Patent Application
20120289660
The present invention relates to a rubber-reinforced vinyl aromatic (co)polymer having an optimum balance of physico-mechanical proprieties and a high gloss.
More specifically, the present invention relates to a vinyl aromatic (co)polymer reinforced with a diene rubber, having optimum physico-mechanical characteristics, such as impact resistance, tensile modulus, yield strength, ultimate tensile stress, combined with a high gloss.
In the present description and claims the terms rubber and elastomer should be considered synonyms. All the information contained herein should be considered preferred, even when not expressly specified.
Vinyl aromatic (co)polymers reinforced with rubber, in particular diene rubber, polybutadiene, for example, represent a well-known group of engineering polymers known on the market and widely described in literature. Specific examples of these (co)polymers are, for example, styrene/acrylonitrile co-polymers containing polybutadiene particles, dispersed in the polymeric matrix, generally known as ABS resins, and high impact polystyrene, generally known as HIPS, comprising a continuous phase of polystyrene in which rubber particles are dispersed, for example polybutadiene particles.
It is known that the surface gloss of vinyl aromatic (co)polymers, reinforced with rubber particles, can be improved by reducing the rubber particle dimension to values lower than 1 μm. This condition can be obtained by increasing the shear during the polymerization reaction. Shear simply means the friction force imposed by the stirring of the mixture. The greater this force, the smaller the rubber particle diameter will be. As the shear is in relation to the revolution number of the stirrer of the polymerization reactor, this characteristic is an instrument on which it is possible to intervene within certain limits established by the motor power.
Another parameter which can be used for regulating the dimension of the rubber particles dispersed in the matrix is to reduce the viscosity in solution of the diene rubber used in the production of vinyl aromatic (co)polymers. As a diene rubber, however, such as polybutadiene, for example, in order to be handled and packed, must have a sufficient viscosity to avoid the “cold flow” phenomenon, it has so far been considered practically impossible to produce a reinforced vinyl aromatic (co)polymer, with a high surface gloss, using linear low-viscosity polybutadiene homopolymer alone as rubber.
Examples are known in literature in which the production of ABS is described, having improved aesthetical properties (gloss), wherein diene rubbers are used, such as polybutadiene, for example, which have been modified to reduce the viscosity in solution and which are suitable for producing ABS co-polymers with enhanced aesthetical properties. For example;
The Applicant has now surprisingly found that it is possible to produce vinyl aromatic (co)polymers having an enhanced gloss, with the same the physico-mechanical characteristics, using a diene rubber as reinforcing elastomer. By using linear diene rubbers having a viscosity (measured in solution at 5% by weight in styrene) equal to (or even higher than) that of block polybutadiene-polystyrene co-polymers or radial rubbers, i.e. diene rubbers structured as described hereunder, dispersed rubber particles are in fact obtained with smaller dimensions and therefore final polymers with enhanced aesthetical properties, having the same mechanical properties.
An object of the present invention therefore relates to a rubber-reinforced vinyl aromatic (co)polymer comprising a polymeric matrix and a rubber phase consisting of a diene rubber dispersed and/or grafted to the polymeric matrix wherein said rubber phase is selected from at least one of the following:
(i) a linear diene rubber with a solution viscosity lower than 70 cPs, preferably between 40 and 60 cPs;
(ii) a partially radial diene rubber having a solution viscosity lower than 70 cPs, preferably between 40 and 60 cPs wherein up to 15% by weight, preferably from 1 to 120, of the polymeric chains is terminated with a quantity of tetra-functional coupling agent (non-limiting example, silicon tetrachloride) which is such as to generate a terminal radial structure of said chains of linear diene rubber;
(iii) a three-chain diene rubber, having a solution viscosity lower than 70 cPs, preferably between 40 and 60 cPs, i.e. a linear diene rubber coupled with a tri-functional agent (a non-limiting example is methyl trichlorosilane with a Si:Li ratio of 1:3);
(iv) a mixture of linear diene rubbers (i) and radial diene rubbers (v) in a maximum ratio between them (i)/(v) ranging from 99.5/0.5 to 85/15;
The radial diene rubbers (v) can be commercial radial polybutadiene rubbers.
The diene rubber (i), (ii), (iii) or (iv) used in the vinyl aromatic (co)polymer object of the present invention, can be either natural or synthetic. Suitable synthetic rubbers are those consisting of a polymer of a 1,3-conjugated diene containing from 4 to 6 carbon atoms, and in particular polybutadiene, high and medium cis polybutadiene, polyisoprene.
Particularly preferred is polybutadiene having:
This type of polybutadiene is obtained by anionic polymerization of butadiene in a solution of aliphatic or cyclo-aliphatic solvents or a mixture thereof, with the use of lithium-alkyl initiators. The polymerization can be carried out in batch reactors or continuous reactors; in batch reactors, the initiator, normally consisting of primary or secondary butyl lithium, is added to the reaction mixture consisting of the solvent and monomer charged in such a quantity that the amount of total solids at the end of the polymerization is not higher than 20% by weight; it is known to experts in the field that said reaction can be carried out in the presence of Lewis bases in a higher or lower quantity depending on the content of vinyl or 1,2 units which are to be present in the polymeric chain. Ethers are among the most widely-used Lewis bases, tetrahydrofurane in particular, which already in a quantity of 100 ppm with respect to the solvent is capable of considerably accelerating the reaction, maintaining the content of vinyl unit at levels <12%; with higher quantities of THF, the microstructure is progressively modified up to vinyl unit contents higher than 40% for quantities of THF equal to 5,000 ppm. High vinyl unit quantities, however, are not necessary if not harmful for the use of polybutadiene in the field of plastic material modification; it is preferable for the content of these units not to exceed the value of 15% even if, for a higher grafting efficiency, it is possible to use polybutadiene with a higher content of 1,2 units. It is also known to experts in the art that reactions carried out in the absence of ethers or tertiary amines are sufficiently rapid to guarantee the complete polymerization of the monomer in times not longer than 1 hour, with final temperatures not higher than 120° C. and, in any case, controlled by the initial temperature of the reaction mixture which cannot be lower than 35-40° C. to avoid an insufficiently rapid starting reaction and incompatible with normal production cycles. The reactor can be equipped with cooling jackets, however these are not particularly efficient as a result of the unfavourable surface/volume ratio typical of industrial reactors whose volume is never smaller than 20 m3; a more efficient temperature control is obtained by means of a partial evaporation of the solvent which is condensed and subsequently fed to the reaction reactor; this type of reactor, called “boiling reactor” is quite efficient for the control of the reaction temperature and, in the state of the art, represents the best way for effectively limiting the natural increase in temperature due to the heat of the butadiene polymerization. Carrying out the polymerization in batch reactors causes the formation of a polymer which, before a possible addition of a coupling agent, has a monomodal molecular weight distribution, wherein the ratio between the weight average molecular weight (Mw) and the number average molecular weight (Mn) is very close to 1 and normally between 1 and 1.2. Carrying out the polymerization in a continuous reactor, of the CSTR type, or in various reactors in continuous of the CSTR type arranged in series, on the contrary, causes the formation of a polymer with a monomodal molecular weight distribution in which the Mw/Mn ratio is between 1.8 and 2.5, the polymer, in both cases, at the end of the polymerization is linear and has chain-ends which are still active. These chain-ends consists of the species polybutadiene-lithium. The possible addition of a protogene agent (an alcohol, for example) or a silicon halo-derivative wherein the ratio between the halogen and silicon is equal to 1 (a non-limiting example is trimethyl chlorosilane TMCS) causes the termination of the butadiene-lithium chain-end and maintains the linear macrostructure of the molecule. The addition of a polyfunctional substance capable of reacting with the active chain ends, on the other hand, causes the formation of a branched macrostructure characterized in that it has a node from which a number of branches depart having the same functionality as the polyfunctional substance used. As a non-limiting example, the use of silicon tetrachloride is known to experts in the field, which, when added to the reaction environment in a Si:Li ratio=1:4, causes the formation of a radial polymer which, if the polymer has been prepared in a batch reactor, has the four branches with the same lengths, whereas in the case of a polymer prepared in continuous, the four branches are different. If, on the other hand, the Si:Li ratio is lower than 1:4, partially radial structures (ii) are obtained. If a trifunctional silicon compound is used as coupling agent (a non-limiting example is methyl trichloro-silane), tri-chain rubbers are obtained (iii). The normal production process of polybutadiene subsequently comprises, after the addition of a pair of antioxidants consisting of a primary antioxidant of the phenolic type and a secondary antioxidant, typically an organic compound of trivalent phosphorous, the elimination of the solvent which is effected by means of the combined action of water and vapour in stirred containers. This produces a suspension of rubber granules in water from which, after draining on nets, the rubber is sent to a drying section consisting of two mechanical extruders. In the first extruder (expeller) a squeezing operation is carried out, which eliminates most of the water which is drained through side slits of the extruder whereas the complete drying is effected in a second extruder (expander) in which the rubber subjected to mechanical action is heated to a temperature of 160-180° C. Part of the vapour is eliminated from an aperture (vent) situated at the end of the extruder, whereas a part is eliminated at the outlet from the head. The rubber granules are then sent with belts or other conveying means to a packager where they are baled. The nature of polybutadiene (unsaturated rubber) requires a strict control of the finishing conditions, as experts in the field are aware of complications deriving from the formation of lumps of insoluble substances (gels) which are normally formed in the finishing area, in particular in the expander. These gels cause a deterioration in the quality of the rubber destined for use in the field of the modification of plastic materials by the formation of substantial surface defects. A great deal of attention must therefore be paid in defining the finishing conditions of polybutadiene with the consequent necessity of effecting numerous analyses for process and product control.
The polymeric matrix of the rubber-reinforced (co)polymers of the present invention can be either a (co)polymer deriving from one or more vinyl aromatic monomers or a (co)polymer deriving from one or more vinyl aromatic monomers and one or more comonomers, for example acrylic comonomers. The term vinyl aromatic monomer, as used in the present description and claims, comprises ethylenically unsaturated compounds having the general formula
wherein R represents hydrogen or an alkyl radical having from 1 to 4 carbon atoms, n is zero or an integer ranging from 1 to 5 and Y represents a halogen or an alkyl radical having from 1 to 4 carbon atoms. Examples of vinyl aromatic monomers having the above general formula are: styrene, α-methyl styrene, methyl styrene, ethyl styrene, butyl styrene, dimethyl styrene, mono-, di-, tri-, tetra- and penta-chlorostyrene, bromo-styrene, methoxy-styrene, acetoxy-styrene, etc. Preferred vinyl aromatic monomers are styrene and/or α-methyl styrene.
The vinyl aromatic monomers having general formula (I) can be used alone or in a mixture of up to 50% by weight with other co-polymerizable monomers. Examples of these monomers are (meth)acrylic acid, C1-C4 alkyl esters of (meth)acrylic acid such as methyl acrylate, methyl methacrylate, ethyl acrylate, ethyl methacrylate, isopropyl acrylate, butyl acrylate, amides and nitriles of (meth)acrylic acid, such as acrylamide, methacrylamide, acrylonitrile, methacrylonitrile, butadiene, ethylene, divinyl benzene, maleic anhydride, etc. Preferred copolymerizable monomers are acrylic monomers such as acrylonitrile and methyl methacrylate. The quantities of vinyl aromatic monomer and acrylic monomer used for the production of the copolymer vary in relation to the desired physico-mechanical properties in the vinyl aromatic copolymer reinforced with final rubber. The quantity of acrylic monomer generally ranges from 5 to 45% by weight, preferably from 15 to 35% by weight and, correspondingly, the quantity of vinyl aromatic monomer ranges from 95 to 55% by weight, preferably from 85 to 65% by weight, based on the total weight of the vinyl aromatic monomer-acrylic monomer copolymer. The quantity of diene rubber (1), (ii), (iii) or (iv) in the rubber-reinforced (co)polymer generally ranges from 4 to 30% by weight, preferably from to 25% by weight, with respect to the weight of the (co)polymer.
The rubber-reinforced (co)polymer object of the present invention can be prepared by means of any conventional technique used for producing crosslinked high impact co-polymers, such as mass polymerization, polymerization in solution, emulsion and mass-suspension. The specimens obtained from the (co)polymer object of the present invention have a gloss at 60° higher than 85.
Some illustrative examples are provided for a better understanding of the present invention and for its embodiment, which should in no way be considered as being of a limitative nature.
The method includes the preparation of a solution of polybutadiene in styrene at 5% by weight and the subsequent measurement of the viscosity at 25° C. using a Cannon Fenske capillary tube whose dimension must be selected so as to avoid that the elution time through the capillary is neither too short nor too long. In the case of the polymers examined, the Model 300, valid within the range of 50-250 cP, is used.
The determination of the average molecular weight of the SAN matrix was effected on chromatographic equipment consisting of: a degasser system, pump, injector: WATERS Alliance 2695, set of Phenogel columns (300×7.6 mm) of 5 microns, porosity 106, 105, 104, 103 Angstrom, a Waters 410 differential refractive index detector, UV Waters 2487 detector, chromatographic analysis software: Millenium 32 version 3.2 (Waters).
The dimensions and morphology of the rubber phase dispersed in the SAN matrix were determined via T.E.M. (Transmission Electronic Microscopy), F. Lenz, A. Wiss—Mikroscopie 63, 1956, page 56. The morphology of the rubber particles was determined by visual inspection of the micrographies and the characterization of the various structures was effected in accordance with the classification described in “Teilchenbildung bei der Herstellung von Kautschukmodifiziertem Polystyrol” of Adolf Echte 58/89 (1977), page 175-198, and in EP 716.664. For the calculation of the statistical parameter average volumetric Diameter of the particles DV the following formula was applied:
wherein Di represents the diameter of the i-th particle whereas for the calculation of the percentage of particles of the “core shell” type or with a “mixed” structure (labyrinth or brain) the stereological method was used, described in C. Maestrini et al. Journal of Material Science, Vol. 27, 1992, page 5994. The T.E.M. analysis was carried out on a transmission electron microscope Philips CM120.
The notched Izod value (on injection moulded specimens) was determined in accordance with the standard method ISO 180/1A—ISO 179 (values expressed as kJ/m2). Another parameter relating to the impact resistance of the materials is represented by the Ball Drop, determined in accordance with the standard method ISO 6603/2 on two different thicknesses specimens (2 mm and 3 mm).
The tensile strength (yield strength, yield elongation, stress at break, elongation at break, tensile modulus) and the flexural strength properties (maximum stress, elastic modulus) were measured on injection moulded specimens in accordance with the standard methods ISO 527, ISO 178 and expressed as MPa, with the exception of the yield elongation and elongation at break which are expressed as percentages.
3.6 kg of linear polybutadiene (i), having a solution viscosity at 5% in styrene (SM)=44 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of partially radial polybutadiene (ii) (with a content of branched end groups of 10% by weight), having a solution viscosity at 5% in styrene (SM)=45 CPs, g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of three-arm polybutadiene (iii), having a solution viscosity at 5% in styrene (SM)=42 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), in a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.4 kg of linear polybutadiene (i), having a solution viscosity at 5% in styrene (SM)=44 CPs, 0.2 kg of radial polybutadiene, having a solution viscosity at 5% in styrene (SM)=209 CPs, forming a mixture (iv), having a solution viscosity at 5% in styrene (SM)=59 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), in a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.2 kg of linear polybutadiene (1), having a solution viscosity at 5% in styrene (SM)=44 CPs, 0.4 kg of radial polybutadiene, having a solution viscosity at 5% in styrene (SM)=209 CPs, forming a mixture (iv), having a solution viscosity at 5% in styrene (SM)=65 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), in a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of polybutadiene SOL B 183 (modified polybutadiene containing 10% by weight of styrene, produced by Polimeri Europa) (solution viscosity at 5% in styrene (SM)=30 CPs), 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of polybutadiene INTENE P30 (four-arm star polybutadiene, produced by Polimeri Europa) (solution viscosity at 5% in styrene (SM)=45 CPs), 20 g of anti-oxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of partially radial polybutadiene (II) (with a content of branched end groups of 25% by weight), having a solution viscosity at 5% in styrene (SM)=65 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
2.7 kg of linear polybutadiene (i), having a solution viscosity at 5% in styrene (SM)=44 CPs, 0.9 kg of radial polybutadiene, having a solution viscosity at 5% in styrene (SM)=209 CPs, forming a mixture (IV), having a solution viscosity at 5% in styrene (SM)=85 CPs, 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), in a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
3.6 kg of polybutadiene INTENE 40 (linear polybutadiene, produced by Polimeri Europa) (solution viscosity at 5% in styrene (SM)=95 CPs), 20 g of antioxidant ANOX PP 18 in 21.8 kg of styrene monomer and 7.6 kg of ethylbenzene, are dissolved in a 60-litre batch-type autoclave, equipped with a temperature regulator and stirring system, stirring for 5 hours at 85° C. 12.4 g of initiator 1,1-di(terbutylperoxy)cyclohexane (Tx22E50) are then added.
The solution thus obtained is fed, after mixing under heat (at a temperature of 60° C.) with a feed of acrylonitrile (weight ratio solution/acrylonitrile 82.5/17.5), into a first PFR reactor equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 112° C. to 120° C., where the pre-polymerization is effected with grafting and phase inversion.
48 g of the transfer agent n-dodecylmercaptan (NDM) are added to the mixture leaving the first reactor which is then transferred to a second PFR reactor also equipped with a stirrer and temperature regulation system, with a thermal profile of the reactor increasing from 150° C. to 165° C.
The mixture obtained is fed to a devolatilizer operating under vacuum at a temperature of 235° C. in order to crosslink the rubber and remove the unreacted monomers and solvent from the polymer. The molten polymer thus obtained is granulated so as to obtain the end-product whose characteristics are indicated in Table 1.
| Number | Date | Country | Kind |
|---|---|---|---|
| MI2008A 002224 | Dec 2008 | IT | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2009/008861 | 12/10/2009 | WO | 00 | 5/21/2012 |
