WO2020047958A1 - 一种超临界流体制备无模立体结构发泡制品的方法 - Google Patents

一种超临界流体制备无模立体结构发泡制品的方法 Download PDF

Info

Publication number
WO2020047958A1
WO2020047958A1 PCT/CN2018/111452 CN2018111452W WO2020047958A1 WO 2020047958 A1 WO2020047958 A1 WO 2020047958A1 CN 2018111452 W CN2018111452 W CN 2018111452W WO 2020047958 A1 WO2020047958 A1 WO 2020047958A1
Authority
WO
WIPO (PCT)
Prior art keywords
polymer
dimensional
supercritical fluid
pressure
foamed
Prior art date
Application number
PCT/CN2018/111452
Other languages
English (en)
French (fr)
Inventor
冯云平
Original Assignee
广东奔迪新材料科技有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 广东奔迪新材料科技有限公司 filed Critical 广东奔迪新材料科技有限公司
Priority to EP18915779.5A priority Critical patent/EP3643739B1/en
Priority to KR1020197029996A priority patent/KR102376525B1/ko
Priority to JP2019558561A priority patent/JP7214228B2/ja
Priority to US16/609,739 priority patent/US11286364B2/en
Publication of WO2020047958A1 publication Critical patent/WO2020047958A1/zh

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3403—Foaming under special conditions, e.g. in sub-atmospheric pressure, in or on a liquid
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J9/00—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof
    • C08J9/04—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent
    • C08J9/12—Working-up of macromolecular substances to porous or cellular articles or materials; After-treatment thereof using blowing gases generated by a previously added blowing agent by a physical blowing agent
    • C08J9/122—Hydrogen, oxygen, CO2, nitrogen or noble gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B11/00—Making preforms
    • B29B11/06—Making preforms by moulding the material
    • B29B11/12—Compression moulding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/02—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles for articles of definite length, i.e. discrete articles
    • B29C44/022—Foaming unrestricted by cavity walls, e.g. without using moulds or using only internal cores
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3411—Relieving stresses
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3415—Heating or cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3442—Mixing, kneading or conveying the foamable material
    • B29C44/3446—Feeding the blowing agent
    • B29C44/3453—Feeding the blowing agent to solid plastic material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3469—Cell or pore nucleation
    • B29C44/348—Cell or pore nucleation by regulating the temperature and/or the pressure, e.g. suppression of foaming until the pressure is rapidly decreased
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/35—Component parts; Details or accessories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/60—Measuring, controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2203/00—Foams characterized by the expanding agent
    • C08J2203/06—CO2, N2 or noble gases
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2203/00—Foams characterized by the expanding agent
    • C08J2203/08—Supercritical fluid
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2203/00—Foams characterized by the expanding agent
    • C08J2203/18—Binary blends of expanding agents
    • C08J2203/182—Binary blends of expanding agents of physical blowing agents, e.g. acetone and butane
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2205/00—Foams characterised by their properties
    • C08J2205/04—Foams characterised by their properties characterised by the foam pores
    • C08J2205/044—Micropores, i.e. average diameter being between 0,1 micrometer and 0,1 millimeter
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2323/00—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers
    • C08J2323/02—Characterised by the use of homopolymers or copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond; Derivatives of such polymers not modified by chemical after treatment
    • C08J2323/04—Homopolymers or copolymers of ethene
    • C08J2323/08—Copolymers of ethene
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2367/00—Characterised by the use of polyesters obtained by reactions forming a carboxylic ester link in the main chain; Derivatives of such polymers
    • C08J2367/04—Polyesters derived from hydroxy carboxylic acids, e.g. lactones
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2375/00—Characterised by the use of polyureas or polyurethanes; Derivatives of such polymers
    • C08J2375/04—Polyurethanes
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J2375/00—Characterised by the use of polyureas or polyurethanes; Derivatives of such polymers
    • C08J2375/04—Polyurethanes
    • C08J2375/08—Polyurethanes from polyethers

Definitions

  • the invention relates to the field of foaming processing of polymer materials, in particular to a method for preparing polymer moldless three-dimensional structure foamed products by using supercritical fluid as a physical foaming agent, which can be used for thermoplastics, thermoplastic elastomers or rubber materials.
  • supercritical fluid foamed three-dimensional structure products.
  • the use of supercritical fluids as physical blowing agents for polymer foam molding methods includes continuous extrusion foaming, injection foaming, and batch-type autoclave foaming methods.
  • Continuous extrusion molding is suitable for continuous extrusion of foamed materials with a certain cross-sectional shape.
  • the product has a high expansion ratio but a single shape.
  • Injection foam molding can inject foamed products with complex shapes, but the product has a small expansion ratio. Both have higher productivity.
  • the batch-type autoclaved foaming method is mostly used for polymer bead foaming. Foamed beads also use foaming bead molding equipment to mold foam products of various shapes, with low production efficiency and long production cycles. , Equipment investment is large.
  • Chinese patent CN 102167840A discloses a method for preparing polymer microcellular foamed material by supercritical molding foaming, which includes the following steps: heating the foaming mold on the molding machine, and after reaching the foaming temperature, putting the polymer into The mold and the press are closed, the mold is sealed, the supercritical fluid is filled into the mold, the supercritical fluid swells and diffuses into the polymer, and then the mold is opened to release the pressure and foam to obtain the polymer microcellular foamed material.
  • Chinese patent CN104097288A discloses a supercritical fluid-assisted polymer mold foaming device.
  • the device includes a supercritical fluid delivery system, a mold system, a temperature measurement device, a pressure measurement device, a pressure release device, a display and control system, etc.
  • the supercritical fluid delivery system is connected to a mold system, and the temperature measurement device, pressure measurement device, and pressure release The devices are connected to the mold system respectively.
  • the mold system uses the upper and lower hot plates of the molding press for heating. Utilizing the super penetrating and diffusing ability of supercritical fluid, under a certain temperature and supercritical fluid pressure, after a certain period of time, the supercritical fluid gradually diffuses into the polymer matrix, and then the pressure in the mold is quickly released to obtain a certain shape of foam. material.
  • the device can be used for free foaming or controlled foaming.
  • the above-mentioned molding method using supercritical fluid as a physical foaming agent to prepare polymer molded foamed products can only produce some regular foamed sheets, sheets, and products with simple shapes.
  • the industrial scale production of products is difficult to achieve.
  • Chinese patent CN 107073767 A method for manufacturing a three-dimensional foam product, which discloses a method for manufacturing a three-dimensional foam product with a non-uniform shape, which adopts a two-stage nitrogen autoclave method and has non-uniformity in at least one size Cross-section of a preform.
  • the patent is a two-step method. The first step is to impregnate the preform in a high-pressure tank at high pressure, and the second step is to expand it in a low-pressure tank after cooling.
  • the process flow is as follows: the injection-molded preform undergoes gamma rays to cross-link the material.
  • the crosslinked injection-molded part was placed on a tray in an autoclave and subjected to high-pressure nitrogen impregnation at 400 bar and 165 ° C until the polymer was completely saturated with gas. The pressure was then reduced to 170 bar to nucleate the cell structure, after which the autoclave was cooled to ambient temperature. Once at ambient temperature, the remaining pressure is released and the gas-containing injection-molded part is removed from the autoclave.
  • the second step places the expanded injection molded parts in a refrigerator at -40 ° C overnight to minimize any gas loss before expansion. The next day, the injection-molded part was returned to room temperature, and then placed on a tray in a lower pressure autoclave.
  • the pre-foamed injection-molded part is then heated to a uniform temperature of 167 ° C. under a pressure of 14 bar of nitrogen, and then the pressure is released to atmospheric pressure, so that the molded part expands to form a three-dimensional foamed product.
  • the disadvantages of the molding method are that the process is complicated, the foamed material undergoes radiation cross-linking, the material cannot be recycled and reused, and it is not environmentally friendly; the molding pressure used is high, and the pressure equipment is required to be high; The time required for dissolution and diffusion equilibrium of the preform is long, and the two-step production method is adopted, the production cycle is too long, the production efficiency is low, and the processing cost of the foamed product is high.
  • the present invention proposes a method for preparing polymer moldless three-dimensional foamed products by supercritical fluid, in order to overcome the above-mentioned existing technology that cannot meet the production of foamed products with complex and changeable shapes. It adopts a one-step molding method.
  • the polymer foamed pre-plastic does not need a pre-crosslinking method. It is directly impregnated and foamed in the foaming tank, and no molding mold is required.
  • the three-dimensional foaming tank is always maintained at the target temperature below the polymer during work.
  • the melting temperature or melting point is 1.0-50 °C, the pressure is less than 15MPa, the dipping and foaming time is only 30-120 minutes, the production cycle is extremely short, and the produced product has a three-dimensional foaming structure with a controllable shape and precise dimensions. It can be used for supercritical fluid three-dimensional foamed products such as thermoplastics, thermoplastic elastomers or rubber materials.
  • a method for preparing polymer moldless three-dimensional structure foamed product by supercritical fluid including supercritical fluid transportation system, three-dimensional foaming system, and preheating system, wherein the supercritical fluid transportation system is supercritical CO 2 or supercritical N 2 Transportation system, or N 2 / CO 2 mixed gas;
  • three-dimensional foaming system includes three-dimensional foaming tank, temperature control device, pressure control device, pressure release device, the supercritical fluid transportation system is connected to the three-dimensional foaming system;
  • the preheating system includes a preheating tank, a heating cycle device, and a temperature control device;
  • Adopt a one-step molding method swell and impregnate the polymer with supercritical fluid at high temperature and medium pressure, and free moldless three-dimensional pressure relief foam molding directly in the three-dimensional foaming tank.
  • the specific operation steps are: pressing the polymer raw material to form a foam
  • pre-heat the foamed pre-plastics in the pre-heating system After the temperature rises to the pre-heating temperature, send the foamed pre-plastics into the three-dimensional foaming tank, close the three-dimensional foaming tank sealing cover, and open the air intake valve. Pass in the supercritical fluid, adjust to the target temperature and pressure, the supercritical fluid swells and diffuses into the polymer for 30-120min, and open the pressure release device to release the pressure and foam. You can get the product shape, dimensional accuracy, fine cell and product density. Controlled polymer microcellular foamed article.
  • the polymer is selected from, but not limited to, polyethylene, polylactic acid, polypropylene, polystyrene, polymethyl methacrylate, polycarbonate, acrylonitrile-butadiene-styrene copolymer, Polyethylene terephthalate, polyamide, polyimide, polyphenylene sulfide, polyethersulfone, polyetheretherketone, rubber, silicone rubber, EPDM, ethylene-vinyl acetate copolymer, thermoplastic polyurethane Any one or combination of thermoplastic elastomers.
  • the polymer is an amorphous polymer
  • the target temperature is 1.0-50 ° C. below the polymer melting temperature
  • the pressure is 5-15 MPa.
  • the polymer is a crystalline polymer
  • the target temperature is 1.0-50 ° C. below the melting point of the polymer
  • the pressure is 5-15 MPa.
  • the pressure relief rate of the pressure release device of the three-dimensional foaming tank is 1-1000 MPa / s.
  • the supercritical CO 2 transport system includes a CO 2 liquid storage tank and a CO 2 booster station
  • the supercritical N 2 transport system includes a N 2 liquid storage tank and an N 2 booster station.
  • the supercritical CO 2 delivery system is a N 2 / CO 2 mixed gas, wherein the volume percentage of N 2 is 50-99%.
  • the polymer microcellular foamed product has a volume expansion ratio of 2 to 60 times, an average pore diameter of 0.1 to 100 ⁇ m, and a pore density of 1.0 ⁇ 10 6 to 1.0 ⁇ 10 15 cells / cm 3 .
  • the general plastic processing and molding methods are used to prepare pre-molded parts for polymer foam molding.
  • the foamed pre-molded parts meet the dimensional accuracy after foaming.
  • the foamed pre-molded parts to be processed are pre-prepared in a preheating tank.
  • the preheating temperature is below the softening temperature or melting point of the polymer. After the preheating temperature is reached, it enters the three-dimensional foaming tank together with the rack and closes the three-dimensional foaming tank sealing cover.
  • the three-dimensional foaming tank is always maintained during work.
  • the target temperature is 1.0-50 ° C below the melting or melting point of the polymer.
  • the invention realizes microcellular foaming by introducing a supercritical fluid into a three-dimensional foaming tank.
  • the temperature control system of the three-dimensional foaming tank can control the temperature in the tank, so the supercritical fluid state can be achieved in the three-dimensional foaming tank, the polymer is placed in the supercritical fluid environment at high temperature and pressure, and the supercritical fluid is polymerized The dissolution and diffusion balance in the matrix, and then quickly reduce the pressure to trigger the nucleation, growth, and foaming of the cells in the polymer matrix.
  • the shape can be Control, precise size microcellular foam products
  • the molding pressure used is low, the temperature of the gas-impregnated preplastic is high, the impregnation temperature is near the melting or melting point temperature, and the time required for the dissolution and diffusion balance of the gas-impregnated preplastic is short, which greatly shortens the molding cycle;
  • the formed microcellular foaming material Due to the larger pressure release rate and higher cell nucleation rate when the three-dimensional foaming tank is opened, the formed microcellular foaming material has smaller cells, higher cell density and better performance;
  • a set of three-dimensional foaming tanks can hold multiple layers of products to be foamed, which is suitable for industrial scale production.
  • FIG. 1 is a structural flowchart of a supercritical fluid delivery system and a three-dimensional foaming system according to the present invention
  • FIG. 2 is a schematic diagram of a preheating system according to the present invention.
  • Example 3 is an electron micrograph of a PLA foamed product in Example 1;
  • FIG. 4 is an electron micrograph of a POP COHERE 8102 foamed product according to Example 2 of the present invention.
  • FIG. 5 is an electron microscope scanning view of a 3315 TPU 58315 foamed product according to Example 3 of the present invention.
  • a method for preparing polymer moldless three-dimensional structure foamed product by supercritical fluid including supercritical fluid transportation system, three-dimensional foaming system, and preheating system, wherein the supercritical fluid transportation system is supercritical CO 2 or supercritical N 2 Conveying system, or N 2 / CO 2 mixed gas;
  • three-dimensional foaming system includes three-dimensional foaming tank, temperature control device, pressure control device, pressure release device, temperature control device, pressure control device, pressure release device and three-dimensional foam The tank is connected, and the supercritical fluid delivery system is connected to a three-dimensional foaming system;
  • the preheating system includes a preheating tank, a heating cycle device, and a temperature control device;
  • the specific operation steps are as follows: the polymer raw material is pressure-molded into a foamed preplastic, the foamed preplastic is preheated in a preheating system, and the temperature is raised to a range of 30-50 ° C below the polymer softening temperature or melting temperature.
  • the foamed pre-plastic is sent into the three-dimensional foaming tank, the sealing cap of the three-dimensional foaming tank is closed, the intake valve is opened, and the supercritical fluid is passed in to adjust to the target temperature and pressure.
  • the supercritical fluid swells and diffuses to the polymer for 30-120min
  • opening the pressure release device to release pressure and foam, polymer microcellular foamed products with product shape, dimensional accuracy, fine cell and controllable product density can be obtained.
  • Polylactic acid particles with a number average molecular weight of 100,000 and a melting point of 120 ° C were injection-molded through an injection molding machine mold to form polylactic acid shaped preforms to be foamed.
  • Heat, preheating temperature is in the region of 105 ° C below the melting point of polylactic acid.
  • the three-dimensional foaming tank is always maintained at the target temperature of 125 ° C during work. Open the air inlet valve, and pass in the supercritical fluid.
  • the ratio of supercritical carbon dioxide and supercritical nitrogen mixed gas is 30:70.
  • the working pressure of the three-dimensional foam tank is 10MPa.
  • the supercritical fluid swells and diffuses to the polymer for 80min.
  • the pressure release device opens the exhaust pressure release foam, and the pressure release rate of the three-dimensional foam tank pressure release device is 5 MPa / s, so that polymer microcellular foamed products with product shape, fine cell and controllable product density can be obtained.
  • the volume expansion ratio is 14 times. Based on 100 parts by weight of the polymer, after reaching diffusion equilibrium, the content of supercritical fluid dissolved in the polymer is 15.0 parts.
  • the internal cell morphology was analyzed by a scanning electron microscope, and the average pore diameter was measured to be 6.3 ⁇ m, and the cell density was calculated to be 3.8 X 10 9 cells / cm 3 .
  • the expansion of the polylactic acid shaped pre-plastic is substantially uniform in all directions, and the linear expansion ratio is 2.33 ⁇ 0.15, and finally a foam density product of 90 kg / m 3 is obtained.
  • Polyolefin plastic POP COHERE 8102 with a density of 902kg / m 3 and a melting point of 98 ° C, is injection-molded by an injection molding machine to produce a polyolefin plastic profiled preform to be foamed.
  • the foamed polylactic acid profiled preform to be processed is preheated.
  • the tank is preheated, and the preheating temperature is in the region of 80 ° C below the melting point temperature. After reaching the preheating temperature, enter the three-dimensional foaming tank together with the rack, and close the sealing cap of the three-dimensional foaming tank.
  • the three-dimensional foaming tank is always maintained at the target temperature of 100 ° C during work. Open the air inlet valve and pass in the supercritical fluid.
  • the ratio of the mixed gas of supercritical carbon dioxide and supercritical nitrogen is 20:80.
  • the working pressure of the stereo foam tank at 12MPa.
  • the supercritical fluid swells and diffuses to the polymer for 100min.
  • the pressure release device opens the exhaust pressure release foam, and the pressure release rate of the pressure release device of the three-dimensional foaming tank is 200 MPa / s, so that polymer microcellular foam products with product shape, fine cell and controllable product density can be obtained.
  • the volume expansion ratio is 20 times. Based on 100 parts by weight of the polymer, after the diffusion equilibrium is reached, the content of the supercritical fluid dissolved in the polymer is 18.0 parts.
  • the internal cell morphology was analyzed by scanning electron microscopy, and the average pore diameter was measured to be 32.5 ⁇ m, and the cell density was calculated to be 5.2 ⁇ 10 8 cells / cm 3.
  • the expansion of the polyolefin plastic profiled preform is substantially uniform in all directions, the linear expansion ratio is 2.62 ⁇ 0.15, and finally a foam density product of 45 kg / m 3 is obtained.
  • TPU 58315 density 1120kg / m 3 , melting temperature is 135 ° C. It is made by injection molding machine mold to make TPU shaped pre-plastics to be foamed.
  • the TPU shaped pre-plastics to be processed is preheated in a preheating tank.
  • the thermal temperature is 120 ° C below the melting point temperature.
  • After reaching the preheating temperature enter the three-dimensional foaming tank together with the rack, and close the three-dimensional foaming tank sealing cap.
  • the three-dimensional foaming tank is always maintained at the target temperature of 140 ° C during work. Open the air inlet valve and pass in the supercritical fluid.
  • the ratio of supercritical carbon dioxide and supercritical nitrogen mixed gas is 50:50.
  • the working pressure of the stereo foam tank at 13MPa.
  • the supercritical fluid swells and diffuses to the polymer for 90min.
  • the pressure release device opens the exhaust pressure release foam.
  • the pressure release rate of the three-dimensional foam tank pressure release device is 60 MPa / s.
  • the three-dimensional foam tank releases the supercritical fluid pressure in the tank to 2 MPa through the pressure release device, and then releases it. Press to atmospheric pressure, and then open the sealing cover, you can get polymer microcellular foam products with product shape, fine cell and controllable product density.
  • the volume expansion ratio is 11 times. Based on 100 parts by weight of the polymer, after the diffusion equilibrium is reached, the content of the supercritical fluid dissolved in the polymer is 12.0 parts.
  • the internal cell morphology was analyzed by a scanning electron microscope, and the average pore diameter was measured to be 72 ⁇ m, and the cell density was calculated to be 4.6 ⁇ 10 7 cells / cm 3 .
  • the expansion of the TPU special-shaped pre-plastic is substantially uniform in all directions, and the linear expansion ratio is 2.22 ⁇ 0.15, and finally a foam density product of 101 kg / m 3 is obtained.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Injection Moulding Of Plastics Or The Like (AREA)
  • Molding Of Porous Articles (AREA)

Abstract

一种超临界流体制备聚合物无模立体结构发泡制品的方法，包括超临界流体输送系统、立体发泡系统、预热系统，将聚合物原料加压成型得发泡预塑件，然后将发泡预塑件在预热系统内预热，升温至预热温度后将发泡预塑件送入立体发泡系统内，通入超临界流体，超临界流体向聚合物溶胀扩散完成后泄压即可，本发明通过合理的工艺技术和参数改进，在立体发泡罐内采用一步法高温中压的超临界流体溶胀聚合物，自由无模立体泄压发泡成型，得到产品形状、尺寸精度、泡孔细密和制品密度可控的聚合物微孔发泡制品，泡孔成核速率较高，形成的微孔发泡材料泡孔更小，孔密度更高，性能更优异。

Description

一种超临界流体制备无模立体结构发泡制品的方法 技术领域
本发明涉及高分子材料发泡加工领域，特别涉及一种利用超临界流体作为物理发泡剂制备聚合物无模立体结构发泡制品的方法，可用于热塑性塑料、热塑性弹性体或橡胶材料等的超临界流体发泡立体结构制品。
背景技术
利用超临界流体作为物理发泡剂用于聚合物发泡成型方法主要有连续挤出发泡、注射发泡、间歇形式的釜压发泡方法。连续挤出成型适合于连续挤出具有一定断面形状的发泡材料，制品的发泡倍率高，但形状单一；注射发泡成型可以注射形状复杂的发泡制品，但制品的发泡倍率小，两者都有较高的生产效率。间歇式的釜压发泡方法多用于聚合物的珠粒发泡，发泡珠粒还要利用发泡珠粒的成型设备来模压成各种形状的发泡制品，生产效率低，生产周期长，设备投资大。
中国专利CN 102167840 A公开了一种超临界模压发泡制备聚合物微孔发泡材料的方法，包括如下步骤，将模压机上的发泡模具升温，待达到发泡温度后，将聚合物放入模具，模压机合模，模具密封，向模具内充入超临界流体，超临界流体向聚合物溶胀扩散，然后模压机开模泄压发泡，即可得到聚合物微孔发泡材料。
中国专利CN 104097288 A公开了一种超临界流体辅助聚合物模压发泡装置。该装置包括超临界流体输送系统、模具系统、温度测量装置、压力测量装置、压力释放装置、显示和控制系统等，超临界流体输送系统与模具系统相连，温度测量装置、压力测量装置、压力释放装置分别与模具系统相连。模具系统利用模压机的上、下热板进行加热。利用超临界流体超强的渗透和扩散能力，在一定的温度和超临 界流体压力作用下，经过一定时间，超临界流体逐渐扩散进聚合物基体，然后快速释放模内压力获得一定形状的发泡材料。该装置可用于自由发泡，也可用于可控发泡。
上面所述的利用超临界流体作为物理发泡剂制备聚合物模压发泡制品的成型方法，只能生产一些规整的发泡板材、片材和简单形状的制品，对一些较为形状复杂的发泡制品的工业化规模生产就很难实现。
中国专利CN 107073767 A用于制造三维泡沫制品的方法，公开了一种用于制造非均匀形状的三维泡沫制品的方法，该方法采用了两阶段氮气压力釜方法和在至少一个尺寸上具有非均匀横截面的预制件。专利是使用两步法，第一步是预制件先在高压罐里高压浸渍，第二步是待冷却后在低压罐膨胀。其工艺流程为：注塑成型预制件经历γ射线以将材料交联。将交联的注塑成型件放置在高压压力釜中的托盘上，并且在400巴和165℃下经历氮气高压浸渍，直到聚合物完全被气体饱和。然后将压力降低至170巴，以使泡孔结构成核，之后将压力釜冷却至环境温度。一旦处于环境温度，就将剩余的压力释放并且从高压压力釜中移出含有气体的注塑成型件。第二步将膨胀注塑成型件放置在-40℃的冰箱中过夜以使在膨胀之前的任何气体损耗最小化。次日，使注塑成型件恢复至室温，之后放置在较低压力的压力釜中的托盘上。然后在14巴的氮气的压力下将预发泡注塑成型件加热至167℃的均匀温度，之后将释放压力至大气压，使得成型件膨胀以形成三维发泡制品。其成型方法的缺陷是工艺复杂，发泡材料经历辐射交联，材料无法回收循环使用，不环保；使用的成型压力高，压力设备要求高；浸渍温度在软化点附近，浸渍温度低，气体浸渍预制件溶解扩散平衡所需的时间长，而且采用二步法生产方法，生产周期过长，生产效率较低，发泡制品加工成本高。
发明内容
针对上述存在的问题，本发明提出了一种超临界流体制备聚合物无模立体发泡制品的方法，以克服现有技术存在的上述无法满足形状复杂多变的发泡制品的生产，其特征是采用一步成型法，聚合物发泡预塑件不需要预交联方式，直接在发泡罐浸渍发泡，无需成型模具，立体发泡罐在工作中始终维持在目标温度为低于聚合物熔化温度或熔点温度1.0-50℃，压力小于15MPa，浸渍发泡时间只需30-120分钟，生产周期极短，生产出来的制品为立体发泡结构，形状可控，尺寸精确。可用于热塑性塑料、热塑性弹性体或橡胶材料等的超临界流体立体发泡制品。
为了实现上述的目的，本发明采用以下的技术方案：
一种超临界流体制备聚合物无模立体结构发泡制品的方法，包括超临界流体输送系统、立体发泡系统、预热系统，其中超临界流体输送系统为超临界CO 2或超临界N 2输送系统，或N 2/CO 2混合气体；立体发泡系统包括立体发泡罐、温度控制装置、压力控制装置、压力释放装置，所述超临界流体输送系统与立体发泡系统相连；所述预热系统包括预热罐、加热循环装置、温控装置；
采用一步成型法，通过高温中压的超临界流体溶胀浸渍聚合物，直接在立体发泡罐自由无模立体泄压发泡成型，具体操作步骤为：将聚合物原料加压成型得发泡预塑件，将发泡预塑件在预热系统内预热，升温至预热温度后将发泡预塑件送入立体发泡罐内，关闭立体发泡罐密封盖，打开进气阀，通入超临界流体，调节至目标温度和压力，超临界流体向聚合物溶胀扩散30-120min，打开压力释放装置泄压发泡，即可得到产品形状、尺寸精度、泡孔细密和制品密度可控的聚合物微孔发泡制品。
优选的，所述聚合物选自但不限于聚乙烯、聚乳酸、聚丙烯、聚苯乙烯、聚甲基丙烯酸甲酯、聚碳酸酯、丙烯晴-丁二烯-苯乙烯共聚物、聚对苯二甲酸乙二醇酯、聚酰胺、聚酰亚胺、聚苯硫醚、聚醚砜、 聚醚醚酮，橡胶、硅橡胶、三元乙丙橡胶、乙烯-醋酸乙烯共聚物、热塑性聚氨酯、热塑性弹性体中的任意一种或组合物。
优选的，聚合物选用无定形聚合物，所述目标温度为低于聚合物熔化温度1.0-50℃，压力为5-15MPa。
优选的，聚合物选用结晶聚合物，所述目标温度为低于聚合物熔点温度1.0-50℃，压力为5-15MPa。
优选的，所述的立体发泡罐压力释放装置的泄压速率为1-1000MPa/s。
优选的，所述超临界CO 2输送系统包括CO 2液态储罐、CO 2增压站，所述超临界N 2输送系统包括N 2液态储罐、N 2增压站。
优选的，所述超临界CO 2输送系统为N 2/CO 2混合气体，其中N 2的体积百分比为50-99％。
优选的，聚合物微孔发泡制品体积膨胀倍率为2-60倍，平均孔径为0.1-100μm，孔密度为1.0×10 6-1.0×10 15个/cm 3。
首先利用一般的塑料加工成型手段，制备出用于聚合物发泡成型预塑件，发泡预塑件满足发泡后的各向尺寸精度，待加工发泡预塑件在预热罐内预热，预热温度在聚合物软化温度或熔点温度以下区域，待达到预热温度后，连同料架一起进入立体发泡罐，关闭立体发泡罐密封盖，立体发泡罐在工作中始终维持在目标温度为低于聚合物熔化温度或熔点温度1.0-50℃。打开进气阀，通入超临界流体，在目标温度和工作压力5-15MPa下超临界流体向聚合物溶胀扩散30-120分钟，压力释放装置打开排气泄压发泡，即可得到产品形状、尺寸精度、泡孔细密和制品密度可控的聚合物微孔发泡制品。待立体发泡罐内气体排完，立体发泡罐密封盖快速开门，产品移出立体发泡罐，其后进入下一个生产周期。
本发明通过向立体发泡罐内导入超临界流体实现微孔发泡。立体发泡罐的温控系统可以实现对罐内温度的控制，因此可以在立体发泡 罐内实现超临界流体状态，使聚合物处于高温高压的超临界流体环境，并达到超临界流体向聚合物基体内的溶解扩散平衡，然后通过迅速降低压力，引发聚合物基体内泡孔的成核、生长和发泡定型，通过精确控制压力、温度和泄压速率，得到立体发泡结构，形状可控，尺寸精确的微孔发泡制品
由于采用上述的技术方案，本发明的有益效果是：
1.在立体发泡罐内采用一步法高温中压的超临界流体溶胀聚合物，自由无模立体泄压发泡成型，得到立体发泡制品；
2.无需发泡材料辐射交联，材料可回收循环使用；
3.使用的成型压力较低，气体浸渍预塑件温度高，浸渍温度在熔化或熔点温度附近，气体浸渍预塑件溶解扩散平衡所需的时间短，大大缩短了成型周期；
4.突破了现有技术只能制备形状单一的微孔发泡制品的限制，可以制得立体发泡结构，形状可控，尺寸精确的微孔发泡制品；
5.由于立体发泡罐打开时泄压速率较大，泡孔成核速率较高，形成的微孔发泡材料泡孔更小，孔密度更高，性能更优异；
6.一套立体发泡罐可以放置多层待发泡制品，适合于工业化规模生产。
附图说明
为了更清楚地说明本发明实施例的技术方案，下面将对实施例描述所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。
图1为本发明超临界流体输送系统、立体发泡系统结构流程图；
图2为本发明预热系统示意图；
图3实施例1PLA发泡制品电镜扫描图；
图4为本发明实施例2POP COHERE 8102发泡制品电镜扫描图；
图5为本发明实施例3TPU 58315发泡制品电镜扫描图。
图中：1超临界流体输送系统、2 N 2液态储罐、3 N 2增压站、4 CO 2液态储罐、5 CO 2增压站、6进气阀、7立体发泡系统、8压力控制装置、9温度控制装置、10压力释放装置、11消音器、12排气阀、13预热系统、14温控装置、15加热循环装置。
具体实施方式
为使本发明实施例的目的、技术方案和优点更加清楚，下面将结合本发明实施例，对本发明实施例中的技术方案进行清楚、完整地描述。基于本发明的实施例，本领域普通技术人员在没有作出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
一种超临界流体制备聚合物无模立体结构发泡制品的方法，包括超临界流体输送系统、立体发泡系统、预热系统，其中超临界流体输送系统为超临界CO 2或超临界N 2输送系统，或N 2/CO 2混合气体；立体发泡系统包括立体发泡罐、温度控制装置、压力控制装置、压力释放装置，温度控制装置、压力控制装置、压力释放装置分别与立体发泡罐相连，所述超临界流体输送系统与立体发泡系统相连；所述预热系统包括预热罐、加热循环装置、温控装置；
具体操作步骤为：将聚合物原料加压成型得发泡预塑件，将发泡预塑件在预热系统内预热，升温至聚合物软化温度或熔点温度以下30-50℃区域后将发泡预塑件送入立体发泡罐内，关闭立体发泡罐密封盖，打开进气阀，通入超临界流体，调节至目标温度和压力，超临界流体向聚合物溶胀扩散30-120min，打开压力释放装置泄压发泡，即可得到产品形状、尺寸精度、泡孔细密和制品密度可控的聚合物微孔发泡制品。
实施例1：
将数均分子量为10万，熔点为120℃的聚乳酸粒子通过注塑机模具注塑，制成待发泡聚乳酸异形预塑件，待加工发泡聚乳酸异形预 塑件在预热罐内预热，预热温度在聚乳酸熔点温度以下105℃区域。待达到预热温度后，连同料架一起进入立体发泡罐，关闭立体发泡罐密封盖，立体发泡罐在工作中始终维持在目标温度125℃。打开进气阀，通入超临界流体，超临界二氧化碳和超临界氮气混合气体比例为30:70，在目标温度下，立体发泡罐工作压力在10MPa下超临界流体向聚合物溶胀扩散80min，压力释放装置打开排气泄压发泡，立体发泡罐压力释放装置的泄压速率为5MPa/s，即可得到产品形状、泡孔细密和制品密度可控的聚合物微孔发泡制品。体积膨胀倍率为14倍，以聚合物重量为100份计，达到扩散平衡后，溶解在聚合物中的超临界流体含量为15.0份。通过扫描电镜分析其内部泡孔形态，测量得平均孔径为6.3μm，计算得泡孔密度为3.8 X 10 9个/cm 3。聚乳酸异形预塑件的膨胀在所有方向上是基本上均匀的，线性膨胀比率是2.33±0.15，最终得到90kg/m 3的泡沫密度制品。
实施例2：
聚烯烃塑料POP COHERE 8102，密度902kg/m 3，熔点为98℃，通过注塑机模具注塑，制成待发泡聚烯烃塑料异形预塑件，待加工发泡聚乳酸异形预塑件在预热罐内预热，预热温度在熔点温度以下80℃区域。待达到预热温度后，连同料架一起进入立体发泡罐，关闭立体发泡罐密封盖，立体发泡罐在工作中始终维持在目标温度100℃。打开进气阀，通入超临界流体，超临界二氧化碳和超临界氮气混合气体比例为20:80，在目标温度下，立体发泡罐工作压力在12MPa下超临界流体向聚合物溶胀扩散100min，压力释放装置打开排气泄压发泡，立体发泡罐压力释放装置的泄压速率为200MPa/s，即可得到产品形状、泡孔细密和制品密度可控的聚合物微孔发泡制品。体积膨胀倍率为20倍，以聚合物重量为100份计，达到扩散平衡后，溶解在聚合物中的超临界流体含量为18.0份。通过扫描电镜分析其内部泡孔形态，测量得平均孔径为32.5μm，计算得泡孔密度为5.2 X 10 8个/cm3。 聚烯烃塑料异形预塑件的膨胀在所有方向上是基本上均匀的，线性膨胀比率是2.62±0.15，最终得到45kg/m 3的泡沫密度制品。
实施例3：
TPU 58315，密度1120kg/m 3，熔化温度为135℃，通过注塑机模具注塑，制成待发泡TPU异形预塑件，待加工发泡TPU异形预塑件在预热罐内预热，预热温度在熔点温度以下120℃区域。待达到预热温度后，连同料架一起进入立体发泡罐，关闭立体发泡罐密封盖，立体发泡罐在工作中始终维持在目标温度140℃。打开进气阀，通入超临界流体，超临界二氧化碳和超临界氮气混合气体比例为50:50，在目标温度下，立体发泡罐工作压力在13MPa下超临界流体向聚合物溶胀扩散90min，压力释放装置打开排气泄压发泡，立体发泡罐压力释放装置的泄压速率为60MPa/s，立体发泡罐通过压力释放装置将罐内的超临界流体压力泄至2MPa，然后再泄压到大气压，再打开密封盖，即可得到产品形状、泡孔细密和制品密度可控的聚合物微孔发泡制品。体积膨胀倍率为11倍，以聚合物重量为100份计，达到扩散平衡后，溶解在聚合物中的超临界流体含量为12.0份。通过扫描电镜分析其内部泡孔形态，测量得平均孔径为72μm，计算得泡孔密度为4.6 X 10 7个/cm 3。TPU异形预塑件的膨胀在所有方向上是基本上均匀的，线性膨胀比率是2.22±0.15，最终得到101kg/m 3的泡沫密度制品。
以上实施例仅用以说明本发明的技术方案，而非对其限制；尽管参照前述实施例对本发明进行了详细的说明，本领域的普通技术人员应当理解：其依然可以对前述各实施例所记载的技术方案进行修改，或者对其中部分技术特征进行等同替换；而这些修改或者替换，并不使相应技术方案的本质脱离本发明各实施例技术方案的精神和范围。
在本说明书的描述中，参考术语“一个实施例”、“示例”、“具体示例”等的描述意指结合该实施例或示例描述的具体特征、结构、材 料或者特点包含于本发明的至少一个实施例或示例中。在本说明书中，对上述术语的示意性表述不一定指的是相同的实施例或示例。而且，描述的具体特征、结构、材料或者特点可以在任何的一个或多个实施例或示例中以合适的方式结合。
以上公开的本发明优选实施例只是用于帮助阐述本发明。优选实施例并没有详尽叙述所有的细节，也不限制该发明仅为的具体实施方式。显然，根据本说明书的内容，可作很多的修改和变化。本说明书选取并具体描述这些实施例，是为了更好地解释本发明的原理和实际应用，从而使所属技术领域技术人员能很好地理解和利用本发明。本发明仅受权利要求书及其全部范围和等效物的限制。

Claims (8)

  1. 一种超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：包括超临界流体输送系统、立体发泡系统、预热系统，其中超临界流体输送系统为超临界CO 2或超临界N 2输送系统，或N 2/CO 2混合气体；立体发泡系统包括立体发泡罐、温度控制装置、压力控制装置、压力释放装置，所述超临界流体输送系统与立体发泡系统相连；所述预热系统包括预热罐、加热循环装置、温控装置；
    采用一步成型法，通过高温中压的超临界流体溶胀浸渍聚合物，直接在立体发泡罐自由无模立体泄压发泡成型，具体操作步骤为：将聚合物原料加压成型得发泡预塑件，将发泡预塑件在预热系统内预热，升温至预热温度后将发泡预塑件送入立体发泡罐内，关闭立体发泡罐密封盖，打开进气阀，通入超临界流体，调节至目标温度和压力，超临界流体向聚合物溶胀扩散30-120min，打开压力释放装置泄压发泡，即可得到产品形状、尺寸精度、泡孔细密和制品密度可控的聚合物微孔发泡制品。
  2. 根据权利要求1所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：所述聚合物选自但不限于聚乙烯、聚乳酸、聚丙烯、聚苯乙烯、聚甲基丙烯酸甲酯、聚碳酸酯、丙烯晴-丁二烯-苯乙烯共聚物、聚对苯二甲酸乙二醇酯、聚酰胺、聚酰亚胺、聚苯硫醚、聚醚砜、聚醚醚酮，橡胶、硅橡胶、三元乙丙橡胶、乙烯-醋酸乙烯共聚物、热塑性聚氨酯、热塑性弹性体中的任意一种或组合物。
  3. 根据权利要求2所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：聚合物选用无定形聚合物，所述目标温度为低于聚合物熔化温度1.0-50℃，压力为5-15MPa。
  4. 根据权利要求2所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：聚合物选用结晶聚合物，所述目标温度为低于聚合物熔点温度1.0-50℃，压力为5-15MPa。
  5. 根据权利要求3或4所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：所述的立体发泡罐压力释放装置的泄压速率为1-1000MPa/s。
  6. 根据权利要求3或4所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：所述超临界CO 2输送系统包括CO 2液态储罐、CO 2增压站，所述超临界N 2输送系统包括N 2液态储罐、N 2增压站。
  7. 根据权利要求1所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：所述超临界CO 2输送系统为N 2/CO 2混合气体，其中N 2的体积百分比为50-99％。
  8. 根据权利要求3或4所述的超临界流体制备聚合物无模立体结构发泡制品的方法，其特征在于：聚合物微孔发泡制品体积膨胀倍率为2-60倍，平均孔径为0.1-100μm，孔密度为1.0×10 6-1.0×10 15个/cm 3。
PCT/CN2018/111452 2018-09-06 2018-10-23 一种超临界流体制备无模立体结构发泡制品的方法 WO2020047958A1 (zh)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP18915779.5A EP3643739B1 (en) 2018-09-06 2018-10-23 Method for preparing foamed product of moldless three-dimensional structure by means of supercritical fluid
KR1020197029996A KR102376525B1 (ko) 2018-09-06 2018-10-23 초임계 유체에 의한 무몰드 입체 구조 발포 제품의 제조방법
JP2019558561A JP7214228B2 (ja) 2018-09-06 2018-10-23 超臨界流体により発泡時に金型を要することなくポリマーの微細孔発泡製品を製造する方法
US16/609,739 US11286364B2 (en) 2018-09-06 2018-10-23 Method for preparing polymer mould-free stereostructure foamed product from supercritical fluid

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201811035299.9 2018-09-06
CN201811035299.9A CN109385058B (zh) 2018-09-06 2018-09-06 一种超临界流体制备无模立体结构发泡制品的方法

Publications (1)

Publication Number Publication Date
WO2020047958A1 true WO2020047958A1 (zh) 2020-03-12

Family

ID=65418463

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2018/111452 WO2020047958A1 (zh) 2018-09-06 2018-10-23 一种超临界流体制备无模立体结构发泡制品的方法

Country Status (6)

Country Link
US (1) US11286364B2 (zh)
EP (1) EP3643739B1 (zh)
JP (1) JP7214228B2 (zh)
KR (1) KR102376525B1 (zh)
CN (1) CN109385058B (zh)
WO (1) WO2020047958A1 (zh)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3643739A4 (en) * 2018-09-06 2020-12-30 Guangdong Speed New Material Technology Co., ltd PROCESS FOR THE MANUFACTURING OF A POLYMER FORM-FREE FOAMED PRODUCT WITH A STEREO STRUCTURE FROM SUPER CRITICAL FLUID
CN112959590A (zh) * 2021-02-09 2021-06-15 苏州申赛新材料有限公司 一种可精确控制发泡倍率的发泡方法

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110016213B (zh) * 2019-03-21 2021-07-30 北京工商大学 一种具有微纳米复合泡孔的聚乳酸发泡材料及其制备方法
CN109955423B (zh) * 2019-04-30 2024-04-02 广东奔迪新材料科技有限公司 一种大型超高压热塑性聚合物发泡成型装置及其方法
CN110305359A (zh) * 2019-07-31 2019-10-08 苏州申赛新材料有限公司 一种使用超临界流体制备发泡粒子的装置
CN110667025A (zh) * 2019-09-05 2020-01-10 微碳(上海)材料科技有限公司 一种二氧化碳超临界物理溶解渗透发泡工艺
CN110480913B (zh) * 2019-09-24 2023-08-18 四川大学 多组分多相复杂体系自平衡超临界发泡方法及装置
CN110982110B (zh) * 2019-12-23 2022-07-26 苏州申赛新材料有限公司 一种发泡制品的制备工艺及发泡制品
CN111253612A (zh) * 2020-02-11 2020-06-09 安徽理工大学 一种聚合物功能微球的发泡方法
KR102397310B1 (ko) * 2020-04-08 2022-05-12 에이치디씨현대이피 주식회사 용매를 사용하지 않는 고발포 폴리우레탄 폼 제조방법 및 이 제조방법에 의해 제조된 폴리우레탄 폼
EP3925751A1 (en) * 2020-06-18 2021-12-22 Basf Se Process for continuously producing expanded foam particles
KR102374674B1 (ko) * 2021-02-09 2022-03-16 아비만엔지니어링 주식회사 제품 경량화 발포 시스템 및 제품 경량화 발포 성형 방법
CN113527801A (zh) * 2021-07-16 2021-10-22 福建三盛实业有限公司 一种超临界流体聚合物微孔发泡物及其制备方法
CN114083740B (zh) * 2021-11-19 2024-04-30 苏州申赛新材料有限公司 一种基于空间限制的制备双色发泡板材的方法
CN114311487A (zh) * 2022-02-21 2022-04-12 山东大学 一种聚合物超临界流体混合发泡系统及方法
CN114605688A (zh) * 2022-04-07 2022-06-10 江苏中科聚合新材料产业技术研究院有限公司 一种超临界环氧预浸料发泡板材及其制备方法
CN114872258A (zh) * 2022-04-21 2022-08-09 河南广播电视大学 一种形状记忆聚合物发泡材料的制备方法
CN115160695B (zh) * 2022-07-28 2024-05-10 江苏集萃先进高分子材料研究所有限公司 一种球形电解槽液保温材料、制备方法及应用
CN115505162A (zh) * 2022-09-29 2022-12-23 宁波格林美孚新材料科技有限公司 一种使用超临界二氧化碳发泡的消失模铸造模型材料及其制备方法和应用

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3953558A (en) * 1972-12-19 1976-04-27 Kanegafuchi Kagaku Kogyo Kabushiki Kaisha Method of moulding foamed synthetic resin pellets of polyolefine
CN102167840A (zh) 2011-04-12 2011-08-31 姜修磊 超临界模压发泡制备聚合物微孔发泡材料的方法
CN102504323A (zh) * 2011-11-07 2012-06-20 常州天晟新材料股份有限公司 可工业化的超临界流体技术制备聚合物发泡材料的方法
CN203282653U (zh) * 2013-04-09 2013-11-13 青岛科技大学 一种超临界流体辅助聚合物模压发泡装置
CN104097288A (zh) 2013-04-09 2014-10-15 青岛科技大学 一种超临界流体辅助聚合物模压发泡装置
CN106146874A (zh) * 2016-06-01 2016-11-23 湖州长园特发科技有限公司 一种超临界流体发泡聚烯烃材料及其制备方法
CN107073767A (zh) 2014-05-23 2017-08-18 索特泡沫体股份有限公司 用于制造三维泡沫制品的方法

Family Cites Families (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5158986A (en) * 1991-04-05 1992-10-27 Massachusetts Institute Of Technology Microcellular thermoplastic foamed with supercritical fluid
US5670102A (en) * 1993-02-11 1997-09-23 Minnesota Mining And Manufacturing Company Method of making thermoplastic foamed articles using supercritical fluid
US5830923A (en) * 1996-05-22 1998-11-03 E. I. Du Pont De Nemours And Company Foamed fluoropolymer
JP2000281829A (ja) * 1999-03-30 2000-10-10 Sumitomo Chem Co Ltd 発泡体
JP2002059449A (ja) * 2000-08-21 2002-02-26 Inoac Corp 樹脂発泡成形品の製造方法
JP2002207487A (ja) * 2000-08-30 2002-07-26 Nitto Denko Corp 微孔性防音材
JP2002348398A (ja) * 2001-05-23 2002-12-04 Idemitsu Petrochem Co Ltd 樹脂発泡体及びその製造方法
JP2003261707A (ja) * 2002-03-07 2003-09-19 Fujikura Ltd 樹脂発泡体の製法
JP2003326539A (ja) * 2002-05-16 2003-11-19 Denso Corp 樹脂成形品およびその製造方法
JP3854537B2 (ja) * 2002-05-22 2006-12-06 日立マクセル株式会社 熱可塑性樹脂発泡体の成形方法
JP2004017285A (ja) * 2002-06-12 2004-01-22 Japan Steel Works Ltd:The 薄肉発泡成形体の成形方法及び薄肉発泡成形体並びに発泡体成形装置
JP3967212B2 (ja) * 2002-07-01 2007-08-29 ポリプラスチックス株式会社 発泡射出成形品及び発泡射出成形方法
KR101150973B1 (ko) * 2010-01-21 2012-05-30 충남대학교산학협력단 닫힌셀을 포함하는 폴리올레핀계 수지 발포체 및 이의 연속 제조방법
EP2570454B1 (en) * 2010-05-10 2019-09-18 Nitto Boseki CO., LTD. Method of foam molding of resin reinforced with flat glass fibers
CN102863143B (zh) * 2012-10-15 2015-02-11 童少斌 一种无模法泡沫玻璃连续发泡装置及发泡工艺
US9375866B2 (en) * 2013-03-15 2016-06-28 Nike, Inc. Process for foaming thermoplastic elastomers
CN104277237A (zh) * 2013-07-10 2015-01-14 宁波大学 一种聚合物发泡材料的制备方法
US9926423B2 (en) * 2013-08-02 2018-03-27 Nike, Inc. Low density foam, midsole, footwear, and methods for making low density foam
JP6322168B2 (ja) 2015-07-27 2018-05-09 京楽産業．株式会社 遊技機
TWI614111B (zh) * 2015-12-16 2018-02-11 寶成工業股份有限公司 熱可塑高分子之發泡鞋底及熱可塑高分子之發泡鞋底的製作方法
CN105639837A (zh) * 2016-03-29 2016-06-08 丁荣誉 覆膜爆米花聚氨酯鞋材及其生产工艺
JP6506724B2 (ja) 2016-05-18 2019-04-24 象印マホービン株式会社 水加熱装置
CN106336523A (zh) * 2016-08-31 2017-01-18 杭州博适特新材料科技有限公司 一种制备热塑性聚合物发泡珠粒的方法
US20180273718A1 (en) * 2016-12-02 2018-09-27 Dongguan Hailex High Polymer Material Science and Technology, Co., Ltd. Method for preparing foamed structure
CN107674233A (zh) * 2017-10-19 2018-02-09 宁波致微新材料科技有限公司 聚碳酸酯微孔发泡材料的制备方法
CN107785516B (zh) * 2017-10-31 2024-02-13 深圳市宝尔爱迪科技有限公司 可自拆装的电池盖结构
CN109385058B (zh) * 2018-09-06 2020-08-11 广东奔迪新材料科技有限公司 一种超临界流体制备无模立体结构发泡制品的方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3953558A (en) * 1972-12-19 1976-04-27 Kanegafuchi Kagaku Kogyo Kabushiki Kaisha Method of moulding foamed synthetic resin pellets of polyolefine
CN102167840A (zh) 2011-04-12 2011-08-31 姜修磊 超临界模压发泡制备聚合物微孔发泡材料的方法
CN102504323A (zh) * 2011-11-07 2012-06-20 常州天晟新材料股份有限公司 可工业化的超临界流体技术制备聚合物发泡材料的方法
CN203282653U (zh) * 2013-04-09 2013-11-13 青岛科技大学 一种超临界流体辅助聚合物模压发泡装置
CN104097288A (zh) 2013-04-09 2014-10-15 青岛科技大学 一种超临界流体辅助聚合物模压发泡装置
CN107073767A (zh) 2014-05-23 2017-08-18 索特泡沫体股份有限公司 用于制造三维泡沫制品的方法
CN106146874A (zh) * 2016-06-01 2016-11-23 湖州长园特发科技有限公司 一种超临界流体发泡聚烯烃材料及其制备方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3643739A4

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3643739A4 (en) * 2018-09-06 2020-12-30 Guangdong Speed New Material Technology Co., ltd PROCESS FOR THE MANUFACTURING OF A POLYMER FORM-FREE FOAMED PRODUCT WITH A STEREO STRUCTURE FROM SUPER CRITICAL FLUID
CN112959590A (zh) * 2021-02-09 2021-06-15 苏州申赛新材料有限公司 一种可精确控制发泡倍率的发泡方法

Also Published As

Publication number Publication date
EP3643739A4 (en) 2020-12-30
KR102376525B1 (ko) 2022-03-18
KR20200028879A (ko) 2020-03-17
US20210332210A1 (en) 2021-10-28
CN109385058A (zh) 2019-02-26
CN109385058B (zh) 2020-08-11
EP3643739A1 (en) 2020-04-29
US11286364B2 (en) 2022-03-29
EP3643739B1 (en) 2023-01-25
JP7214228B2 (ja) 2023-01-30
JP2020535032A (ja) 2020-12-03

Similar Documents

Publication Publication Date Title
WO2020047958A1 (zh) 一种超临界流体制备无模立体结构发泡制品的方法
WO2018040624A1 (zh) 一种制备热塑性聚合物发泡珠粒的方法
CN102167840B (zh) 超临界模压发泡制备聚合物微孔发泡材料的方法
US8591799B2 (en) Methods for blow molding solid-state cellular thermoplastic articles
JP7165413B2 (ja) 熱可塑性ポリマー粒子の型内モールド発泡成形装置及びその成形方法
JP2007516108A (ja) ガス含侵ポリマーから熱成形された製品を製造する方法
JPH06506724A (ja) 超微孔質発泡材料
CN109551701A (zh) 一种半结晶聚合物原位发泡模塑成型方法
CN109021379A (zh) 辐射交联聚丙烯发泡材料、制备方法及其应用
US3578549A (en) Expandable plastic articles
CN112851999A (zh) 一种二次发泡制备高发泡倍率聚合物基泡沫珠粒的方法
CN111319182A (zh) 一种分级控压式开模发泡工艺、装置及获得的发泡产物
JP2001105447A (ja) 発泡成形体の製造方法
JPS5912455B2 (ja) ポリオレフイン系合成樹脂発泡成形体の製造方法及び装置
WO2020220382A1 (zh) 一种大型超高压热塑性聚合物发泡成型装置及其方法
TW201441008A (zh) 用於吹塑成形固態多孔熱塑性物件的方法
EP3154762B1 (en) Low temperature process for integrating a polymeric foam with a polymeric body
JP2000351153A (ja) 二軸延伸ポリエチレンテレフタレートシートの成形方法
JP3146004B2 (ja) オレフィン系合成樹脂発泡成形体の製造方法
CN215943509U (zh) 一种发泡装置
CN113001864A (zh) 一种基于发泡注塑制坯的聚合物微发泡装置和工艺
JP2000119453A (ja) ポリオレフィン樹脂成形体およびその製造方法
JP2006082473A (ja) 熱可塑性樹脂発泡シートの真空成形方法
JPH1016036A (ja) ブロー成形方法およびブロー成形品
JPH09324065A (ja) シリコーンゴム系発泡体の製造方法

Legal Events

Date Code Title Description
ENP Entry into the national phase

Ref document number: 2019558561

Country of ref document: JP

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2018915779

Country of ref document: EP

Effective date: 20191029

NENP Non-entry into the national phase

Ref country code: DE