Filtration membranes from blends containing polysulfone and polyoxazoline and methods for making same - Patents.com

Abstract

Asymmetric membrane. The asymmetric membrane comprises a membrane wall having first and second porous surfaces and an interior located between the surfaces, a first asymmetric region facing the first surface and a second asymmetric region facing the second surface, the asymmetric membrane being made from a polymer blend comprising an aromatic sulfone polymer and a poly(2-oxazoline), the asymmetric membrane being in the form of a flat sheet.

Description

[Background technology]

[0001] Microporous polymer membranes are used in a wide range of industrial, pharmaceutical or medical applications for high precision filtration. In these applications, membrane separation processes are becoming increasingly important, since they have the advantage that the substances to be separated are not thermally stressed or even affected. Microfiltration membranes allow the removal of fine particles or microorganisms, for example, with a small size down to the submicron range, and are therefore suitable for producing purified water for use in laboratories or in the semiconductor industry. Furthermore, many applications of membrane separation processes are known in the beverage industry, in the biotechnology field or in wastewater technology. Summary of the Invention

[0002] Thus, in one aspect, the present disclosure provides an asymmetric membrane comprising a membrane wall having first and second porous surfaces and an interior located between the surfaces, a first asymmetric region facing the first surface and a second asymmetric region facing the second surface, wherein the asymmetric membrane is made from a polymer blend comprising an aromatic sulfone polymer and a poly(2-oxazoline), and wherein the asymmetric membrane is in the form of a flat sheet.

[0003] In another aspect, the present disclosure provides a method for producing a method for manufacturing a pharmaceutical composition comprising: The method includes preparing a casting solution including an aromatic sulfone polymer and a poly(2-oxazoline), adjusting the casting solution to a casting temperature, pouring the casting solution onto a carrier to form a film, transporting the film disposed on the carrier through an environmentally controlled zone, introducing the film disposed on the carrier into a coagulation medium to initiate coagulation of the film to form a membrane structure, and stabilizing the membrane structure in the coagulation medium. [Brief description of the drawings]

[0004] [Figure 1]1 is an SEM image showing a cross section of the membrane of Example 1. [Diagram 2] 1 is an SEM image showing a cross section of the membrane of Example 2. [Diagram 3] 1 is an SEM image showing a cross section of the membrane of Example 3. [Figure 4] 1 is an SEM image showing a cross section of the membrane of Example 4. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0005] Before any embodiment of the present disclosure is described in detail, it is understood that the invention is not limited in its application to the details of use, configuration, and arrangement of components set forth in the following description. The invention is capable of other embodiments and can be practiced or carried out in various ways that will be apparent to those skilled in the art upon reading this disclosure. It is also understood that the terminology and terminology used herein is for descriptive purposes and should not be considered limiting. The use of "including," "comprising," or "having," and variations thereof herein, is meant to encompass the items listed thereafter and their equivalents, as well as additional items. It is understood that other embodiments may be utilized and structural or logical changes may be made without departing from the scope of the present disclosure.

[0006] The present disclosure provides an integral asymmetric membrane, particularly for filtration, in the form of a flat sheet, made from a polymer blend comprising an aromatic sulfone polymer and poly(2-oxazoline), the membrane wall having a first and second porous surface and an interior located between the surfaces, the membrane wall having a porous structure with a pore size distribution, the first asymmetric region facing the first surface and the second asymmetric region facing the second surface.In some embodiments, the asymmetric membrane can be in the form of a flat sheet.

[0007] Asymmetric membranes generally have a separation layer with a minimum pore size that determines the separation properties of the membrane, and a support layer with larger pores that are responsible for the mechanical stability of the membrane. An integral asymmetric membrane is understood to be a membrane with at least one separation layer or region and one support layer or region, where the separation layer and the support layer are made of the same material and are formed simultaneously during the manufacture of the membrane. As a result, both layers are bonded together as an integral unit. In the transition from the separation layer to the support layer, there is only a change in the membrane structure, for example, in terms of pore size. Integral asymmetric membranes and their manufacturing methods are described, for example, in EP 0361085 (B1).

[0008] The membrane may have an essentially isotropic region between the first asymmetric region and the second asymmetric region. Within the context of the present disclosure, an essentially isotropic region is understood to be a region of the membrane wall having an essentially constant pore size, whereby the evaluation is performed by scanning or transmission electron microscopy images. An isotropic region can also be considered as a region in which the flow channels extending through the membrane wall have an essentially constant average diameter. As is true for all membranes, the actual pore size also varies somewhat in the membrane according to the invention, i.e., it has a certain pore size distribution, even if the pore size distribution appears visually isotropic. Thus, in some embodiments, in the essentially isotropic region, the pore size changes by up to approximately 15-20%. Due to the preferred presence of an isotropic region where the pore size does not increase further, an improved mechanical stability is achieved while at the same time preserving a high fouling loading capacity.

[0009] In some embodiments, the pore size of the first asymmetric region may be larger than the pore size of the second asymmetric region. In some embodiments, the average pore size of the first asymmetric region may be larger than the average pore size of the second asymmetric region. The average diameter of the pores in the first asymmetric region may be 2 to 50 μm. The average diameter of the pores in the second asymmetric region may be 2 to 40 μm. In some embodiments, the pore size of the first asymmetric region may be 0.1 to 30 μm, or 0.1 to 15 μm. In some embodiments, the pore size of the second asymmetric region may be 0.1 to 10 μm, or 0.1 to 5 μm. In some embodiments, the pore size of the isotropic region is larger than the pore size of the first asymmetric region and the pore size of the second asymmetric region. In some embodiments, the average pore size of the isotropic region is larger than the average pore size of the first asymmetric region and the average pore size of the second asymmetric region. In some embodiments, the average pore size of the isotropic region is smaller than the average pore size of the first asymmetric region and the average pore size of the second asymmetric region.

[0010] The average pore diameter or pore size of the pores can be determined, for example, by the method described in US Patent Application Publication No. 2017 / 0304780 (Asahi et al.). The average pore diameter or pore size of the pores can be determined by photographing the cross section of the membrane with a scanning electron microscope (SEM). For example, the magnification is set to 50,000 times, and the field of view is set to a cross section perpendicular to the length direction of the membrane, or a cross section parallel to the length direction and passing through the center of the membrane horizontally with respect to the cross section. After photographing the initially set field of view, the photographed field of view is moved horizontally in the film thickness direction, and the next field of view is photographed.

[0011] This photographing operation is repeated until a cross-sectional photograph of the membrane from the outer surface to the inner surface is taken without any gaps, and the obtained photographs are combined to obtain a single membrane cross-sectional photograph. In this cross-sectional photograph, the average pore diameter of the pores in each region (2 μm in the circumferential direction of the membrane) × (1 μm from the outer surface to the inner surface) from the outer surface to the inner surface is calculated, and the gradient structure of the membrane cross section is quantified every 1 μm from the outer surface to the inner surface. By such quantification, it can be determined whether the membrane has a gradient type porous structure.

[0012] The average pore diameter or pore size can be calculated by a method using image analysis. Specifically, a binarization process is performed on the pore and solid parts using Image-pro plus manufactured by Media Cybernetics, Inc. The distinction between the pore and solid parts is based on their brightness, and the parts that cannot be distinguished and noise are corrected with a freehand tool. The edge parts that form the outline of the pore parts and the porous structure observed behind the pore parts are identified as pore parts. After the binarization process, the pores are assumed to be perfect circles, and the diameter of the pores is calculated from the area value of the pores. This calculation is performed for each of all the pores, and the average pore diameter is calculated for each area of ​​1 μm × 2 μm. The pore parts located at the end of the field of view and partially within the field of view are also counted (i.e., the diameter is calculated assuming that the area of ​​the pore parts partially within the field of view is the area of ​​one perfect circle).

[0013] The aromatic sulfone polymer and the poly(2-oxazoline) may be distributed throughout the membrane. The aromatic sulfone polymer and the poly(2-oxazoline) may be evenly distributed throughout the membrane. The aromatic sulfone polymer and the poly(2-oxazoline) may be evenly distributed throughout the membrane.

[0014] The membrane may have an aromatic sulfone polymer and a poly(2-oxazoline) distributed throughout at least one of a first asymmetric region, a second asymmetric region, and an isotropic region.

[0015] The aromatic sulfone polymers of the present disclosure can be used, such as polysulfone, polyethersulfone, polyphenylenesulfone, polyarylethersulfone, or copolymers or modifications of these polymers, or mixtures of these polymers. In a preferred embodiment, the aromatic sulfone polymer can be a polysulfone or polyethersulfone having repeating molecular units as shown in formulas (I) and (II) as follows: [ka]

[0016] More preferably, polyethersulfones according to formula (II) are used, as can aromatic sulfone polymers, for example, since they have a lower hydrophobicity than polysulfones. The polyethersulfones may have a molecular weight (MW) of from about 72 kg / mol.

[0017] In some embodiments, the poly(2-oxazoline) of the present disclosure can be poly(2-ethyl-2-oxazoline) (PEtOx). Poly(2-ethyl-2-oxazoline) has high protein repellency. The residues of poly(2-oxazoline) can generally be altered to change the properties of the polymer, for example, from hydrophilic to hydrophobic. Poly(2-oxazoline) can have a molecular weight of about 25 kg / mol to about 500 kg / mol. Poly(2-oxazoline) can have a molecular weight from about 50 kg / mol.

[0018] Poly(2-ethyl-2-oxazoline) may have a molecular weight of about 25 kg / mol to about 500 kg / mol. Poly(2-ethyl-2-oxazoline) may have a molecular weight of about 25 kg / mol to about 100 kg / mol. Poly(2-ethyl-2-oxazoline) may have a molecular weight of about 50 kg / mol.

[0019] In some embodiments, the poly(2-oxazolines) of the present disclosure can be prepared by cationic ring-opening polymerization of various 2-oxazoline monomers. Polymerization of 2-alkyl substituted 2-oxazoline monomers provides poly(2-alkyl-2-oxazolines).

[0020] The poly(2-oxazoline) can be present in a concentration of 0.05-30 wt% (weight percent), 0.5-30 wt%, 1-30 wt%, 5-30 wt%, or 10-30 wt% based on the weight of the membrane. The poly(2-oxazoline) can be present in a concentration of greater than 0.05 wt%, greater than 0.5 wt%, greater than 1 wt%, greater than 2 wt%, greater than 3 wt%, greater than 4 wt%, greater than 5 wt%, greater than 6 wt%, greater than 7 wt%, greater than 8 wt%, greater than 9 wt%, greater than 10 wt%, greater than 15 wt%, or greater than 20 wt% based on the weight of the membrane. The poly(2-oxazoline) can be present in a concentration of less than 30 wt%, less than 28 wt%, less than 25 wt%, less than 23 wt%, less than 20 wt%, less than 15 wt%, or less than 10 wt% based on the weight of the membrane.

[0021] The poly(2-oxazoline) may be distributed throughout the membrane. The poly(2-oxazoline) may be evenly distributed throughout the membrane. The poly(2-oxazoline) may be evenly distributed throughout the membrane.

[0022] The membrane may have poly(2-oxazoline) distributed throughout at least one of the first asymmetric region, the second asymmetric region, and the isotropic region.

[0023] In some embodiments, the polymer blend may further include a hydrophilic polymer. Exemplary hydrophilic polymers may include polyvinylpyrrolidone, polyethylene glycol, polyvinyl alcohol, polyglycol monoester, polysorbitate, carboxymethylcellulose, polyacrylic acid, polyacrylate, or modifications or copolymers of these polymers. In some embodiments, the hydrophilic polymer may be polyethylene glycol. In some embodiments, the polymer blend does not include polyvinylpyrrolidone. In some embodiments, the polymer blend may be a hydrophobic polymer blend. In some embodiments, the hydrophilic polymer may be present at a concentration of 1-75% by weight based on the weight of the membrane.

[0024] In some embodiments, the polymer blend may include a solvent. Exemplary solvents may include glycol, butyrolactone, caprolactam, or combinations thereof. In some embodiments, the polymer blend may include more than 7 wt%, more than 10 wt%, more than 20 wt%, more than 30 wt%, more than 40 wt%, more than 50 wt%, more than 60 wt%, more than 70 wt%, more than 80 wt%, or more than 90 wt% polyvinylpyrrolidone. In some embodiments, the polymer blend may include less than 3 wt%, less than 2 wt%, or less than 1 wt% polyvinylpyrrolidone.

[0025] In some embodiments, a combination membrane is provided. The combination membrane can include at least two asymmetric membranes of the present disclosure. The at least two asymmetric membranes are stacked adjacent to each other.

[0026] The present disclosure also provides a method for producing a membrane, comprising the steps of: preparing a homogeneous casting solution comprising an aromatic sulfone polymer and a poly(2-oxazoline); adjusting the homogeneous casting solution to a casting temperature; and pouring the homogeneous casting solution onto a carrier to form a film, wherein the carrier is temperature-controllable and has a temperature different or the same as the casting temperature of the casting solution, and the carrier is moved at a velocity v 1 conveying the film disposed on the carrier through an environmentally controlled zone; introducing the film disposed on the carrier into a coagulation medium to initiate coagulation of the film to form a membrane structure; and applying a pressure to the film at a rate v 2 The method includes the steps of recovering the membrane structure from the carrier in the solidification medium by a recovery device moving at high speed, thereby tensioning the membrane structure, stabilizing the membrane structure in the solidification medium, extracting the resulting membrane, and subsequently drying the membrane.

[0027] The method is to calculate the carrier velocity v 1 A velocity greater than v 2The method may further include stretching the membrane structure by adjusting the pore size. In some embodiments, the membrane structure is stretched up to 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, or 50%. Stretching the membrane structure may result in internal stresses in the membrane cross section. In some embodiments, the stresses on the two different surfaces of the membrane are not equal. The resulting stresses are higher on the side facing the carrier, and therefore it is exactly this side that becomes the first asymmetric region facing this first surface, which has a larger pore size. Therefore, this first side is usually used as the upstream side of the membrane in the filtration process. The pores in the second asymmetric region facing the second surface (downstream side) are smaller than the pores in the first asymmetric region facing the first surface (upstream side). In some embodiments, the pore size of the first asymmetric region is more than 2 times, 3 times, 4 times, 5 times, 6 times, 7 times, 8 times, 9 times, or 10 times larger than the pore size of the second asymmetric region. The open upstream side (larger pore size in the first asymmetric region facing the first surface) can provide better throughput performance.

[0028] When the membrane is stretched in one direction, pores are generated in the first and second asymmetric regions that are oriented in the stretching direction. When the membrane is stretched in one direction, pores are generated in the first and second asymmetric regions that are elongated in the stretching direction, for example, ovoid pores are generated. In some embodiments, the elongated pores have an elliptical cross section. For elongated pores, the longest dimension of the pore opening is oriented in the stretching direction. In some embodiments, the elongated pores are on the first and second surfaces of the membrane. In some embodiments, the pores in the first and second asymmetric regions can be elongated in the same or different directions.

[0029] In some embodiments, the first asymmetric region extends from the outer edge of the inner isotropic region to the first (upstream) surface of the membrane. In some embodiments, the second asymmetric region extends from the outer edge of the inner isotropic region to the second (downstream) surface of the membrane.

[0030] In some embodiments, the average pore size of the pores in the first asymmetric region decreases in a direction from the first surface of the membrane to the interior of the membrane. In some embodiments, the average pore size of the pores in the second asymmetric region decreases in a direction from the second surface of the membrane to the interior of the membrane. In some embodiments, the average pore size of the pores in the first asymmetric region increases in a direction from the first surface of the membrane to the interior of the membrane. In some embodiments, the average pore size of the pores in the second asymmetric region increases in a direction from the second surface of the membrane to the interior of the membrane.

[0031] The casting solution may include a hydrophilic polymer. Exemplary hydrophilic polymers may include polyvinylpyrrolidone, polyethylene glycol, polyvinyl alcohol, polyglycol monoesters, polysorbitates, carboxymethylcellulose, polyacrylic acid, polyacrylates, or modifications or copolymers of these polymers. In some embodiments, the hydrophilic polymer may be polyethylene glycol. In some embodiments, the casting solution does not include polyvinylpyrrolidone.

[0032] The casting solution may contain a solvent. The solvent system used to prepare the casting solution should be compatible with the membrane-forming sulfone polymer. Preferably, the solvent system contains a polar aprotic solvent such as dimethylformamide, dimethylacetamide, dimethylsulfoxide, N-methylpyrrolidone, γ-butyrolactone or a mixture thereof, or a protic solvent such as ε-caprolactam. In addition, the solvent system may contain up to 80% by weight of a latent solvent, where in the context of the present invention a latent solvent is understood as a solvent that dissolves the sulfone polymer poorly or only at elevated temperature. When ε-caprolactam is used as the solvent, for example, γ-butyrolactone, propylene carbonate, polyalkylene glycols may be used. In addition, the solvent system may contain a non-solvent for the membrane-forming polymer, such as, for example, water, glycerin, low molecular weight polyethylene glycols having a weight average molecular weight of less than 1,600 Daltons, or low molecular weight alcohols such as ethanol or isopropanol.

[0033] For the implementation of the method according to the invention and for the formation of the characteristic structure of the membrane according to the invention, it is advantageous to set the viscosity of the casting solution to a value below 30 Pa s, more advantageously below 20 Pa s, for which the viscosity is determined at 60° C. The setting of the viscosity can be effected in particular by the choice and the concentration of the hydrophilic second polymer used in the method according to the invention.

[0034] The casting solution can be poured to form the film by conventional forming tools, such as, for example, a sheet extrusion die, a casting mold, or a doctor blade, according to methods known per se. The casting solution is set to the forming temperature in the forming tool at the latest. The casting solution is poured onto a carrier that can be temperature-controlled, and here too, conventional carriers can be used that can later collect the solidified film. For example, coated paper or steel tape can be used. Preferably, the temperature-controllable carrier is a heated roll, i.e. a casting roller, that can be temperature-controlled, onto which the film is poured.

[0035] The temperature of the carrier may be different from the casting temperature of the casting solution. In some embodiments, the temperature of the carrier is higher than the casting temperature of the casting solution. This creates a viscosity gradient in the casting solution across the thickness of the poured film. Due to the increase in the carrier temperature, the poured film has a lower viscosity in the region of the carrier, which causes a coarser pore structure to form during subsequent contact with the solidification medium. In some embodiments, the carrier temperature is preferably at least 15°C, more preferably at least 20°C, higher than the casting temperature.

[0036] To create an asymmetric structure, the film disposed on the carrier can be transported through an environmentally controlled zone where a defined temperature and a defined relative humidity are set. Preferably, the temperature of the environmentally controlled zone is in the range of 25-60° C. and the relative humidity is preferably set at a value in the range of 20-95%. The retention time of the film in the environmentally controlled zone and the overflow rate of air over the poured film in the environmentally controlled zone should be determined so that pre-coagulation is induced by the increase in air humidity acting as a non-solvent.

[0037] After passing through the environmentally controlled zone, the film arranged on the carrier is introduced into a coagulation medium, in which coagulation is initiated for the formation of a membrane structure. Preferably, the coagulation medium is adjusted to a temperature higher than room temperature, more preferably has a temperature higher than 30° C. In a preferred embodiment of the method according to the invention, the coagulation medium is water or a water bath.

[0038] In the solidification medium, the film is first precipitated to form a membrane structure to the extent that the membrane structure already has sufficient stability and can be withdrawn from the carrier, i.e. preferably from the casting roller. The withdrawal from the casting roller is carried out by a withdrawal device, for example by a drawing-off roller, where, according to the invention, the withdrawal speed v 2 is the carrier velocity v 1 The speed of the collection device is preferably greater than v 2 Carrier speed v 1 to is in the range of 1.01:1 to 1.5:1, thereby achieving a high surface porosity on the side of the resulting membrane facing the carrier.

[0039] Following the recovery device, the coagulation is completed and the membrane is stabilized in subsequent coagulation baths. These coagulation baths can have a higher temperature compared to the first aforementioned coagulation bath. The temperature can also be increased stepwise from bath to bath. Thereby, in the coagulation bath, extraction of the solvent system and of a part of the usually hydrophilic second polymer from the membrane structure occurs simultaneously, so that the coagulation bath simultaneously functions as a washing or extraction bath. As the coagulation or washing medium in these coagulation or washing baths, water is preferably used.

[0040] In some embodiments, the casting solution can have 10-70 wt% aromatic sulfone polymer by weight of the solution and 5-30 wt% poly(2-oxazoline) by weight of the solution. The casting solution may further include 5-80 wt% solvent for the polymer component by weight of the solution, 0-80 wt% latent solvent for the polymer component by weight of the solution, and 0-70 wt% non-solvent for the polymer component by weight of the solution. In some embodiments, the casting solution may include 15-50 wt% gamma-butyrolactone by weight of the solution and 10-50 wt% polyethylene glycol or caprolactam by weight of the solution.

[0041] In some embodiments, the casting solution can have 5-30 wt % of the aromatic sulfone polymer and the poly(2-oxazoline) by weight of the solution, 5-30 wt % of the hydrophilic polymer by weight of the solution, and 20-60 wt % of the solvent by weight of the solution.

[0042] In particular, due to their porous upstream side, the membranes are distinguished by a high throughput and therefore by a high transmembrane flux of water. The membranes according to the invention preferably have a flux of at least 2000 L / m 2 In some embodiments, the filtration medium preferably has a throughput of at least 3000 L / m of beer or water. 2 , 3500L / m 2 , 4000L / m 2 , 4500L / m 2 , 5000L / m 2 , 5500L / m 2 , 6000L / m 2 , or 6500 L / m 2 The throughput is .times. ...

[0043] The present invention provides polymeric membranes with excellent protein repulsion properties. These membranes therefore block slower and exhibit higher throughput behavior and therefore longer life span. These membranes further exhibit a nearly asymmetric structure that is promising for the preparation of highly selective membranes.

[0044] The described methods provide membranes in which the aromatic sulfone polymer and poly(2-oxazoline) are distributed throughout the membrane. The described methods further provide membranes in which the aromatic sulfone polymer and poly(2-oxazoline) are evenly distributed throughout the membrane. The described methods further provide membranes in which the aromatic sulfone polymer and poly(2-oxazoline) are evenly distributed throughout the membrane.

[0045] The described methods provide membranes having poly(2-oxazoline) distributed throughout the membrane. The described methods further provide membranes having poly(2-oxazoline) evenly distributed throughout the membrane. The described methods further provide membranes having poly(2-oxazoline) evenly distributed throughout the membrane.

[0046] Making the upstream side porous in combination with the protein-repelling properties of the membrane can provide better filtration properties, resulting in less fouling and higher throughput.

[0047] The membrane according to the invention in the form of a flat sheet, i.e. the flat membrane according to the invention, is particularly suitable for microfiltration. In the membrane, the separation layer or separation region is the layer or region of the membrane that has a minimum pore size. The separation layer serves to retain certain particles, molecules or microorganisms in or on the membrane, depending on the pore size of the separation layer.

[0048] In some embodiments, the separation layer can be an isotropic region of the membrane. In some embodiments, the separation layer can be a first asymmetric region and / or a second asymmetric region. In some embodiments, the membrane has a first separation layer including a first asymmetric region and a second separation layer including a second asymmetric region. In some embodiments, the membrane has a first separation layer including a first asymmetric region, a second separation layer including a second asymmetric region, and an isotropic region sandwiched between the first and second asymmetric regions. In some embodiments, the separation layer can be a region other than the first asymmetric region, the second asymmetric region, and the isotropic region. This type of membrane has, as a rule, a diameter of the separation pores of 0.01 to 10 μm, preferably 0.1 to 5 μm, more preferably 0.2 to 2 μm. Preferably, the flat membrane according to the present invention has a thickness of 10 to 300 μm, more preferably 30 to 220 μm. In some embodiments, the support layer can be at least one of the isotropic region, the first asymmetric region, and the second asymmetric region. For example, if the separating layer is the isotropic region of the membrane, the supporting layer can be the first asymmetric region and / or the second asymmetric region.

[0049] In some embodiments, a method of using an asymmetric membrane or a combination membrane is provided. The asymmetric membrane or combination membrane can be used to filter a liquid composition. The liquid composition can be an aqueous composition, such as water or beer. In some embodiments, the asymmetric membrane or combination membrane can be used to remove one or more microorganisms from the liquid composition. The microorganism can be bacteria or yeast, such as Lactobacillus brevis or Saccharomyces cerevisiae. In some embodiments, when filtering a liquid composition through a membrane or combination membrane, a log10 reduction in colony forming unit (cfu) count of more than 1, 2, 3, 4, or 5 can be achieved. In some embodiments, when filtering a liquid composition through a membrane or combination membrane, a log10 reduction in cfu count of 1 to 7 is achieved.

[0050] The following examples are intended to illustrate, but not limit, the present disclosure. EXAMPLES

[0051] Objects and advantages of this invention are further illustrated by the following examples, but the particular materials and amounts thereof recited in these examples, as well as other conditions and details, should not be construed to unduly limit this invention. [Table 1]

[0052] Method A. How to determine transmembrane flow (TMF) Sample disks (90-130 mm diameter) were punched from the membrane sheets. A single disk was placed flat in a sample holder with the fluid inlet port located above the disk and the fluid outlet port located below the disk. The disk was oriented in the holder such that the surface of the disk with the smaller pores faced the fluid inlet and the surface of the disk with the larger pores faced the fluid outlet, and the holder was sealed. The exposed frontal surface area of ​​the membrane was 43.2 cm. 2 Deionized water (25°C) was pumped at a specified pressure of 0.1-0.2 bar, where the water entered the inlet, flowed through the membrane in the direction of gravity, and then exited through the outlet port into a receiving vessel. Water was collected for 1 min and measured either gravimetrically or volumetrically. The transmembrane flux (TMF) was calculated using Equation 1:

[0053] Formula 1.

number

[0054] Method B. Determining the Maximum Separation Pore (Bubble Point) The maximum separation pore diameter (d max ) is determined by the bubble point (BP) method (ASTM Nos. 128-61 and F316-86), and the method described in German Patent No. 3617724 (Reichelt) is suitable. As shown in Equation 2, d max is the vapor pressure associated with the bubble point, P B is obtained from

[0055] Formula 2. d max =s B / P B [In the formula, s B is a constant that depends mainly on the wetting fluid used during the measurement. In the examples of this disclosure, the wetting fluid was water. B is 2.07 μm bar at 25 °C.

[0056] Method C. How to determine membrane throughput (TP) of beer samples Prior to testing, the beer samples were degassed for 17 hours at 0.2 bar and 25°C. The experiments were carried out using a test rig equipped with a sample tank and a plunger pump operating at a constant flow rate of 80 mL / min. The back pressure during filtration was determined using a pressure sensor placed between the pump and the filter holder.

[0057] 13.7cm 2 A membrane disk of was cut from the membrane sheet. The membrane was pre-wetted with water for 5 minutes and then placed flat in a filter holder. The holder contained a fluid inlet port located above the disk and a fluid outlet port located below the disk. Beer was pumped into the sealed holder through the inlet port, flowed in the direction of gravity through the membrane and out the outlet port into a receiving vessel. The membrane was oriented in the holder such that the surface of the membrane with the larger pores and higher porosity (i.e., the upstream membrane surface) faced the inlet port. Before starting the measurements, the device was filled with the beer to be tested and the filled device was degassed using the vent valve. Filtration was stopped when a back pressure of 1.0 bar was reached. The filtration time was recorded.

[0058] The total volume of beer passing through the filter was calculated as the product of the flow rate (L / min) and the time (min) elapsed until the back pressure reached 1.0 bar. Throughput (L / m at 1.0 bar) 2 ) to the filter front surface area (m2) at (1.0 bar) 2 The beer content was determined as the total volume (L) of beer per 1000 ml of beer. Two types of beer samples were tested: a Pilsner and a Belgian-style white beer.

[0059] Method D. Method for determining the reduction of Lactobacillus brevis or Saccharomyces cerevisiae in a sample after membrane filtration.

[0060] Lactobacillus brevis and Saccharomyces cerevisiae were obtained from the DSMZ German Collection of Microorganisms and Cell Cultures, Braunschweig, Germany.

[0061] Streak plates of L. brevis were prepared on MRS agar from frozen stock samples and incubated at 30°C for 72 h in the absence of oxygen. L. brevis cultures were initiated by transferring a single colony from the streak plate to 10 mL of MRS medium in a sterile culture flask. The L. brevis culture flask was incubated at 30°C for 72 h. The resulting cell culture was diluted with acetate buffer (pH 4.0) to obtain a cell number of approximately 2 × 10 6 ~2×10 7 The minimum concentration of cfu / mL (cfu = colony forming units) was adjusted. This was the starting concentration of bacteria for filtration.

[0062] Streak plates of S. cerevisiae were prepared on Sabouraud agar from frozen stock samples and incubated at 30°C for 72 hours. S. cerevisiae cultures were initiated by transferring a single colony from the streak plate to 1 L of yeast medium in a sterile culture flask. The S. cerevisiae culture flask was incubated at 30°C for 24 hours with shaking. The cultures were serially diluted in sterile distilled water to obtain approximately 2 × 10 6 ~2×10 7 A sample was obtained with a resulting S. cerevisiae concentration in cfu / mL, which was the starting concentration of bacteria for filtration.

[0063] Sample disc (127cm 2 ) was cut from the membrane and placed flat in a filter holder. The sealed filter holder contained a fluid inlet port located above the disk and a fluid outlet port located below the disk. A culture sample (1 L) was pressure filtered (2.07 bar) such that the culture sample entered the holder through the inlet port, flowed in the direction of gravity through the membrane, and exited the outlet port into a receiving vessel. The membrane was oriented in the holder such that the surface of the membrane with the larger pores and higher porosity (i.e., the upstream membrane surface) faced the inlet port. The filtrate (1 L) was collected into a receiving vessel using a sterile technique.

[0064] For L. brevis, the filtrate samples were serially diluted with sterile distilled water and 0.2 mL of each diluted sample was streaked onto MRS agar plates. Alternatively, when high retention performance was expected, the complete filtrate was filtered undiluted through a 0.2 μm membrane sterile filter and the filter was transferred onto MRS agar plates. The inoculated plates were incubated at 30°C for 7 days and the colony forming units (cfu) in each plate were counted by visual inspection. The corresponding concentrations (cfu / mL) of L. brevis in the test samples and filtrate samples were calculated based on the dilution factor.

[0065] For S. cerevisiae, the complete filtrate was filtered undiluted through a 0.2 micron membrane sterilizing filter and the filter was transferred onto Sabouraud agar plates. The inoculated plates were incubated at 30° C. for 7 days and the colony forming units (cfu) in each plate were counted by visual inspection. The corresponding concentrations (cfu / mL) of S. cerevisiae in the test samples and filtrate samples were calculated based on the dilution factor.

[0066] Bacterial retention by the membrane was calculated as logarithmic reduction value (LRV) according to formula 3.

[0067] Formula 3. LRV= log 10 [Bacteria concentration in sample before filtration (cfu / mL) / Bacteria concentration in filtrate (cfu / mL)]

[0068] Method E. How to Determine Viscosity of a Casting Solution The viscosity of the casting solution was measured at 60 °C and 10 s using a HAAKE RheoStress 1 rheometer (Thermo Fisher Scientific, Waltham, MA) equipped with a Z20DIN sensor device (Thermo Fisher Scientific, Waltham, MA). -1 The shear rate was determined.

[0069] Example 1 A mixture of 50% by weight of γ-butyrolactone and 50% by weight of ε-caprolactam was adjusted to 40° C. in a thermostatically controlled tank, stirred, and 18.75 kg of poly(2-ethyl-2-oxazoline) was added. The tank was heated to 50° C. and the mixture was stirred for 2 hours. Then, 1.5 kg of glycerol and 1.2 kg of water were added. The mixture was stirred for 30 minutes at 50° C., and then 1.95 kg of sulfonated polyethersulfone (SPES, with a sulfonation degree of 5%) and 22.8 kg of polyethersulfone (PES) were added. The mixture was stirred for 10 minutes. Oxygen was largely removed from the tank by creating a vacuum and applying nitrogen. The tank was heated to 50° C. and a homogeneous solution was obtained after 24 hours of vigorous stirring. The solution was then degassed by vacuum. The resulting casting solution had a viscosity of 7.4 Pa s at 60° C. and a tan δ of 85.6.

[0070] The completed casting solution was poured onto a metal casting roller adjusted to 40°C using a casting mold adjusted to 50°C to form a film with a thickness of about 160 micrometers. The film placed on the casting roller was transported through an environmentally controlled zone where it was exposed to an environment of 40°C and 40% relative humidity for about 35 seconds. From the environmentally controlled zone, the film was introduced into a coagulation bath of water adjusted to 40°C. After a holding time of 35 seconds for the formation of the membrane structure, the membrane was withdrawn from the coagulation bath and transported to a washing bath by a take-off roller with a speed increased by 16% compared to the casting roller speed. As the roller speed increased, the membrane structure was pulled and the surface pores opened. In the washing bath, the membrane was fixed in water at a temperature increasing stepwise up to 90°C to extract the solvent and polymer additive from the membrane. The membrane was dried using a drum dryer (60-80°C). Within the washing and drying area, there was a further increase in the roller speed of about 5%.

[0071] The finished membrane was a hydrophilic asymmetric membrane. An SEM image of the cross-sectional structure of the membrane is provided in FIG. 1. The membrane had a cross-sectional structure with an internal separation layer (i.e., the layer with the smallest pore size) at a distance of about 5 μm from one surface of the membrane (the downstream surface). The pore size of the separation layer increased towards the interior of the membrane forming a second asymmetric region. The pore size then remained essentially unchanged over a region of about 3 / 4 of the wall thickness forming an essentially isotropic region. Before reaching the opposite surface of the membrane (the upstream surface), the pore size increased to form a first asymmetric region. The pores on both sides of the membrane were elongated in the stretch direction.

[0072] Membrane thickness, transmembrane flux and bubble point measurements are reported in Table 2. Membrane throughput measurements using beer as the fluid are reported in Table 3. Microbial reduction (LRV) after filtration of either L. brevis or S. cerevisiae samples is reported in Table 4.

[0073] Example 2 The same procedure was followed as reported in Example 1, except that the coagulation water bath was adjusted to 37°C instead of 40°C.

[0074] The completed membrane was a hydrophilic asymmetric membrane. An SEM image of the cross-sectional structure of the membrane is provided in FIG. 2. The membrane had a cross-sectional structure with an internal separation layer (i.e., the layer with the smallest pore size) at a distance of about 5 micrometers from one surface of the membrane (the downstream surface). The pore size of the separation layer increased in a direction toward the interior of the membrane forming a second asymmetric region. The pore size then remained essentially unchanged over a region of about 4 / 5 of the wall thickness forming an isotropic region. Before reaching the opposite surface of the membrane (the upstream surface), the pore size increased to form a first asymmetric region. The pores on both sides of the membrane were elongated in the stretch direction.

[0075] Membrane thickness, transmembrane flux and bubble point measurements are reported in Table 2. Membrane throughput measurements using beer as the fluid are reported in Table 3. Microbial reduction (LRV) after filtration of either L. brevis or S. cerevisiae samples is reported in Table 4.

[0076] Example 3 The same procedure was followed as described in Example 1 for the formation of a flat sheet membrane, except that the take-up rollers were operated at the same speed as the casting rollers resulting in no stretching of the membrane.

[0077] The completed membrane was a hydrophilic asymmetric membrane. An SEM image of the membrane is provided in FIG. 3 showing the cross-sectional structure of the membrane. The membrane had a cross-sectional structure with two asymmetric regions being the separating layers. The first separating layer was adjacent to the first membrane surface and the pore size increased in a direction towards the inner portion of the membrane forming the first asymmetric region. The pore size remained essentially unchanged across the central portion of the membrane forming the isotropic region. The pore size then began to decrease in a direction towards the second surface forming the second asymmetric region as the second separating layer.

[0078] Membrane thickness, transmembrane flux and bubble point measurements are reported in Table 2. Membrane throughput measurements using beer as the fluid are reported in Table 3. Microbial reduction (LRV) after filtration of either L. brevis or S. cerevisiae samples is reported in Table 4. [Table 2] [Table 3] [Table 4]

[0079] Example 4 A mixture of 67.2 kg of a mixture of 50% by weight of γ-butyrolactone and 50% by weight of ε-caprolactam was adjusted to 40° C. in a temperature-controlled tank, stirred, and 10.5 kg of finely dispersed poly(2-ethyl-2-oxazoline) was added while stirring until the mixture was homogenous. Then, 26.1 kg of PEG200, 26.1 kg of PEG600 and 0.6 kg of water were added, followed by 19.5 kg of polyethersulfone (PES). The PES was sprinkled into the tank while stirring, and the reaction was maintained for 4 hours. Oxygen was then largely removed from the tank by creating a vacuum and applying nitrogen. The tank was heated to 50° C., and a homogenous solution was obtained after 24 hours of vigorous stirring. The solution was degassed by vacuum. The resulting casting solution had a viscosity of 1.2 Pa s at 60° C. and a tan δ of 56.7.

[0080] The completed casting solution was poured onto a metal casting roller conditioned at 70°C using a casting mold conditioned at 50°C and 60% relative humidity to form a film with a thickness of about 180 micrometers. The film placed on the casting roller was transported through an environmentally controlled zone where it was exposed to an environment of 50°C relative humidity for about 35 seconds. From the environmentally controlled zone, the film was introduced into a coagulation bath of water conditioned at 70°C. After formation of the membrane structure, the membrane was collected by a take-off roller and subsequently transported to a washing bath. In the washing bath, the membrane was fixed in water at a temperature gradually increasing up to 90°C to extract the solvent and polymer additives from the membrane. A drum dryer (60-80°C) was used to dry the membrane. Within the washing and drying zone, there was a further increase in the roller speed of about 9%.

[0081] The completed membrane was a hydrophilic asymmetric membrane. An SEM image of the membrane is provided in Figure 4, which shows the cross-sectional structure of the membrane. The membrane had a cross-sectional structure of two asymmetric regions, with an isotropic region sandwiched between the asymmetric regions. The first asymmetric region had a first open porous layer adjacent to one surface of the membrane, with the pore size within the region decreasing in a direction toward the inner portion of the membrane. The pore size remained essentially unchanged across the central portion of the membrane forming the isotropic region. The pore size increased in a direction toward the opposite surface of the membrane forming the second asymmetric region. As a result, the inner isotropic region was a separating layer. In this configuration, the first asymmetric region had larger pores than the second asymmetric region, and both the first and second asymmetric regions had larger pores than the isotropic region. The TMF of the membrane was 45 mL / (cm 2 The pressure was 1.0 MPa (1.0 MPa) and the bubble point was 2.1 bar.

[0082] Example 5 Using a stack of two membranes instead of a single membrane, the throughput of Pilsner beer was measured using the procedure described in Method C. The stack consisted of two membrane disks from Example 1. For assembly, the first membrane disk in the stack was placed directly above the second membrane disk so that during operation the beer sample first flows through the first disk and then through the second disk. The disks were oriented in the stack such that for each membrane, the upstream surface of the membrane (the surface with the larger pores) faces the inlet port of the filter holder. The membrane throughput with beer as the fluid is reported in Table 6.

[0083] Example 6 The procedure described in Example 5 was followed, except that the membrane disks from Example 1 were replaced with the membrane disks from Example 2. The disks were oriented in the stack such that, for each membrane, the upstream surface of the membrane (the surface with the larger pores) faced the inlet port of the filter holder. The membrane throughput using beer as the fluid is reported in Table 6.

[0084] Example 7 The procedure described in Example 5 was followed, except that one disk from Example 1 and one disk from Example 2 were used in the stack. The disk from Example 1 was the first membrane in the stack, and the disk from Example 2 was the second membrane in the stack. In the assembly, the first membrane disk in the stack (Example 1) was placed directly above the second membrane disk (Example 2) so that during operation, the beer sample flows first through the first disk and then through the second disk. The disks were oriented in the stack such that for each membrane, the upstream surface of the membrane (the surface with the larger pores) faces the inlet port of the filter holder. The membrane throughput with beer as the fluid is reported in Table 6. [Table 5]

[0085] Example 8 The procedure described in Method D was used to measure the log reduction of L. brevis (cfu counts) upon filtration of culture samples through the membrane filter discs of a two-disc stack. The stack consisted of two membrane discs from Example 1. For assembly, the first membrane disc in the stack was placed directly above the second membrane disc, so that during operation, the culture sample flows first through the first disc and then through the second disc. The discs were oriented in the stack such that for each membrane, the upstream surface of the membrane (the surface with the larger pores) faces the inlet port of the filter holder. The reduction in L. brevis counts (LRV) after filtration of the samples through the membrane stack is reported in Table 7.

[0086] Example 9 The procedure described in Example 8 was followed, except that the membrane disks from Example 1 were replaced with the membrane disks from Example 2. The disks were oriented in the stack such that for each membrane, the upstream surface of the membrane (the surface with the larger pores) faced the inlet port of the filter holder. The reduction in L. brevis counts (LRV) after filtering the samples through the membrane stack are reported in Table 7.

[0087] Example 10 The procedure described in Example 8 was followed, except that one disk from Example 1 and one disk from Example 2 were used in the stack. The disk from Example 1 was the first membrane in the stack, and the disk from Example 2 was the second membrane in the stack. For assembly, the first membrane disk in the stack was placed directly above the second membrane disk, so that during operation, the culture sample first flows through the first disk and then through the second disk. The disks were oriented in the stack such that, for each membrane, the upstream surface of the membrane (the surface with the larger pores) faces the inlet port of the filter holder. The reduction in L. brevis counts (LRV) after filtering the samples through the membrane stack is reported in Table 7. [Table 6]

[0088] All references and publications cited herein are expressly incorporated by reference in their entirety into this disclosure. Exemplary embodiments of the invention have been discussed and reference has been made to possible variations within the scope of the invention. For example, features described in the context of one exemplary embodiment may be used in the context of other embodiments of the invention. These and other variations and modifications of the invention will be apparent to those skilled in the art without departing from the scope of the invention, and it should be understood that the invention is not limited to the exemplary embodiments described herein. Therefore, the present invention should be limited only by the claims provided below and their equivalents.

Claims

1. An asymmetric membrane, a membrane wall having first and second porous surfaces and an interior located between said surfaces; a first asymmetric region facing the first surface; a second asymmetric region facing the second surface; the asymmetric membrane is made from a polymer blend comprising an aromatic sulfone polymer and poly(2-oxazoline); The asymmetric membrane, wherein the asymmetric membrane is in the form of a flat sheet.

2. A combination membrane comprising at least two asymmetric membranes according to claim 1, wherein the at least two asymmetric membranes are stacked adjacent to each other.

3. preparing a casting solution comprising an aromatic sulfone polymer and a poly(2-oxazoline); adjusting the casting solution to a casting temperature; pouring the casting solution onto a carrier to form a film; transporting the film disposed on the carrier through an environmentally controlled zone; introducing the film disposed on the carrier into a solidification medium to initiate solidification of the film to form a membrane structure; and stabilizing the membrane structure in the solidification medium.

Images