially absorbed onto poorly hydrophilic surfaces, thus permanently impairing the permeation and selectivity properties of the filter during the course of treatment.

[0022] We hypothesize that the amount of vitamin E in the hollow fiber membrane causes immobilization of polyvinylpyrrolidone at the membrane surface, thus leading to improved, i.e., reduced, hemolysis in large-pore hollow fiber membranes intended for separating plasma from blood. In this context, the term "large-pore" refers to hollow fiber membranes having the sieving coefficients described above for albumin, immunoglobulin M (IgM), or low-density lipoprotein (LDL). Preferably, the openings at the surface of the blood-contacting layer have a width of 0.1 to 10 μm to substantially separate plasma from blood. In prior art embodiments, these openings are so large that blood cells penetrate the openings at the membrane surface of the hollow fiber membrane during the process of separating plasma from blood and may rupture due to the process-related transmembrane pressure difference. As determined by scanning electron microscopy, fewer blood cells penetrate the openings at the membrane surface of the hollow fiber membranes according to the present invention, resulting in the observed reduced hemolysis of the hollow fiber membrane. In an advantageous embodiment, the proportion of vitamin E, in particular α-tocopherol or tocotrienol, in the hollow fiber membrane is between 0.01 and 0.15% by weight, more preferably between 0.03 and 0.1% by weight, based on the total weight of the hollow fiber membrane.

[0023] For the purposes of this application, "sieving coefficient for albumin" refers to the permeability of a hollow fiber membrane to albumin as determined in accordance with DIN EN ISO 8637-3:2018. Albumin is a plasma protein with a molecular weight of 66 kDa. This embodiment allows for the separation of a portion of plasma proteins from blood or a selective range of plasma proteins from plasma during cascade filtration. The hollow fiber membrane preferably has a sieving coefficient for albumin of 60-100%, more preferably 70-100%.

[0024] Within the meaning of the present application, the term "sieving coefficient for immunoglobulin M" is to be understood as the permeability of a hollow fiber membrane to immunoglobulin M (IgM) determined according to the method of DIN EN ISO 8637-3:2018. IgM is a plasma protein with a molecular weight of 950 kDa. This embodiment allows for the separation of plasma protein fractions from blood or, in the case of cascade filtration, from plasma with a larger, specific molecular weight range of plasma proteins. The hollow fiber membrane provided by this embodiment can be used in treatments requiring the separation of plasma according to a defined molecular weight range, for example, in specific plasma exchange. The hollow fiber membrane preferably has a sieving coefficient for IgM of 60-100%, more preferably 70-100%.

[0025] Within the meaning of the present application, the term "sieving coefficient for low-density lipoproteins" is to be understood as the permeability of a hollow fiber membrane to low-density lipoproteins (LDL) determined according to the method of DIN EN ISO 8637-3:2018. LDL is a plasma protein with a molecular weight of 2,700 kDa. This embodiment allows for the total separation of plasma proteins from blood in separation processes, such as nonspecific plasma exchange. The hollow fiber membrane provided by this embodiment can be used in treatments requiring complete separation of plasma from blood. The hollow fiber membrane preferably has a sieving coefficient for LDL of 80 to 100%, more preferably 90 to 100%.

[0026] Within the meaning of the present application, the "blood contact layer" is understood to be one layer of the hollow fiber membrane that constitutes the layer exposed to the patient's blood in extracorporeal blood treatment. Advantageously, the blood contact layer has a thickness of 1 μm to 15 μm, preferably 2 to 10 μm, more preferably 3 to 6 μm, and its porous structure is designed to allow effective separation of plasma from blood. Preferably, the pore size in the blood contact layer can be 0.1 to 10 μm. Within the scope of the present application, the "support layer" is understood to be a layer that provides the necessary mechanical stability for the hollow fiber membrane that is further processed into a hollow fiber membrane filter and during sterilization treatment. The thickness of the support layer is preferably 25 to 79 μm, or 30 to 77 μm, or 34 to 74 μm. Preferably, the pore structures of the blood contact layer and the support layer are different. The pores of the blood contact layer are also preferably smaller than those of the support layer. Different pore structures can be selectively controlled by the manufacturing process of the hollow fiber membrane with a non-solvent induced phase inversion process, for example, by a "wet and dry" spinning process. Temperature induced phase inversion processes are also contemplated.

[0027] Within the meaning of the present application, a "hydrophobic polymer" is understood to be a polymer having a solubility in water of less than 0.1 g / l. For the purposes of the present invention, hydrophobic polymers that can be used are polysulfone (PSU), polyethersulfone (PES), polyphenylsulfone, copolymers containing sulfone groups, polyetherimide (PEI), polyamide (PA), polycarbonate (PC), polystyrene (PS), polymethyl methacrylate (PMMA), polyacrylonitrile (PAN), polyimide (PI), and polyurethane (PU). Within the meaning of the present application, a "hydrophilic polymer" is understood to be a polymer having a solubility in water of at least 1 g / l. For the purposes of the present invention, polyvinylpyrrolidone (PVP) or polyethylene glycol and their copolymers can be used as hydrophilic polymers. In the context of the present application, the term "solubility in water" means that the hydrophobic / hydrophilic polymer dissolves in water to give an optically transparent solution as determined by visual observation in the visible wavelength range of light without the occurrence of any turbidity, sol-gel formation, aggregation, or precipitation.

[0028] Within the meaning of the present application, the term "vitamin E" is to be understood as a general term for fat-soluble substances with antioxidant properties. In particular, this term encompasses the frequently occurring forms of vitamin E: tocopherol, tocotrienol, tocomonoenol (T1), and MDT (marine tocopherol).

[0029] In a first embodiment, the present invention is characterized in that the hollow fiber membrane is composed of at least two coextruded layers, one of which forms a blood contact layer and the other of which forms a support layer. This embodiment provides two layers in the hollow fiber membrane, thereby improving the individual layers in terms of their functions as a blood contact layer and a support layer. In particular, the thickness, composition, and pore structure of the blood contact layer and the support layer can differ in function. This embodiment offers the advantage that the blood contact layer is optimized for hemolysis, while the support layer is advantageously designed for mechanical stability, particularly for sterilization resistance of the hollow fiber membrane.

[0030] In the embodiment according to the first aspect and in the above-described embodiments, the invention is characterized in that the blood contact layer is the inner layer of the hollow fiber membrane and the support layer is the outer layer, which allows the blood contact layer to be designed particularly precisely with regard to its separation behavior.

[0031] In yet another embodiment according to the first aspect, the present invention is characterized in that the hydrophobic polymer comprises or consists of polysulfone and / or the hydrophilic polymer comprises or consists of polyvinylpyrrolidone. The term "polysulfone" is understood to mean a polymer having sulfone groups in the main chain or side chains of the polymer. Within the meaning of the present application, the term "polysulfone (PSU)" is understood as a general term for all polymers containing sulfone groups. Typical representatives of polysulfone-based materials are polysulfone (PSU), polyethersulfone (PES), polyphenylsulfone, and copolymers containing sulfone groups. Polysulfone materials have proven to be steam sterilizable, have good hemocompatibility, and are therefore superior to other materials for the production of blood-treating membranes.

[0032] [ka]

[0033] In yet another version of the first aspect, the hollow fiber membrane is characterized by a polyvinylpyrrolidone content of 4-9% by weight, preferably 5-8%, and more preferably 5-7%. The polyvinylpyrrolidone content imparts hydrophilic properties to blood. In this context, the term "hydrophilic hollow fiber membrane" means that the hollow fiber membrane can be fully wetted by blood without requiring a prior hydrophilization treatment, such as pressure rinsing of the hollow fiber membrane with water. The easy wettability of the hollow fiber membrane by blood enables effective separation of plasma or a portion of plasma in a plasma separation process.

[0034] The term "polyvinylpyrrolidone" defines a polymer containing repeating units of vinylpyrrolidone or its derivatives. PVP is a water-soluble polymer that hydrophilizes hydrophobic polysulfone materials, making them more wettable by blood and thus improving the hemocompatibility of hollow fiber membranes made from polysulfone. Other comonomers can be added to vinylpyrrolidone, e.g., vinyl acetate polymers. These copolymers have the advantage that they form particularly stable hydrogels. Surprisingly, it has been found that the tendency to hemolysis is particularly reduced when the PVP content is set very high.

[0035] [ka]

[0036] In yet another embodiment of the first aspect, the hollow fiber membrane is characterized in that it exhibits an internal diameter of 250-400 μm, preferably 280-380 μm, more preferably 300-360 μm. If the internal diameter is too small, the transmembrane pressure increases and thus the tendency for hemolysis increases, while if the internal diameter is too large, the filtration performance decreases.

[0037] In yet another embodiment according to the first aspect or one of the above-mentioned embodiments of the first aspect, the hollow fiber membrane is characterized by a wall thickness ranging from 40 to 80 μm. The wall thickness provides a favorable strength for the hollow fiber membrane. Wall thicknesses greater than about 80 μm have a negative effect on the filtration properties of the hollow fiber membrane. Advantageous wall thicknesses are 50 to 70 μm, more preferably 60 to 70 μm.

[0038] In yet another embodiment according to at least one of the above-described embodiments of the first aspect, the hollow fiber membrane has a polyvinylpyrrolidone content of 30-60 wt %, preferably 35-55 wt %, more preferably 40-50 wt %, in the blood contact layer near the surface, as determined by XPS measurements. The polyvinylpyrrolidone content in the near-surface layer of the blood contact layer can be adjusted during production of the hollow fiber membrane by a preset ratio of hydrophobic polymer, preferably PSU, to hydrophilic polymer, preferably PVP, in the spun mass. In one embodiment, the composition of the spun mass from which the blood contact layer is obtained is selected so that a higher proportion of PVP is present compared to the support layer. It is hypothesized that this proportion of vitamin E in the spun mass forming the blood contact layer of the hollow fiber membrane immobilizes PVP in the near-surface layer during the manufacturing process of the hollow fiber membrane, thus resulting in a higher proportion of PVP in the blood contact layer, particularly near the surface of the blood contact layer. Electron microscope images according to Figures 4 and 5 show that fewer blood cells penetrate the openings of the blood contact layer in hollow fiber membranes according to the invention than in comparable hollow fiber membranes without vitamin E. Surprisingly, this different finding correlates with the lower hemolytic effect observed for hollow fiber membranes according to the invention compared to the reference hollow fiber membrane. Clearly, penetration of blood cells into the openings of the blood contact layer is a crucial cause of the hemolysis observed on hollow fiber membranes for separating plasma from blood.

[0039] In yet another embodiment according to at least one of the above-mentioned embodiments of the first aspect, the hollow fiber membrane is characterized in that the near-surface layer of the hollow fiber membrane opposite the blood-contacting layer has a polyvinylpyrrolidone content of 25-50 wt.%, preferably 30-45 wt.%, more preferably 30-40 wt.%, as determined by XPS measurements. This embodiment ensures low adsorption of plasma components even on the surface opposite the blood-contacting side.

[0040] In yet another embodiment according to at least one of the above-mentioned embodiments of the first aspect, the hollow fiber membrane is characterized in that the difference in PVP content in wt. % between the near-surface layer on the blood-contacting side and the near-surface layer on the face of the hollow fiber membrane opposite the blood-contacting side, as determined by XPS measurement, is at least 5 wt. %, preferably at least 7 wt. %, more preferably at least 10 wt. This embodiment has particularly low total adsorption of blood and plasma components.

[0041] In another embodiment, the hollow fiber membrane is characterized in that the blood contact layer forms the inner layer of the hollow fiber membrane. This embodiment therefore reduces the tendency for hemolysis compared to embodiments in which the blood contact layer forms the outer layer of the hollow fiber membrane. Furthermore, such an embodiment reduces the amount of residual blood that accumulates in the filter after treatment has ended.

[0042] In yet another version of the first aspect, the hollow fiber membrane is characterized in that the blood contact layer has a thickness of 1 to 15 μm. The thickness of the blood contact layer contributes little to the mechanical stability of the hollow fiber membrane due to its high porosity. The thickness of the blood contact layer should not be too large compared to the support layer to avoid compromising the strength of the hollow fiber membrane.

[0043] In a second aspect, the present invention relates to a method for producing a hollow fiber membrane according to the present invention, said method comprising the following process steps: providing a spinning mass A comprising 15-25% by weight of a hydrophobic polymer, 4-8% by weight of a hydrophilic polymer, 0.2-2% by weight of a polar protic substance, and 0.001-0.05% by weight of vitamin E, in particular α-tocopherol or tocotrienol, and 83.799-64.95% by weight of a polar aprotic solvent; providing a spinning mass B comprising 8 to 12% by weight of a hydrophobic polymer, 3 to 7.5% by weight of a hydrophilic polymer, 0.001 to 0.05% by weight of vitamin E, in particular α-tocopherol or tocotrienol, and 88.999 to 81.95% by weight of a polar aprotic solvent; providing an internal precipitant comprising 70-90 wt. % polar aprotic solvent and 10-30 wt. % polar protic mixed liquid; co-extruding the spinning mass A, the spinning mass B, and the internal precipitant through the spinning nozzle to form a spun yarn, wherein the internal precipitant is extruded through a central bore of the spinning nozzle, the spinning mass B is extruded through a first concentric annular slit surrounding the central bore, and the spinning mass A is extruded through a second concentric annular slit surrounding the first concentric annular slit and the central bore of the spinning nozzle; passing the spun yarn through a spinning gap; introducing the yarn into a precipitation bath; and Precipitating spun yarn to form hollow fiber membranes.

[0044] The manufacturing process is based on the so-called "wet-dry" spinning process. In the "wet-dry" process, the spinning mass is extruded through a spinning nozzle, passes through a dry spinning gap, and then is introduced into a precipitation bath. The "spinning gap" refers to the vertical section between the outlet opening of the spinning nozzle and the precipitation bath, through which the extruded spinning yarn passes before being introduced into the precipitation bath. The "spinning mass" is a homogeneous polymer solution. It is understood that the "spinning yarn" is the spinning mass extruded from the nozzle that has not yet formed the final membrane structure. In this method for producing hollow fiber membranes, the spinning process is carried out by coextrusion of two spinning masses and an internal precipitant. Spinning mass A forms the support layer of the hollow fiber membrane. Spinning mass B forms the blood-contacting layer of the hollow fiber membrane. The composition of spinning masses A and B and the composition of the internal precipitant, as well as the selection of spinning parameters such as temperature control of the spinning mass, temperature control of the spinning nozzle, spinning speed, and spinning gap height, affect the porous properties of the hollow fiber membrane. In this context, a "polar aprotic" solvent is understood as a solvent that dissolves the hydrophobic and hydrophilic polymers in the spinning mass but only has low CH acidity. Typical representatives of polar aprotic solvents are dimethyl sulfoxide (DMSO), dimethylformamide (DMF), dimethylacetamide (DMAc), and N-methylpyrrolidone (NMP). A "polar protic substance" is understood as a CH acidic substance. Preferred representatives are water, ethanol, or methanol.

[0045] The temperature of the precipitation bath is adjusted to 50-80°C, in particular 60-70°C. Temperature control of the precipitation bath allows for adjustment of the atmospheric humidity in the spinning gap, which in turn supports the formation of pores on the outside of the spun yarn. The precipitation bath preferably consists of an aqueous solution, particularly suitable being water containing less than 5% by weight of one of the aprotic polar solvents mentioned.

[0046] The proportions of the individual components in the spin mass are decisive for the viscosity of the spin mass. The viscosity of spin mass solution A is 7000-18000 mPa·s, in particular 9000-14000 mPa·s. Spinning solution A typically contains 15 to 25 wt%, preferably 18 to 23 wt%, more preferably 19 to 21 wt% of a hydrophobic polymer, in particular polysulfone (PSU), 4 to 8 wt%, preferably 5 to 7 wt%, more preferably 5 to 6 wt% of a hydrophilic polymer, in particular polyvinylpyrrolidone (PVP), 0.02 to 2 wt%, preferably 0.5 to 1.5 wt%, more preferably 0.8 to 1.2 wt% of a polar protic substance, preferably water, 0.001 to 0.05 wt%, preferably 0.005 to 0.03 wt%, more preferably 0.008 to 0.02 wt% of vitamin E, in particular α-tocopherol or tocotrienol, and 80.799 to 64.95 wt%, or 76.495 to 64.95 wt%, or 75.192 to 64.95 wt% of a polar aprotic solvent, preferably DMAc. Preferred is, for example, 17.5 to 22.5% by weight of PSU, 5 to 8% by weight of PVP, 0.008 to 0.02% by weight of vitamin E, especially α-tocopherol or tocotrienol, the remainder to 100% by weight being DMAc.

[0047] The viscosity of spinning mass solution A was determined using a rotational viscometer (VT 550 from Haake, Germany) at 40 °C in step r.2 (6 rpm) with a rotor “MV1 (MV-DIN)” from Haake (shear rate 7.7 / s).

[0048] The viscosity of spinning mass solution B is preferably less than 1000 mPa-s, and contains 8 to 12 wt. %, preferably 9 to 11 wt. %, more preferably 9.5 to 10.5 wt. % of a hydrophobic polymer, preferably PSU, 3 to 7.5 wt. %, preferably 4.5 to 7 wt. %, more preferably 5 to 6 wt. % of a hydrophilic polymer, preferably PVP, 0.001 to 0.05 wt. %, preferably 0.005 to 0.03 wt. %, more preferably 0.008 to 0.02 wt. % of vitamin E, in particular α-tocopherol or tocotrienol, and 88.999 to 81.95 wt. %, or 86.495 wt. %, or 85.492 wt. % of a polar aprotic solvent, preferably DMAc. Preferably, it is 9-10% by weight of PSU, 5-6% by weight of PVP, 0.008-0.02% by weight of vitamin E, particularly α-tocopherol or tocotrienol, with the remainder up to 100% by weight being DMAC.

[0049] The viscosity of spinning mass solution B was determined according to a rotational viscometer (VT 550 from Haake, Germany) at 40 °C in step r.3 (30 rpm) using a rotor "MV1 (MV-DIN)" from Haake (shear rate 38.7 / s).

[0050] The different viscosities of the two spin masses A and B result in different porosities in the two coextruded layers: spin mass A provides the support layer of the hollow fiber membrane, and spin mass B provides the blood contact layer of the hollow fiber membrane.

[0051] Regarding the viscosity of spin mass solution B, this should typically not be below 300 mPa-s, otherwise spin mass B may no longer be extruded uniformly.

[0052] In the context of the present invention, the membrane wall thickness and the inner diameter of the hollow fiber membranes may vary. The membrane wall thickness of the hollow fiber membranes according to the present invention is typically 40-80 μm, preferably 50-70 μm, more preferably 60-70 μm.

[0053] The desired porous structure of Layer B is formed by the treatment according to the present invention with an internal precipitant comprising or consisting of 70-90 wt. %, preferably 75-85 wt. %, more preferably 78-82 wt. % of a polar aprotic solvent, preferably DMAc, and 10-30 wt. %, preferably 25-15 wt. %, more preferably 22-18 wt. % of a polar mixed liquid, preferably water. For the purposes of the present invention, a "polar protic mixed liquid" is a CH acidic liquid, preferably water, ethanol, or methanol.

[0054] In a version according to the second aspect, the treatment is characterized in that the spun masses A and B are tempered to 60-80°C, preferably 65-75°C, and / or the internal precipitant is tempered to 50-70°C, preferably 55-65°C.

[0055] The rate of membrane formation in the spinning process is affected by the spinning speed. The spinning speed is 300 to 500 mm per second, preferably 350 to 480 mm per second, and more preferably 380 to 430 mm per second. "Spinning speed" refers to the speed at which the spun yarn passes through the spinning gap. Furthermore, the height of the spinning gap affects membrane formation in the spinning process. In the process according to the present invention, the spinning gap is 5 to 80 mm, preferably 10 to 50 mm, and more preferably 15 to 40 mm.

[0056] Additionally, a washing process for the hollow fiber membranes is combined with the spinning process. The precipitated hollow fiber membranes pass through several rinsing baths during the process. The temperature of the rinsing baths is typically in the range of 60-80°C. In the rinsing baths, the hollow fiber membranes are freed from solvent and excess PVP that was not fixed to the hollow fiber membrane after precipitation. The hollow fiber membranes are freed from this portion of polyvinylpyrrolidone as much as possible, because otherwise, PVP that may leach from the hollow fiber membranes could enter the bloodstream during therapeutic treatment.

[0057] After the rinsing step, the hollow fiber membrane is dried, which is preferably carried out at 90-160°C, preferably 100-150°C, more preferably 120-140°C.

[0058] In yet another embodiment according to the second aspect, the method is characterized by: the hydrophobic polymer of the spun mass A comprises or consists of polysulfone, and / or the hydrophilic polymer of the spun mass A comprises or consists of polyvinylpyrrolidone, and / or The polar protic substance of the spun mass A comprises or consists of water, and / or the polar aprotic solvent of the spinning mass A comprises or consists of dimethyl sulfoxide, dimethyl formamide, dimethyl acetamide, N-methylpyrrolidone, or mixtures thereof; and / or the hydrophobic polymer of the spun mass B contains or consists of polysulfone, and / or the hydrophilic polymer of the spun mass B comprises or consists of polyvinylpyrrolidone, and / or the polar aprotic solvent of the spinning mass B comprises or consists of dimethyl sulfoxide, dimethyl formamide, dimethyl acetamide, N-methylpyrrolidone, or mixtures thereof; and / or The polar protic liquid mixture of the internal precipitate water comprises or consists of water.

[0059] In yet another version according to the second aspect, the process is characterized in that the internal precipitant does not contain a hydrophilic polymer. Surprisingly, it has been found that high concentrations of a hydrophilic polymer, such as PVP, can be produced in the near-surface layer of the blood-contacting layer by the method of the present invention without the need to add a corresponding hydrophilic polymer, such as PVP, to the internal precipitant.

[0060] The hollow fiber membranes are sterilized following their production. The hollow fiber membranes are first used to manufacture hollow fiber membrane filters. The manufacture of hollow fiber membrane filters is known to those skilled in the art and will not be described in detail here. In this regard, reference is also made to the description of this method contained herein, which describes the manufacture of experimental hollow fiber membrane filters.

[0061] Methods for sterilizing hollow fiber membrane filters according to the invention are also known in the art. The sterilization of the hollow fiber membranes described herein was carried out according to the method described in detail in DE 102016224627 A1.

[0062] In a third aspect, the present invention relates to a sterile hollow fiber membrane filter comprising a plurality of hollow fiber membranes according to the first aspect of the invention or produced by the method according to the second aspect of the invention, wherein the hollow fiber membrane filter has been previously sterilized by a steam sterilization process.

[0063] Description of the invention based on the drawings method Below, methods for characterizing hollow fiber membranes according to the present invention and comparative hollow fiber membranes are described.

[0064] 1. Fabrication of Hollow Fiber Membrane Filters To manufacture the hollow fiber membrane filter, hollow fiber membranes with an inner diameter of 330 μm and a wall thickness of 65 μm are used. The hollow fiber membranes are bundled and sealed at the ends of the hollow fiber membrane filter housing with a hardenable embedding mass material to form a first space ("blood side") that encloses the interior of the hollow fiber membranes and a second space ("filtrate side") that encloses the space between the hollow fiber membranes. The embedding material used is a polyurethane from BASF (elastogran) (polyol C6947 and isocyanate 136 20). The housing diameter, embedding height at the bundle ends, and effective length of the hollow fiber membranes correspond to the plasmaFlux P1 and P2 plasma filters available from Fresenius Medical Care, Bad Homburg, Germany. The effective length of the hollow fiber membrane is the length of the hollow fiber membrane without any embedding, which can be used to determine permeation properties such as sieving coefficient, hemocompatibility data, and ultrafiltration coefficient. The effective membrane area obtained from the active hollow fiber membrane length of the investigated hollow fiber membrane filters was 0.3 and 0.6 m in two different embodiments. 2The filters are steam sterilized according to DE 102016224627.

[0065] 2. Measurement method for determining polyvinylpyrrolidone content in hollow fiber membranes 1 g of membrane is removed from a sterile hollow fiber membrane filter as described in Method 1 and placed in an isothermal generator (Porotec, Hofheim / Ts, Germany). Measurements start at 0% relative humidity and wait until the weight is constant. Afterwards, the humidity is increased in 10% steps and wait until the weight is constant until 60% relative humidity is reached. Measurements are performed at 25°C and 40°C.

[0066] For the determination of PVP content, the water absorption of polysulfone granules and PVP powder as used in the embodiment was determined for comparison, and the results are shown in the table below. TIFF0007770343000003.tif21145 The determination of the PVP content of the hollow fiber membrane samples examined at a test temperature of 25°C is carried out by Equation 1: TIFF0007770343000004.tif10150 formula 1 The determination of the PVP content of the hollow fiber membrane samples examined at a test temperature of 40°C is carried out by Equation 2: TIFF0007770343000005.tif10150 formula 2

[0067] 3. Exposure of test blood (hemolysis test) To determine the hemocompatibility of the hollow fiber membrane under investigation, human test blood is placed in contact with the hollow fiber membrane. Hemocompatibility in this context refers to the hemolytic and adsorption properties (triglyceride and platelet adsorption) of the hollow fiber membrane. For this purpose, 500 ml of human whole blood is drawn with a 17G (1.5 mm) needle from a healthy donor who is not taking any medications that may affect blood coagulation or platelet properties. The drawn blood is heparinized as described below. 750 IU of heparin diluted with 50 ml of saline is placed in a blood bag. The whole blood is added to the donated heparin solution and mixed to give a heparin concentration of 1.5 IU per ml of the mixture. The method for determining the hemocompatibility of the hollow fiber membrane is initiated within 30 minutes of the blood donation.

[0068] The hollow fiber membrane to be investigated was tested in a hollow fiber membrane filter in an apparatus shown schematically in FIG. 1. As shown in FIG. 1, the apparatus 1-1 includes the hollow fiber membrane filter to be investigated for plasma separation 1-2 in the configuration described in Method 1. The apparatus further includes a piping system 1-3, a peristaltic pump 1-4, a blood collection site 1-5, a reservoir 1-6 for blood, a pressure sensor 1-7 at the blood outlet 1-8 of the hollow fiber membrane filter 1-2, and a pressure sensor 1-9 at the blood inlet 1-10 of the hollow fiber membrane filter 1-2. 113 ml of heparinized blood as described herein was used for this determination. The blood was pumped through the apparatus 1-1 via the hollow fiber membrane filter 1-2 with the aid of a peristaltic pump 1-4 (manufacturer: Fresenius Medical Care, Germany) through the piping system 1-3 (material: PVC, manufacturer: Fresenius Medical Care, Germany). A new hose system was used for each measurement. The entire device 1-1 was rinsed with 0.9% (w / v) saline for 30 minutes before measurement. To prime the device with blood, the rinse solution was replaced by blood introduced into the device at a low pumping speed and drained until the device was filled with pure blood or the filtrate side of the hollow fiber membrane filter was filled with plasma. The blood filling volume was 113 ml. The replaced solution was discarded.

[0069] The filtered plasma is discharged from the hollow fiber membrane filter and reintroduced into the blood downstream of the blood outlet 1-8 of the hollow fiber membrane filter 1-2. The exposure experiment is carried out, for example, at 37°C for a predetermined period in an incubator (Memmert, Germany). At the start of the measurement and after a predetermined time, samples are taken at the blood collection site 1-5. The pressure at the blood outlet 1-8 and the blood inlet 1-10 is measured to ensure constant conditions during the determination. In the event of a significant pressure change, the measurement must be discarded. Blood was pumped through the device at a flow rate of 200 ml / min.

[0070] 4. Measurement method for measuring transmembrane pressure during filtration tests The transmembrane pressure (TMP) is determined according to the pressure gauges P1, P2, and P3 shown in Figure 1. Equation 3 applies: TIFF0007770343000006.tif9150 formula 3

[0071] 5. Measurement methods for determining platelet concentration in blood To determine the platelet concentration in the blood, blood samples taken at predetermined times before and after the exposure test are evaluated. The analytical data are determined using a K-4500 device from Symex (blood cell count determination) using the electrical resistance measurement principle. A capillary tube suitable for measuring red blood cells and platelets is used in the device's measuring unit. The measuring transformer and electrodes are immersed in a conductive liquid so that a constant current can flow between the inner and outer electrodes. Non-conductive platelets are drawn through the opening of the measuring transducer. As the cells pass, they displace the diluent. Because the electrical resistance of the cells is higher than that of the diluent, a voltage change proportional to the resistance change occurs. The voltage increase is proportional to the cell volume, making it possible to distinguish between red blood cells and platelets. The determined platelet count is a measure of blood clotting occurring in the blood-contacting layer of the hollow fiber membrane. High platelet adsorption loss increases the tendency for clotting and therefore the tendency for blockages to form in the filter.

[0072] 6. Measurement method for determining hemoglobin level (HGB) Plasma samples taken at predetermined times before and after the exposure experiment are evaluated. HGB is measured using the sodium lauryl sulfate (SLS) method. Hemoglobin concentration is determined in an HGB cuvette at a wavelength of 555 nm. A spectrophotometer EVOLUTION 210 (Thermo Fisher Scientific, Dreieich, Germany) equipped with a 7x cell holder is used for this purpose using the "free hemoglobin" measurement method. 1.5 ml semi-micro PMMA disposable cells from Brand, Giessen, Germany are used. Hemoglobin originates from blood cells, particularly red blood cells, destroyed during plasma separation. The determined hemoglobin value is a measure of the hemolytic activity of the hollow fiber membrane under investigation. The lower the determined hemoglobin value, the lower the hemolytic activity of the hollow fiber membrane. Free hemoglobin is a measure of red blood cell destruction.

[0073] 7. Measurement Method for Triglyceride Concentration Blood samples taken at predetermined times before and after the exposure test are evaluated to determine the triglyceride concentration in the blood. The percent triglyceride loss is determined from this difference. Triglyceride concentration is determined by the following method: A whole blood sample is drawn into a 1.2 ml Li-Heparin Monovette (Ref. No. 06.1666.001, Sarstedt company, Nümbrecht, Germany) and centrifuged at 4000 rpm for 10 minutes. The plasma is transferred into a sample container. Triglycerides are converted and utilized in a color reaction. The Wahlefeld method uses lipoprotein lipase for the complete hydrolysis to glycerol, followed by oxidation to dihydroxyacetone phosphate and hydrogen peroxide. The resulting hydrogen peroxide forms a red pigment under the catalysis of peroxidase with 4-aminophenazone and 4-chlorophenol in the Trinder end-point reaction, which can be determined photometrically as a proportion of triglycerides. A Cobas INTEGRA 400 Plus analyzer (Roche Diagnostic, Mannheim, Germany) equipped with the "TRIGL" method is used for this purpose. This method allows the reduction in triglyceride concentration in mg / dl to be calculated after the exposure time.

[0074] 8. Measurement method for determination of red blood cells on the membrane surface by scanning electron microscopy At the end of the exposure experiment, the pump speed is increased until the desired transmembrane pressure (TMP) is reached. For the comparative hollow fiber membrane examples described below, a TMP of 130 mmHg was set, and for the examples described below, a TMP of 183 mmHg was set. The experiment is then stopped, and the filters are washed with isotonic saline. Individual hollow fiber membranes are harvested from the hollow fiber membrane filters. The removed hollow fiber membranes are opened to expose their inner surfaces, which can then be examined under a scanning electron microscope. The scanning electron microscope is performed at an accelerating voltage of 5 kV and a magnification of 3000x. A qualitative description of the penetration behavior of red blood cells into the membranes is provided.

[0075] 9. Measurement method for the determination of polyvinylpyrrolidone in the near-surface layer (XPS) The content of polyvinylpyrrolidone in the near-surface layer of the blood contact layer was measured by photoelectron spectroscopy (XPS or ESCA). This method is used to determine the amount of polyvinylpyrrolidone in a 5-10 nm layer adjacent to the surface of the blood contact layer of the hollow fiber membrane. This layer examined by the XPS method is referred to as the "near-surface layer" for the purposes of this application. To examine the near-surface layer, predetermined measurement conditions are set for this purpose.

[0076] The method is described below: The hollow fiber membrane is cut longitudinally with a scalpel so that the inner surface of the hollow fiber membrane, which in this case represents the surface of the blood contact layer, is exposed. The sample is fixed on a sample plate and placed in the sample chamber. The following measurement conditions are set: -Equipment: Thermo VG Scientific, Type K-Alpha -Excitation radiation: monochromatic X-ray radiation, Al Kα, 75W -Sample spot diameter: 200 μm - Passing energy: 30 eV - Angle between source and analyzer: 54° -Spectral resolution for Ag3d signals: 0.48 eV -Vacuum: 10 -8 mbar -The charge was compensated with the assistance of a flood gun. XPS measurements were performed at Nanoanalytics in Münster, Germany. The PVP content in the near-surface layer was determined using the values ​​determined in atomic % for nitrogen (N) and sulfur (S) according to Equation 4. Known molecular weights of the repeating units in PVP and polysulfone were used. TIFF0007770343000007.tif8157 formula 4 Equation 4 is valid for the use of bisphenol A-based polysulfones. For other polysulfones, the molecular weight of the sulfur-containing repeat unit must be used. In the case of copolymers, the proportion of sulfur-containing repeat units in the copolymer must be taken into consideration. The PVP content in the near-surface layer is carried out using three hollow fiber membrane samples and the average of these measurements is calculated.

[0077] 10. Method for determination of albumin, IgM, LDL-sieving coefficients A hollow fiber membrane filter as described in Method 1 is used to determine the LDL sieving coefficient. Human whole blood is used for the measurement according to the standard DIN EN ISO 8637-3:2018. For the measurement of the LDL sieving coefficient, an apparatus as described in Figure 2 is used. Before starting the measurement, the system is filled with 2 l of saline under full ventilation and rinsed. After the rinsing step, the hollow fiber membrane filter 2-2 is emptied on the filtrate side, which requires closing the blood outlet 2-3. The filtrate is collected at the lower filtrate outlet 2-4 in measurement mode. Human whole blood with the following composition is used for the measurement: Hematocrit (HKT) in %: 40±2 Total protein (TP) in %: 6±0.5 Triglycerides (mg / dl): 200-300 The following measurement conditions are set: TIFF0007770343000008.tif36140

[0078] After the rinsing step, the blood side of the hollow fiber membrane filter 2-2 is filled with human whole blood. To avoid dilution effects, the first 200 ml is discarded. The whole blood is then circulated within the device 2-1. After 10 minutes, the filtrate pump 2-5 is started to transfer plasma to the filtrate side. After a further circulation time of 30 minutes under filtrate accumulation, pressure values ​​are recorded, and samples are taken at the sampling sites 2-10 (blood inlet) and 2-20 (filtrate), and the respective concentrations of LDL, IgM, and albumin are determined. For this purpose, the automated analyzer "Cobas Integra 400 plus" from "Roche Diagnostic" is used with the corresponding specific methods. The sieving coefficient S is calculated by Equation 5: TIFF0007770343000009.tif10170 formula 5 C F = concentration of analyte in the filtrate C in = concentration of analyte in blood at filter inlet The transmembrane pressure (TMP) is determined according to Equation 6: TIFF0007770343000010.tif9150 formula 6

[0079] example Example: Method of Producing Hollow Fiber Membranes According to the Invention Spin mass A, spin mass B, and an internal precipitant medium are provided for producing hollow fiber membranes according to the present invention. Spin mass A is prepared by mixing 20 wt. % polysulfone (Solvay Udel 3500, LCD), 6 wt. % polyvinylpyrrolidone (ISP, PVP K90), 1 wt. % water, 0.01 wt. % vitamin E, and 72.99 wt. % dimethylacetamide (DMAc). Spin mass B is prepared by mixing 10 wt. % polysulfone, 5.5 wt. % polyvinylpyrrolidone, 0.01 wt. % vitamin E, and 84.49 wt. % DMAc. The spin masses are tempered to 72°C while carefully degassing them until they become constant. The consistency is reached when no more bubbles appear over a period of 1 hour. For the spinning process, the spin mass is tempered to 70°C. The internal precipitant consists of 80 wt. % DMAc and 20 wt. % water. For the spinning process, the precipitant is tempered to 60°C. A spinning nozzle as described in DE 10211051 was used. For the spinning process, the internal precipitant, spinning mass A, and spinning mass B were co-extruded through the spinning nozzle to form a spun yarn. The precipitant was extruded through the central bore of the spinning nozzle. Spinning mass B was extruded through a first concentric annular slit surrounding the central bore of the spinning nozzle. Spinning mass A was extruded through a second concentric annular slit surrounding the first concentric annular slit and the central bore of the spinning nozzle. The slit width of the annular slit and the diameter of the central bore were selected to obtain a hollow fiber membrane having the geometric dimensions described herein. The spinning block and therefore the spinning nozzle were tempered to 60°C for the spinning process. The extruded yarn passed through a 20mm spinning gap at a spinning speed of 400mm / s. The temperature of the precipitation bath (water) was 65°C. The hollow fiber membranes obtained by precipitation in the precipitation bath were rinsed in six water baths and dried at 130°C for 10 minutes. The hollow fiber membranes had an inner diameter of 330 μm, a wall thickness of 65 μm, and the thickness of the selective inner layer obtained from spun mass B, which was the blood contact layer, was 4 μm. The hollow fiber membranes were wound up and bundled to be processed into hollow fiber membrane bundles containing 1296 or 2592 hollow fiber membranes.

[0080] Comparative Example: Hollow Fiber Membrane Production In comparison with the production of the Examples, spin agglomerates A and B were provided without vitamin E. Consequently, the proportion of DMAc in spin agglomerate A was 73 wt % and the proportion of DMAc in spin agglomerate B was 85 wt %. The respective proportions of PSU, PVP, and water in spin agglomerates A and B were maintained. All other parameters of the hollow fiber membrane production of the Examples were also maintained. The hollow fiber membranes from Example 1 and Comparative Example 1 were fabricated into hollow fiber membrane filters using the configuration described in Method 1 and were also sterilized by steam sterilization as in the Examples.

[0081] result The hollow fiber membranes of the examples and comparative examples were tested according to the methods described above, and the results are shown in Table 1: Table 1 TIFF0007770343000011.tif62145

[0082] The total PVP content in the hollow fiber membranes of the Examples is significantly increased compared to the Comparative Example. Furthermore, the values ​​for triglyceride concentration, platelet concentration in the hemolysis test, and reduction of free hemoglobin in the Examples are significantly improved compared to the Comparative Example. Based on the results, it is clear that the hollow fiber membranes made according to the Examples have a lower hemolysis effect and a lower tendency to adsorb platelets and triglycerides than the hollow fiber membranes made according to the Comparative Example.

[0083] These results are also confirmed by scanning electron microscope images taken after hemolysis tests on the hollow fiber membranes of the example and comparative example, respectively. Figure 3 shows a cross-section of a hollow fiber membrane of the comparative example that underwent a hemolysis test. The figure shows the support layer 3-1 and the blood contact layer 3-2. Adherent blood cells from the hemolysis test can be seen in the blood contact layer. The recognized blood cells are red blood cells. Figure 3 also shows that some of the blood cells have penetrated the blood contact layer.

[0084] Figure 4 shows a cross section of a hollow fiber membrane manufactured according to the example and subjected to a hemolysis test. Figure 4 shows the support layer 4-1 and the blood contact layer 4-2. Furthermore, as in Figure 4, blood cells adhering to the surface of the blood contact layer are visible from the hemolysis test. However, in contrast to Figure 3, blood cells that have penetrated the blood contact layer 4-2 are not visible in Figure 4. Apparently, the process of blood cell penetration into the blood contact layer does not occur to the same extent in the hollow fiber membrane according to the present invention as in the comparative hollow fiber membrane. It is hypothesized that this process of blood cell penetration into the blood contact layer is crucial for the destruction of blood cells, and that the hemolysis of large-pore hollow fiber membranes, such as those used in plasma exchange, is based to a significant extent on this process. [Explanation of symbols]

[0085] 4-1 Support Layer 4-2 Blood Contact Layer

Claims

1. 1. A hollow fiber membrane for separating plasma from blood, comprising a blood contact layer and a support layer, each comprising a hydrophobic polymer, a hydrophilic polymer, and vitamin E, particularly α-tocopherol or tocotrienol, wherein the vitamin E, particularly the α-tocopherol or the tocotrienol, is present in an amount of 0.005 to 0.25% by weight, based on the total weight of the hollow fiber membrane; characterised by a sieving coefficient for albumin, determined in accordance with DIN EN ISO 8637-3:2018, of 50 to 100%; or characterised by a sieving coefficient for immunoglobulin M determined in accordance with DIN EN ISO 8637-3:2018 of 50 to 100%; or characterized in that it has a sieving coefficient for low-density lipoproteins, determined in accordance with DIN EN ISO 8637-3:2018, of 80 to 100%, preferably 90 to 100%; and The hollow fiber membrane, wherein the blood contact layer in the near-surface layer has a polyvinylpyrrolidone content of 35 to 50 wt. % as determined by XPS measurement.

2. 10. The hollow fiber membrane of claim 1, wherein the hollow fiber membrane is comprised of at least two coextruded layers, one of the at least two coextruded layers forming the blood contact layer and another of the at least two coextruded layers forming the support layer.

3. the hydrophobic polymer comprises or consists of polysulfone; and / or 3. The hollow fiber membrane of claim 1, wherein the hydrophilic polymer comprises or consists of polyvinylpyrrolidone.

4. 4. The hollow fiber membrane according to claim 1, wherein the polyvinylpyrrolidone content is 4-9% by weight, preferably 5-8%, more preferably 5-7%, based on the total weight of the hollow fiber membrane.

5. A hollow fiber membrane according to any one of claims 1 to 4, characterized in that it has a diameter of 250 to 400 µm.

6. 6. The hollow fiber membrane according to claim 1, characterized in that it has a wall thickness of 40 to 80 μm.

7. 7. The hollow fiber membrane according to claim 1, wherein the blood contact layer forms the inner layer of the hollow fiber membrane.

8. 8. The hollow fiber membrane according to claim 1, wherein the blood contact layer has a thickness of 1 to 15 μm.

9. A method for producing a hollow fiber membrane according to any one of claims 2 to 8, comprising the steps of: providing a spinning mass A comprising 15-25 wt. % of a hydrophobic polymer, 4-8 wt. % of a hydrophilic polymer, 0.2-2 wt. % of a polar protic substance, and 0.001-0.05 wt. % of vitamin E, in particular α-tocopherol or tocotrienol, and 80.799-64.95 wt. % of a polar aprotic solvent; providing a spinning mass B comprising 8-12 wt. % of a hydrophobic polymer, 3-7.5 wt. % of a hydrophilic polymer, 0.001-0.05 wt. % of vitamin E, in particular α-tocopherol or tocotrienol, and 88.999-81.95 wt. % of a polar aprotic solvent; providing an internal precipitant comprising 70-90 wt. % of a polar aprotic solvent and 10-30 wt. % of a polar protic mixed liquid; a step of co-extruding a spun mass A, a spun mass B, and the internal precipitant through a spinning nozzle to form a spun yarn, wherein the internal precipitant is extruded through a central bore of the spinning nozzle, the spun mass B is extruded through a first concentric annular slit surrounding the central bore, and the spun mass A is extruded through a second concentric annular slit surrounding the first concentric annular slit and the central bore of the spinning nozzle; Passing the spun yarn through a spinning gap; introducing the yarn into a precipitation bath; precipitating the spun yarn to form a hollow fiber membrane; The method, characterized in that it comprises:

10. 10. The method according to claim 9, wherein the spun masses A and B are tempered to 60-80°C and / or the internal precipitant is tempered to 50-60°C.

11. 11. The method according to claim 10, characterized in that the spinning gap is between 5 and 80 mm and / or the spinning speed is between 300 and 500 mm / s.

12. said hydrophobic polymer of spun mass A comprises or consists of polysulfone; and / or the hydrophilic polymer of spun mass A comprises or consists of polyvinylpyrrolidone, and / or said polar protic substance of the spun mass A comprises or consists of water, and / or the polar aprotic solvent of the spun mass A comprises or consists of dimethyl sulfoxide, dimethyl formamide, dimethyl acetamide, N-methylpyrrolidone, or mixtures thereof; and / or said hydrophobic polymer of spun mass B comprises or consists of polysulfone; and / or said hydrophilic polymer of spun mass B comprises or consists of polyvinylpyrrolidone, and / or the polar aprotic solvent of the spinning mass B comprises or consists of dimethyl sulfoxide, dimethyl formamide, dimethyl acetamide, N-methylpyrrolidone, or mixtures thereof; and / or The polar protic mixed liquid of the internal precipitation water comprises or consists of water; 12. The method according to claim 10 or 11.

13. The method according to any one of claims 10 to 12, characterized in that the internal precipitant does not contain a hydrophilic polymer.

14. 1. A sterile hollow fiber membrane filter comprising: A filter of a plurality of hollow fiber membranes according to any one of claims 1 to 8 or produced according to any one of claims 9 to 13. Equipped with The hollow fiber membrane filter is pre-sterilized by steam sterilization. The sterile hollow fiber membrane filter is characterized in that:

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