Patent Application
20230395936
The present disclosure relates to the field of battery separators, and in particular to a polyolefin microporous membrane and a manufacturing system thereof, and a battery separator and an electrochemical apparatus.
Polyolefin microporous membranes are usually used in battery separators, electrolytic capacitor separators, ultrafiltration membranes and microfiltration membranes and medical membranes, etc. For digital lithium ion batteries and power lithium ion batteries, lightness and thinning have become a trend while ensuring the performance of the separators. The development of the polyolefin microporous membranes toward thin film can increase a layer number of the electrode layers, helping increase the energy density and the capacity of the lithium batteries. This makes high output possible. However, the existing ultrathin polyolefin microporous membranes have poor strength. When the ultrathin polyolefin microporous membranes serving as separators and the electrodes are wound together under high tension, the ultrathin polyolefin microporous membranes may break up easily. Therefore, in the prior arts, it is still impossible to manufacture an ultrathin high-strength separator with uniform thickness and stable quality.
In the Chinese patent application number CN 102136557 A, there is disclosed a preparation method for a lithium ion battery separator. In this method, ultrahigh molecular polyethylene is used as the main material to prepare a good-strength separator with a thickness of up to 20 μm.
In the Japanese patent JPH0873643 A, there is disclosed that a preparation method for a lithium ion battery separator. In this method, polyethylene with a viscosity average molecular weight above 100,000 is used to prepare a separator with specific thickness, permeability, porosity, and tensile elongation, which has a thickness of 20 to 40 μm.
The formulas and methods disclosed in the above patents and applications can address the problem of membrane strength in conventional technology. However, there is still the following defect: excessively large membrane thickness which fails to satisfy the requirements of ultra-thinness and high strength. The technical difficult point of the ultrathin high-strength polyolefin microporous membranes lies in that the performances such as thickness, strength, and porosity, of the ultrathin separators cannot be considered at the same time and the separators have poor thickness uniformity.
Therefore, in order to solve the above defects existing in the prior arts, the present disclosure provides a polyolefin microporous membrane having high porosity, ultra-thinness, high strength good thickness uniformity, and capable of improving the battery performance and reducing the battery costs.
In order to, achieve the above objectives, the technical scheme of the present disclosure is implemented as follows.
One object of the present disclosure is to provide a polyolefin microporous membrane with a thickness of 2 to 30 μm and a puncture strength of 1000 to 2000 gf.
Furthermore, a tensile strength along an MD direction is 3200 to 5000 kgf/cm2, and a tensile strength along a TD direction is 2800 to 4800 kgf/cm2.
Furthermore, an elongation along the MD direction is 47 to 98% and an elongation along the TD direction is 63 to 110%.
Furthermore, a porosity is 40% to 57%, a maximum pore size is 33 to 48 nm, and a gas permeability is 10 to 400 seconds/100 ml.
Furthermore, an impedance is 0.3 to 0.9 Ω/cm2.
Furthermore, the polyolefin microporous membrane is made of polyethylene with a weight average molecular weight of 4.0 to 8.0×106.
Another object of the present disclosure is to provide a system for manufacturing any one of the above polyolefin microporous membranes. The system sequentially includes, along a production line direction, a dual-spindle extruder, a casting machine, a pore-forming agent removing unit, a first stretching apparatus, a second stretching apparatus, a heat treatment machine, and a winding machine.
Furthermore, the pore-forming agent removing unit includes a tank, a driving hot roller, a driven hot roller, and a pore-forming agent removal liquid; the tank is a sealed tank, and a polyolefin microporous thin sheet from the casting machine passes through a path which is an open design.
Furthermore, the pore-forming agent removal liquid is located inside the sealed tank; the driving hot roller is located higher than a liquid level of the pore-forming agent removal liquid; the driven hot roller is immersed in the pore-forming agent removal liquid.
Furthermore, the second stretching apparatus and the heat treatment machine are integrated together.
Another object of the present disclosure is to provide a battery separator, which includes any one of the above polyolefin microporous membranes.
Furthermore, the separator is one of a ceramic-coated separator, a PVDF-coated separator, and an aramid-coated separator.
Another object of the present disclosure is to provide an electrochemical apparatus, including any one of the above polyolefin microporous membranes or any battery separator serving as an element for separating positive and negative electrodes.
The present disclosure has the following beneficial effects: compared with the existing microporous membranes, the polyolefin microporous membrane prepared by using the method of the present disclosure can better satisfy the applications having high requirements for uniform thickness, ultra-thinness, and high strength for the microporous membranes, and hence is suitable for the field of the power lithium ion battery separators.
Numerals of the elements are described below:
The specific examples of the present disclosure will be elaborated below in combination with accompanying drawings. It should be understood that the specific examples described herein are used only to describe and explain the present disclosure rather than limit the present disclosure.
An example of the present disclosure provides a polyolefin microporous membrane with a thickness of 2 to 30 μm and a puncture strength of 1000 to 2000 gf.
Furthermore, a tensile strength along an MD direction is 3200 to 5000 kgf/cm2, and a tensile strength along a TD direction is 2800 to 4800 kgf/cm2.
Furthermore, an elongation along the MD direction is 47 to 98% and an elongation along the TD direction is 63 to 110%.
Furthermore, a porosity is 40% to 57%, a maximum pore size is 33 to 48 nm, and a gas permeability is 10 to 400 seconds/100 ml.
Furthermore, an impedance is 0.3 to 0.9 Ω/cm2.
Furthermore, the polyolefin microporous membrane is made of polyethylene with a weight average molecular weight of 4.0 to 8.0×106.
A specific example of the present disclosure provides a system for manufacturing any one of the above polyolefin microporous membranes. The system sequentially includes, along a production line direction, a dual-spindle extruder, a casting machine, a pore-forming agent removing unit, a first stretching apparatus, a second stretching apparatus, a heat treatment machine, and a winding machine.
Furthermore, the pore-forming agent removing unit includes a tank, a driving hot roller, a driven hot roller, and a pore-forming agent removal liquid; the tank is a sealed tank, and a polyolefin microporous thin sheet from the casting machine passes through a path which is an open design.
Furthermore, the pore-forming agent removal liquid is located inside the sealed tank; the driving hot roller is located higher than a liquid level of the pore-forming agent removal liquid; the driven hot roller is immersed in the pore-forming agent removal liquid.
Furthermore, the second stretching apparatus and the heat treatment machine are integrated together.
A specific example of the present disclosure provides a battery membrane, which includes any one of the above polyolefin microporous membranes.
Furthermore, the separator is one of a ceramic-coated separator, a PVDF-coated separator, and an aramid-coated separator.
A specific example of the present disclosure provides an electrochemical apparatus, which includes any one of the above polyolefin microporous membranes or any battery separator serving as an element for separating positive and negative electrodes.
A specific example of the present disclosure provides a preparation method for the polyolefin microporous membrane claimed by the present disclosure, and sequentially includes the following steps.
(1) Polyolefin resin and a pore-forming agent are mixed and heated to a mixed solution in a molten state.
(2) The mixed solution is extruded out of a die head and cooled to form a cast thin sheet containing the pore-forming agent.
(3) The cast thin sheet passes through a boiled pore-forming agent removing unit to remove the pore-forming agent.
(4) The cast thin sheet with the pore-forming agent removed is stretched along at least one axial direction to obtain a basal membrane.
(5) The basal membrane is stretched again along at least one axial direction for molding to obtain the polyolefin microporous membrane.
The boiled pore-forming agent removing unit includes a tank, a driving hot roller 1, a driven hot roller 2, and a pore-forming agent removal liquid 3; the driving hot roller 1 and the driven hot roller 2 may be heated at the temperature of 50° C. to 140° C.; the residual rate of the pore-forming agent of the polyolefin microporous membrane is less than 0.05%, and preferably, 0.02%, and more preferably, 0.01%, and most preferably 0.
Furthermore, the pore-forming agent accounts for 40-50% of a total weight of the polyolefin resin and the pore-forming agent, and a kinematic viscosity at the temperature of 60° C. is 5 to 200 mm2/s.
In the present disclosure, no special limitation is made to the pore-forming agent used herein as long as it can fully dissolve polyolefin. The pore-forming agent may be but is not limited to, for example, one or more of a liquid paraffin, a mineral, oil, and a soy bean oil. Most preferably, the pore-forming agent is a liquid paraffin.
The liquid paraffin as a pore-forming agent and the polyolefin resin, for example, polyethylene resin are melted, mixed, and extracted to form a porous structure with several layers of orientations inside a porous base material, which greatly increases a successive stretching multiple of the gel-like membrane sheet. The higher the stretching multiple and the crystallization degree are, the higher the mechanical strength of the porous base material.
Hence, the liquid paraffin, as a pore-forming agent, can improve the tensile strength and the puncture strength of the porous thin membrane, and thus realize further thinning of the porous membrane.
Furthermore, the weight average molecular weight of the polyolefin resin is 4.0−8.0×106, and the polyethylene resin accounts for 50-60% of a total weight of the polyolefin resin and the pore-forming agent.
In the present disclosure, the term “polyolefin” refers to a polymer prepared by polymerizing or copolymerizing one or more olefins, which includes but is not limited to polyolefin resin that is selected from one or more of polyethylene, polypropylene, polyisoprene, or polybutylene. Furthermore, preferably, the polyolefin resin is polyethylene.
Furthermore, the driving hot roller 1 and the driven hot roller 2 are heated by hot oil flowing in the rollers.
Furthermore, the pore-forming agent removal liquid 3 is an organic solvent mutually soluble with the pore-forming agent. Preferably, the pore-forming agent removal liquid is dichloromethane.
Furthermore, the tank is a sealed tank, and a polyolefin microporous thin sheet from the casting machine passes through a path which is an open design.
As shown in
By introducing a heat transfer oil, the driving hot roller 1 and the driven hot roller 2 are heated to 50° C. to 140° C. Herein, the specific method of heating the driving hot roller 1 and the driven hot roller 2 is the same as the roller heating method at the time of MD and TD stretches 6 and 7, and both methods belong to the conventional technical means well known to those skilled in the art. Therefore, it is not necessary to make redundant descriptions herein. At this time, the polyolefin microporous thin sheet heated by the driving hot roller 1 and the driven hot roller 2 immersed in the pore-forming agent removal liquid 3 will heat dichloromethane at the temperature of 0 to 10° C. in a normal state to a temperature of 30° C. to 39.8° C.
During a heating process, the liquid molecules in the pore-forming agent removal liquid 3 will gain more kinetic energy due to heat transfer and become very active. The energy generated by the kinetic energy is enough to counteract an acting force between molecules, and thus its viscosity is lowered. Furthermore, the increased temperature speeds up molecular motion or vibration, such that the intermolecular repulsive force is increased. In order to achieve a balance again, the intermolecular distance will be increased and accordingly, the attractive force and repulsive force are decreased. As a result, the attractive force and the repulsive force reach a balance again, so as to reduce the tension of the liquid surface. In this way, the pore-forming agent removal liquid 3 will more easily enter the micropores, so as to improve the exchange rate and increase the efficiency of removing the pore-forming agent. In this case, the residual rate of the pore-forming agent will be lower than 0.05%. Furthermore, by preparing raw material formulas of different pore-forming agent proportions and using the different heated temperatures of the driving hot roller 1 and the driven hot roller 2, the efficiency of removing the pore-forming agent is improved such that the residual rate of the pore-forming agent is lower than 0.02%, or lower than 0.01% or even 0.
Furthermore, the stretch in step (4) is an asynchronous bidirectional stretch (MD+TD), or synchronous bidirectional stretch (SBS).
As shown in
As shown in
Furthermore, the basal membrane in step (5) is stretched at the stretch ratio of 2 to 4 times again along at least one axial direction.
After being stretched with high multiples by using different methods, the final product separator will have more orientations and thus have a significantly-increased mechanical strength (tensile strength and puncture strength). Further, the phenomenon of closed or staggered micropores of the thin sheet generated due to slipping will be avoided, and more straight pores are generated. Thus, more lithium ion channels with a high straight pore ratio will be created, thus reducing the impedance of the separator.
The present disclosure will be detailed below by way of examples.
In the following examples and control examples, the membrane performance test is performed in the following method.
Membrane thickness: it is measured by using a Mahr thickness gauge in a spacing of in a width range of the finished product, and then an average membrane thickness value is obtained.
Air permeability value: at room temperature, an oken type air permeability meter is used to set a time for 100 cc of gas to pass through the separator, and a stable value is obtained after five seconds of stable measurement.
Porosity: a sample of 100 mm×100 mm is taken and weighed by using an electronic balance and in combination with polyethylene density, and calculation is performed based on the formula: (1−weight/s ample area)/weight×0.957×100%.
Maximum pore size: it is measured by using a narrow pore meter based on the bubble point method with nitrogen.
Tensile strength & elongation at break: it was measured by using an electronic universal material testing machine XJ830, with the sample specification 15 mm×20 cm and a travel speed of 200 mm/min.
Puncture strength: a test sample is clamped and measured by using an electronic universal material testing machine XJ830 with a front end diameter of 1 mm (0.5 mmR) and a travel speed of 50 mm/min.
Thermal shrinkage rate: a 100 mm×100 mm microporous membrane is maintained in a high temperature test chamber Espec SEG-021H for 1 h at the temperature of 110° C., and measured for length by using an image measuring instrument XTY-5040, and then the lengths along the TD and MD directions before and after drying are calculated based on the formula: (before heat treatment−after heat treatment)/before heat treatment×100%.
Kinematic viscosity: it is measured by using a kinematic viscosity meter DSY-004 at the measurement temperature of 60° Cafter being stabilized for 1 h.
Residual oil rate: a 10 mm×10 mm separator sample is cut and weighed by using an electronic balance; in the Ultrasonic Cleaner 1740T, pure water is placed and a 500 ml beaker with 300 ml of pure dichloromethane is placed, and then the sample is placed in, and ultrasonically treated for 60 s and then dried in the drying oven of 105° C. for 5 min; and weights before and after cleaning are weighed by using an electronic balance and then the residual oil rate is calculated based on the formula: (weight before treatment−weight after treatment)/(weight before treatment)×100%.
Impedance: by using a battery chamber sample injector, an electrolyte is injected to a ⅔ scale of the battery chamber, and then a resistance test channel is selected by using an Agilent data collector KEYSIGHT 34972A, and running is clicked on to wait for automatic analysis data of the equipment.
Firstly, polyethylene with a weight percent of 50% (Mw is 8.0×106) and white oil with a weight percent of 50% were delivered into an extruder at the flow rate of 500 kg/h for extrusion and then extruded out through a T-type die head under the conditions of 220° C. and 100 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. Next, the cast thin sheet entered the pore-forming agent removing unit. The driving hot roller 1 and the driven hot roller 2 were heated to 140° C. through a heat transfer oil. Further, the dichloromethane in the tank was heated to 39.8° C. and at this time, the pore-forming agent removal procedure was started. The cast thin sheet with the pore-forming agent removed was stretched 10 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 120° C., and next stretched 10 times along a width direction (TD) 7 at the temperature of 100° C., and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 30 μm.
Firstly, polyethylene with a weight percent of 55% (Mw is 6.0×106) and white oil with a weight percent of 45% were delivered into an extruder at the flow rate of 650 kg/h for extrusion, and then extruded out through a T-type die head under the conditions of 220° C. and 100 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. Next, the cast thin sheet entered the pore-forming agent removing unit. The driving hot roller 1 and the driven hot roller 2 were heated to 100° C. through a heat transfer oil. Further, the dichloromethane in the tank was heated to 35° C. and at this time, the pore-forming agent removal procedure was started. The cast thin sheet with the pore-forming agent removed was stretched 20 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 120° C., and next stretched 15 times along a width direction (TD) 7 at the temperature of 100° C., and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 14 μm.
Firstly, polyethylene with a weight percent of 55% (Mw is 6.0×106) and white oil with a weight percent of 45% were delivered into an extruder at the flow rate of 400 kg/h for extrusion and then extruded out through a T-type die head under the conditions of 220° C. and 100 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. Next, the cast thin sheet entered the pore-forming agent removing unit. The driving hot roller 1 and the driven hot roller 2 were heated to 100° C. through a heat transfer oil. Further, the dichloromethane in the tank was heated to 35° C. and at this time, the pore-forming agent removal procedure was started. The cast thin sheet with the pore-forming agent removed was stretched 20 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 120° C., and next stretched 15 times along a width direction (TD) 7 at the temperature of 100° C., and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 9 μm.
Firstly, polyethylene with a weight percent of 55% (Mw is 6.0×106) and white oil with a weight percent of 45% were delivered into an extruder at the flow rate of 300 kg/h for extrusion, and then extruded out through a T-type die head under the conditions of 220° C. and 100 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. Next, the cast thin sheet entered the pore-forming agent removing unit. The driving hot roller 1 and the driven hot roller 2 were heated to 100° C. through a heat transfer oil. Further, the dichloromethane in the tank was heated to 35° C. and at this time, the pore-forming agent removal procedure was started. The cast thin sheet with the pore-forming agent removed was stretched 20 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 120° C., and next stretched 15 times along a width direction (TD) 7 at the temperature of 100° C., and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 7 μm.
Firstly, polyethylene with a weight percent of 60% (Mw is 4.0×106) and white oil with a weight percent of 40% were delivered into an extruder at the flow rate of 500 kg/h for extrusion, and then extruded out through a T type die head under the conditions of 220° C. and 100 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. Next, the cast thin sheet entered the pore-forming agent removing unit. The driving hot roller 1 and the driven hot roller 2 were heated to 50° C. through a heat transfer oil. Further, the dichloromethane in the tank was heated to 30° C. and at this time, the pore-forming agent removal procedure was started. The cast thin sheet with the pore-forming agent removed was stretched 35 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 120° C., and next stretched 20 times along a width direction (TD) 7 at the temperature of 100° C., and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 2 μm.
In a conventional process, firstly, polyethylene with a weight percent of 20% (Mw is 3.5×106) and white oil with a weight percent of 80% were delivered into an extruder at the flow rate of 90 kg/h for extrusion, and then extruded out through a T type die head under the conditions of 180° C. and 80 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. The cast thin sheet was stretched 9 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 110° C., and next stretched 8 times along a width direction (TD) 7 at the temperature of 110° C., and then subjected to extraction procedure in the dichloromethane tank of 15° C. to remove the pore-forming agent, and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 2 μm.
In a conventional process, firstly, polyethylene with a weight percent of 20% (Mw is 3.5×106) and white oil with a weight percent of 80% were delivered into an extruder at the flow rate of 300 kg/h for extrusion and then extruded out through a T-type die head under the conditions of 180° C. and 80 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. The cast thin sheet was stretched 9 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 110° C., and next stretched 8 times along a width direction (TD) 7 at the temperature of 110° C., and then subjected to extraction procedure in the dichloromethane tank of 15° C. to remove the pore-forming agent, and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 7 μm.
In a conventional process, firstly, polyethylene with a weight percent of 20% (Mw is 3.5×106) and white oil with a weight percent of 80% were delivered into an extruder at the flow rate of 380 kg/h for extrusion, and then extruded out through a T type die head under the conditions of 180° C. and 80 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. The cast thin sheet was stretched 9 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 110° C., and next stretched 8 times along a width direction (TD) 7 at the temperature of 110° C., and then subjected to extraction procedure in the dichloromethane tank of 15° C. to remove the pore-forming agent, and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 9 μm.
In a conventional process, firstly, polyethylene with a weight percent of 20% (Mw is 3.5×106) and white oil with a weight percent of 80% were delivered into an extruder at the flow rate of 600 kg/h for extrusion and then extruded out through a T type die head under the conditions of 180° C. and 80 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. The cast thin sheet was stretched 9 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 110° C., and next stretched 8 times along a width direction (TD) 7 at the temperature of 110° C., and then subjected to extraction procedure in the dichloromethane tank of 15° C. to remove the pore-forming agent, and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 14 μm.
In a conventional process, firstly, polyethylene with a weight percent of 20% (Mw is 3.5×106) and white oil with a weight percent of 80% were delivered into an extruder at the flow rate of 800 kg/h for extrusion, and then extruded out through a T type die head under the conditions of 180° C. and 80 rpm, and then cooled by contact with a cold roller of 35° C. to form a cast thin sheet. The cast thin sheet was stretched 6 times by using a stretching machine along a mechanical direction (MD) 6 at the temperature of 110° C., and next stretched 8 times along a width direction (TD) 7 at the temperature of 110° C., and then subjected to extraction procedure in the dichloromethane tank of 15° C. to remove the pore-forming agent, and then subjected to secondary TD stretch 9 by two times at the temperature of 120° C. for molding, and then wound by a winding roller to obtain a polyolefin microporous membrane with a thickness of 30 μm.
Separator performance test results of examples 1 to 5 and control examples 1 to 5 are shown in Table 1.
By comparison of examples 1 to 5 and the control examples 1 to 5, it can be seen that the polyolefin microporous membrane has approximate air permeability, but is superior in porosity and thermal shrinkage rate and significantly improved in puncture strength and tensile strength and significantly reduced in impedance.
In the present disclosure, the polyolefin microporous membrane has excellent performance and its thickness, tensile strength, puncture strength, air permeability, porosity, and thermal shrinkage rate all can satisfy the applications having high requirements for the thickness and mechanical strength of the microporous membranes, and hence suitable for the field of power lithium ion battery separators.
The polyolefin microporous membrane prepared by the method of the present disclosure is also suitable for the fields such as humidifying membrane, water purification membrane, artificial dialysis membrane, nanofiltration membrane, ultrafiltration membrane, reverse osmosis membrane and the like, and a cell reproduction substrate and the like.
The contents of common knowledge involved above will not be described in detail (it is a conventional practice in this field to regulate the thickness of the separator by a feed amount) and also can be understood by those skilled in the arts.
The above examples are used only to illustrate the principle and effect of the present disclosure rather than to limit the present disclosure. Those skilled in the arts can make modifications or changes to the above examples without departing from the spirit and scope of the present disclosure. Therefore, all equivalent modifications or changes made by persons having common knowledge in the art without departing from the spirit and technical idea of the present disclosure shall all be covered by the claims of the present disclosure.
| Number | Date | Country | Kind |
|---|---|---|---|
| 202011478177.4 | Dec 2020 | CN | national |
This Application is a national stage application of PCT/CN2021/118236. This application claims priorities from PCT Application No. PCT/CN2021/118236, filed Sep. 14, 2021, and from the Chinese patent application 202011478177.4 filed Dec. 15, 2020, the content of which are incorporated herein in the entirety by reference.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/CN2021/118236 | 9/14/2021 | WO |
