KR101004580B1 - Microporous polyethylene film through liquid-liquid phase separation mechanism and preparing method thereof - Google Patents

Abstract

The present invention relates to a polyethylene microporous membrane which can be used as a battery separator, and a method of manufacturing the same. Polyethylene microporous membrane according to the present invention is prepared from 20-55% by weight of polyethylene and 80-45% by weight of diluent having a thermodynamic liquid-liquid phase separation temperature between 160 ° C and 280 ° C. After the mixing to form a thermodynamic single phase above the liquid-liquid phase separation temperature by forming a phase separation zone inside the extruder to adjust to below the liquid-liquid phase separation temperature to sufficiently induce phase separation and then molding through a die It is done. The polyethylene microporous membrane according to the present invention exhibits excellent puncture strength and gas permeability.

Polyethylene, microporous membrane, battery, separator

Description

Polyporous polyethylene film through liquid-liquid phase separation mechanism and preparing method

The present invention relates to a polyethylene microporous membrane and a method of manufacturing the same. More specifically, the present invention relates to a polyethylene microporous membrane and a method of manufacturing the same, which have excellent extrusion kneading property and elongation property and have excellent puncture strength and gas permeability at the same time, thereby improving the performance and stability of a battery using the same.

Polyolefin microporous films are widely used as battery separators, separation filters, and microfiltration membranes due to their chemical stability and excellent physical properties.

There are three main methods for making a microporous membrane from polyolefins. The first method is to make a microporous membrane in the form of non woven fabric by making polyolefin into a thin fiber, and the second method is to make a thick polyolefin film and stretch it at low temperature to form a lamellar crystal part of the polyolefin. The dry method of forming micro voids by inducing micro cracks. The third method is to knead polyolefins with diluent at high temperature to form a single phase. It is a wet method that extracts and creates voids in polyolefin. The third wet method is thinner and more uniform in thickness than the other two methods, and it is widely used for separators of secondary batteries such as lithium ion batteries because of its thin film and excellent physical properties.

The method of manufacturing a porous film by a wet method is classified into a solid-liquid phase separation method and a liquid-liquid phase separation method according to a process in which the diluent mixed with the polymer (resin) constituting the film undergoes phase separation to form pores. Both methods are identical until the polymer and diluent are mixed at high temperature to form a single phase, but in the case of solid-liquid phase separation, no phase separation occurs until the polymer crystallizes and becomes solid during cooling. In other words, as the polymer chains crystallize, the phase separation occurs while pushing the diluent out of the crystal, and thus the size of the phase separation phase is very small compared to the size of the polymer crystal, and the shape of the separated phase, There is a disadvantage in that the structure such as the size can not be variously adjusted. In this case, there is a limit to the application to the secondary battery separator having the high permeability required in the high capacity secondary battery currently being developed by the secondary battery manufacturer. In addition, it is known that there is no method other than increasing the molecular weight of the polymer resin, such as a method of mixing ultra-high molecular weight polyethylene which is expensive, difficult to mix, and greatly increases the processing load, in order to increase the mechanical strength. As a representative composition of the solid-liquid phase separation, it is widely known to mix paraffin oil or mineral oil with polyolefin resin, and U.S. Patent 4,539,256, U.S. Patent 4,726,989, U.S. Patent 5,051,183 , US Pat. No. 5,830,554, US Pat. No. 6,245,272, US Pat. No. 6,566,012, and the like.

In the case of liquid-liquid phase separation, before the polymer crystallizes and solidifies into solid, phase-separation occurs due to thermodynamic instability of the polymer material, which is also in the liquid state and the diluent, which is also in the liquid state, above the temperature at which the polymer crystallizes. Academia has been well established in terms of phase change and phase separation. In the case of the microporous membrane by liquid-liquid phase separation, the pore size of the microporous membrane by the high-liquid phase separation is basically 2 to 1000 times larger than the microporous membrane by the liquid-liquid phase separation, depending on the combination of the polymer and the diluent. Not only can control the temperature and size of the phase of the liquid phase separation, but also control the size of the phase according to the difference between the thermodynamic liquid-liquid phase separation temperature and the temperature at which the actual phase separation proceeds, and the residence time at each step. There is this.

U.S. Patent No. 4,247,498 introduces a combination of various polymers and diluents that are capable of liquid-liquid phase separation, and that diluents can be extracted from such liquid-liquid phase-separated compositions to produce products of a wide range of thicknesses. Described. US Pat. No. 4,867,881 describes an invention for drawing oriented microporous membranes by stretching, extracting, drying and heat setting a composition prepared by liquid-liquid phase separation. In the above patents, the liquid mixture is extruded in the form of a thermodynamic single phase by maintaining a temperature above the liquid-liquid phase separation until mixing and extruding, and the resin melt is extruded into the atmosphere and then cooled in a relatively short process of several seconds which is cooled by a casting roll or the like. -Since liquid phase separation occurs, it cannot provide enough time for phase separation, and thus, the effect of phase separation is less, and the porosity is difficult to control during the extrusion and cooling process, so that the essential properties of the secondary battery separator are excellent. There is a limit to simultaneously obtaining mechanical strength and transmittance. Particularly, U.S. Patent No. 4,867,881 does not specifically describe the stretching temperature in the claims, but in the case of the embodiment using the high density polyethylene, the stretching temperature is drawn at a low temperature of at least 20 ° C. or lower and 60 ° C. or lower than the melting temperature of the high density polyethylene. In this case, tearing of the polymer occurs due to forced low-temperature stretching, and as a result, the permeability can be improved. It can be seen that the rapid permeability increase with increasing the draw ratio in the example well supports this phenomenon. However, such low-temperature stretching can be judged as a method to be performed because the structure of the pores is not sufficiently obtained during the extrusion and cooling process, and when performing low-temperature stretching, needle holes, or abnormal size, which are the most important factors of product defects for battery separators Not only is the probability of large holes occurring, but also the risk of sheet breakage is increased.

Accordingly, the present inventors have conducted extensive research to solve the above-mentioned problems of the prior art, and after mixing polyethylene and diluent in a single phase, the liquid-liquid phase separation is sufficiently performed in the extruder, and thus the temperature in the phase separation state. It was found that the microporous membrane exhibiting high permeability can be obtained by controlling the phase and residence time in a wide range to obtain a desired degree of phase separation and pore size. At the same time, when the phase separation proceeds sufficiently, the remaining of the diluent remaining in the phase separated polyethylene phase Since the content is further reduced, it is possible to draw at a high temperature close to the melting temperature of the polyethylene during the stretching in the post-process, which gives more stability to the stretching operation, the orientation effect on the polyetherene phase-separated to a high content is increased, Due to the fact that it shows higher mechanical strength at the same molecular weight. Not to have completed the present invention.

Accordingly, an object of the present invention is to provide a polyethylene microporous membrane having high permeability and excellent mechanical strength that can be used as a high capacity secondary battery separator.

Another object of the present invention is to provide a method for producing the polyethylene microporous membrane with high productivity through an economic process.

Polyethylene microporous membrane according to the present invention for achieving the above object is

(a) A liquid containing 20 to 55% by weight of polyethylene (component I) and 80 to 45% by weight of diluent (component II) having the property of liquid-liquid phase separation with component I at 160 to 280 ° C. Melting / kneading / extruding above the liquid phase separation temperature to form a thermodynamic single phase in the extruder;

(b) extruding the single phase melt through a die by passing liquid-liquid phase separation through a zone controlled to a liquid-liquid phase separation temperature range;

(c) liquid-liquid phase separation is performed to shape the extruded melt into a sheet form;

(d) stretching the sheet in a sequential or simultaneous stretching method including a roll method or a Tenter method such that the transverse direction and the longitudinal direction are each 4 times or more and the total draw ratio is 25-50 times;

(e) extracting component II from the stretched film and drying; And

(f) heat-setting to remove residual stress of the dried film such that the shrinkage of the film is 5% or less in the longitudinal and transverse directions; Is produced by

The polyethylene microporous membrane has a gas permeability (Darcy's permeability constant) of 2.0x10 ^-5 or more, and a value obtained by multiplying the gas permeability and puncture strength is 0.45x10 ^-5 Darcy.N / μm or more, Shrinkage is characterized by less than 5% each.

Looking at the present invention in more detail as follows.

As described above, according to the present invention, by controlling the size of the pores by the sufficient phase separation in the extruder, by reducing the content of the diluent in the phase separated polyethylene phase to increase the stretch workability, maximize the orientation effect during stretching The present invention provides a polyethylene microporous membrane having a high permeability and excellent mechanical strength without processing problems due to an increase in molecular weight and a method for producing the same.

The basic theory of making polyethylene microporous membrane from polyethylene used in the present invention is as follows.

Low molecular weight organic materials (hereinafter referred to as diluents), which are partially compatible with the temperature of the polyethylene, may form a thermodynamic single phase with the polyethylene at temperatures higher than the temperature at which the polyethylene melts. Slow cooling of these thermodynamic single phase polyethylene and diluent solutions results in phase separation of polyethylene and diluent during the cooling process before the polyethylene crystallizes and solidifies. This is called liquid-liquid phase separation because both polyethylene and diluent have phase separation in the liquid state. In this case, each phase separated from each other is a polyethylene rich phase in which polyethylene constitutes most of the content, and a diluent rich phase composed of a small amount of polyethylene and diluent dissolved in the diluent. phase). When two phases are thermodynamically separated, both phases are in a state of mobility (or temperature), and the phases of the phases become larger due to coarsening. . At this time, the degree of phase separation of the phase separated by the call scanning action is dependent on the residence time in the liquid-liquid phase separation state and the temperature at which the liquid-liquid phase separation state is maintained. That is, the larger the residence time (proportional to the quarter square of the residence time), the larger the difference between the temperature at which the liquid-liquid phase separation occurs and the temperature at which the liquid-liquid phase separation actually proceeds, the larger the size of each phase. The increase in the size of each phase stops when the temperature of the melt drops below the crystallization temperature of the polyethylene-containing phase and the polyethylene-containing phase crystallizes. Therefore, the liquid-liquid phase separation of the melt proceeds completely, and the polyethylene poly-containing phase is solidified by solidifying the polyethylene-containing phase, followed by extracting the dilutive poly-containing phase with an organic solvent, thereby forming a porous polyethylene film.

Therefore, the basic pore structure of the microporous membrane is determined during the phase separation process. That is, the size and structure of the diluent multi-containing phase made after phase separation determine the pore size and structure of the final microporous membrane. Therefore, it is possible to control the pore structure according to the thermodynamic phase separation temperature of the composition, the rate and time of phase separation during processing, and the depth of the phase separation induction temperature.

In addition, the basic physical properties of the microporous membrane are determined according to the polyethylene concentration in the polyethylene-containing phase during the phase separation process. When the phase separation is sufficiently performed and the polyethylene concentration of the polyethylene-containing phase is sufficiently high, the fluidity of the polyetherene chain is decreased during the stretching after cooling, resulting in an increase in the forced orientation effect, thereby increasing the mechanical strength after the stretching. It gets bigger. In other words, assuming sufficient phase separation with diluent using a resin having the same molecular weight, the mechanical strength is much better than that of a composition that is not.

The present inventors have found the following facts as a result of long research. In other words, in order to simultaneously obtain excellent permeability and mechanical properties required as an excellent battery separator, liquid-liquid phase separation is sufficiently performed to increase the size of the multifunctional polyphase, and the high concentration of polyethylene is present so that the polyethylene phase is contained. Therefore, it is necessary to maximize the orientation effect on the polyethylene during the stretching process in the post-process, and as described above, the biggest influence is the composition and processing conditions for proceeding sufficient liquid-liquid phase separation.

Based on this, using a composition having an appropriate phase separation temperature, the product produced by controlling the degree of liquid-liquid phase separation in the extruder, polyethylene microporous having excellent permeability and mechanical properties even with a resin having a lower molecular weight than the conventional invention The film can be made and the workability is greatly improved.

Polyethylene microporous membrane according to the present invention is 20 to 55% by weight polyethylene (component I) and 80 to 45% by weight of the diluent (component II) having the property of liquid-liquid phase separation with the component I at 160 ~ 280 ℃ Melt-kneading / extruding the mixture to be above the liquid-liquid phase separation temperature to form a thermodynamic single phase in the extruder, and passing the melt through a section in the extruder controlled to a liquid-liquid phase separation temperature range. After the step of advancing through the die by the phase separation and the step of forming liquid-liquid phase separation to form the extruded melt in the form of a sheet, the sheet in the transverse direction, by a sequential or co-drawing method including a roll or Tenter method 4 times or more in the longitudinal direction and 25-50 times the total draw ratio, and the component II is extracted from the stretched film and dried to remove residual stress of the dried film to shrink the film. It is a polyethylene microporous membrane, characterized in that it is produced through the step of heat setting so that the rate is 5% or less in the longitudinal direction, transverse direction.

Polyolefin microporous membranes commonly used in the prior art include various polyethylenes (low density polyethylene, linear low density polyethylene, medium density polyethylene, high density polyethylene, etc.) and polypropylene. However, in the case of polyethylene and polypropylene except high-density polyethylene, the structural regularity of the polymer is lowered, and the lamellar completion of the resin itself is lowered and the thickness is reduced. In addition, when a comonomer is present during the polymerization reaction, a low molecular weight molecule is produced because the reactivity of the comonomer is lower than that of ethylene. Therefore, the high density polyethylene is preferably a content of comonomer is 2% by weight or less. As the comonomer, alpha olefins such as propylene, butene-1, hexene-1, 4-methylpentene-1, and octene-1 may be used, but more preferably, propylene, butene-1, and hexene are relatively highly reactive. -1 or 4-methylpentene-1 is suitable.

The weight average molecular weight of polyethylene is 2x10 ⁵ or more and less than 4.5x10 ⁵ , preferably 3x10 ⁵ to 4x10 ⁵ . If the weight average molecular weight is lower than 2x10 ⁵ , the microporous membrane having excellent final properties cannot be obtained. If the weight average molecular weight is higher than 4.5x10 ⁵ , the extruder load increases due to the viscosity increase during the extrusion process, and the kneading decreases due to the large viscosity difference with the diluent. Is generated, and the surface shape of the sheet to be extruded becomes rough. The solution to this problem is to increase the extrusion temperature or make the shear configuration of the screw configuration of the twin screw compound higher, but in this case, deterioration of the resin occurs, thereby reducing physical properties. In particular, when the ultra high molecular weight polyethylene is used, the above problem may be more serious.

As the diluent used in the present invention, all organic liquid compounds having the property of liquid-liquid phase separation at 160 to 280 ° C. at a composition ratio of 100% by mixing with 20 to 55% by weight of polyethylene are possible. Examples thereof include phthalic acid esters such as dibutyl phthalate, dihexyl phthalate and dioctyl phthalate; Aromatic ethers such as diphenyl ether and benzyl ether; Fatty acids having 10 to 20 carbon atoms, such as palmitic acid, stearic acid, oleic acid, linoleic acid, and linolenic acid; Fatty acid alcohols having 10 to 20 carbon atoms, such as palmitic alcohol, stearic acid alcohol, and oleate alcohol; Palmitic acid mono-, di-, or triesters, stearic acid mono-, di-, or triesters. One or two or more fatty acids of saturated and unsaturated fatty acids having 4 to 26 carbon atoms of fatty acid groups such as oleic acid mono-, di- or triester, linoleic acid mono-, di- or triester Fatty acid esters having 8 to 8 carbon atoms and ester-bonded alcohols. Mixtures of these materials can be used, provided that the conditions of polyethylene and liquid-liquid phase separation at 160-280 ° C. are used, in particular one or more of paraffin oil, mineral oil or wax can be used.

When the liquid-liquid phase separation temperature falls below 160 ° C, the temperature of the rear end of the extrusion should be sufficiently lowered below 160 ° C in order to proceed the liquid-liquid phase separation sufficiently, but in this case, the extrusion should be performed at a temperature close to the melting point of polyethylene. The polyethylene is not melted sufficiently and the viscosity is very high, which mechanically extrudes the extruder, and the surface of the sheet is rough, so that extrusion cannot be performed normally. On the contrary, when the liquid-liquid phase separation temperature rises above 280 ° C, kneading should be carried out at a sufficient temperature of 280 ° C or higher to make a thermodynamic single phase during initial extrusion. However, in this case, the temperature is too high to rapidly promote the oxidative decomposition reaction of the composition. As a result, it is impossible to produce a product having the desired physical properties.

The composition of the polyethylene and diluent used in the present invention is preferably 20 to 55% by weight of polyethylene and 80 to 45% by weight of diluent. When the content of the polyethylene exceeds 55% by weight (ie, when the diluent is less than 45% by weight), the porosity decreases and the pore size becomes small, and the interconnection between the pores decreases so that the permeability is greatly reduced. On the other hand, if the content of the polyethylene is less than 20% by weight (that is, when the diluent exceeds 80% by weight), the kneading property of the polyethylene and the diluent is reduced, so that the polyethylene is not thermodynamically kneaded with the diluent and is in a gel form. Extrusion may cause problems such as fracture and thickness unevenness during stretching.

If necessary, general additives such as an oxidative stabilizer, a UV stabilizer, an antistatic agent, and the like may be further added.

The composition is melt extruded at a higher temperature than liquid-liquid phase separation of the composition using a biaxial compounder, kneader or short-barrier mixer designed for kneading the diluent with polyethylene to obtain a single phase mixture. This single-phase melt is passed through a biaxial compounder, kneader or short-barrier mixer or section inside such equipment with a residence time longer than 30 seconds to maintain liquid-liquid phase separation temperature below -10 ° C. It should be generated / progressed in the machine. The melt separated in this manner inside the processing machine is extruded through a die and cooled to form a sheet. Polyethylene and oil may be pre-blended and introduced into the compounder, or from separate feeders, respectively. If the temperature for causing / separating the phase separation in the processing machine is higher than the liquid-liquid phase separation temperature of -10 ° C., or if the residence time in this phase separation section is less than 30 seconds, the phase separation does not occur sufficiently and the pore size becomes small. As a result, the permeability of the final product is reduced and relatively many diluents coexist inside the polyethylene-containing phase, so that the stretching effect is lowered and the mechanical properties are not increased.

As a method of forming a sheet-shaped molding from the melt, a general casting or calendering method using water cooling or air cooling may be used.

Next, the stretching process may be performed by a rolling or tenter type sequential or simultaneous stretching. Here, the draw ratio is four times or more in the longitudinal direction and the transverse direction, respectively, and the total draw ratio is preferably 25 to 50 times. When the draw ratio in one direction is less than four times, the orientation in one direction is not sufficient, and at the same time, the balance of physical properties between the longitudinal direction and the transverse direction is broken, and the tensile strength and puncture strength are lowered. In addition, if the total draw ratio is less than 25 times unstretched, if more than 50 times is likely to break during stretching, there is a disadvantage that the shrinkage of the final film is increased. Although the stretching temperature varies depending on the composition ratio, it is preferable to perform at a temperature lower than 3-20 ℃ than the melting temperature of the polyethylene itself. When stretching at a temperature higher than 3 ° C, the strength of the film inside the stretching machine is so weak that the stretching is uneven.When stretching at a temperature lower than 20 ° C, there is a possibility of product defects in which relatively large holes such as needle holes are generated. It is high and the breakage of the sheet occurs frequently during operation.

The stretched film is extracted and dried using an organic solvent. The organic solvent usable in the present invention is not particularly limited, but any solvent capable of extracting the diluent used in resin extrusion may be used, but preferably methyl ethyl ketone, methylene chloride, which has high extraction efficiency and rapid drying, Hexane and the like are suitable. As the extraction method, all general solvent extraction methods, such as an immersion method, a solvent spray method, and an ultrasonic method, may be used individually or in combination. The content of residual diluent at the time of extraction should be 2% by weight or less. If the residual diluent exceeds 2% by weight, the physical properties are lowered and the transmittance of the film is reduced. The amount of residual diluent (extraction rate) depends greatly on the extraction temperature and extraction time. The extraction temperature is preferably high in order to increase the solubility of the diluent and the solvent. However, the extraction temperature is preferably 40 ° C. or lower in consideration of safety problems due to the boiling of the solvent. If the extraction temperature is below the freezing point of the diluent, the extraction efficiency is greatly reduced, so it must be higher than the freezing point of the diluent. Extraction time depends on the thickness of the film produced, but 2 to 4 minutes is suitable when producing a general microporous membrane of 10 to 30㎛ thickness.

The dried film is finally subjected to a heat setting step to remove residual stress to reduce the shrinkage of the final film to less than 5% in the longitudinal and transverse directions. The heat setting is to fix the film and apply heat to forcibly hold the film to be shrunk to remove residual stress. The higher the heat setting temperature is advantageous to lower the shrinkage rate, but if it is too high, the permeability of the film is partially blocked due to partial melting of the film, thereby decreasing the permeability. The preferred heat setting temperature is preferably selected in the temperature range in which 10 to 30% by weight of the crystalline portion of the film is melted. If the heat setting temperature is selected in the temperature range lower than the melting temperature of 10% by weight of the crystal part of the film, the reorientation of polyethylene molecules in the film is insufficient, there is no effect of removing the residual stress of the film, the crystal part of the film If 30% by weight of is selected in the temperature range higher than the melting temperature, the microporous is blocked by partial melting, the permeability is reduced.

Here, the heat setting time may be relatively short when the heat setting temperature is high, and may be relatively long when the heat setting temperature is low. Preferably about 15 second-2 minutes are suitable.

The polyethylene microporous membrane of the present invention prepared according to the above has the following physical properties.

(1) The puncture strength is 0.17 N / µm or more.

The puncture strength indicates the strength of the film against a pointed material. When used as a battery separator, if the puncture strength is not sufficient, the film may be torn due to the abnormality of the electrode surface or the dendrite generated at the electrode surface during battery use. Short may occur. The film having a puncture strength of more than 0.17 N / μm according to the present invention has a breaking point weight of 272 g or more when the film is used with the thinnest 16 μm thickness among the separator films currently being widely used, and can be safely used for all applications. .

(2) The Darcy's permeability constant is 2.0 × 10 ^-5 Darcy or higher.

The higher the gas permeability, the better, and the efficiency of the porous membrane is greatly increased at 2.0 × 10 ⁻⁵ Darcy or more, thereby improving ion permeability and charge / discharge characteristics in the battery. The film having a gas permeability of 2.0 × 10 ⁻⁵ Darcy or more according to the present invention is excellent in charge / discharge characteristics, low temperature characteristics, and lifespan of high rate charge / discharge lamps.

(3) The product of gas permeability and puncture strength is not less than 0.45 × 10 ^-5 .

In the case of adjusting the processing conditions, the higher the gas permeability, the lower the puncture strength, and conversely, the higher the puncture strength, the lower the gas permeability. Therefore, the higher the value multiplied by the two values, the higher the puncture strength and gas permeability at the same time can be said to be an excellent separator. Since the value obtained by multiplying the puncture strength and the gas permeability of the separator according to the present invention is 0.45 × 10 ⁻⁵ or more, the two characteristics are excellent at the same time.

(4) Shrinkage is 5% or less in the transverse and longitudinal directions, respectively.

Shrinkage is measured after leaving the film at 105 ° C. for 10 minutes. If the shrinkage is high, the possibility of shrinkage due to heat generated during charging and discharging of the battery is increased, thereby deteriorating battery stability. The lower the shrinkage ratio, the better, and the film according to the present invention can be used safely as a battery separator by preventing the separator from contracting due to self-heating of the battery to prevent the short-circuiting of the electrodes by contacting each other.

In addition to these physical properties, the polyethylene microporous membrane of the present invention is excellent in extrusion kneading property and stretchability.

Polyethylene microporous membrane prepared according to the method of the present invention can be easily extruded and stretched to increase the productivity by producing a stable product, the produced product has a high gas permeability and excellent punching strength and low shrinkage rate for battery separators and various It can be useful for filters.

Hereinafter, the present invention will be described in more detail with reference to the following examples, but the scope of the present invention is not limited thereto.

[Example]

The molecular weight and molecular weight distribution of polyethylene were measured by high temperature gel permeation chromatography (GPC) by Polymer Laboratory.

The viscosity of the diluent was measured with a CAV-4 Automatic Viscometer from Cannon.

Polyethylene and diluent were kneaded in a twin screw extruder having a diameter of 30 mm. There are 20 sections from the first die to the last die of the twin screw extruder, all of the same length except for the last die portion. The screws were installed in lengths from the beginning to 12 sections, and the length / diameter ratio of the screws was 47. In the 14th section, gear pumps are installed to produce sheets of constant thickness. The residence time of the whole extruder was slightly different depending on the composition, but it was about 6 minutes, especially since the residence time to the pressure gauge hanging between the 13th and 14th sections was about 3 minutes. The time to pass the -20th section is also about 3 minutes. It is calculated that it takes about 26 seconds for each section, assuming that the time passing through each of the 14-20th sections is constant. In order to induce liquid-liquid phase separation inside the extruder, the temperature of the 15th to 20th sections was tested in comparison with the liquid-liquid phase separation temperature of the composition.

The extruded melt was extruded from a T-shaped die and formed into a sheet of 600 to 1,200 mu m thick by a casting roll, which was used for stretching. In order to know the presence of gel due to poor melting and kneading, a film having a thickness of 200 μm was separately prepared and the number of gels in an area of 2000 cm 2 was counted. For the production of high quality microporous membranes, the number of gels per 2000 cm 2 should be 20 or less.

Stretching of the sheet was carried out simultaneously with changing the stretching ratio and stretching temperature in a tenter type continuous stretching machine. The stretching speed was kept at 2.0 m / min.

Extraction of the diluent was carried out in an immersion manner using methylene chloride. The residence time in the extractor was 2 minutes, and residual diluent in the film was processed to 2% or less.

The heat setting was performed by drying the film from which the diluent was extracted, fixing the film in a tenter-type continuous frame, and changing the temperature and time in a convection oven.

The molded film was subjected to DSC analysis to analyze the melting phenomenon of the crystal part with temperature. Analytical conditions were 5 mg of sample weight and 10 ° C./min scanning rate.

The prepared film measured tensile strength, puncture strength, gas permeability and shrinkage, which are the most important physical properties in the microporous membrane, and the results are shown in Table 1 below.

※ How to measure properties

(1) Tensile strength was measured by ASTM D882.

(2) The puncture strength was measured by the strength when the pin with a radius of 0.5 mm broke the film at a speed of 120 mm / min.

(3) Gas permeability was measured from a porometer (CFP-1500-AEL manufactured by PMI). In general, the gas permeability is expressed as the Gurley number, but the Gurley number is difficult to know the relative permeability according to the pore structure of the film itself because the influence of the film thickness is not corrected. In order to solve this problem, Darcy's permeability constant was used in the present invention. Darcy's permeability constant is obtained from Equation 1 below and nitrogen is used in the present invention.

C = (8 FTV) / (πD ² (P ² -1))

Where C = Darcy Permeability Constant

       F = flow rate

       T = sample thickness

V = gas viscosity (0.185 for N ₂ )

       D = sample diameter

       P = pressure

In the present invention, the average value of Darcy's permeability constant was used in the range of 100 to 200 psi.

(4) Shrinkage was measured in% in the longitudinal and transverse shrinkage after leaving the film at 105 ℃ for 10 minutes.

Example 1

As the component I, a high density polyethylene having a weight average molecular weight of 2.1 × 10 ⁵ and a melting temperature of 135 ° C. was used, and as the component II, dibutyl phthalate (component A in the following table) was used. The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The first 12 sections of the total 20 sections of the extruder were set to 250 ° C, the two sections of the 13th and 14th sections were set to 220 ° C, and the temperature from the 15th to 20th sections was set to the liquid-liquid phase separation temperature of the composition. Phase separation was carried out by adjusting to 185 ° C. below. Stretching conditions, stretching ratio, heat setting temperature and time were carried out as shown in the table below.

[Example 2]

As component I, a high density polyethylene having a weight average molecular weight of 3.0 × 10 ⁵ and a melting temperature of 134 ° C. was used. It carried out similarly to Example 1 except the extending | stretching temperature being 126 degreeC.

Example 3

As the component I, a high-density polyethylene having a weight average molecular weight of 3.8 × 10 ⁵ and a melting temperature of 132 ° C. was used. The contents of the components I and II were 20% by weight and 80% by weight, respectively.

Stretching was performed at a stretching ratio of 49 times (longitudinal x transverse direction = 7 x 7) at 120 ° C. The heat setting was set at 118 ° C. in order to adjust the melting degree of the crystal to 20% by weight, and the time was 18 seconds. Other content was carried out similarly to Example 1 above.

Example 4

As the component I, a high-density polyethylene having a weight average molecular weight of 3.8 × 10 ⁵ and a melting temperature of 133 ° C. was used, and the contents of the components I and II were 55 wt% and 45 wt%, respectively.

The stretching was performed at a stretching ratio of 25 times (longitudinal x transverse direction = 5 x 5) at 130 ° C. The heat setting was 117 ℃ and the time was 20 seconds. Other content was carried out similarly to Example 1 above.

Example 5

As the component I, the high-density polyethylene used in Example 4 was used, and as the component II, dibutyl phthalate and a paraffin oil having a 40 ° C kinematic viscosity of 160 cSt were mixed 2: 2 (component B in the following table). The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The extrusion temperature of the screw portion was maintained at 230 ° C, and the temperature of the extruder 14-20th section was maintained at 170 ° C to sufficiently induce liquid-liquid phase separation. Drawing was performed at 122 degreeC, and other conditions were performed similarly to Example 1.

Example 6

As the component I, the high-density polyethylene used in Example 4 was used, and as the component II, dibutyl phthalate and a paraffin oil having a 40 ° C kinematic viscosity of 160 cSt were mixed 1: 2 (component C in the following table). The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The extrusion temperature of the screw portion was maintained at 210 degrees, and the temperature of the extruder section 14-20 was maintained at 150 ° C to sufficiently induce liquid-liquid phase separation. Drawing was performed at 122 degreeC, and other conditions were performed similarly to Example 1.

Example 7

As the component I, the high density polyethylene used in Example 4 was used, and as the component II, oleic acid triglyceride and linoleic acid triglyceride were mixed 1: 2 (component D in the following table). The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The extrusion temperature of the screw portion was maintained at 210 ° C, and the temperature of the extruder section 14-20 was maintained at 160 ° C to sufficiently induce liquid-liquid phase separation. Stretching was performed at 125 ° C., and other conditions were carried out in the same manner as in Example 1.

Comparative Example 1

As the component I, the high density polyethylene used in Example 4 was used, and as the component II, dibutyl phthalate (component A in the following table) was used. The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The temperature of the extruder section 14-20 was maintained at 230 ° C. to allow phase separation after the melt emerged from the die after extrusion. Drawing was performed at 118 degreeC, and other conditions were performed similarly to Example 1.

Comparative Example 2

As the component I, the high density polyethylene used in Example 4 was used, and as the component II, dibutyl phthalate (component A in the following table) was used. The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The temperature in the 14-19th section of the extruder was maintained at 230 ° C, and the die temperature, the 20th section, was maintained at 185 ° C. Stretching was performed at 118 ° C, and other conditions were carried out in the same manner as in Example 1.

Comparative Example 3

The high density polyethylene used in Example 4 was used as component I, and dioctyl phthalate (component E in the following table) was used as component II. The contents of component I and component II were 40% by weight and 60% by weight, respectively.

The extrusion temperature of the screw portion was 200 ° C., and the temperature of the extruder section 14-20 was maintained at 150 ° C., the lowest temperature that can be extruded. Stretching was performed at 116 ° C, and other conditions were carried out in the same manner as in Example 1.

[Comparative Example 4]

As the component I, the high density polyethylene used in Example 4 was used, and as the component II, paraffin oil (component F in the following table) having a 40 ° C kinematic viscosity of 120 cSt was used. The contents of component I and component II were 40% by weight and 60% by weight, respectively.

Stretching was carried out at 117 ℃, all other conditions were performed in the same manner as in Example 1.

[Comparative Example 5]

The contents were carried out in the same manner as in Comparative Example 4 except that the contents of the components I and II were 30% by weight and 70% by weight, respectively, and the drawing temperature was 115 ° C.

[Comparative Example 6]

As the component I, high density polyethylene having a weight average molecular weight of 1.7 × 10 ⁵ was used, and was carried out in the same manner as in Example 1 except that the stretching temperature was 128 ° C.

Comparative Example 7

As the component I, a high density polyethylene having a weight average molecular weight of 4.8 × 10 ⁵ was used, and was carried out in the same manner as in Example 1 except that the stretching temperature was 125 ° C.

Comparative Example 8

As the component I, high density polyethylene having a weight average molecular weight of 3.8 × 10 ⁵ was used, and the contents of the component I and the component II were 15 wt% and 85 wt%, respectively, except that the stretching temperature was 115 ° C. The same procedure was followed.

[Comparative Example 9]

As the component I, a high density polyethylene having a weight average molecular weight of 3.8 × 10 ⁵ was used, except that the components I and II contained 60% by weight and 40% by weight, respectively, and the drawing temperature was 128 ° C. The same procedure was followed.

Experimental conditions of the Examples and Comparative Examples and the results obtained therefrom are summarized in Tables 1 to 3 below.

All simple modifications and variations of the present invention fall within the scope of the present invention, and the specific scope of the present invention will be apparent from the appended claims.

Claims (7)

(a) A mixture containing 20 to 55% by weight of polyethylene (component I) and 80 to 45% by weight of diluent (component II) having the property of liquid-liquid phase separation with component I at 160 to 280 ° C in an extruder Melting and kneading at or above the liquid-liquid phase separation temperature to form a melt as a thermodynamic single phase; (b) preparing the melt in a single phase in the extruder, and then passing through a phase separation zone in the extruder controlled to a liquid-liquid phase separation temperature range in the extruder to proceed liquid-liquid phase separation, wherein liquid-liquid In the phase separation state, the extrusion temperature is below the liquid-liquid phase separation temperature -10 ° C, and the residence time in the extruder in the liquid-liquid phase separation state is 30 seconds or more); (c) liquid-liquid phase separation is performed to shape the extruded melt into a sheet form; (d) stretching the sheet in a sequential or simultaneous stretching method including a roll method or a Tenter method such that the transverse direction and the longitudinal direction are each 4 times or more and the total draw ratio is 25-50 times; (e) extracting component II from the stretched film and drying; And (f) removing the residual stress of the dried film and heat-setting the shrinkage of the film to be 5% or less in each of the longitudinal and transverse directions; as a polyethylene microporous membrane produced by The polyethylene microporous membrane has a gas permeability (Darcy's permeability constant) of 2.0x10 ^-5 or more, and a value obtained by multiplying the gas permeability and perforation strength is 0.45x10 ^-5 Darcy.N / μm or more, and has transverse and longitudinal directions. Polyethylene microporous membrane, characterized in that the shrinkage is 5% or less each. The method of claim 1, The phase separation zone in the extruder is characterized in that the degree of phase separation is adjusted by adjusting the length of the melting and kneading zone and the phase separation zone or the extrusion amount to change the holding time in the phase separation zone or the temperature of the phase separation zone to adjust the degree of phase separation. Polyethylene microporous membrane. The method of claim 1, Component I is a polyethylene microporous membrane, characterized in that the polyethylene having a weight average molecular weight of 2x10 ^{5 to} 4.5x10 ⁵ . The method of claim 1 The component II is a phthalic acid ester selected from dibutyl phthalate, dihexyl phthalate, and dioctyl phthalate; Aromatic ethers selected from diphenyl ether and benzyl ether; Fatty acids having 10 to 20 carbon atoms selected from palmitic acid, stearic acid, oleic acid, linoleic acid and linolenic acid; Fatty acid alcohols having 10 to 20 carbon atoms selected from palmitic alcohol, stearic acid alcohol and oleate alcohol; Palmitic acid mono-, di-, or triesters, stearic acid mono-, di-, or triesters. One or two or more fatty acids of saturated and unsaturated fatty acids having 4 to 26 carbon atoms in the fatty acid group selected from oleic acid mono-, di- or triester, linoleic acid mono-, di- or triester 1 to 8, polyethylene microporous membrane, characterized in that at least one component selected from fatty acid esters ester-bonded with alcohol having 1 to 10 carbon atoms. The method of claim 4, wherein Component II is a polyethylene microporous membrane, characterized in that it further comprises one or more components selected from paraffin oil, mineral oil or wax. The method of claim 1, The sheet molding is a polyethylene microporous membrane, characterized in that the molding by molding or calendering method using water cooling or air cooling. The method of claim 1, The heat-setting is a polyethylene microporous membrane, characterized in that the heat-setting step in the temperature range of 10-30% by weight of the crystal portion of the extracted and dried film is heat-setting in a Tenter method with a heat setting time of 15 seconds to 2 minutes.