Continuous method for producing solid, hollow or open profiles

Abstract

Disclosed herein is a method for producing a polystyrene foam. The polystyrene is dosed with a gas and the polystyrene and gas are mixed in an extruder in order to obtain a homogenous mixture. The homogeneous mixture is cooled as it travels through the extruder and is then extruded from the die at a pressure of less than 7 MPa to form a foam with a smooth skin.

Claims

1. A method for producing solid, hollow or open profiles, based on polystyrene, comprising: dosing polymers comprising polystyrene, plasticizing the components in an extruder in order to obtain a homogenous mixture, injecting a pressurized gas via an injection port in an amount from 0.2 to 0.4% by weight based on the polymers comprising polystyrene, kneading and pressurizing said homogeneous mixture and gas until complete dissolution of the gas in order to obtain a mixture in a single phase, gradually cooling said mixture while maintaining the pressure required for solubilizing the gas, to a temperature above 135 C., having said mixture in a single phase, pass from a die into ambient conditions to form a foam, where the mixture passes onto the die at a rate of 50 to 120 kilograms of polystyrene per hour; and where the pressure at the shaping tool is 3 MPa to 7 MPa; and drawing the foam with a motor to produce a calibrated foam having a density of 290 to 350 kilograms per cubic meter and having a cell size of 25 to 100 micrometers.

2. The method according to claim 1, wherein the gradual cooling is controlled so as to provide a homogeneous temperature profile in a cross-section perpendicular to the flow, until the optimum foaming temperature is obtained.

3. The method according to claim 1, wherein the polymer is selected from the group consisting of polystyrene, acrylonitrile-butadiene-styrene (ABS), styrene-butadiene-styrene (SBS), styrene-ethylene-butadiene-styrene (SEBS) and mixtures thereof.

4. The method according to claim 1, wherein several kinds of polystyrenes which differ in viscosity, are used either alone or mixed with other copolymers of styrene and a diene monomer.

5. The method according to claim 1, wherein a portion or the whole of the surface of the profile is altered by adding by co-extrusion an additional layer of material thereto.

6. The method according to claim 5, wherein the co extruded material is in the foamed or compact state.

7. The method according to claim 1, wherein the gas used is CO2.

8. The method according to claim 1, wherein compounds facilitating extrusion of the polystyrene mixture, selected from the group consisting of esters of C4-C20 mono-alcohols, fatty acid amides, polyethylene waxes, oxidized polyethylene waxes, styrene waxes, C1-C4 alcohols, siliconized compounds and mixtures thereof, are added.

9. The method according to claim 8, wherein the compounds facilitating extrusion of the polystyrene mixture are injected with regularity and accuracy at a suitable location of the shaping tool via a distributor ring, in order to exclusively and regularly line the flow channel of the die.

10. The method according to claim 1, wherein the dosing comprises adding additives and adjuvants to the polymers.

11. The method according to claim 1, wherein the calibrated foam is produced by a calibration system; wherein the calibration system is temperature-controlled.

12. A method for producing solid, hollow or open profiles, the method comprising: dosing a polymer including polystyrene; plasticizing the polymer including the polystyrene in an extruder to obtain a homogenous mixture; injecting a pressurized gas into the extruder in an amount from 0.2 to 0.4% by weight of the homogenous mixture; kneading and pressurizing said homogeneous mixture and gas until dissolution of the gas to obtain a mixture in a single phase; cooling the mixture to a temperature in excess of 135 C. while maintaining the pressure required for solubilizing the gas; passing the mixture from a die at a rate of 50 to 120 kilograms of polystyrene per hour; to form a foam; where the foaming occurs outside the die and where the pressure at the die is 3 MPa to 7 MPa pounds per square inch; and drawing the foam with a motor to produce a calibrated foam having a density of 290 to 350 kilograms per cubic meter and having a cell size of 25 to 100 micrometers.

Description

BRIEF DESCRIPTION OF THE FIGURES

(1) The FIGURE is a depiction of an extruder with the barrel temperatures and pressures.

DETAILED DESCRIPTION OF THE INVENTION

(2) Other particularities and features of the invention will become apparent from the detailed description of a few advantageous embodiments presented hereinbelow, as an illustration.

1. Manufacturing Method

(3) 1.1. Dosage of the Components:

(4) The components of the formulation are individually dosed by a volumetric or gravimetric type dosage station, in order to specifically achieve the desired composition. The raw materials preferably are in the form of regular granules, if possible with the same size and the same shape from one component to the other. It will also be preferred that the apparent density be in a narrow range between the different components, in order not to cause premature demixtion.

(5) 1.2. Extruder:

(6) The thereby dosed components are conveyed towards the feeder of a plasticizing extruder. This extruder preferably includes two co-rotary or counter-rotary screws, either self-cleaning or not. The screw used involves the use of a diamond mixer also known as pinapple mixer. Indeed, this screw design facilitates homogenization of the polymer with the gas and other additives that are added to the extruder. The cylinder includes several heating zones. An exemplary extruder that includes the heating zones along with the relevant pressures and temperatures is shown in the FIGURE. The range of pressure within the extruder is comprised from 2.5 megaPascals (MPa) to 10 MPa. The range of pressure within the extruder is comprised from 2.5 MPa to 10 MPa, the range of pressure within the heat exchanger inlet is from 5 MPa to 15 MPa and the range of die pressure is from 3 MPa to 7 MPa. The temperature within the extruder zones is from 170 C. to 260 C. in order to plasticize the solid components dosed at the feeder, while kneading them to homogenize the whole. At the most favorable location from the viscosity and pressure point of view, in the cylinder, pressurized gas is injected via an injection port bored into the cylinder. The gas injection occurs within the extruder between barrels two and three. The pressure of the gas at the point of entry is from 2.5 MPa to 10 MPa. The gas will be maintained in its condensed phase, in particular, in the supercritical state in the case of CO.sub.2 (see point 2.2). The mixture of the components and the gas is kneaded and pressurized in order to obtain good homogeneity and optimum dissolution of the gas in the molten mixture so as to obtain a single phase. The cylinder zones are then gradually colder in order to maintain the pressure required for solubilizing the gas.

(7) 1.3. Cooling:

(8) It may be achieved by two arrangements: i) A dynamic heat exchanger by using a configuration with long screws: as the first portion of the cylinder has been used for plasticizing and homogenizing solid components with the gas as described in the previous point b), the second portion of the screw, the zones of which are cooled by the flow of a coolant fluid, provides the cooling of the monophase mixture. The design of the screw of the latter portion is specifically adapted to generate the least possible heat by shearing, which increases the potential cooling capacity and therefore benefits productivity. The design of the cooling section of the screw will be adapted so as to achieve at the inlet of the die the optimum temperature, with the homogeneity of which in a cross-section perpendicular to the flow, it is possible to obtain the advantageous claimed combination of density and cell size. ii) A static heat exchanger: the homogeneous mixture of the plasticized components+the gas leaves the cylinder of the extruder so as to pass through a heat exchanger, through which a coolant fluid flows, the design of which should provide control over the mixing temperature to within a tenth of a degree, so that the optimum foaming temperature at the die may be obtained with the desired accuracy and graduality. The exchanger should further be designed in order to smooth out the temperature profile in a cross-section perpendicular to the flow, in order to make the temperature profile at the exit of this exchanger, as flat as possible. By adding a static exchanger after the cylinder of the extruder, it is further possible to increase the permissible flow rate.

(9) 1.4. Homogenization:

(10) The cooled mixture is optionally again homogenized, by having it pass into a static mixer which will divide the flux into several channels which will be crossed and redistributed, in order to make the temperature profile of a perpendicular section of the flux as flat as possible.

(11) 1.5. Relaxation:

(12) A section for relaxation of the flux may optionally be added, by placing an empty tube over a suitable distance. This allows the internal stresses due to shearing, as well as visco-elastic memory effects to be released and to provide a more regular flow of the flux.

(13) 1.6. Foaming Die:

(14) The monophase mixture, homogeneous in composition and in temperature, of the plasticized components and the gas will now pass into the shaping tool, consisting of a die guiding the flux towards the intended foaming shape. The pressure drop undergone by the mixture from the outlet of the cylinder constantly reduces the pressure of the mixture; at one moment, this pressure drops below the critical threshold where the previously solubilized gas will oversaturate the mixture and gas bubbles will then originate, forming a second discrete phase. Ideally, the zone where these primary bubbles form should not be passed too early, otherwise pre-foaming may occur giving a deformed and unstable foam with a not very attractive surface. In one exemplary embodiment, the foaming occurs after the homogeneous mixture has been expelled from the die. In an exemplary embodiment, the die temperature ranges from 150 to 170 C., specifically about 153 to 165 C.

(15) The die pressure ranges from 3 MPa to 7 MPa, specifically 3 MPa to 6 MPa, and more specifically 3 MPa to 5 MPa.

(16) The measures of actions on the location where this critical demixing step occurs, are multiple: viscosity of the components, temperature of the tool, proportion of gas, shape of the tool, throughput of the extruder . . . all these parameters should be optimized for each foam profile to be achieved.

(17) 1.7. Shaping:

(18) The foam emerges into the atmosphere, at a high temperature, and freely expands. The viscosity of the cell walls increases with cooling, and migration of the gas into the cells, until the cell structure is set. But this process takes time, and the shape of the foam is not immediately stable. In order to control the dimensions of the foam, it is passed through a calibration system, by drawing it by a motor at the end of the extrusion line. The calibrators, possibly temperature-controlled calibrators for more efficient control of the shape, especially at the beginning when the foam is the hottest, gradually impose to the foamed mass, its definitive shape.

(19) 1.8. In-Line Co-Extrusion (Optional):

(20) It is possible to alter a portion or all the surface of the solidified primary foam profile by adding by co-extrusion an additional layer of material thereto. This secondary layer, which should compatible with the first in order to provide good cohesion, may have the function of reinforcing the mechanical properties, a decorative effect, the secondary layer may be compact or foamed.

(21) 1.9. In-Line Ornamentation (Optional):

(22) It is possible to print decorative patterns on a selected portion of the profile, for example via a heating roll pressed against the locally preheated foam, or by a press system advancing with the profile, or any other method known to one skilled in the art.

(23) 1.10. Drawing and Cutting Operation:

(24) The foam is therefore drawn by a simple or dual powered drawing machine according to the number of profiles extruded in parallel. The profile is then cut to length by a saw, providing a really perpendicular cut.

(25) 1.11. Off-Line Ornamentation (Optional):

(26) It is possible to print decorative patterns on a selected portion of the cut-out profile, for example via a heating roll pressed against the locally preheated foam, or by a press system advancing with the profile, or any other method to one skilled in the art.

2. Raw Materials

(27) 2.1. Polymers:

(28) Polystyrene is used as a base resin. The viscosity of the polystyrene will be adapted according to the foam profile, to the pressure required for obtaining good quality, to the desirable extrusion throughput. Several kinds of polystyrenes, differing in viscosity and therefore in molecular weight, with flow indexes (Melt Flow Rate MFR), from 1 to 25 g/10 minutes, according to ASTM D1238, measured at 200 C. and with a load of 5.0 kg, may be used alone or as a mixture. Copolymers of styrene and a diene monomer, which have a better impact strength and better elasticity, may also be added. For example: suitable acrylonitrile-butadiene-styrene (ABS), styrene-butadiene-styrene (SBS), styrene-ethylene-butadiene-styrene (SEBS), also having variable flow indexes (Melt Flow Rate MFR), according to the foam to be obtained.

(29) Recycled material, compatible with all the components, for example scraps of foamed profiles, milled, degassed, and densified beforehand may also be added.

(30) In the case of a co-extruded layer on the base foam, the materials are selected according to whether they are able to form a sufficiently cohesive bond with the base foam. These may be thermoplastics, thermosetting materials.

(31) 2.2. Gas:

(32) The gas used is preferably CO.sub.2, stored in a pressurized tank and at a temperature such that it is in the liquid state. By no means should 31.1 C. be exceeded, beyond this temperature, CO.sub.2 becomes supercritical and therefore has a significantly lower density than the liquid, which makes its pumping delicate. The CO.sub.2 is pumped in conduits cooled to significantly below the critical temperature, in order to maintain the liquid state up to the device for controlling the injection flow rate. This is a flowmeter operating according to the Coriolis effect, which allows the mass of the dosed gas per unit time to be linked to a difference in vibration velocity induced by the passage of the fluid in a vibrating conduit. As this flowmeter only works for liquids, it is therefore essential that the CO.sub.2 remains in this state. The liquid CO.sub.2 is then brought into the cylinder of the extruder via in injection port provided with a non-return valve.

(33) 2.3. Additives:

(34) a. Nucleating Agent: The cells of the foam are regularized by using a compound which will promote homogeneous distribution of the cells in the foam. These may be passive products, which do not react chemically, such as talc, calcium carbonate, silica, . . . . So-called active products may also be used which will decompose under the action of heat by giving off a gas phase. The reaction promotes homogeneous nucleation, as well as the presence of domains of finely divided gas. The combinations of citric acid and sodium bicarbonate, azodicarbonamide, and OBSH are well known.

(35) b. Additives Assisting the Process: These are compounds facilitating extrusion of the polystyrene mixture, by an internal or external lubrication effect. This is generally a molecule having a low molecular weight. Among the known products, let us mention esters of C4-C20 mono-alcohols, fatty acid amides, polyethylene waxes, oxidized polyethylene waxes, styrene waxes, C1-04 alcohols, siliconized compounds, etc. These compounds may either be added to the mixture as soon as it enters the extruder, either as a master polystyrene-based mixture, or injected as a liquid into the extruder, or even injected with regularity and accuracy at the suitable location of the extrusion tool via a distributor ring, in order to exclusively and regularly line the flow channel of the die so as to form a film with a very low friction coefficient.

(36) c. Pigments: The foam mass may be uniformly colored by using pigments added to the feeder of the extruder. It is also possible to obtain a wood effect by using associations of color pigments with very different viscosities, for example combining a bright colored master mixture based on a high viscosity polymer with a dark colored master mixture based on a low viscosity polymer.

(37) d. Other Additives: Let us further mention unexhaustively: Fire retardants, either halogenated [chlorinated, brominated, fluorinated, . . . ] or not [hydroxides, phosphates, expansible graphite, . . . ]; UV stabilizers; Antioxidants; Various mineral fillers; Strengthening fibers (glass, cellulose, . . . ) Additives acting on the melt viscosity (high molecular weight acrylic copolymers)

3. Exemplary Embodiments

(38) The following examples illustrate the conditions for obtaining the representative foams of the invention and their morphological aspects. The key extrusion parameters, the dimension of the profiles and the extracted amount of heat during cooling, are grouped in a table.

(39) The polymer used is a crystalline polystyrene, MFI=15. A nucleating agent of the citric acid+sodium bicarbonate type was added in order to control the size of the cells. The foaming gas is 100% CO.sub.2.

(40) When a heat exchanger is used (Examples Nos. 1 to 5), the extracted amount of heat is calculated in order to reach the optimum die temperature. In the absence of an exchanger (Example No. 6), with no access to the temperature of the mass in the cylinder before the cooling section, it is not possible to evaluate this amount of heat. However, the optimum extrusion temperature is indicated.

(41) TABLE-US-00001 Example No. 1 2 3 4 5 6 Dimensions W I mm mm 120 * 15 40 * 20 38 * 16 150 * 17 19 * 12 40 * 20 Current dm.sup.3/m 1.26 0.42 0.39 2.23 0.2 0.42 volume/meter Density kg/m.sup.3 344 311 295 343.6 308.2 297 Exchanger? YES YES YES YES YES NO PS mass flow rate kg PS/h 120 90 80 130 50 80 CO.sub.2 mass flow rate g CO.sub.2/min 4.8 4.6 4.1 5 2.9 4.3 CO.sub.2 concentration weight % 0.2 0.3 0.3 0.2 0.4 0.3 Exchanger inlet T C. 192 189 188 193 184 Die T C. 154.8 157.4 163.5 156.9 161.6 159.5 DELTA T 37.2 31.6 24.5 36.1 22.4 Cooling power kJ/h 8225.87 5242.82 3613.21 8647.36 2065.20

(42) It is seen that the amounts of heat are logical according to the densities, dimensions and extrusion rates. Examples 2 and 3 however illustrate that the optimum extrusion temperatures at the die also are a function of the complexity of the shapes: in spite of their similar volumes, the shape of Example 3 is much more tortuous than that of Example 2, increasing frictions, but the method in each case is sufficiently adaptive and flexible so that foams with a regular and fine cell structure may be obtained.

(43) The foam emanating from the die has a smooth skin. The smooth skin is indicative of the fact that foaming takes place outside of the die. If the foaming took place in the die, then the pores at the surface would rupture because of contact between the die surface and the foam. This would lead to the formation of a rough foam surface.