WO2000043444A1 - Procedimiento e instalacion para producir espuma, y bloques y placas de espuma producidos - Google Patents
Procedimiento e instalacion para producir espuma, y bloques y placas de espuma producidos Download PDFInfo
- Publication number
- WO2000043444A1 WO2000043444A1 PCT/ES2000/000002 ES0000002W WO0043444A1 WO 2000043444 A1 WO2000043444 A1 WO 2000043444A1 ES 0000002 W ES0000002 W ES 0000002W WO 0043444 A1 WO0043444 A1 WO 0043444A1
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- WO
- WIPO (PCT)
- Prior art keywords
- mixture
- ethanol
- plasticized mixture
- plasticized
- temperature
- Prior art date
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Classifications
-
- 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
- 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
- B29C44/04—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 consisting of at least two parts of chemically or physically different materials, e.g. having different densities
- B29C44/0484—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 consisting of at least two parts of chemically or physically different materials, e.g. having different densities by having different solubility of the foaming agent
-
- 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
- B29C44/3419—Quick 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
-
- 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
- C08J9/125—Water, e.g. hydrated salts
-
- 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
- C08J9/127—Mixtures of organic and inorganic blowing agents
-
- 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
- C08J2201/00—Foams characterised by the foaming process
- C08J2201/02—Foams characterised by the foaming process characterised by mechanical pre- or post-treatments
- C08J2201/03—Extrusion of the foamable blend
-
- 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
- C08J2203/12—Organic compounds only containing carbon, hydrogen and oxygen atoms, e.g. ketone or alcohol
-
- 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
- C08J2325/00—Characterised by the use of homopolymers or copolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by an aromatic carbocyclic ring; Derivatives of such polymers
- C08J2325/02—Homopolymers or copolymers of hydrocarbons
- C08J2325/04—Homopolymers or copolymers of styrene
- C08J2325/06—Polystyrene
Definitions
- the invention relates to a process and an installation for the production of foam polystyrene, as well as to the blocks and plates (such as sheets and panels) of foam obtained with them.
- GB-A-1 220 053 describes "a process for the production of foamed thermoplastic polymers wherein the pressure of a homogeneous pressurized mixture of the molten thermoplastic polymer and a system of foaming agents is relieved, said system comprising a first foaming agent that is completely miscible with the molten thermoplastic polymer at said pressure and which is a solvent of said thermoplastic polymer under the conditions of temperature and pressure of the homogeneous mixture and a second different foaming agent having a solubility of at least 0.01% by weight in the thermoplastic polymer and a critical temperature lower than the temperature of the mixture homogeneous at the point where said pressure is relieved, said first foaming agent having a lower boiling point at 10 or more ° C at said temperature of the mixture "(claim
- thermoplastic polymer under the pressure and temperature conditions of the pressurized vessel "(page 2, col. 1, lines 40-44), that" the substances most suitable for use as the first foaming agent are liquids whose boiling points at atmospheric pressure are higher than the ambient temperature "(page 2, col. 2, lines 69-72), which the" ethanof can
- CO 2 is usually less than 10% by weight (page 3, col. 1, lines 29-34) and suggesting that, in fact, the foaming caused by the first foaming agent (eg, ethanol), alone, it can result in a small number of very large bubbles or cells, to the detriment of the commercial value of the product (page 3, column 1, lines 10-14).
- first foaming agent eg, ethanol
- agents other than CO 2 will not be referred to as "foaming agents” in this description, but as "control agents” since, rather than used for foaming, they are used to allow the foaming produced basically by the foaming agent itself (CO 2 ) to be suitably produced.
- the inventors of the present have experimentally verified that ethanol acts as a solvent for polystyrene, thus decreasing the viscosity of the plasticized mixture, which allows working - for the same amount of CO 2 incorporated in the plasticized mixture - at lower pressures in The entire production line, including the final extrusion head.
- the decrease in viscosity also has the effect of reducing both the internal friction of the melt and its friction with the mechanical components with which it comes into contact and, as a result, decreasing the temperature of the plasticized mixture, which It is especially important near the matrix of the final extrusion head.
- the inventors of the present have also experimentally verified the beneficial effects of ethanol by absorbing heat from the molten mixture, at the time of foaming.
- the objective of the present invention is to overcome these drawbacks.
- the inventors have found that, when ethanol is used as a foaming control agent produced by CO 2 , the optimum characteristics of the foam are obtained if the ethanol is incorporated in a minimum and just enough quantity to give the plasticized mixture the viscosity necessary to absorb as much CO 2 as possible and to ensure that the foaming caused by ethanol is kept minimal.
- the inventors have also found that this decrease in the amount of ethanol used, by itself, would have the potential inconvenience of damaging the necessary decrease in temperature, since one of the effects of ethanol is to act as a coolant in the plasticized mixture.
- the inventors propose using a second control agent, added to the plasticized mixture after the addition of ethanol and consisting of H 2 O 2 .
- H 2 O 2 does not dissolve polystyrene or modify it, therefore, its characteristics mean that the physical properties of the foam are maintained or improved and that it can be obtained with greater thicknesses than with the use of ethanol alone, such as Foaming control agent produced by CO 2 .
- ethanol alone, such as Foaming control agent produced by CO 2 .
- the use of a much smaller amount of ethanol allows to reach more quickly the mentioned physical properties that are considered critical (dimensional stability, resistance and self-extinguishing capacity).
- the inventors have also found that the advantages of the invention are optimized if the polystyrene used to constitute the polymer mixture is a polystyrene of molecular weight less than about
- this low molecular weight polystyrene has the main objective of allowing the process to be carried out with a lower viscosity than conventionally found, which allows dissolving in the plasticized mixture a greater amount of CO 2 , reducing the amount of ethanol used and, mainly, keep the temperature rise inevitably caused by friction low.
- the invention provides, according to a first aspect, a process for the production of foam polystyrene, in which initial stage a mixture of polystyrene with conventional nucleating agents, plasticizers and additives is plasticized at a pressure Y at a temperature respectively above atmospheric pressure and at room temperature to form a "meit" plasticized mixture, which plasticized mixture decompresses and cools sharply at atmospheric pressure and at room temperature, when extruded through a final extrusion die , in which process a foaming agent intended to produce the desired foaming and constituted entirely of CO 2 , is injected into the plasticized mixture so that said foaming agent dissolves in the plasticized mixture, characterized in that a plasticized mixture is also injected into the plasticized mixture.
- the first control agent being destined to dissolve and refrigerate the plasticized mixture and being constituted by ethanol
- the second control agent is only intended to cool the plasticized mixture and is constituted by H 2 O 2
- the injected amount of ethanol being just enough p
- the maximum possible solution of CO 2 in the plasticized mixture and the injected amount of H 2 0 2 being such that the foaming caused by ethanol is kept minimal.
- the plasticized mixture to be extruded is constituted by 2.25-5% by weight of CO 2 , by 0.3-3.0% by weight of ethanol and by 0.2 -1.7% by weight of H 2 0 2 , the remainder being polystyrene and nucleating agents, plasticizers and conventional additives.
- the plasticized mixture to be extruded is constituted by 3.0-4.0% by weight of CO 2 , by 0.6-1, 25% by weight of ethanol and by 0 , 25-1% by weight of H 2 0 2 , the remainder being polystyrene and nucleating agents, plasticizers and conventional additives.
- the temperature and pressure profiles of the procedure are maintained with decreasing values of temperature, of the order of between 200 and 100 ° C and with decreasing pressure values of the order of between 20 and 7.6 MPa (200 bar and 76 bar, approx.), respectively, always maintaining CO 2 in supercritical conditions, up to The final extrusion.
- polystyrene has a molecular weight of less than about 150,000, a flow rate of approximately 20 g / 10 min (ISO 1133H) and a softening temperature VICAT VST B 50 (according to ISO 306 B 50) greater than 100 ° C.
- the invention provides an installation for carrying out the process defined above, which includes an extruder-plasticizer and a dynamic mixer arranged in series, the first of which has means to effect the initial plasticization of the mixture and the injection of the CO 2 and ethanol, and the second of which is provided with a cooling device and feeds the plasticized mixture to an extrusion head that carries the final extrusion die, existing, between the extruder-plasticizer and the dynamic mixer, about means for the injection of H 2 O 2 , in which installation, immediately after the extruder-plasticizer and immediately after the dynamic mixer, a first static mixer and a second static mixer are respectively interleaved, and the means for injection of H 2 O 2 are arranged between the extruder-plasticizer and the first mixture static clarifier
- the installation upstream of the extruder-plasticizer, the installation includes a first tank for the reception of CO 2 from an external source, the first tank being kept under conditions of pressure and temperature of the same order as those of the external source , a second CO 2 tank in which it is maintained at a pressure of about 7 MPa (70 bar, approx.) and at room temperature, and an injection pump to pump CO 2 from the second tank and inject it into the extruder-plasticizer and capable of raising the pressure of CO 2 from about 7 MPa (70 bar, approx.) to about 30 MPa (300 bar, approx.).
- the passage of CO 2 from the first tank and towards the second tank is carried out through another pump, downstream of which a heating device is provided that raises the temperature of the CO 2 leaving the other pump to approximately room temperature.
- the passage of CO 2 between the second tank and the injection pump passes through a cooling device that lowers the temperature of CO 2 to prevent overheating during the pumping operation.
- the injection pump is refrigerated.
- the injection pump is cooled by cooling its head.
- the procedure is carried out in an installation as defined in the immediately preceding paragraphs 15 and includes the steps of: a) initially plasticizing in the extruder-plasticizer a mixture of polystyrene with conventional nucleating agents, plasticizers and additives, being polystyrene of a molecular weight less than about 150,000, a flow rate of approximately 20 g / 10 min
- the invention provides foam blocks and plates produced using the procedure or installation indicated above, characterized in that, after 42 days of their production and after having been subjected to heating at 70 ° C for 2 days, they have suffered a decrease in each of its linear dimensions (length, width and thickness) of less than 5% with respect to the original dimension.
- the test to determine the self-extinguishing coefficient, carried out on those one hour after its extrusion gives a flame height less than 11 cm.
- FIG. 1 represents a very schematic view of an installation in which the procedure of the invention
- Fig. 2 represents a schematic view of the conditioning and feeding arrangement of CO 2 in the same installation.
- the installation includes an extruder-plasticizer 1 and a dynamic mixer 2, arranged in series or tandem.
- the extruder-plasticizer 1 receives the initial load of polystyrene and conventional nucleating agents, plasticizers and additives, as it is schematized by means of the feed hopper 3, which feeds said initial load or mixture in the extruder-plasticizer 1 that plasticizes it and homogenize to give a plasticized mixture (in fact, the plasticization and homogenization of the plasticized mixture continues throughout the installation until immediately before final extrusion).
- the general structure of the extruder-plasticizer 1 is that of a conventional plasticizing installation and is prepared to work at pressures above 20 MPa (200 bar, approx.) And at temperatures above 225 ° C.
- the extruder-plasticizer 1 is also provided with injection devices 4 and 5, respectively for C0 2 and ethanol, at temperatures close to the environment and pressures of the order of 20 MPa (200 bar, approx.)
- a device 6 for the injection of H 2 O 2 is provided , at a temperature close to the ambient and at a pressure greater than 20 MPa (200 bar, approx.).
- the dynamic mixer 2 is intended to leave the plasticized mixture in the optimal conditions for its extrusion and foam- - li ⁇
- the final extrusion head 8 and its matrix 7 are not part of the invention and should therefore be considered conventional, in the same way as the foam discharge conveyor 13.
- a first static mixer 15 and a second static mixer 16 are interleaved respectively, to reinforce the homogenization action of the extruder-plasticizer 1 and the dynamic mixer 2.
- a first tank 20 for receiving CO 2 from an external source 21 (the first being maintained tank 20 under conditions of pressure and temperature of the same order as those of the external source 21), a second CO 2 tank 22 that is maintained at a pressure of about 7 MPa (70 bar, approx.), and a pump 25 injection of CO 2, via device 4, into the kneader-extruder 1 and capable of raising the pressure of CO2 from about 7 MPa (about 70 bar.) to about 30 MPa (300 bar, approx. ).
- the passage of CO 2 from the first tank 20 and into the second tank 22 is carried out through another pump 23, downstream of which a heating device 24 is provided that raises the temperature of the CO 2 leaving the another pump 23 until about ambient.
- the passage of CO 2 between the second tank 22 and the injection pump 25 passes through a cooling device 26 that lowers the temperature of the CO 2 to avoid overheating during the CO 2 pumping operation towards the extruder-plasticizer 1, through the device 4.
- the injection pump 25 is cooled by passage of coolant through its head.
- Example 1 Effect of the use of low molecular weight polystyrene in foaming with CO 2 controlled only with ethanol
- polystyrene foam is produced by extrusion in the installation described above.
- the foam that is obtained at the exit of the lips of the matrix 7 with the final extrusion of the plasticized mixture has a width of 630 mm and a thickness of 60 mm.
- the mixture includes 0.4% talc to regulate cell size and 2.5% hexabromocyclododecane as a flame retardant.
- the foams of Tests 3 and 4 have an extrusion skin of better quality, more uniform over the entire surface and finer, without deterioration of the other technical characteristics.
- P 1 pressure in the extruder-plasticizer 1.
- P 2 pressure in the dynamic mixer 2.
- P 3 pressure in the final extrusion head 8.
- Temp. ref. Extrusion reference temperature, taken at the final extrusion head.
- Example 2 Effect of the use of [CO 2 + ethanol] and [CO 2 + ethanol + H 2 O 2 ] All Tests 7-13 indicated below were performed under the same conditions as those described in the first paragraph from the previous Example 1. The products tested have the thicknesses indicated in Table 2 below.
- Tests 7-10 A first series of tests (Tests 7-10 was performed using conventional polystyrene (Tests 7 and 8) and low molecular weight polystyrene (Tests 9 and 10), using only ethanol as a control agent.
- 3.5 pph (3.5 parts by weight per 100 parts by weight of polymer mixture) of the foaming agent, CO 2 is injected between 1 and 1, 1 pph of ethanol and between 0 , 4 and 0.45 pph of H 2 O 2 .
- the exempted polystyrene foam that is obtained according to Tests 11-13 has a uniform and good quality extrusion skin, with a percentage of closed cells greater than 95%.
- the self-extinguishing coefficient of the foam thus obtained is much better than in the samples obtained using only ethanol as a control agent (Assays 7-10), as shown in the following Table 2. Likewise, they have a better dimensional stability when the foam is subjected to high temperatures.
- Quantity and dimensions of the samples From the plate to be tested, 4 specimens were cut to the dimensions of 90 mm x 190 mm. The thickness of the specimen is that of the original plate up to 60 mm. Plates thicker than 60 mm are cut to 60 mm thick.
- Test procedure The sample is placed on a support. A burner is used and the height of its flame is adjusted to 20 mm, the burner moving horizontally until the flame is at a distance of 15 mm from the rear face of the specimen. After 15 seconds, the burner is removed. Then, the maximum height that the flame reaches (on the back of the specimen) is measured and the time it takes for the flame to extinguish, both before and after the burner has been removed.
- a mixture of low molecular weight polystyrene and additives is fed into the installation as in the previous Example 2 (Tests 11-13).
- the amount of H 2 O 2 is progressively increased. As soon as this amount reaches 3 pph the process begins to destabilize.
- the pressure in the extruder-plasticizer 1 begins to oscillate widely, between 10 and 15 MPa (100 and 150 bar, approx.). It follows that the current of the dynamic mixer motor 2 also oscillates. These variations indicate that the plasticized mixture is not homogeneous because they are not being incorporated correctly. The foaming and control agents in the plasticized mixture.
- the amount of H 2 O 2 is reduced to 2.5 pph and the process gradually stabilizes.
- a mixture of low molecular weight polystyrene and additives is fed into the installation, as in the previous Example 3.
- 3.5 pph of foaming agent, CO 2 , and 4.5 pph of control agent are injected into the initially plasticized mixture , constituted by ethanol.
- Said plasticized mixture is extruded through the lips of the final extrusion die, obtaining a 630 mm foam.
- the thickness of said foam at the exit of the gauge is 51 mm on average, measured with a king's foot at 3 points along its width.
- the thickness is re-measured over the entire width of the plate, giving an average value of 47 mm on average.
- the thickness has decreased 4 mm.
- the amount of ethanol is increased to 7 pph and that of CO 2 is decreased to 2.5 pph.
- the thickness is measured again at the outlet of the gauge and when the foam reaches the blade. Under these conditions, the thickness has already decreased 9 mm.
- the experiment is continued, stopping the foaming agent CO 2 and injecting only ethanol, at 9 pph. After 30 min a change in the foam structure is observed. At a glance you see that the size of the cells is much larger than in all the tests previously performed.
- the thickness of the plate has increased to 55 mm at the outlet of the gauge. However, upon reaching the blade (time elapsed 15 min) the plate has a thickness of 26 mm on average. Thus, the thickness has been reduced 29 mm.
- the walls tend to collapse.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Mechanical Engineering (AREA)
- Inorganic Chemistry (AREA)
- Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
- Extrusion Moulding Of Plastics Or The Like (AREA)
- Laminated Bodies (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002347267A CA2347267C (en) | 1999-01-20 | 2000-01-05 | Process and apparatus for producing foam |
US09/807,914 US6572800B1 (en) | 1999-01-20 | 2000-01-05 | Process and apparatus for producing foam |
AU18663/00A AU1866300A (en) | 1999-01-20 | 2000-01-05 | Process and apparatus for producing foam and foam blocks and boards produced |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ES9900099 | 1999-01-20 | ||
ESP9900099 | 1999-01-20 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000043444A1 true WO2000043444A1 (es) | 2000-07-27 |
Family
ID=8306970
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/ES2000/000002 WO2000043444A1 (es) | 1999-01-20 | 2000-01-05 | Procedimiento e instalacion para producir espuma, y bloques y placas de espuma producidos |
Country Status (10)
Country | Link |
---|---|
US (1) | US6572800B1 (es) |
EP (1) | EP1022303B1 (es) |
AT (1) | ATE201032T1 (es) |
AU (1) | AU1866300A (es) |
CA (1) | CA2347267C (es) |
DE (1) | DE69900101T2 (es) |
ES (1) | ES2156458T3 (es) |
GR (1) | GR3036228T3 (es) |
PT (1) | PT1022303E (es) |
WO (1) | WO2000043444A1 (es) |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030225172A1 (en) * | 2002-05-31 | 2003-12-04 | Miller Larry M. | To enhance the thermal insulation of polymeric foam by reducing cell anisotropic ratio and the method for production thereof |
DK1493681T3 (da) * | 2003-07-04 | 2007-04-02 | Anton Volpini De Maestri Verpa | Fremgangsmåde og indretning til fremstilling af syntetiske flaskelukninger |
DE102005020794A1 (de) * | 2005-05-04 | 2006-11-09 | Coperion Werner & Pfleiderer Gmbh & Co. Kg | Anlage zur Erzeugung einer Schaumkunststoff-Folie |
US8119701B2 (en) * | 2005-10-24 | 2012-02-21 | Owens Corning Intellectual Capital, Llc | Method of manufacturing polystyrene foam with polymer processing additives |
US20070173554A1 (en) * | 2005-10-27 | 2007-07-26 | Yadollah Delaviz | Method of manufacturing polystyrene foam with polymer processing additives |
US7624910B2 (en) | 2006-04-17 | 2009-12-01 | Lockheed Martin Corporation | Perforated composites for joining of metallic and composite materials |
DE102007008749A1 (de) | 2007-02-22 | 2008-08-28 | Ursa Insulation, S.A.- Grupo Uralita | Kunststoffe, enthaltend Metallpulver, bestehend aus Sn oder einer Sn-Legierung |
EP2291440A1 (en) * | 2008-06-04 | 2011-03-09 | Owens Corning Intellectual Capital, LLC | Extruded polystyrene foam containing propylene carbonate, ethylene carbonate or butylene carbonate as a process aids |
IT1397297B1 (it) * | 2009-11-25 | 2013-01-04 | Polymtec Trading Ag Ora Polymtec Engineering Ag | Articolo a base di polistirolo estruso, procedimento ed impianto per ottenere tale articolo |
US20110306689A1 (en) * | 2010-06-09 | 2011-12-15 | Fina Technology, Inc. | Expandable Polystyrene and Methods of Forming the Same |
CN101921404A (zh) * | 2010-08-13 | 2010-12-22 | 刘志辉 | Co2塑料发泡剂制备方法及co2塑料发泡剂注入系统 |
CN102514173B (zh) * | 2011-12-07 | 2014-05-21 | 浙江大学 | 动态微通道塑料挤出成型装置及方法 |
CN113910524B (zh) * | 2021-10-14 | 2023-01-24 | 宿迁嘉禾塑料金属制品有限公司 | 一种拖把用聚乙烯醇超临界发泡工艺及智能化生产线 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4436679A (en) * | 1981-11-09 | 1984-03-13 | Maryland Cup Corporation | Method and apparatus for generating foamed thermoplastic materials |
EP0464581A2 (de) * | 1990-07-04 | 1992-01-08 | BASF Aktiengesellschaft | Verfahren zur Herstellung von Schaumstoffplatten mit hoher Druckfestigkeit |
EP0528536A1 (en) * | 1991-07-24 | 1993-02-24 | Mobil Oil Corporation | High melt index polystyrene foam and method |
US5244927A (en) * | 1992-06-09 | 1993-09-14 | The Dow Chemical Company | Low density styrene polymer foams and process for preparing same |
Family Cites Families (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB1220053A (en) | 1967-01-23 | 1971-01-20 | Ici Ltd | Foamed thermoplastic polymers |
GB1230992A (es) | 1967-08-04 | 1971-05-05 | ||
US4211739A (en) * | 1978-07-10 | 1980-07-08 | Condec Corporation | Foam extrusion apparatus and method |
DE3741095A1 (de) | 1987-12-04 | 1989-06-15 | Basf Ag | Verfahren zur herstellung von schaumstoffen mit hoher druckfestigkeit |
US5250577A (en) | 1989-08-02 | 1993-10-05 | The Dow Chemical Company | Polystyrene foam made with only carbon dioxide as a blowing agent and a process for making the same |
DE3943265C2 (de) | 1989-12-29 | 1996-08-01 | Gefinex Jackon Gmbh | Verfahren zur Herstellung von Kunststoffschaum |
US5082608A (en) * | 1990-06-14 | 1992-01-21 | Owens-Illinois Plastic Products Inc. | Polystyrene foam sheet manufacture |
US5158986A (en) | 1991-04-05 | 1992-10-27 | Massachusetts Institute Of Technology | Microcellular thermoplastic foamed with supercritical fluid |
US5340844A (en) | 1992-04-24 | 1994-08-23 | The Dow Chemical Company | Polystyrene foam and a process for making the same |
AT398771B (de) | 1992-11-13 | 1995-01-25 | Union Ind Compr Gase Gmbh | Verfahren zur herstellung aufgeschäumter kunststoffe |
US5269987A (en) | 1992-12-22 | 1993-12-14 | Reedy Michael E | Process for producing alkenyl aromatic foams using a combination of atmospheric and organic gases and foams produced thereby |
US6113374A (en) * | 1996-08-14 | 2000-09-05 | Owens Corning Fiberglass Technology, Inc. | Foam extrusion apparatus |
US6174471B1 (en) * | 1999-03-15 | 2001-01-16 | The Dow Chemical Company | Open-cell foam and method of making |
-
1999
- 1999-11-12 PT PT80200642T patent/PT1022303E/pt unknown
- 1999-11-12 EP EP99203785A patent/EP1022303B1/en not_active Expired - Lifetime
- 1999-11-12 DE DE69900101T patent/DE69900101T2/de not_active Expired - Lifetime
- 1999-11-12 ES ES99203785T patent/ES2156458T3/es not_active Expired - Lifetime
- 1999-11-12 AT AT99203785T patent/ATE201032T1/de active
-
2000
- 2000-01-05 WO PCT/ES2000/000002 patent/WO2000043444A1/es active Application Filing
- 2000-01-05 CA CA002347267A patent/CA2347267C/en not_active Expired - Fee Related
- 2000-01-05 AU AU18663/00A patent/AU1866300A/en not_active Abandoned
- 2000-01-05 US US09/807,914 patent/US6572800B1/en not_active Expired - Fee Related
-
2001
- 2001-07-13 GR GR20010401080T patent/GR3036228T3/el unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4436679A (en) * | 1981-11-09 | 1984-03-13 | Maryland Cup Corporation | Method and apparatus for generating foamed thermoplastic materials |
EP0464581A2 (de) * | 1990-07-04 | 1992-01-08 | BASF Aktiengesellschaft | Verfahren zur Herstellung von Schaumstoffplatten mit hoher Druckfestigkeit |
EP0528536A1 (en) * | 1991-07-24 | 1993-02-24 | Mobil Oil Corporation | High melt index polystyrene foam and method |
US5244927A (en) * | 1992-06-09 | 1993-09-14 | The Dow Chemical Company | Low density styrene polymer foams and process for preparing same |
Also Published As
Publication number | Publication date |
---|---|
GR3036228T3 (en) | 2001-10-31 |
PT1022303E (pt) | 2001-10-30 |
CA2347267A1 (en) | 2000-07-27 |
DE69900101D1 (de) | 2001-06-13 |
EP1022303B1 (en) | 2001-05-09 |
AU1866300A (en) | 2000-08-07 |
US6572800B1 (en) | 2003-06-03 |
ATE201032T1 (de) | 2001-05-15 |
EP1022303A1 (en) | 2000-07-26 |
DE69900101T2 (de) | 2001-09-06 |
CA2347267C (en) | 2007-07-17 |
ES2156458T3 (es) | 2001-06-16 |
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