Patent Application
20210189084
The present disclosure relates to an expandable vinyl aromatic polymer composition with improved mechanical and thermal insulation properties, the production process for its preparation it, as well as the manufactured articles that can be obtained from such composition.
The present disclosure relates to an expandable vinyl aromatic polymer composition with improved mechanical and insulating properties which includes:
The compositions give high impact absorption strength, such as a “cushioning” effect, flexibility, excellent compression properties and softness to the touch, as well as good thermal insulation features, to the end manufactured articles containing them.
The main field of application of the compositions described and claimed is as flexible packaging material in both the food and industrial sectors, where a sense of softness to the touch, cushioning properties on impact and thermal insulation are required.
A balance between mechanical properties (flexibility), insulating capability, pleasantness (softness) to the touch and high degree of sintering that open up new market segments from which standard expandable polystyrene (EPS) is currently excluded is achieved with the composition according to this disclosure.
In the present patent application, all the operating conditions included in the text are to be considered to be preferred conditions, even if not expressly stated.
For the purposes of this description the term “comprises” or “includes” also comprises the term “consists of” or “essentially consists of”.
For the purposes of this description, descriptions of ranges will always include the end members unless otherwise specified.
Expandable polymers are generally produced in the form of pearls or granules, which as a result of the action of heat, provided for example by steam, are first expanded to the desired density and then, after a particular ageing time, are sintered in closed moulds to produce blocks or the desired end products.
Expandable beads can be obtained by a process of batch polymerization in an aqueous suspension. This process, well known to those skilled in the art, includes the following stages:
A good quality product can be obtained through this suspension process, but it has several drawbacks, such as:
In the state of the art suitable compositions for forming packaging are prepared using very expensive processes—aqueous suspension or granulation followed by post-impregnation in aqueous suspension.
The aqueous suspension process produces batches of granules with a particular average diameter size ranging from the smallest fractions (0.1-0.3 mm) to the coarsest fractions (over 2 mm). Smaller fractions are used in the lost foam and moulding industries for both food and industrial packaging. Coarse fractions are used for thermal insulation. For flexible packaging, the application for products containing the compositions to which this patent application relates, only the fractions with weighted mean diameters between 0.4-0.6 mm, 0.6-0.9 mm, 0.9-1.2 mm and 1.2-1.6 mm are used, depending on the type of product.
The aqueous suspension process produces large quantities of unwanted fractions, even when sophisticated technologies such as the use of Na sulfate and other additives are used to reduce particle size distribution. Fractions smaller or larger than the 0.4 to 1.6 mm fraction, inevitably produced with the suspension, cannot be used.
Granulation followed by post-impregnation is also expensive as penetration of the expansion agent into the center of the granule requires long impregnation cycles in the reactor. With the latter technology only the desired fraction of granules is prepared, but two plants are needed: a polymerization and granulation plant and a post-impregnation plant. This latter system is very similar to the suspension system, with the difference that granules instead of drops of styrene monomer are suspended. Impregnation with the expansion agent is therefore much more expensive because we already have a polymer granule that must be softened above the softening temperature or Tg (glass transition temperature), then made spherical and then impregnated. This stage is very critical because if the expansion agent does not reach the center of the granule the final foam will have a center which has expanded little or is sometimes still compact. The presence of this poorly expanded center causes the wires for cutting blocks to break, with consequent shutdown of the processing plant.
The Tg of a polymer material is defined as the temperature at which the second order transition between the solid and liquid state of a polymer composition occurs, as for example described in “Principles and applications of Thermal Analysis” by Paul Gabbott, Blackwell Publishing Ltd., 2008.
U.S. Pat. No. 6,232,358 (published in 1999) discloses a styrene resin composition modified with rubber that is capable of providing a foam with a high expansion ratio, excellent impact resistance and flexibility and satisfactory appearance. As a method of preparation the document provides the example of granulation followed by post-impregnation, but the process is expensive because the styrene resin is first prepared, then extruded, then the granules are suspended in water and impregnated for 5 hours.
Penetration of the expansion agent to the center of the granule requires long impregnation cycles (5 hours) in the reactor. With this latter technology only the desired fraction is prepared, but two plants are required—the polymerization/granulation and the post-impregnation plants. Impregnation with expansion agent is therefore much more expensive because polymer granules which must be softened at a temperature higher than the Tg, then made spherical and then impregnated, are already available. This stage is very critical because if the expansion agent does not reach the center of the granules, the final expanded material will have a center that has expanded little or is sometimes still compact.
The presence of this poorly expanded center causes the wires for cutting blocks to break, with consequent shutdown of the processing plant.
Another example of the same method of preparation is document EP 0722974 (published in 1996) which discloses expanded styrene beads modified with rubber, and articles of styrene resin modified with rubber.
A further example is document EP 1266929 (published in 2012) which discloses expandable polystyrene resin particles that are particles of expandable polystyrene resin (d) including modified polystyrene resin particles (c) containing an expansion agent (e), modified polystyrene resin particles (c) comprising a polystyrene resin and rubber polymer particles (b) dispersed in the resin, in which the rubber polymer particles (b) are uniformly dispersed in a continuous phase of the polystyrene resin or in a state in which the particle density (b) is higher in a central portion of the resin particle than in a portion of its surface layer, and the modified polystyrene resin particles (c) are modified polystyrene resin particles prepared by impregnating a mixture of monomers essentially comprising a styrene monomer and a conjugated diene monomer, and comprising the styrene monomer in a greater quantity than the conjugated diene monomer in the polystyrene resin particles (a), and the performance of copolymerization.
Another example is document DE 19710442 (published in 1998) which describes an expandable styrene polymer (I) containing:
By contrast, U.S. Pat. No. 5,166,221 (EP 0425973 published in 1991) discloses expandable styrene polymers containing 10 to 90% by weight of a styrene-diene star-block copolymer containing 2 to 45% by weight of diene and 1 to 10% by weight of a C3-C6 hydrocarbon as an expansion agent can be processed to provide foams that have high resistance to aromatics. The document provides as an example a method of preparation that comprises polymerization in aqueous suspension, but large amounts of unwanted fractions are produced with this technology, even though sophisticated technologies are used to reduce the distribution (e.g. the use of Na sulfate and other additives). The smaller or larger fractions inevitably produced with the suspension cannot be used.
Another example of polymerization in aqueous suspension is EP 0872513 (published in 1998) which describes a styrene polymer expandably modified with rubber (I) including:
By contrast WO 1994/025516 (published in 1994) describes expanded particles for a styrene polymer modified with rubber comprising a plurality of closed cells defined by cell walls that form a matrix for the particles, in which each of the cell walls comprises two surfaces separated by a distance equal to the thickness of the cell wall. The method of preparation comprises extrusion with granulation in water.
One example of the same method of preparation is U.S. Pat. No. 3,558,534 (published in 1971) which describes expandable aromatic alkenyl polymers that do not acquire or retain a static charge and are prepared by incorporating a small amount of a rubbery polymer into the expandable polymer.
A further example is JP 2004115690 (published in 2004) which describes a method for manufacturing a good quality expandable particle that does not contain foam through using a styrene-type resin, in particular a recycled styrene-type resin product.
The technology of continuous bulk preparation (e.g. EP 1541621, published in 2005) according to the following steps is also known:
The object of the present disclosure is to prepare a vinyl aromatic polymer composition suitable for the preparation of flexible packaging.
In a preferred aspect of the present disclosure it is possible to prepare these compositions in a single stage using continuous bulk processing technology.
Thus the object of the present disclosure is an expandable vinyl aromatic polymer composition with improved mechanical and insulating properties comprising:
The term “comprising” and its derivatives is not intended to exclude the presence of any additional components, stages or procedures, whether or not they are disclosed in this text. To avoid any doubt, all compositions claimed in this text through the use of the term “comprising” may include any additive, coadjuvant or other additional compounds, of the polymer or other type, unless indicated otherwise.
Further objects and advantages of the present disclosure will be more clearly apparent from the following description, provided purely by way of example and not limited thereto, which illustrates preferred embodiments of the present disclosure.
The property of cushioning a package expresses its ability to absorb energy following an impact. Performance is expressed in terms of an “impact factor” (maximum deceleration expressed in multiples of the acceleration due to gravity g (in m/s2) following impact as a function of the “static stress” (force per unit area in KPa).
For the purposes of this disclosure vinyl aromatic polymer (a) will mean a polymer obtained from at least 65% by weight of a vinyl aromatic monomer.
The vinyl aromatic monomers that can be used to prepare the vinyl aromatic polymer (a) used in the compositions described and claimed in the present disclosure have the general formula (I):
In formula (I) R is hydrogen or a methyl group; n is zero or an integer ranging from 1 to 3, Y is selected from a halogen, preferably chlorine or bromine, a chloromethyl, an alkyl group or an alkoxyl group having 1 to 3 carbon atoms.
Preferred vinyl aromatic monomers having formula (I) are selected from styrene, α-methylstyrene, methylstyrene, ethylstyrene, vinyltoluene isomers, ethylstyrene isomers, propylstyrene isomers, chlorostyrene isomers, methylchlorostyrene isomers, methoxystyrene isomers, acetoxystyrene isomers, hydroxystyrene isomers, methylhydroxystyrene isomers, and mixtures thereof. More preferably styrene and α-methylstyrene may be selected from these vinyl aromatic monomers. Styrene is the predominant vinyl aromatic monomer and is preferably at least 50% of the mixture of vinyl aromatic monomers used to prepare vinyl aromatic polymer (a), more preferably at least 75%, even more preferably at least 85%. The other preferred co-monomer is α-methylstyrene.
Vinyl aromatic monomers of general formula (I) may be used alone, in a mixture or in a mixture of up to 35% by weight of other copolymerizable vinyl monomers.
Preferred copolymerizable vinyl monomers are selected from among (meth)acrylic acid, maleic anhydride, alkyl esters of (meth)acrylic acid having from 1 to 18 carbon atoms, amides and nitriles of (meth)acrylic acid. Among said (meth)acrylic acid esters those preferred are compounds selected from among ethyl acrylate, methyl methacrylate, butyl acrylate, 2-ethylhexyl acrylate, dodecyl acrylate, dodecyl methacrylate, stearyl acrylate, stearyl methacrylate, glycidyl methacrylate, ethylene glycol dimethacrylate, and their mixtures.
Among said (meth)acrylic acid nitriles those preferred are compounds selected from among acrylamide, methacrylamide, dimethylaminoethyl methacrylate, acrylonitrile, methacrylonitrile. Other copolymerizable vinyl co-monomers may be butadiene and divinyl benzene.
The weight average molecular weight MW of the polymer and/or copolymer (a) measured by the Gel Permeation Chromatography (GPC) technique described in the Experimental Part (ASTM method D5296-11 GPC PS) is between 90 kDa and 300 kDa.
MW below 90 kDa give a too high fluidity which causes the pearls to collapse during the expansion process. MW over 300 kDa give an insufficient expansion rate and an unsuitable final density for the foamed part.
Compositions according to the present disclosure may include a quantity of vinyl aromatic polymer (a) from 60 to 96% by weight, preferably from 67 to 88% by weight, more preferably from 69 to 83% by weight, compared to the sum of (a), (b) and (c) as defined above.
For the purposes of this disclosure vinyl aromatic copolymer (c) is defined as a copolymer produced from at least one vinyl aromatic monomer, as defined above, containing a rubbery component as a dispersed phase.
Some examples of vinyl aromatic copolymer (c) are “Edistir®850E”, “Edistir®ICE R830D”, “Edistir®RC600”, produced and marketed by Versalis s.p.a.
The rubbery component used in vinyl aromatic copolymer (c) is between 1% and 10% by weight and may be selected from polybutadiene, polyisoprene, butadiene and/or isoprene copolymers with styrene or with other vinyl monomers.
Some examples of suitable rubbery components are polybutadiene, such as “Intene® 40”, “Intene® 50” and “Intene® 60”, produced and marketed by Versalis s.p.a.
Alternatively, there are also styrene-diene block copolymers available on the market, such as “SOLPRENE® 1205”, “SOLPRENE® S1430”, “SOLPRENE® 308” and “SOLPRENE® 314” produced and marketed by Dynasol, or “Europrene® SOL B 183”, produced and marketed by Versalis s.p.a.
Copolymer (c) can be prepared according to any known suspension, mass-suspension or continuous bulk polymerization process.
If not already specified, the amount of dispersed polybutadiene may be conveniently determined using the iodometric titration method described below in the Experimental Part.
In a preferred aspect of the present disclosure vinyl aromatic copolymer (c) is prepared by pre-polymerization of the vinyl aromatic monomer in the presence of suitable free-radical initiators and the rubbery component in a first reactor until a conversion of less than 50% by weight of the monomers fed is achieved.
Subsequently polymerization is completed in one or more successive reactors until the monomers are completely polymerized. The resulting polymer is then devolatilized and granulated.
Compositions according to the present disclosure may comprise a quantity of vinyl aromatic copolymer (c) from 1 to 30% by weight, preferably from 9 to 25% by weight, more preferably from 13 to 24% by weight, even more preferably from 15 to 25% by weight and yet more preferably from 17 to 22% by weight in comparison to the sum of (a), (b) and (c) as defined above.
The rubbery component dispersed in vinyl aromatic copolymer (c) may vary between 1 to 10% by weight, preferably between 2 and 10% by weight, more preferably between 3 and 9% by weight, even more preferably between 4 and 9% by weight, yet more preferably between 5 and 9% by weight, even more preferably between 6 and 8.5% by weight and yet even more preferably between 7 and 8.5% by weight.
It follows, therefore, that if copolymer (c) is present as 1% by weight, the rubbery component, present in quantities from 1% to 10% by weight compared to copolymer (c), may vary between 0.01% and 1% by weight in comparison with the sum of (a), (b) and (c) as defined above.
Similarly, in the case where copolymer (c) is present as 30% by weight, the rubbery component present as 1% to 10% by weight compared to copolymer (c), may vary between 0.3% to 3% by weight in comparison with the sum of (a), (b) and (c) as defined above.
Likewise, as shown in the Examples, if copolymer (c) is present in a quantity of 15%, 20%, 25% by weight of the sum of (a), (b) and (c) as defined above, the rubbery component present in a quantity of 7%, 7.5%, 8.5% will have the following values with respect to the sum of (a), (b) and (c) as defined above.
In a preferred aspect of the present disclosure the rubbery component dispersed in vinyl aromatic copolymer (c) is polybutadiene (PB) and/or styrene-diene block copolymers.
Compositions according to the present disclosure may include from 3% to 10% by weight, preferably from 3% to 8% by weight, of at least one expansion agent (b).
Any expansion agent that can be incorporated into a polymer can be used in the compositions to which this disclosure relates.
Preferably expansion agents may be liquid substances with a boiling point varying between 10° C. and 100° C. at atmospheric pressure; preferably between 20° C. and 60° C. Expansion agents that may be used in this disclosure are selected from aliphatic or cycloaliphatic hydrocarbons containing from 3 to 6 carbon atoms; for example, n-pentane, iso-pentane, cyclopentane, butane, isobutane and their mixtures; or halogenated derivatives of aliphatic hydrocarbons containing 1 to 3 carbon atoms, such as dichlorodifluoromethane, 1,2,2-trifluoroethane and 1,1,2-trifluoroethane; or carbon dioxide.
Compositions according to the present disclosure may include a quantity of expansion agent (b) from 3 to 10% by weight, preferably from 3 to 8% by weight, more preferably from 4 to 7% by weight with respect to the sum of (a), (b) and (c) as defined above.
In order to encourage retention of the expansion agent in polymer matrix (a), additives that can form weak bonds with the expansion agent (e.g. hydrogen bonds) or strong bonds (e.g. acid-base adducts) may be used. Preferably these additives are selected from methyl alcohol, isopropyl alcohol, dimethyl carbonate, or derivatives containing an amine group. Additional additives (generally introduced in conventional vinyl aromatic polymers) such as nucleating agents, for example polyethylene waxes or talc, antioxidants, pigments, stabilizers, antistatic agents and release agents, may be added to the compositions according to the present disclosure.
In a preferred aspect of the present disclosure the polymer compositions with improved mechanical and insulating properties comprise:
In a further preferred aspect of the present disclosure the polymer compositions comprise:
In another preferred aspect of the present disclosure the polymer compositions comprise:
In yet another preferred aspect of the present disclosure the polymer compositions comprise:
The polymer compositions according to the present disclosure may be prepared according to methods known in the art.
In one aspect of the present disclosure the polymer compositions according to the present disclosure are conveniently prepared by a continuous bulk process comprising the following stages in sequence:
One cutting die plate used is for example that described in U.S. Pat. No. 7,320,585 with a cutting system of the “Spraying Nozzles System” type. The expandable granules/pearls to which this disclosure relates can also be produced with a different type of die plate where the polymer is cut in a granulation chamber full of water, a system known as “underwater” cutting. In this case the polymer remains completely immersed in water during the cutting stage, and the water pressure in the granulation chamber is over 300 KPa.
At the end of the continuous bulk process the final compositions according to the present disclosure obtained are in the form of spheroidal-shaped polymer granules with different average diameters that can be used according to the nature of the individual manufactured article, and conveniently of between 0.4-0.6 mm, 0.6-0.9 mm, 0.9-1.2 mm and 1.2-1.6 mm.
In one embodiment of the present disclosure the polymer compositions according to the present disclosure including:
A number of demonstration examples are provided below for a better understanding of the disclosure and its scope of application. These examples do not in any way constitute a limitation of the scope of the present disclosure.
Experimental Part
Determination of Molecular Weight (MW) and Molecular Weight Distribution (MWD) by GPC.
The compositions according to the present disclosure have a weight average molecular weight (MW) of between 90 and 300 kDalton, measured by high performance molecular size-exclusion chromatography according to ASTM D5296-11, and have a fluidity index (Melt Flow Index MFI at 200° C., 5 kg) of between 2.5 and 50.
The flow index is measured according to ISO 1133, fourth edition, 2005.
Molecular weight distribution is measured by high performance molecular size-exclusion chromatography according to ASTM D5296-11 using a refractive index detector (RID), and is performed on the polymer after separation from the dry residue and subsequent precipitation.
Determination of Polybutadiene Content by Iodometric Titration
The iodometric titration is performed using the 785 DMP Titrino Metrohm Titrator according to this method.
(a) Blank Analysis as Follows
1) Preparation (time 15 min)
2) Addition of Wijs reagent (time 15 min)
3) Determination (time 15 min)
(b) Sample Analysis
1) Preparation (time 25 min)
2) Addition of Wijs reagent (time 20 min)
3) Determination (time 15 min)
Expression of the result (% of PB)
Where:
Vb=ml of thiosulfate solution used for blank test
Vc=ml of thiosulfate solution used for the sample
NS
p=weighing polymeric sample (gr)
Preparation of a Composition by a Continuous Bulk Process
In a stirred reactor, 90 parts of ethyl benzene and 910 parts of styrene were fed for a total of 1000 parts. The reaction was conducted at 125° C. with an average residence time of 2 hours. The fluid composition from the outlet was then fed to a second reactor where the reaction was completed at 135° C. with an average residence time of 2 hours.
The reactive polymer composition, with 72% conversion, was heated to 240° C. and then fed to the diverter to remove the solvent and residual monomer.
The resulting composition had a glass transition temperature of 101° C., a melt flow index (MFI 200° C., 5 kg) of 5 g/10 min, a molecular weight MW of 210000 g/mol and a MW/Mn ratio of 2.2, where MW is the weight average molecular weight and Mn is the number average molecular weight. The vinyl aromatic composition was fed to a heat exchanger to lower its temperature to 200° C. (component (a) of the disclosure).
200 parts of impact-resistant polystyrene (HIPS, High Impact Polystyrene) with 7% polybutadiene determined iodometrically (commercially available, Edistir® 850E, Versalis spa), as vinyl aromatic copolymer (c) were fed to an extruder. A gear pump increased the feed pressure of the plasticized HIPS to 260 bar absolute: 60 parts of a mixture of n-pentane (70%) and iso-pentane (30%), expansion agent (b), and 750 parts of the vinyl aromatic composition (a) from the heat exchanger were then added. The ingredients were then mixed with static mixing elements for an average calculated (residence) time of 7 minutes.
The final composition contained 20% by weight of copolymer (c) with 7% polybutadiene, 6% by weight of a mixture of n-pentane (70%) and iso-pentane (30%), (component (b)) and 74% by weight of polystyrene (component (a)). The quantity of polybutadiene therefore corresponded to 1.4% by weight of the total composition.
The composition was then delivered to the die plate, where it was extruded through a number of holes with a diameter of 0.6 mm, immediately cooled with a jet of water and cut with a series of rotating knives (as described in US 2005/0123638). The granulation pressure was 500 KPa absolute and the shear displacement rate was selected so as to obtain granules with an average diameter of 1.1 mm. Water was used as a spray liquid and nitrogen as a carrier gas. The water temperature was 45° C.
The resulting granulated beads were dried with a centrifugal dryer and then coated. The coating was prepared by adding 1 part of glyceryl monostearate, 1 part of glyceryl tristearate, 1 part of zinc stearate per 1000 parts of dried granulated pearls. The coating additives were mixed with the granulate by means of a continuous screw mixer. The size of the expandable granules subjected to the expansion process, understood as the weighted mean diameter, was between 0.9 and 1.2 mm.
The product was pre-expanded in a discontinuous pre-expander produced by the AMD company, model P125 D (usable volume at level: 125 liters), using steam at a temperature of 100° C. The vapour pressure used for pre-expansion of the polymer granules was set to 1.1 bar absolute (110 KPa). The amount of expandable granules fed to the pre-expander was 1000 g. The expanded pearls were left to mature for 12 hours and then used to mold blocks (size 1040×1030×550 mm).
Some slabs obtained from the block of expanded material were put into a stove at 70° C. for 3 days (residual pentane less than 0.15%): samples for bending, compressive, cushioning and thermal conductivity tests were then obtained.
The thermal conductivity at 15.8 g/l measured according to ISO 8301 (1991) was 36.7 mW/mK.
The bending force, measured at 30 mm (5% deformation) according to ISO 1209-2, was 209 KPa (specimen size—350×100×25 mm).
Compressive stress at 10%, according to ISO 844 (2007) was 110 KPa at 17.4 g/l (specimen size=50×50×50 mm).
The density of the expanded slabs was 18.0 g/l and sintering was 90% (number of fractured pearls per 100 examined).
The cushioning tests were carried out according to ISO 4651 (1988).
This composition had an excellent balance of mechanical properties (both bending and compression and cushioning), sintering and thermal insulation.
Preparation of a Composition by a Continuous Bulk Process
Example 1 was repeated using 25% of copolymer (c).
The final composition contained 25% by weight of copolymer (c), 7% polybutadiene, 5% by weight of a mixture of n-pentane (70%) and iso-pentane (30%), (component (b)) and 70% by weight of polystyrene (component (a)). The quantity of polybutadiene therefore corresponded to 1.75% by weight of the total composition.
The thermal conductivity was 38 mW/mK at 16.50 g/l. The compressive stress at 10% was 100 KPa. The bending force, measured at 30 mm (5% deformation) was 204 KPa. The density of the expanded sheets was 18.0 g/l and sintering was 80%.
Preparation of a Composition by a Continuous Bulk Process
Example 1 was repeated using 15% of copolymer (c).
The final composition contained 15% by weight of copolymer (c), 7% polybutadiene, 6% by weight of a mixture of n-pentane (70%) and iso-pentane (30%), (component (b)) and 79% by weight of polystyrene (component (a)). The quantity of polybutadiene therefore corresponded to 1.05% by weight of the total composition.
The thermal conductivity was 36 mW/mK at 16.40 g/l. The compressive stress at 10% was 110 KPa.
The bending force, measured at 30 mm (5% deformation) was 215 KPa. The density of the expanded sheets was 18.2 g/l and the sintering 85%.
Preparation of a Composition by a Continuous Bulk Process
Example 1 was repeated using a different copolymer (c), i.e. impact resistant polystyrene with 8.5% polybutadiene (PB) determined by the iodometric method (commercially available, Edistir® ICE R830D, Versalis spa).
At the end of the process as described in Example 1 a composition with the same percentage values was obtained, but the copolymer c) used in this example had a higher percentage of polybutadiene, 8.5% instead of 7%. The quantity of polybutadiene therefore corresponded to 1.7% by weight of the total composition.
Thermal conductivity was 34.8 mW/mK at 16.5 g/l. The bending force, measured at 30 mm (5% deformation) was 198 KPa. The compressive stress at 10% was 99.5 KPa. The density of the expanded sheets was 18.3 g/l and sintering 85%.
Preparation of a Composition by a Continuous Bulk Process
Example 1 was repeated using an impact resistant polystyrene with 7.5% PB determined by the iodometric method (commercially available, Edistir®RC600, Versalis spa). In this case the quantity of component (b) was 4.7%.
At the end of the process as described in Example 1 a composition was obtained with the same percentage values of copolymer (c), but the copolymer c) used in this example had a higher percentage of polybutadiene, 7.5% instead of 7%. The quantity of polybutadiene therefore corresponded to 1.5% by weight of the total composition.
The thermal conductivity was 35 mW/mK at 15.60 g/l. The bending force, measured at 30 mm (5% deformation), was 191 KPa. The compressive stress at 10% was 90 KPa. The density of the expanded sheets was 18.0 g/l and sintering 80%. The cushioning tests are reported in
Preparation of a Composition by a Suspension Process
A mixture of 150 parts by weight of water, 0.2 parts of sodium pyrophosphate, 80 parts of styrene, 0.25 parts of t-butylperoxy-2-ethylhexanoate, 0.25 parts of t-butyl perbenzoate and 20 parts of copolymer (c) used in Example 1 were loaded into a sealed stirred vessel.
The batch was heated to 90° C. with stirring. After about 2 hours at 90° C., 4 parts of a 10% solution of polyvinylpyrrolidone were added. Always with stirring, it was heated for another 2 hours at 100° C.; 7 parts of a 70/30 mixture of n-pentane and i-pentane were added, it was heated for another 4 hours at 125° C., then cooled down and discharged.
The expanded polymer granules thus produced contained 20% of copolymer (c) with 7% polybutadiene, 6% of a mixture of n-pentane (70%) and iso-pentane (30%) (component b) and 74% polystyrene (component a).
The granules were then recovered and washed with demineralised water containing 0.05% of a non-ionic surfactant consisting of a fatty alcohol condensed with ethylene oxide and propylene oxide, sold by Huntsman under the trade name Empilan 2638. The granules were then dried in a lukewarm stream of air, 0.02% of a non-ionic surfactant consisting of a condensate of ethylene oxide and propylene oxide based on glycerine, sold by Dow (Voranol CP4755), was added and the granules were then screened by separating out the fraction with a diameter of between 0.9 and 1.2 mm.
This fraction accounted for 50%, 20% being the fraction between 0.4 and 0.9 mm, 5% the fraction between 0.2 and 0.4 mm and 25% the coarse fraction between 1.5 and 3 mm.
The same coating as in Example 1 was then added to the fraction between 0.9 and 1.2 mm. The product was pre-expanded, moulded and characterized in the same way as in Example 1. The thermal conductivity was 37.5 mW/mK at 15.9 g/l.
The bending force, always measured at 30 mm (5% deformation), was 205 KPa.
The compressive stress, again at 10%, was 100 KPa. The density of the expanded slabs was 18.3 g/l and sintering 80%.
As may be seen, both mechanical properties and conductivity are comparable with those in Example 1 but the useful fraction (0.9-1.2 mm) was only 50%. The yield was only 50%, the rest being waste.
Preparation of a Comparative Composition Containing 94% of Polymer (c)
940 parts of a vinyl aromatic composition of Edistir® R850 E (used in Example 1 above) originating from the polymerization section were placed in a heated vessel and fed to a heat exchanger to lower its temperature to 200° C.
A gear pump increased the feed pressure of the plasticized HIPS to 260 bar: 60 parts of a mixture of n-pentane (70%) and iso-pentane (30%) were then added, as in Example 1.
The composition was then mixed by means of static mixing elements for a calculated average (residence) time of 7 minutes. The composition was then distributed in the system, where it was extruded through a number of holes with a diameter of 0.6 mm, immediately cooled with a jet of water and cut with a series of rotating knives in the same way as in Example 1.
The quantity of polybutadiene therefore corresponded to 6.58% by weight of the total composition, since polymer (c) was the only constituent of the composition.
The product was pre-expanded, moulded and characterized in the same way as in Example 1.
The thermal conductivity was 39 mW/mK at 16 g/l. The bending force, always measured at 30 mm (5% deformation), was 180 KPa.
The compressive stress, again at 10%, was 70 KPa. The density of the expanded slabs was 18.1 g/l and sintering 60%. The cushioning tests are reported in
Preparation of a Composition by a Continuous Bulk Process
Example 5 was repeated using 9% copolymer (c) or Edistir®RC600. The final composition contained 9% by weight of copolymer c) with 7.5% polybutadiene, 5% by weight of pentane (component (b)) as a mixture of n-pentane (70%) and iso-pentane (30%), and 86% by weight of polystyrene (component (a)). The quantity of polybutadiene therefore corresponded to 0.675% by weight of the total composition.
Thermal conductivity was 34.1 mW/mK at 18.1 g/l. The bending force, measured at 30 mm (5% deformation), was 234 KPa. Compressive stress at 10% was 112 KPa. The density of the expanded slabs was 18.0 g/l and sintering 75%. The cushioning tests are reported in
Preparation of a Composition by a Continuous Bulk Process
90 parts of ethyl benzene and 910 parts of styrene for a total of 1000 parts were fed to a stirred reactor. The reaction was conducted at 125° C. with an average residence time of 2 hours. The fluid composition from the outlet was then fed to a second reactor where the reaction was completed at 135° C. with an average residence time of 2 hours.
The reactive polymer composition, with a conversion of 72%, was heated to 240° C. and then fed to the devolatiliser to remove the solvent and residual monomer.
The resulting composition had a glass transition temperature of 101° C., a melt flow index (MFI 200° C., 5 kg) of 5.3 g/10 min, a molecular weight MW of 208000 g/mol and a MW/Mn ratio of 2.2, where MW is the weight average mean molecular weight and Mn is the number average molecular weight. The vinyl aromatic composition was fed to a heat exchanger to lower its temperature to 200° C. (component (a) of the disclosure). A gear pump increased the pressure of component feed (a); 60 parts of a mixture (component (b)) of n-pentane (70%) and iso-pentane (30%) were then added, as in Example 1. The ingredients were then mixed by means of static mixing elements for an average calculated (residence) time of 7 minutes. The final composition contained 6% by weight of a mixture of pentane (component (b)) and 94% by weight of polystyrene (component (a)). The quantity of polybutadiene therefore corresponded to 0% by weight of the total composition.
The product was pre-expanded, moulded and characterized in the same way as in Example 1.
Thermal conductivity was 38.6 mW/mK at 17.2 g/l. In the bending stress test the sample did not reach 30 mm (corresponding to 5% deformation) but broke earlier, at 20.7 mm.
The compressive stress, again at 10%, was 75 KPa. The density of the expanded slabs was 18.2 g/l and sintering 25%.
Analysis
As may be seen from
This capacity is measured with the impact factor expressed in multiples of the earth's acceleration g and is the deceleration caused by the product's absorption of the impact energy.
The sintering values in Examples 1, 2, 3, 4, 5, 6 and 8 are higher than those for comparison Examples 7 (6.58% rubbery component) and 9 (0% rubbery component).
The thermal conductivity values for Examples 1, 2, 3, 4, 5, 6 and 8 are higher than those for comparison Examples 7 (6.58% rubbery component) and 9 (0% rubbery component).
The bending behaviour of Examples 1, 2, 3, 4, 5, 6, 7 and 8 is better than that of Example 9 (0% rubbery component).
The compressive behaviour of Examples 1, 2, 3, 4, 5, 6 and 8 is better than that of comparison Examples 7 (6.58% rubbery component) and 9 (0% rubbery component).
| Number | Date | Country | Kind |
|---|---|---|---|
| 102018000008073 | Aug 2018 | IT | national |
The present application is a national stage entry application claiming priority from PCT Application No. PCT/EP2019/071543, filed Aug. 12, 2019, which claims priority based upon Italy Application No. 102018000008073, filed Aug. 13, 2018, both of which are incorporated herein by reference in their entireties.
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2019/071543 | 8/12/2019 | WO | 00 |
