Patent Grant
10790491
The present invention is directed to a microporous membrane made from a blend of ultra high molecular weight (UHMW) polyolefins.
Microporous membranes are used in a variety of applications including: separators for electrochemical devices (e.g., batteries, fuel cells, and capacitors), separation devices (e.g., mass transfer devices, and filtration devices), medical devices (e.g., blood oxygenation and dialysis), pressure regulators, synthetic papers, to name a few.
The process for manufacturing microporous polyolefin membranes can be broadly divided into the dry (or CELGARD) process and the wet process.
The CELGARD process involves melting a crystalline polyolefin resin, extruding the melt into a film, annealing the film, and orienting (or stretching) the film to form micropores. The CELGARD process involves no extraction step (i.e., solvent handling), and therefore it is inherently simpler than the wet process.
The wet process involves mixing of a polyolefin resin with a hydrocarbon liquid or some other low molecular weight substance, heating and melting the mixture, extruding the melt into a sheet, orienting (or stretching) the sheet, and extracting the liquid from the sheet with a volatile solvent. The wet process is used to make microporous membranes containing ultra high molecular weight polyethylene (UHMWPE).
The wet process, typically, includes one of the following phase separation mechanisms: (1) liquid-liquid phase separation; or (2) solid-liquid phase separation. The liquid-liquid phase separation, also known as TIPS, refers to formation of a polymer-rich liquid matrix and a dispersed polymer-lean liquid, with subsequent solidification of the polymer. The solid-liquid phase separation, also known as GEL process, refers to polymer crystallization from a melt blend.
Microporous membranes made of UHMWPE which are filled or unfilled with particulates are commercially available from Daramic of Owensboro, Ky., Tonen Chemical of Tokyo, Japan, and Asahi Chemical of Tokyo, Japan. These types of membranes are also disclosed in, for example, U.S. Pat. Nos. 6,824,865; 6,666,969; 6,566,012; 6,245,272; 6,153,133; 6,096,213; 5,993,954; 5,922,492; 5,853,633; 5,830,554; 5,786,396; 5,741,848; 5,281,491; 5,051,183; 4,873,034; 4,734,196; 4,650,730; 4,620,955; 4,600,633; 4,588,633; 4,539,256; and Japanese Patent Nos. 3497569 (Kokai JP08-064194); 3258737 (Kokai JP06-212006).
In one end use, battery separators for secondary lithium ion batteries, there is a continuing demand to decrease the thickness of the separator while maintaining or increasing its strength (i.e., the puncture strength).
Accordingly, there is a need for new membranes to meet these and other requirements.
A membrane is a microporous sheet made of a blend of a first ultra high molecular weight polyethylene and a second ultra high molecular weight polyethylene. Each polyethylene has a molecular weight, both of those molecular weights are greater than 1 million, and one molecular weight is greater than the other. Additionally, the intrinsic viscosity (IV) of the membrane is greater than or equal to 6.3.
For the purpose of illustrating the invention, there is shown in the drawings a form that is presently preferred; it being understood, however, that this invention is not limited to the precise arrangements and instrumentalities shown.
A membrane refers to a microporous sheet made from a blend of at least two ultra high molecular weight polyolefins. These blends will be discussed in greater detail below. The membrane or microporous sheet may be characterized by one or more of the following parameters: thickness, porosity, average pore size, puncture strength, MacMullin Number, Gurley Number, intrinsic viscosity (IV), and shutdown temperature. Each of these will be discussed below.
The thickness of the membrane may be less than 5 mils (125 microns). In another embodiment, the thickness may range from 10 microns to 50 microns. In yet another embodiment, the thickness may range from 10 microns to 25 microns.
The porosity of the membrane may be between 25 and 85%. In one embodiment, porosity ranges from 32-58%. In yet another embodiment, porosity ranges from 43-57%.
The average pore size of the membrane may be between 0.01-0.5 microns. In one embodiment, the average pore size ranges from 0.025-0.09 microns. In yet another embodiment, the average pore size ranges from 0.027-0.054 microns.
The puncture strength may be greater than or equal to 300 gr-force/mil. Puncture strength is determined by averaging 10 measurements across the width of the final product using a Midtech Stevens LFRA texture analyzer and a needle with a 1.65 mm diameter and a 0.5 mm radius recording data at a rate of 2 mm/sec with a maximum amount of deflection of 6 mm.
The MacMullin Number (Nmac) may be in the range of 6-15. MacMullin Number is a measure of resistance to movement of ions. MacMullin Number is the ratio of the resistance (r) of the electrolyte saturated separator to the resistance (r0) of an equivalent volume of electrolyte. (Nmac=r/r0. Also see U.S. Pat. No. 4,464,238 which is incorporated herein by reference.
The Gurley Number (normalized to one mil thickness) may be less than 60 sec/10 cc/mil thickness. In one embodiment, the Gurley number ranges from 12 to 56 sec/10 cc/mil. The Gurley Number is the time in seconds required to pass 10 cc of air through one square inch of a film under a pressure of 12.2 inches of water as measured by a Gurley densometer (e.g., Model 4120) according to ASTM D-726(B).
The intrinsic viscosity (IV) of the membrane may be greater than or equal to 6.3 dl/g. In another embodiment, the IV may be greater than or equal to 7.7 dl/g. The IV of the film is not the weighted average of the pre-extruded resins composing the membrane because during extrusion the polymers undergo chain scission and the molecular weight is thereby lowered. Intrinsic viscosity, as used herein, refers to the measure of the capability of a polymer in solution to enhance the viscosity of the solution. The intrinsic viscosity number is defined as the limiting value of the specific viscosity/concentration ratio at zero concentration. Thus, it becomes necessary to find the viscosity at different concentrations, and then extrapolate to zero concentration. The variation of the viscosity number with concentration depends on the type of molecule as well as the solvent. In general, the intrinsic viscosity of linear macromolecular substances is related to the weight average molecular weight or degree of polymerization. With linear macromolecules, viscosity number measurements can provide a method for the rapid determination of molecular weight when the relationship between viscosity and molecular weight has been established. IV is measured by first dissolving 0.02 g of the membrane in 100 ml of decalin at 150° C. for one hour, and then, determining its intrinsic viscosity at 135° C. via an Ubbelohd viscometer. This is according to ASTM D4020 (RSV values reported herein).
The shutdown temperature may be less than 140° C. In one embodiment, the shutdown temperature may be less than 135° C. In yet another embodiment, the shutdown temperature may be less than 130° C.
The membrane may be a blend of ultra high molecular weight polyolefins having differing molecular weights. In one embodiment, these ultra high molecular weight polyolefins may be ultra high molecular weight polyethylene (UHMWPE). In another embodiment, the membrane is a blend of a first ultra high molecular weight polyethylene having a first molecular weight and a second ultra high molecular weight polyethylene having a second molecular weight, the first molecular weight and the second molecular weight being greater than 1 million and being different from one another. In another embodiment, the membrane is a blend of a first ultra high molecular weight polyethylene having a first molecular weight, a second ultra high molecular weight polyethylene having a second molecular weight, the first molecular weight and the second molecular weight being greater than 1 million and being different from one another, and a third polyolefin having a third molecular weight, the third molecular weight being less than 1 million. In yet another embodiment, the membrane may have an IV greater than or equal to 6.3 dl/g. In another embodiment, the membrane may have an IV greater than or equal to 7.7 dl/g.
The first ultra high molecular weight polyethylene may have an IV in the range of 7<IV<15. For example, such materials are commercially available from Ticona of Florence, Ky. as GUR 4012 (IV=10).
The second ultra high molecular weight polyethylene may have an IV of greater than or equal to 15. For example, such materials are commercially available from: Ticona of Florence, Ky. as GUR 4120 (4022) (IV=21) and 4130 (4032) (IV=24); and DSM of Beek, Netherlands as STAMYLAN UH 034 (IV=15).
The third polyolefin may be any ‘melt processable’ polyolefin. ‘Melt processable,’ as used herein, means that the polymer will flow when melted at its melt temperature. Such melt processable polymers may have a molecular weight less than 1.0×106 and may have a molecular weight less than or equal to 0.5×106. Such polymers include, for example, polyethylene, polypropylene, polybutylene, polypentene. In one embodiment, the polyolefin is polyethylene, for example high density polyethylene (HDPE). For example, such HDPE's are commercially available from Ticona of Florence, Ky. as GHR 8020 (MW=0.35×106 and 2110 (MW=0.5×106). One function of this component is to allow shutdown when the membrane is used as a battery separator.
The membrane IV values are measured after formation of the microporous sheet. The membrane IV value is not merely the weighted average of the IV's of the starting materials because during mixing and gellation in the extruder, the polymers undergo chain scission. Chain scission thus results in an IV lower than the weighted average of the starting components.
In those embodiments of the membrane with only the first and second UHMWPE components, the blends may comprise any weight percent of both components, for example 1-99% of each component. In one embodiment, the blend may comprise 20-80% by weight of the resins of the first component and 80-20% by weight of the second component. In another embodiment with only the first and second components, the blend may comprise 40-60% of the first component and 60-40% of the second component.
In those embodiments of the membrane with the first UHMWPE, second UHMWPE, and third polyolefin, the blend may comprise a weight ratio of first:second:third components of 1-6:1-6:1-6. In another embodiment of this membrane, the ratio of components may be in the range of 1-6:1-3:1-6. In yet another embodiment, the blend may comprise a weight ratio of 1-5.5:1-2:1-5.5.
The membrane may be manufactured by a wet process. The initial resin components may be formed into a dry blend by mixing the initial resin components with about 10% of a processing oil, discussed below. This dry blend may be charged into a twin screw extruder for mixing with the balance of the processing oil being injected into the extruder prior to kneading of all components in the extruder. This mixture may be extruded into a nonporous sheet through a slot die. Optionally, any portion, or all, of the processing oil may be removed from the sheet, via extraction (conventional), prior to orientation (stretching). The sheet may be subjected to orientation, for example, biaxial orientation. Thereafter, if necessary, any remaining processing oil is extracted (i.e., conventional extraction techniques). Alternatively, the initial polymer components may be charged directly into the extruder and all of the oil injected into the extruder prior to the kneading section(s) of the extruder, and then processed as set out above. In either embodiment described above, it is also possible to inject a portion of the oil prior to the first kneading section in the extruder and then inject the balance of the oil after the first kneading section(s). While not necessary, the inclusion of VEL (viscoelastic lubricant), discussed below, has been found beneficial to the processing of the forgoing. At extrusion, the resin may comprise about 10-55% by weight of the total mixture, the balance being processing oil or processing oil and VEL. In another embodiment, at extrusion, the resin may comprise about 10-40% of the total mixture.
Processing oil has little solvating effect on the UHMWPE at lower temperatures (e.g., 60° C.), but has a significant solvating effect at elevated temperatures (e.g., 200° C.). Such oils include paraffinic oils, naphthenic oils, and aromatic oils, as well as other materials including the phthalate ester plasticizers such as dibutyl phthalate, bis(2-ethylene)phthalate, diisodecyl phthalate, dicyclohexyl phthalate, butyl benzyl phthalate, and ditridecyl phthalate. Additional oils, plasticizers, and/or solvents are mentioned in U.S. Pat. Nos. 3,351,495; 4,588,633; 4,833,172; 5,248,461; and 5,948,557, and only the related portions of the foregoing patents with regard to such oils, plasticizers, and/or solvents are incorporated herein by reference.
VEL are compounds that, when added to the foregoing resin mixtures, improve the processability of the mixtures. Improved processability refers to a reduction in fusion time (the time it takes the polymeric system to melt (or dissolve) into a flowable solution). Improved processability is also seen as a reduction in energy consumption by the extruder motor and as a reduction in mixture temperature when comparing systems with and without the lubricants. The results arising from this phenomenon include, but are not limited to, decreasing energy consumption, decreased thermal and mechanical degradation of the polymer, increased polymer strength, decreased machine wear, and increased polymer throughputs.
Such VELs are selected from the material classes consisting of: fatty acid esters, ethoxylated fatty acid esters, glycol esters, PEG esters, glycerol esters, ethoxylated esters, sorbitol esters, ethoxylated sorbitol esters, aromatic ethoxylates, alcohol ethoxylates, mercaptan ethoxylates, modified ethoxylates, amide surfactants, phosphate esters, phosphonate esters, phosphite esters, alkyl sulfates, fatty acid ethers, alkyl ether sulfates, alkylaryl ether sulfates, sulfonates, naphthalene sulfonates, sulfosuccinates, sulfonated esters, sulfonated amides, alkyl ether carboxylates, alkylaryl ether carboxylates, quaternary amines, amino quaternary amines, ethoxylated amines, imidazoline derivatives, betaines, sultaines, aminopropionate, catechol derivatives, saturated fatty acids, unsaturated fatty acids, and combinations thereof. For example, such lubricants are commercially available. An exemplary list is set out in the Table below.
Another aspect of the invention relates to a method of controlling the physical properties of the membrane by pre-extraction of a portion of the processing oil (or processing oil and VEL) prior to orientation. It has been determined that physical properties may be strongly affected by the processing oil content of the precursor during orientation. Thus, one may control the physical properties of the membrane by the amount of oil removed from the membrane before orientation.
For example, average pore size and porosity are strongly affected by the oil content of the precursor prior to orientation. Referring to
The present invention is further illustrated by the following non-limiting examples. The property values set forth in the Tables are a compilation of individual runs at the stated conditions. In all of the following examples the initial solution of processing oil (or processing oil and VEL, as indicated) and resins were extruded, via a twin screw extruder, through a slot die, then either 1) subjected to extraction (partial or complete) of the processing oil, then stretched (biaxially), and finally, if necessary, full extraction of any remaining processing oil, or 2) subjected to no pre-stretching extraction, then stretched (biaxially), and finally full extraction of the processing oil. Experimental work included formulations with and without viscoelastic lubricants (VEL). Percent composition means % by weight of the total blend. Ratios are expressed as weight ratios.
In an initial experiment, a microporous film was produced from a formulation containing 33% of HDPE, 33% of a first UHMWPE (IV=10), and 33% of a second UHMWPE (IV=24) with an oil to resin ratio of 3:1, but no VEL. From this work, it was determined that during extrusion, the resin mixture loses between 20-30% of its IV when compared to the weighted average IV of the pre-extruded resin blend. Thus, while it was possible to make the microporous membranes without VEL, the use of VEL is preferred.
In subsequent experimentation, microporous films were produced from formulations set out in Table 1.
The processing parameters and film properties are set out in Tables 2 (formulations with blends of a first UHMWPE and a second UHMWPE) and 3 (formulations with blends of HDPE, first UHMWPE, and second UHMWPE).
The present invention may be embodied in other forms without departing from the spirit and the essential attributes thereof, and, accordingly, reference should be made to the appended claims, rather than to the foregoing specification, as indicated the scope of the invention.
This application is a divisional application of co-pending U.S. application Ser. No. 11/386,612 filed Mar. 22, 2006.
| Number | Name | Date | Kind |
|---|---|---|---|
| 3351495 | Larsen et al. | Nov 1967 | A |
| 3976612 | Kaji et al. | Aug 1976 | A |
| 4539256 | Shipman | Sep 1985 | A |
| 4588633 | Kono et al. | May 1986 | A |
| 4600633 | Kono et al. | Jul 1986 | A |
| 4620955 | Kono et al. | Nov 1986 | A |
| 4650730 | Lundquist et al. | Mar 1987 | A |
| 4734196 | Kono et al. | Mar 1988 | A |
| 4833172 | Schwarz et al. | May 1989 | A |
| 4873034 | Kono et al. | Oct 1989 | A |
| 5051183 | Takita et al. | Sep 1991 | A |
| 5248461 | Pluyter et al. | Sep 1993 | A |
| 5281491 | Rein et al. | Jan 1994 | A |
| 5741848 | Nogata et al. | Apr 1998 | A |
| 5786396 | Takita et al. | Jul 1998 | A |
| 5830554 | Kaimai et al. | Nov 1998 | A |
| 5853633 | Kono et al. | Dec 1998 | A |
| 5922492 | Takita et al. | Jul 1999 | A |
| 5948557 | Ondeck et al. | Sep 1999 | A |
| 5993954 | Radovanovic et al. | Nov 1999 | A |
| 6096213 | Radovanovic et al. | Aug 2000 | A |
| 6153133 | Kaimai et al. | Nov 2000 | A |
| 6245272 | Takita et al. | Jun 2001 | B1 |
| 6566012 | Takita et al. | May 2003 | B1 |
| 6666969 | Funaoka et al. | Dec 2003 | B1 |
| 6824865 | Funaoka et al. | Nov 2004 | B1 |
| 6924956 | Kurihara | Apr 2005 | B2 |
| 6949315 | Samii | Sep 2005 | B1 |
| 20020106557 | Fraser-Bell | Aug 2002 | A1 |
| 20030059657 | Stone et al. | Mar 2003 | A1 |
| 20030193110 | Yaritz | Oct 2003 | A1 |
| 20060121269 | Miller et al. | Jun 2006 | A1 |
| Number | Date | Country |
|---|---|---|
| 06-212006 | Aug 1994 | JP |
| 08-064194 | Mar 1996 | JP |
| 2000195490 | Jul 2000 | JP |
| Entry |
|---|
| Schwartz, S. S. et al., Plastics Materials and Processes, Van Nostrand Reinhold Co. (New York, NY), (p. 74-77), (1982). |
| Number | Date | Country | |
|---|---|---|---|
| 20160043372 A1 | Feb 2016 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 11386612 | Mar 2006 | US |
| Child | 14920925 | US |
