ABS molding materials

The present invention relates to a rubbermodified, impact-resistant acrylonitrile-butadiene-styrene (ABS) molding material.
ABS molding materials may be prepared by bulk, solution, suspension or emulsion polymerization, as desired (see Winnacker-Kuchler, Chemische Technologie, Volume 6, Organische Technologie II, Carl Hanser Verlag, 4th Edition, 1982, pp. 384 ff.; Encyclopedia of Polymer Science and Engineering, Volume 1, John Wiley & Sons, New York--Chichester--Brisbana--Toronto--Singapore, pp. 388-424; Polymere Werkstoffe, Volume III, Technologie 2, Editor H. Batzer, Georg Thieme Verlag, Stuttgart--New York, 1984, pp. 9-23).
The mechanical properties of the ABS molding materials polymerized in bulk or solution on the one hand and those prepared in emulsion on the other hand are substantially identical. The advantage of the bulk or solution process is, in particular, the lower production costs (inter alia higher rubber effectiveness, no effluent) and the paler inherent color of its products, requiring less pigment for coloring. However, these products have the disadvantage compared with ABS prepared in emulsion of lower surface gloss, which is attributable to the fact that ABS polymerized in bulk or solution has significantly larger dispersed rubber particles.
There has therefore been a number of attempts to overcome this problem by appropriate modifications to the process and to prepare ABS with very small dispersed rubber particles by bulk or solution polymerization.
Solution ABS with small particles and good surface gloss can be prepared using either particularly low-molecular-weight polybutadiene (cf. JA-A-63/199,177) or styrene-butadiene block rubber (cf. EP 0 054 141, JA-A-63/207,804, JA-A-63/207,803 and JA-A-54/070,350), or by observing specific reaction conditions during or until phase inversion.
It is common to all the products produced in this way that they have high surface gloss, but low notched impact strength, since the rubber concentration in the solution or bulk polymerization process cannot be increased at will. In order to increase the rubber effectiveness of the solution ABS with small particles, attempts have been made to accommodate hard matrix occlusions in the dispersed rubber particles. To this end, polybutadiene, together with styrene-butadiene block rubber and polystyrene-acrylonitrile, has been dissolved and polymerized in styrene and acrylonitrile (cf. BE 888 804). The gel content of the resultant graft rubber increases due to included polystyrene-acrylonitrile. However, due to the compatibility with the polystyrene-acrylonitrile matrix itself formed in the process, the added polystyrene-acrylonitrile is distributed between this matrix and the rubber particles, which means that a very large amount of polystyreneacrylonitrile must be added even before the polymerization in order to effectively increase the rubber particle size; however, this results in viscosity problems during the polymerization before phase inversion.
A similar procedure is described in U.S. Pat. No. 3,442,981, with the polybutadiene being replaced only by styrene-butadiene block rubber.
GB 1,229,917 proposes the bulk suspension polymerization of a styrene solution of polybutadiene and polystyrene to give impact-resistant polystyrene. Here again, it is expected that the polystyrene added before the polymerization is distributed between the two phases rubber and polystyrene. The increase in the rubber effectiveness is probably only marginal. The same applies if the process is carried out exclusively by suspension polymerization (cf. GB 1,243,051).
It is an object of the present invention to prepare high-gloss and simultaneously high impact strength ABS molding materials by solution or bulk polymerization and to achieve greater effectiveness with respect to the formation of rubber occlusions.
We have found that this object is achieved by dissolving one or more styrene-butadiene block rubbers, together with at least one further polymer, in the initially introduced monomers, ie. styrene and acrylonitrile, and, if necessary, a solvent and then polymerizing the mixture in a conventional manner.
For the purposes of the present invention, further polymers are various types of polymer.
A particularly important polymer is polystyrene itself.
Another likewise suitable polymer is polycyclohexyl (meth)acrylate.
A further polymer which satisfies the same requirements as polystyrene or polycyclohexyl (meth)acrylate is polyphenylene ether.
In addition, the "further" polymer may be a mixture of the abovementioned polymers, for example a mixture of polystyrene and polycyclohexyl (meth)acrylate or polystyrene and polyphenylene ether. An important embodiment of the invention replaces the styrene-butadiene block copolymer by a mixture of a styrene-butadiene block copolymer and polybutadiene.
In a further, important embodiment of the invention, the molding material additionally contains a conventional solution ABS, ie. a graft copolymer ("solution ABS") prepared by solution, bulk or bulk-suspension polymerization and having main chains comprising polybutadiene and graft branches of a copolymer comprising styrene and acrylonitrile; this molding material has a mean rubber particle size of 0.6 to 10 .mu.m, and its polymer inclusions in the rubber particles have an identical chemical composition to the polymeric matrix.
The following details apply to carrying out the process in practice:
The further polymer added before the polymerization must be compatible with the polystyrene of the styrene-butadiene rubber, ie. must be fully or substantially soluble therein (cf. A. Noshay, Block Copolymers, pp. 8 to 10, Academic Press, 1977 and O. Olabisi, Polymer-Polymer Miscibility, 1979, pp. 117 to 189), but incompatible with the polystyrene-acrylonitrile produced during the polymerization. In this way, the amount of further polymer added regulates the rubber particle size and thus the properties of the ABS molding material produced. Electron photomicrographs after staining with OsO.sub.4 and/or RuO.sub.4 indicate novel rubber morphologies featuring a polymer included inside the rubber particles and itself surrounded by a thin rubber skin.
The polystyrene-acrylonitrile produced during the polymerization is grafted onto the polybutadiene part of the styrene-butadiene block rubber to a varying extent, depending on the reaction conditions, and thus results in binding to the polystyrene-acrylonitrile matrix. In this way, ABS products can be produced which utilize the advantages of solution or bulk polymerization and have a favorable combination of the product properties surface gloss, notched impact strength and rigidity.
Suitable monomers for carrying out the process are, in particular, styrene and acrylonitrile in a ratio of from 90:10 to 60:40. Other monomers, eg. .alpha.-methylstyrene, o-, m- or p-methylstyrene, tert-butylstyrene, methacrylonitrile or (meth)acrylates, may additionally be employed in a conventional manner.
The rubber used is at least one styrene-butadiene block copolymer. In general, two-block rubbers having a total styrene content of from 3 to 70% by weight, preferably from 10 to 50% by weight, and a block styrene content of from 2 to 60% by weight, preferably from 8 to 40% by weight, are employed. The weight average molecular weight of the block copolymers is from 20,000 to 600,000 g/mol. Examples of suitable commercially available products are Buna BL 6533, Buna BL 6426 and Buna BL 6578 from Bayer AG. The total rubber content, based on the polymer matrix, is from 2 to 30% by weight. An important embodiment comprises replacing some of the styrene-butadiene block copolymer by homopolybutadiene; in this case, the total butadiene content, based on the molding material, should be from 2 to 20% by weight and at least 20% of the rubber should be a block copolymer.
The polystyrenes employed are expediently products having a molecular weight (weight average) of from 10,000 to 10,000,000 g, preferably from 40,000 to 500,000 g. The polystyrene can have been obtained by free-radical or anionic polymerization and is used in an amount of from 0.1 to 30% by weight, preferably from 2 to 15% by weight, based on the polymer matrix.
The polycyclohexyl (meth)acrylate employed is a product having a molecular weight (weight average) of from 10,000 to 10,000,000 g, preferably from 40,000 to 500,000 g. The polycyclohexyl (meth)acrylate is generally polymerized by means of free radicals and is used in an amount of from 1 to 30% by weight, preferably from 2 to 15% by weight, based on the polymer matrix.
The polyphenylene ether employed is preferably poly-2,6-dimethyl-1,4-phenylene ether, but it is also possible to employ other polystyrene-compatible and polystyrene-acrylonitrile incompatible polyphenylene ethers and/or polyphenylene ether copolymers. Polyphenylene ethers of this type are obtained by oxidative coupling (cf. U.S. Pat. Nos. 3,661,848, 3,378,505, 3,306,874, 3,306,875 and 3,639,656). Suitable polyphenylene ethers generally have an intrinsic viscosity of from 0.1 to 2.0 dl/g, preferably from 0.3 to 0.7 dl/g, measured in chloroform at 25.degree. C. The polyphenylene ether is likewise used according to the invention in an amount of from 1 to 30% by weight, based on the polymer matrix.
The solvents which can be used for the process according to the invention are either polar or nonpolar compounds or mixtures thereof. Preference is given to methyl ethyl ketone, cyclohexanone, toluene and, in particular, ethylbenzene. The solvents are employed in an amount of up to 30% by weight, based on the reaction mixture.
The polymerization can be carried out either thermally or by addition of free-radical initiators. Suitable free-radical initiators are graft-active peroxides. Particular preference is given to dibenzoyl peroxide, tert-butyl peroctanoate, tert-butyl perpivalate, tert-butyl perneodecanoate and bis(tert-butyl) peroxalate. The initiators are used in amounts of from 0 to 0.5% by weight, based on the monomers employed.
Suitable chain-transfer agents are the conventional mercaptans having from 14 to 18 carbon atoms. Particularly successful mercaptans are n-butyl mercaptan, n-octyl mercaptan and n- and t-dodecyl mercaptan. The amount of mercaptan, if used, is generally from 0.005 to 0.5% by weight, based on the monomers employed.
The polymerization according to the invention is carried out in at least two reaction zones. It is possible to utilize a reactor arrangement comprising one or two stirred reactors with two further polymerization towers arranged one after the other (cf. EP-A-0 054 131) or a reactor cascade having at least two polymerization towers arranged one after the other. However, it is also possible to use arrangements as described in BE 888 804.
Preference is given to a reactor cascade comprising four reaction zones, which are preferably stirred polymerization towers having internal cooling tubes.
The styrene-butadiene block rubber and the "further polymer" are dissolved in styrene and acrylonitrile and, if necessary, another solvent and fed continuously into the first reaction zone, where the polybutadiene part of the styrene-butadiene block rubber is grafted with polystyrene-acrylonitrile, while the phase inversion and the formation of the rubber particle morphology takes place in the second reaction zone. Grafting and phase inversion can also be carried out in a joint reaction zone. Reaction zones three and four, if present, are where the further polymerization of polystyrene-acrylonitrile matrix is carried out up to a solids content of at least 40% by weight, but preferably at least 65% by weight. After the final reaction zone, the polymer melt is degassed, cooled, extruded and granulated.
The continuous bulk or solution polymerization procedure may also be replaced by batchwise or semicontinuous processes.
Furthermore, use may also be made of the bulk-suspension polymerization process which was known hitherto, if the phase inversion is concluded before commencement of the suspension polymerization.
During the polymerization, in particular after preparation of the solution of the rubber and of the further polymer or before processing of the finished polymers, conventional additives, such as internal glidants and antioxidants or UV stabilizers, and lubricants, fillers and the like are added in conventional amounts.
In a particular embodiment of the invention, as stated, a conventional solution ABS is admixed with relatively large rubber particles.
Whereas the graft copolymers of the molding material according to the invention have a rubber particle size of from 0.1 to 3.0 .mu.m, preferably from 0.2 to 1 .mu.m, the added graft copolymer, whose polymer inclusions in the rubber particles have the same composition as the hard matrix, has a particle size of from 0.6 to 10 .mu.m, preferably from 1 to 5 .mu.m.
This embodiment helps meet the demand for also providing the ABS molding materials according to the invention, which as they are have particularly high general toughness, rigidity and surface gloss, with good low-temperature toughness.
In order to achieve this, the materials according to the invention are expediently mixed with a "conventional" ABS polymer in a ratio of from 50:50 to 95:5. Joint melting in the extruder gives a "bimodally distributed" ABS. The same effect is achieved if the materials are mixed immediately after their respective preparation (ie. before degassing) and then freed from solvent together.
The molding materials according to the invention are novel substances or substance mixtures which have a balanced ratio of surface gloss, notched impact strength and rigidity. A blend of ABS polymers having small and large particles (bimodal ABS) is no longer necessary to achieve favorable property combinations. A compounding step (which involves heating the polymer to in some cases up to 300.degree. C.) is thus unnecessary. It thus follows that the process to be used according to the invention also has advantages.
The molding materials according to the invention thus have very good surface gloss, despite a relatively large rubber particle diameter, which is explained by the fact that the rubber particles are themselves well filled with a polymer ("the further polymer") and the rubber skin between the occlusions and the polystyrene-acrylonitrile matrix is very thin. As can be imagined, this has the consequence that the rubber particles at the surface of the finished part shrink less than conventional large particles and thus on cooling form only very small "pits", which hardly scatter the incident light at all. However, the above explanation is purely scientific and in no way restricts the invention.
The molding materials obtained by the process according to the invention can be processed by conventional methods of thermoplastics processing, eg. by extrusion, injection molding, calendering, blow molding, compression molding or sintering; the molding materials prepared by the process according to the invention are particularly preferably injected molded to give moldings.
The product properties listed in the examples and comparative experiments were determined as follows:
The mean particle size d.sub.50 of the dispersed rubber particles by evaluating electron photomicrographs.
The notched impact strength in accordance with DIN 53 453 on moldings injection-molded at 230.degree. C.
The modulus of elasticity, a measure of the rigidity, in accordance with DIN 53 457 on moldings injection-molded at 230.degree. C.
The viscosity of the polystyrene-acrylonitrile matrix as a 0.5% strength by weight solution in dimethylformamide after separation from the rubber phase.
The heat distortion resistance (Vicat B) in accordance with DIN 53 460.
The surface gloss was measured in accordance with DIN 67 530 using a Dr. Lange laboratory reflectometer on the side faces of injection-molded test boxes, at a measurement angle of 55.8.degree. (which differs from DIN 67 530) against a black standard. The test boxes have a length of 11 cm, a width of 4.3 cm and a height of 5 cm and weigh about 26-27 g. They were produced under the injection-molding conditions A or B given below on an Arburg Allround 370 CMD injection-molding machine.
______________________________________Condition A:Material temperature 255.degree. C.Mold-surface temperature 60.degree. C.Injection time 0.14 sec.Injection pressure 1200 barBack pressure 100 barCondition B:Material temperature 255.degree. C.Mold-surface temperature 30.degree. C.Injection time 0.4 sec.Injection pressure 1200 barBack pressure 100 bar______________________________________

EXAMPLES 1 TO 16
Use of Polystyrene as the Further Polymer
Examples 1 to 4
In each case, 11.5 parts by weight (230 g) of the commercially available rubber Buna.RTM. BL 6533 (Bayer AG) were dissolved overnight with various amounts of polystyrene (viscosity=74 ml/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.10 part by weight of a commercially available stabilizer (Irganox.RTM. 1076 from Ciba-Geigy). The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 1.
TABLE 1__________________________________________________________________________Amount of Modulus of Notched impact strength Surface gloss Rubber particle polystyrene elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example added [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________1 -- 2800 2.0 1.8 69 43 0.22 58 2770 3.2 2.5 68 44 0.33 116 2760 8.6 3.6 68 43 0.44 174 2760 7.1 3.4 67 41 0.8__________________________________________________________________________
Examples 5 to 8
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6425 (Bayer AG) were dissolved overnight with various amounts of polystyrene (viscosity=74 ml/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced ar shown in Table 2.
TABLE 2__________________________________________________________________________Amount of Modulus of Notched impact strength Surface gloss Rubber particle polystyrene elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example added [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________5 -- 2800 2.7 1.7 68 43 0.26 58 2750 3.3 2.5 70 42 0.37 116 2770 9.0 3.6 69 43 0.48 174 2780 7.3 3.0 68 43 0.7__________________________________________________________________________
Examples 9 and 10
In each case, 11.5 parts by weight (230 g) of block rubber (Example 9 Buna.RTM. BL 6533; Example 10 Buna BL 6425 from Bayer AG) were dissolved overnight with in each case 116 g of polystyrene (viscosity=74 ml/g) in 1236 g of styrene and 412 g of acrylonitrile. 4.0 g of tert-dodecyl mercaptan and 2.0 g of Irganox 1076 were added to the solution. The reaction mixture was heated to 80.degree. C., and 1.34 g of tert-butyl perpivalate were added, so that a polymer conversion of about 12%/hour was achieved with the reaction temperature kept constant. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. After a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer syrup, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 3.
TABLE 3__________________________________________________________________________ Modulus of Notched impact strength Surface gloss Rubber particle Rubber elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example added [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________ 9 Buna BL 6533 2650 10.2 4.5 65 40 0.710 Buna BL 6425 2600 10.4 4.8 64 41 0.8__________________________________________________________________________
Examples 11 and 12
In each case, 11.5 parts by weight (230 g) of block rubber (Example 11 Buna.RTM. BL 6533; Example 12 Buna BL 6425 from Bayer AG) were dissolved overnight with in each case 116 g of polystyrene (viscosity =74 ml/g) in 1236 g of styrene and 412 g of acrylonitrile. 4.0 g of tert-dodecyl mercaptan and 2.0 g of Irganox 1076 were added to the solution. The reaction mixture was then polymerized thermally at 118.degree. C. with stirring (200 rpm) until a solids content of 40% had been reached. 0.1% dicumyl peroxide was then added to the polymer syrup, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 4.
TABLE 4__________________________________________________________________________ Modulus of Notched impact strength Surface gloss Rubber particle Rubber elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example added [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________10 Buna BL 6533 2600 9.8 3.9 65 40 0.811 Buna BL 6425 2600 9.6 3.7 64 41 0.9__________________________________________________________________________
Examples 13 to 16
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (1/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following four rubber solutions were prepared for the polymerization:
______________________________________Example 13 14 15 16______________________________________Buna BL 6533 [parts by wt.] 11.05 11.05 11.05 11.05 [kg] 27.63 27.63 27.63 27.63Polystyrene [parts by wt.] -- 3.0 5.0 7.0(viscosity = [kg] -- 7.5 12.5 17.574 ml/g)Irganox 1076 [parts by wt.] 0.1 0.1 0.1 0.1 [kg] 0.25 0.25 0.25 0.25Ethylbenzene [parts by wt.] 15.0 15.0 15.0 15.0 [kg] 37.5 37.5 37.5 37.5Styrene [parts by wt.] 55.39 53.14 51.64 50.14 [kg] 138.48 132.85 129.1 125.35Acrylonitrile [parts by wt.] 18.46 17.71 17.21 16.71 [kg] 46.15 44.27 43.02 41.77______________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tert-butyl perpivalate are required:
______________________________________Example 13 14 15 16______________________________________tert-Butyl perpivalate forTower 1 [g/h] 1.35 0.75 0.9 0.85Tower 2 [g/h] 3.15 3.60 3.75 3.90______________________________________
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
______________________________________Example 13 14 15 16______________________________________tert-Dodecyl mercaptan forTower 1 -- -- -- --Tower 2 [g/h] 16 16 16 16Tower 3 [g/h] 50 50 50 50Tower 4 [g/h] -- -- -- --______________________________________
The polymerization was continued in the polymerization towers to the following solids contents:
______________________________________Example 13 14 15 16______________________________________Solids content inTower 1 [% by wt.] 15 18 19 20.5Tower 2 [% by wt.] 25 28 30 31Tower 3 [% by wt.] 45 45 45 45Tower 4 [% by wt.] 65 65 65 65______________________________________
The stirring speed was 150 rpm in the first tower, 100 rpm in the second, 50 rpm in the third and 10 rpm in the fourth (rpm=revolutions per minute). The polymerization in the third and fourth tower reactors was carried out thermally at 130.degree. and 146.degree. C. respectively. After the fourth polymerization tower, the polymer melt was degassed, cooled and granulated. The throughput of ABS molding material was from 11 to 12 kg/h. Product properties of the solution ABS produced are shown in Table 5.
TABLE 5______________________________________Example 13 14 15 16______________________________________Modulus of [N/mm.sup.2 ] 2620 2650 2580 2600elasticityNotched impact strengthat 23.degree. C. [kJ/m.sup.2 ] 3.9 10.8 14.7 17.9at -40.degree. C. [kJ/m.sup.2 ] 2.7 4.5 4.7 5.6Surface glossCondition [%] 70 68 69 68Condition [%] 46 44 44 43BRubber [.mu.m] 0.4 0.4 0.4 0.4particlesized.sub.50Yellowness 9.6 9.8 9.5 9.4indexViscosity of [ml/g] 75.6 76.2 77.3 79.4the PSANmatrix______________________________________
Comparative Experiment 1
For comparison, the properties of an ABS containing 17% by weight of polybutadiene and prepared by emulsion polymerization are used.
A polybutadiene latex is prepared by polymerizing 62 parts of butadiene in the presence of a solution of 0.6 part of tert-dodecyl mercaptan, 0.7 part of sodium C.sub.14 -alkylsulfonate as emulsifier, 0.2 part of potassium peroxodisulfate and 0.2 part of sodium pyrophosphate in 80 parts of water at 25.degree. C. When the reaction is complete, the polymerization autoclave is decompressed. The conversion is 99%. A polybutadiene latex is obtained whose mean rubber particle size is 0.1 .mu.m. The latex obtained is agglomerated by adding 25 parts of an emulsion, a copolymer of 96 parts of ethyl acrylate and 4 parts of methacrylamide having a solids content of 10 parts by weight, giving a polybutadiene latex having a mean particle size of 0.3 .mu.m. 40 parts of water, 0.4 part of sodium C.sub.14 -alkylsulfonate and 0.2 part of potassium peroxodisulfate are added, and 38 parts of a mixture of styrene and acrylonitrile in a ratio of 70:30 are fed in in the course of 4 hours.
The polymerization is carried out at 75.degree. C. with stirring. The conversion, based on styrene-acrylonitrile, is virtually quantitative. The graft rubber dispersion obtained is precipitated by means of calcium chloride solution, and the graft copolymer is separated off and washed with distilled water. The moist graft rubber is blended with polystyrene-acrylonitrile (viscosity 80.7 ml/g; AN content=25% by weight) in a two-screw extruder with degassing so that the resultant ABS product contains 17% by weight of polybutadiene. The product properties are as follows:
TABLE 6______________________________________Modulus of elasticity [N/mm.sup.2 ] 2650Notched impact strengthat 23.degree. C. [kJ/m.sup.2 ] 11.0at -40.degree. C. [kJ/m.sup.2 ] 4.0Surface glossCondition A [%] 68.0Condition B [%] 47.0Rubber particle size [.mu.m] 0.3d.sub.50Yellowness index 32.8Viscosity of the [ml/g] 80.7PSAN matrix______________________________________
Comparative Experiment 2
The solution ABS with small particles (particle diameter.ltoreq.0.5 .mu.m) was prepared as follows:
The polymerization plant comprises a 250 1 rubber dissolution tank, a 250 1 storage tank and four series-connected 30 1 tower reactors (1/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer engaging between the cooling tube layers, and a degassing and granulation unit downstream of the polymerization towers.
18 g of rubber (Buna HX 500 from Bayer AG having a solution viscosity of 90 mPa s as a 5% strength solution in styrene at 25.degree. C.) are dissolved in 22.5 kg of ethylbenzene, 82.1 kg of styrene and 27.4 kg of acrylonitrile with stirring over the course of 5 hours. The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with rubber solution. 20 1/h of rubber solution are pumped into the polymerization plant. In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate.
The polymerization is continued in the first tower to a solids content of 18% by weight, and in the second tower to a solids content of 28% by weight. To this end, 2.1 g/h of tert-butyl perpivalate are added to the first tower and 4.2 g/h to the second. The stirrer speed in both the polymerization towers is 150 rpm.
In the next two reaction towers, the PSAN matrix is formed by thermal polymerization. In the third polymerization tower, a solids content of 45% by weight is produced at 130.degree. C. and a stirrer speed of 50 rpm. In the fourth polymerization tower, a solids content of 70% by weight is obtained by polymerization at 146.degree. C. with stirring at 10 rpm.
All four polymerization towers are operated at capacity. Tert-dodecyl mercaptan as molecular weight regulator is metered into the second and third polymerization towers in an amount of 34 g/h in each case.
After the fourth polymerization tower, the polymer melt is degassed, cooled and granulated. The throughput of ABS molding material is 14 kg/h.
The product properties of the resultant solution ABS with small particles are as follows:
TABLE 7______________________________________Modulus of elasticity [N/mm.sup.2 ] 2200Notched impact strengthat 23.degree. C. [kJ/m.sup.2 ] 6.0at -40.degree. C. [kJ/m.sup.2 ] 5.0Surface glossCondition A [%] 68.0Condition B [%] 42.0Rubber particle size [.mu.m] 0.35d.sub.50Yellowness index 11.8Viscosity of the [ml/g] 77.0PSAN matrix______________________________________
Examples 17 to 30
Use of Polycyclohexyl (Meth)Acrylate as the Further Polymer
Examples 17 to 20
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6533, (Bayer AG) were dissolved overnight with various amounts of polycyclohexyl (meth)acrylate (viscosity=56 ml/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer,. and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 8.
TABLE 8__________________________________________________________________________Amount ofpolycyclo- Modulus of Notched impact strength Surface gloss Rubber particle hexyl(meth)- elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example acrylate [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________17 -- 2800 2.0 1.8 69 43 0.218 58 2770 2.4 1.8 68 43 0.319 116 2740 2.9 1.9 68 43 0.320 174 2680 8.6 2.9 67 41 0.4__________________________________________________________________________
Examples 21 to 24
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6425 (Bayer AG) were dissolved overnight with various amounts of polycyclohexyl (meth)acrylate (viscosity=55 ml/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 9.
TABLE 9__________________________________________________________________________Amount ofpolycyclo- Modulus of Notched impact strength Surface gloss Rubber particle hexyl(meth)- elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example acrylate [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________21 -- 2800 2.7 1.7 68 43 0.222 58 2720 2.0 1.8 69 42 0.323 116 2750 3.1 2.1 67 42 0.324 174 2670 7.8 2.7 67 42 0.4__________________________________________________________________________
Examples 25 and 26
In each case, 11.5 parts by weight (230 g) of block rubber (Example 25 Buna.RTM. BL 6533; Example 26 Buna BL 6425 from Bayer AG) were dissolved overnight with in each case 116 g of polycyclohexyl (meth)acrylate (viscosity=55 ml/g) in 1236 g of styrene and 412 g of acrylonitrile. 4.0 g of tert-dodecyl mercaptan and 2.0 g of Irganox 1076 were added to the solution. The reaction mixture was heated to 80.degree. C., and 1.34 g of tert-butyl perpivalate were added, so that a polymer conversion of about 12%/hour was achieved with the reaction temperature kept constant. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. After a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer syrup, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 10.
TABLE 10__________________________________________________________________________ Modulus of Notched impact strength Surface gloss Rubber particle Rubber elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Example added [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________25 Buna BL 6533 2760 3.5 1.9 69 42 0.326 Buna BL 6425 2740 3.7 2.1 67 43 0.3__________________________________________________________________________
Examples 27 to 30
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (1/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following four rubber solutions were prepared for the polymerization:
TABLE 11______________________________________Example 27 28 29 30______________________________________Buna BL 6533 [parts by wt.] 11.05 11.05 11.05 11.05 [kg] 27.63 27.63 27.63 27.63Polycyclo- [parts by wt.] -- 3.0 5.0 7.0hexyl(meth)- [kg] -- 7.5 12.5 17.5acrylate(viscosity =55 ml/g)Irganox 1076 [parts by wt.] 0.1 0.1 0.1 0.1 [kg] 0.25 0.25 0.25 0.25Ethylbenzene [parts by wt.] 15.0 15.0 15.0 15.0 [kg] 37.5 37.5 37.5 37.5Styrene [parts by wt.] 55.39 53.14 51.64 50.14 [kg] 138.48 132.85 129.1 125.35Acrylonitrile [parts by wt.] 18.46 17.71 17.21 16.71 [kg] 46.15 44.27 43.02 41.77______________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tert-butyl perpivalate are required:
TABLE 12______________________________________ Exampletert-Butyl perpivalate for 27 28 29 30______________________________________Tower 1 [g/h] 1.35 0.75 0.9 0.85Tower 2 [g/h] 3.15 3.60 3.75 3.90______________________________________
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
TABLE 13______________________________________ Exampletert-Dodecyl mercaptan for 27 28 29 30______________________________________Tower 1 -- -- -- --Tower 2 [g/h] 16 16 16 16Tower 3 [g/h] 50 50 50 50Tower 4 [g/h] -- -- -- --______________________________________
The polymerization was continued in the polymerization towers to the following solids contents:
TABLE 14______________________________________ ExampleSolids content in 27 28 29 30______________________________________Tower 1 [% by wt.] 15 18 19 20.5Tower 2 [% by wt.] 25 28 30 31Tower 3 [% by wt.] 45 45 45 45Tower 4 [% by wt.] 65 65 65 65______________________________________
The stirring speed was 150 rpm in the first tower, 100 rpm in the second, 50 rpm in the third and 10 rpm in the fourth (rpm=revolutions per minute). The polymerization in the third and fourth tower reactors was carried out thermally at 130.degree. and 146.degree. C. respectively. After the fourth polymerization tower, the polymer melt was degassed, cooled and granulated. The throughput of ABS molding material was from 11 to 12 kg/h. Product properties of the solution ABS produced are shown in Table 15.
TABLE 15______________________________________Example 27 28 29 3______________________________________Modulus of elasticity 2620 2600 2550 2600[N/mm.sup.2 ]Notched impactstrengthat 23.degree. C. [kJ/m.sup.2 ] 3.9 6.4 8.3 9.8at -40.degree. C. [kJ/m.sup.2 ] 2.7 3.2 3.4 4.5Surface glossCondition A [%] 70 70 69 68Condition B [%] 46 44 43 43Rubber particle size 0.4 0.4 0.4 0.4d.sub.50 [.mu.m]Yellowness index 9.6 8.2 9.3 9.7Viscosity of the 75.6 76.1 77.1 78.4PSAN matrix [ml/g]______________________________________
Examples 31 to 42
Use of Mixtures of Polystyrene and Polycyclohexyl (Meth)Acrylate as the Further Polymer
Examples 31 to 36
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6533 (Bayer AG; 40% by weight of bonded polystyrene, 30% by weight of block polystyrene) were dissolved overnight with various amounts of polystyrene (viscosity=74 ml/g) and polycyclohexyl (meth)acrylate (viscosity=55 ml/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 16.
TABLE 16__________________________________________________________________________ Amount ofAmount of polycyclo-polystyrene hexyl(meth)- Modulus of Notched impact strength Surface gloss Rubber particle added acrylate elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. [g] [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________31 -- -- 2800 2.0 1.8 69 43 0.232 116 -- 2760 8.6 3.6 68 43 0.433 -- 116 2750 2.9 1.9 68 43 0.334 29 87 2700 3.4 1.9 68 44 0.435 58 58 2720 4.9 2.8 68 43 0.436 87 29 2750 6.8 3.4 68 44 0.4__________________________________________________________________________
Examples 37 to 42
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (l/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following six rubber solutions were prepared for the polymerization:
TABLE 17__________________________________________________________________________Example 37 38 39 40 41 42__________________________________________________________________________Buna BL 6533[parts by wt.] 11.05 11.05 11.05 11.05 11.05 11.05[kg] 27.63 27.63 27.63 27.63 27.63 27.63Polystyrene (vicosity = 74 ml/g)[parts by wt.] 5.0 -- 1.0 2.0 3.0 4.0[kg] 12.5 -- 2.5 5.0 7.5 10.0Polycyclohexyl(meth)-acrylate(viscosity = 55 ml/g)[parts by wt.] -- 5.0 4.0 3.0 2.0 1.0[kg] -- 12.5 10.0 7.5 5.0 2.5Irganox 1076[parts by wt.] 0.1 0.1 0.1 0.1 0.1 0.1[kg] 0.25 0.25 0.25 0.25 0.25 0.25Ethylbenzene[parts by wt.] 15 15 15 15 15 15[kg] 37.5 37.5 37.5 37.5 37.5 37.5Styrene[parts by wt.] 51.64 51.64 51.64 51.64 51.64 51.64[kg] 129.1 129.1 129.1 129.1 129.1 129.1Acrylonitrile[parts by wt.] 17.21 17.21 17.21 17.21 17.21 17.21[kg] 43.0 43.0 43.0 43.0 43.0 43.0__________________________________________________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tert-butyl perpivalate are required:
0.9 g/h for tower 1
3.8 g/h for tower 2
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
16 g/h in tower 2
50 g/h in tower 3
The polymerization was continued in the polymerization towers to the following solids contents:
19% by weight in tower 1
30% by weight in tower 2
45% by weight in tower 3
65% by weight in tower 4
The stirring speed was 150 rpm in the first tower, 100 rpm in the second, 50 rpm in the third and 10 rpm in the fourth (rpm=revolutions per minute). The polymerization in the third and fourth tower reactors was carried out thermally at 130.degree. and 146.degree. C. respectively. After the fourth polymerization tower, the polymer melt was degassed, cooled and granulated. The throughput of ABS molding material was from 11 to 12 kg/h. Product properties of the solution ABS produced are shown in Table 18.
TABLE 18__________________________________________________________________________Example 37 38 39 40 41 42__________________________________________________________________________Modulus of elasticity 2580 2550 2550 2500 2540 2550[N/mm.sup.2 ]Notched impact strengthat 23.degree. C. [kJ/m.sup.2 ] 14.7 8.3 9.1 9.3 10.4 12.1at -40.degree. C. [kJ/m.sup.2 ] 4.7 3.4 3.4 3.6 4.1 4.3Surface glossCondition A [%] 69 69 69 69 68 68Condition B [%] 44 43 43 44 44 44Rubber particle size 0.4 0.4 0.4 0.4 0.4 0.4d.sub.50 [.rho.m]Yellowness indeax 9.5 9.3 9.3 9.6 9.3 9.2Viscosity of the 77.3 77.1 78.5 77.9 78.2 77.9PSAN matrix [ml/g]__________________________________________________________________________
EXAMPLES 43 TO 58
Use of Polyphenylene Ether as the Further Polymer
Examples 43 to 46
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6533 (Bayer AG) were dissolved overnight with various amounts of poly-2,6-dimethyl-1,4-phenylene ether (intrinsic viscosity 0.53 dl/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxidebased suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 19.
TABLE 19__________________________________________________________________________Amount of poly-2,6-dimethyl-1,4-phenylene Modulus of Notched impact strength Surface gloss Rubber particle ether added elasticity Vicat B 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. [g] [N/mm.sup.2 ] [.degree.C.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________43 -- 2800 98.2 2.0 1.8 69 43 0.244 58 2850 99.3 3.0 1.9 68 43 0.345 116 2900 101.4 7.3 3.6 68 44 0.446 174 2900 102.3 8.0 4.2 67 42 0.4__________________________________________________________________________
Examples 47 to 50
In each case, 11.5 parts by weight (230 g) of Buna.RTM. BL 6425 (Bayer AG) were dissolved overnight with various amounts of poly-2,6-dimethyl-1,4-phenylene ether (intrinsic viscosity 0.53 dl/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterisation was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 20.
TABLE 20__________________________________________________________________________Amount of poly-phenylene ether Modulus of Notched impact strength Surface gloss Rubber particle added elasticity Vicat B 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. [g] [N/mm.sup.2 ] [.degree.C.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________47 -- 2800 98.4 2.7 1.7 68 43 0.248 58 2850 99.3 3.1 2.2 68 42 0.349 116 2870 101.1 7.2 3.4 69 44 0.450 174 2900 101.9 7.8 4.3 67 41 0.4__________________________________________________________________________
In each case, 11.5 parts by weight (230 g) of block rubber (Example 51 Buna.RTM. BL 6533; Example 52 Buna BL 6425 from Bayer AG) were dissolved overnight with in each case 116 g of poly-2,6-dimethyl-1,4-phenylene ether (intrinsic viscosity 0.53 dl/g) in 1236 g of styrene and 412 g of acrylonitrile. 4.0 g of tert-dodecyl mercaptan and 2.0 g of Irganox 1076 were added to the solution. The reaction mixture was heated to 80.degree. C., and 1.34 g of tert-butyl perpivalate were added, so that a polymer conversion of about 12%/hour was achieved with the reaction temperature kept constant. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. After a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 21.
TABLE 21__________________________________________________________________________ Modulus of Notched impact strength Surface gloss Rubber particle Rubber elasticity Vicat B 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. added [N/mm.sup.2 ] [.degree.C.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________51 Buna BL 6533 2850 103.1 8.6 4.2 65 41 0.552 Buna BL 6425 2790 102.0 8.3 4.0 63 42 0.5__________________________________________________________________________
Examples 53 and 54
In each case, 11.5 parts by weight (230 g) of block rubber (Example 53 Buna.RTM. BL 6533; Example 54 Buna BL 6425 from Bayer AG) were dissolved overnight with in each case 116 g of poly-2,6-dimethyl-1,4-phenylene ether (intrinsic viscosity 0.53 dl/g) in 1236 g of styrene and 412 g of acrylonitrile. 4.0 g of tert-dodecyl mercaptan and 2.0 g of Irganox 1076 were added to the solution. The reaction mixture was then polymerized thermally at 118.degree. C. with stirring (200 rpm) until a solids content of 40% had been reached. 0.1% dicumyl peroxide was then added to the polymer syrup, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 22.
TABLE 22__________________________________________________________________________ Modulus of Notched impact strength Surface gloss Rubber particle Rubber elasticity Vicat B 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. rubber [N/mm.sup.2 ] [.degree.C.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________53 Buna BL 6533 2850 100.7 7.9 3.7 66 41 0.552 Buna BL 6425 2800 101.5 8.2 3.5 67 41 0.6__________________________________________________________________________
Examples 55 to 58
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (1/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following four rubber solutions were prepared for the polymerization:
TABLE 23______________________________________Example 55 56 57 58______________________________________Buna BL 6533 [parts by wt.] 11.05 11.05 11.05 11.05 [kg] 27.63 27.63 27.63 27.63Poly-2,6-di- [parts by wt.] -- 3.0 5.0 7.0methyl-1,4- [kg] -- 7.5 12.5 17.5phenylene ether(Intrinsic vis-cosity 0.53 dl/g)Irganox 1076 [parts by wt.] 0.1 0.1 0.1 0.1 [kg] 0.25 0.25 0.25 0.25Ethylbenzene [parts by wt.] 15.0 15.0 15.0 15.0 [kg] 37.5 37.5 37.5 37.5Styrene [parts by wt.] 55.39 53.14 51.64 50.14 [kg] 138.40 132.85 129.1 125.35Acrylonitrile [parts by wt.] 18.45 17.71 17.21 16.71 [kg] 46.15 44.27 43.02 41.77______________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tert-butyl perpivalate are required:
TABLE 24______________________________________ Exampletert-Butyl perpivalate for 55 56 57 58______________________________________Tower 1 [g/h] 1.4 0.9 1.1 0.9Tower 2 [g/h] 3.2 3.7 3.8 4.1______________________________________
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
TABLE 25______________________________________ Exampletert-Dodecyl mercaptan for 55 56 57 58______________________________________Tower 1 -- -- -- --Tower 2 [g/h] 16 16 16 16Tower 3 [g/h] 50 50 50 50Tower 4 [g/h] -- -- -- --______________________________________
Examples 59 to 70
Use of Mixtures of Polystyrene and Polyphenylene Ether as the Further Polymer
Examples 59 to 64
In each case, 11.5 parts by weight (230 g) or Buna.RTM. BL 6533 (Bayer AG; 40% by weight of bonded polystyrene, 30% by weight of block polystyrene) were dissolved overnight with various amounts of polystyrene (viscosity=74 ml/g) and poly2,6-dimethyl-1,4-phenylene ether (intrinsic viscosity 0.53 dl/g) in a styrene/acrylonitrile mixture (75/25 parts by weight). Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 26.
TABLE 26__________________________________________________________________________Amount of Amount of Modulus of Notched impact strength Surface gloss Rubber particle polystyrene polyphenylene elasticity 23.degree. C. -40.degree. C. Cond. A Cond. B size d.sub.50Ex. added [g] ether [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________59 -- -- 2800 2.0 1.8 69 43 0.260 116 -- 2760 8.6 3.6 68 43 0.461 -- 116 2900 7.3 3.6 68 44 0.462 29 87 2800 7.4 3.7 67 42 0.463 58 58 2780 7.5 3.7 66 43 0.464 87 29 2780 8.0 3.6 68 44 0.4__________________________________________________________________________
Examples 65 to 70
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (l/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following six rubber solutions were prepared for the polymerization:
TABLE 27__________________________________________________________________________Example 65 66 67 68 69 70__________________________________________________________________________Buna BL 6533 [parts by wt.] 11.05 11.05 11.05 11.05 11.05 11.05 [kg] 27.63 27.63 27.63 27.63 27.63 27.63Polystyrene [parts by wt.] 5.0 -- 1.0 2.0 3.0 4.0(viscosity = [kg] 12.5 -- 2.5 5.0 7.5 10.074 ml/g)Poly-2,6- [parts by wt.] -- 5.0 4.0 3.0 2.0 1.0dimethyl-1,4- [kg] -- 12.5 10.0 7.5 5.0 2.5phenylene ether(Intrinsic viscosity0.53 dl/g)Irganox 1076 [parts by wt.] 0.1 0.1 0.1 0.1 0.1 0.1 [kg] 0.25 0.25 0.25 0.25 0.25 0.25Ethylbenzene [parts by wt.] 15 15 15 15 15 15 [kg] 37.5 37.5 37.5 37.5 37.5 37.5Styrene [parts by wt.] 51.64 51.64 51.64 51.64 51.64 51.64 [kg] 129.1 129.1 129.1 129.1 129.1 129.1Acrylonitrile [parts by wt.] 17.21 17.21 17.21 17.21 17.21 17.21 [kg] 43.0 43.0 43.0 43.0 43.0 43.0__________________________________________________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tert-butyl perpivalate are required:
0.9 g/h for tower 1
3.8 g/h for tower 2
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
16 g/h in tower 2
50 g/h in tower 3
The polymerization was continued in the polymerization towers to the following solids contents:
19% by weight in tower 1
30% by weight in tower 2
45% by weight in tower 3
65% by weight in tower 4
The stirring speed was 150 rpm in the first tower, 100 rpm in the second, 50 rpm in the third and 10 rpm in the fourth (rpm =revolutions per minute). The polymerization in the third and fourth tower reactors was carried out thermally at 130.degree. and 146.degree. C. respectively. After the fourth polymerization tower, the polymer melt was degassed, cooled and granulated. The throughput of ABS molding material was from 11 to 12 kg/h. Product properties of the solution ABS produced are shown in Table 28.
TABLE 28______________________________________Example 65 66 67 68 69 70______________________________________Modulus of 2580 2720 2700 2680 2650 2600elasticity[N/mm.sup.2 ]Notched im-pact strengthat 23.degree. C. 14.7 10.0 10.5 10.7 11.3 12.1[kJ/m.sup.2 ]at -40.degree. C. 4.7 3.9 3.9 4.0 4.0 4.1[kJ/m.sup.2 ]Surface glossCondition A 69 67 67 68 68 68[%]Condition B 44 42 41 42 42 42[%]Rubberparticle sized.sub.50 [.mu.m] 0.4 0.5 0.5 0.5 0.5 0.5Yellowness 9.5 12.4 12.1 11.9 11.5 10.5index______________________________________
Examples 71 to 100
In each case, the amounts indicated in Table 29 of styrene-butadiene block copolymer Buna.RTM. BL 6533, Bayer AG) together with the indicated amounts of polybutadiene (Buna HX 500, Bayer AG) and the polymers mentioned in the claims were dissolved overnight in 1648 g of a styrene-acrylonitrile mixture (75/25 parts by weight).
Each of the solutions was heated to 80.degree. C., and 0.04 part by weight of tert-butyl perpivalate was added, so that a polymer conversion of from about 10 to 12%/hour was achieved with the reaction temperature kept constant. At conversion of 20%, 0.2 part by weight of tert-dodecyl mercaptan was added to each experiment as molecular weight regulator, followed by 0.12 part by weight of Irganox.RTM. 1076 as rubber stabilizer. The stirring speed using an anchor stirrer was set at 200 rpm in the 6 1 steel autoclave. When a solids content of 40% had been reached, 0.1% dicumyl peroxide was added to the polymer, and the mixture was dispersed in an aqueous solution of 1.8 g of sodium phosphate, 18 g of an ethylene oxide-based suspension aid (Luviskol.RTM. K 90 from BASF AG) and 50 g of Ertivinol in 1800 g of water with stirring (300 rpm). Complete conversion was ensured by polymerizing using the temperature program below:
3 hours at 110.degree. C.
3 hours at 130.degree. C.
4 hours at 140.degree. C.
The bead polymer obtained was washed thoroughly with distilled water and dried overnight at 80.degree. C. under reduced pressure.
The characterization was carried out on moldings produced from the dried bead polymer. Properties of the ABS products produced are shown in Table 29.
TABLE 29__________________________________________________________________________ Polycyclo- hexyl meth- Notched Polypheny- acrylate Modulus impact RubberBuna Buna Polystyrene lene ether (visc. = of strength Surface particleBL 6533 HX 500 (visc. = 74 ml/g) (0.53 dl/g) 55 ml/g) elasticity 23.degree. C. -40.degree. C. Cond. A Cond. size d.sub.50Ex. [g] [g] [g] [g] [g] [N/mm.sup.2 ] [kJ/m.sup.2 ] [%] [%] [.mu.m]__________________________________________________________________________71 230 -- 116 -- -- 2760 8.6 3.6 68 43 0.472 184 46 116 -- -- 2700 8.9 4.5 67 42 0.473 138 92 116 -- -- 2600 10.5 6.8 67 40 0.574 230 -- -- 116 -- 2900 7.3 3.6 68 44 0.475 184 46 -- 116 -- 2800 7.5 4.5 67 43 0.476 138 92 -- 116 -- 2720 7.8 5.3 66 42 0.477 230 -- -- -- 116 2750 2.9 1.9 68 43 0.378 184 46 -- -- 116 2680 3.1 2.9 67 42 0.379 138 92 -- -- 116 2640 4.0 3.6 68 41 0.480 230 -- 58 58 -- 2780 7.5 3.6 66 43 0.481 184 46 58 58 -- 2750 7.8 4.2 67 42 0.482 138 92 58 58 -- 2700 9.4 5.8 65 42 0.483 230 -- 58 -- 58 2720 4.9 2.8 68 43 0.484 184 46 58 -- 58 2680 7.3 3.2 67 40 0.485 138 92 58 -- 58 2620 8.2 4.8 66 41 0.4__________________________________________________________________________
Examples 86 to 100
The examples below describe the continuous polymerization in a 4-tower cascade.
The polymerization plant comprises a 250 1 rubber tank, a 250 1 storage tank and four series-connected tower reactors (l/d=1100/220 mm) with internal, horizontal, parallel layers of cooling tubes and a stirrer reaching between the cooling tube layers and a degassing and granulation unit downstream of the polymerization towers.
The following four rubber solutions were prepared for the polymerization:
0.25 kg of Irganox 1076 and the amounts indicated in Table 30 of various rubbers and polymers were dissolved with stirring in 129.1 kg styrene, 43.01 kg of acrylonitrile and 37.5 kg of ethylbenzene.
TABLE 30______________________________________ Buna Buna Polystyrene Polyphen- Polycyclohexyl BL HX (visc.= ylene ether (meth)acrylate 6533 500 74 ml/g) (0.53 dl/g) (visc. = 55 ml/g)Ex. [kg] [g] [kg] [kg] [kg]______________________________________86 27.63 -- 12.5 -- --87 22.10 5.33 12.5 -- --88 19.34 8.29 12.5 -- --89 27.63 -- -- 12.5 --90 22.10 5.53 -- 12.5 --91 19.34 8.29 -- 12.5 --92 27.63 -- -- -- 12.593 22.10 5.53 -- -- 12.594 19.34 8.29 -- -- 12.595 27.63 -- 6.25 6.25 --96 22.10 5.53 6.25 6.25 --97 19.34 8.29 6.25 6.25 --98 27.63 -- 6.25 -- 6.2599 22.10 5.53 6.25 -- 6.25100 19.34 8.29 6.25 -- 6.25______________________________________
The finished rubber solution is pumped into the storage tank, from where the polymerization plant is supplied continuously with 20 1/h of rubber solution.
In the first two polymerization towers, the polymerization is initiated at 80.degree. C. by continuously adding tert-butyl perpivalate. The following amounts of tertbutyl perpivalate are required:
0.9 g/h for tower 1
3.8 g/h for tower 2
The regulator (tert-dodecyl mercaptan) is likewise metered continuously into the four polymerization towers:
16 g/h in tower 1
- g/h in tower 2
50 g/h in tower 3
- g/h in tower 4
The polymerization was continued in the polymerization towers to the following solids contents:
19% by weight in tower 1
30% by weight in tower 2
45% by weight in tower 3
65% by weight in tower 4
The stirring speed was 150 rpm in the first tower, 100 rpm in the second, 50 rpm in the third and 10 rpm in the fourth (rpm=revolutions per minute). The polymerization in the third and fourth tower reactors was carried out thermally at 130.degree. and 146.degree. C. respectively. After the fourth polymerization tower, the polymer melt was degassed, cooled and granulated. The throughput of ABS molding material was from 11 to 12 kg/h. Product properties of the solution ABS produced are shown in Table 31.
TABLE 31__________________________________________________________________________Modulus of Notched impact strength Surface gloss Rubber particle elasticity Vicat B 23.degree. C. -40.degree. C. Cond. A Cond. B Yellowness size d.sub.50Ex. [N/mm.sup.2 ] [.degree.C.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [%] [%] Index [.mu.m]__________________________________________________________________________86 2580 100.5 14.7 4.7 69 44 9.5 0.487 2520 100.3 14.9 6.2 68 43 9.8 0.488 2470 99.9 15.2 8.7 67 43 9.8 0.489 2720 102.1 10.0 3.9 67 42 12.4 0.590 2640 102.0 10.8 4.7 66 42 12.5 0.591 2620 101.4 10.9 5.3 66 42 12.7 0.592 2550 100.5 8.3 3.4 69 43 9.3 0.493 2500 100.2 8.8 4.8 67 42 9.5 0.494 2430 99.8 9.2 5.8 66 41 9.2 0.595 2660 101.2 10.8 4.0 68 42 11.5 0.596 2600 100.8 11.2 5.3 67 41 11.4 0.597 2560 100.5 11.8 7.7 67 42 11.9 0.598 2500 101.4 9.8 3.8 69 44 9.6 0.499 2430 101.2 9.9 5.2 67 41 9.2 0.4100 2400 100.9 10.4 6.1 66 42 9.8 0.5__________________________________________________________________________
The examples below (101 to 131) relate to the admixture of conventional solution ABS with the molding materials according to the invention. This conventional solution ABS is in each case referred to as component A, and the molding materials according to the invention as component B. Components A and B were mixed with one another as granules in the stated weight ratio and jointly melted in the extruder at 280.degree. C., mixed and granulated as a blended product.
EXAMPLES 101 to 106
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 529 C) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of ths PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been prepared in accordance with the procedure of Examples 13-16:
__________________________________________________________________________Rubber particle size d.sub.50 0.4 .mu.mBlock rubber content (Buna BL 6533, Bayer 17.0% by weightAG)Additionally adducted polystyrene 10.7% by weightViscosity of the adducted polystyrene 74.0 ml/gViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weightSurface gloss (condition A) 68.0%Surface gloss (condition B) 43.0%__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17102 -- 100 17.9 5.6 2600 68 43103 5 95 18.7 6.5 2560 67 43104 10 90 19.5 8.1 2500 67 41105 20 80 19.4 8.9 2410 65 42106 30 70 19.3 9.6 2350 61 38__________________________________________________________________________
Examples 107 to 111
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 529 C, Bayer AG) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been produced in accordance with the procedure of Example 58:
__________________________________________________________________________Rubber particle size d.sub.50 0.5 .mu.mBlock rubber content (Buna BL 6533, Bayer AG) 17.0% by weightAdditionally adducted polystyrene 10.7% by weightLimiting viscosity of the adducted polystyrene 0.53 dl/gViscosity of the PSAN matrix 78.9 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17107 -- 100 11.2 4.1 2800 65 41108 5 95 13.4 5.8 2630 64 40109 10 90 14.6 6.3 2570 63 40110 20 80 14.6 7.4 2490 59 37111 30 70 14.8 8.2 2350 54 32__________________________________________________________________________
Examples 112 to 116
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 5Z9C, Bayer AG) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been produced in accordance with the procedure of Example 30:
__________________________________________________________________________Rubber particle size d.sub.50 0.4 .mu.mBlock rubber content (Buna BL 6533, Bayer AG) 17.0% by weightAdditionally adducted polycyclohexyl 10.7% by weightmethacrylateViscosity of the polycyclohexyl methacrylate 55.0 ml/gViscosity of the PSAN matrix 78.4 ml/gStyrene content of ths PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17112 -- 100 9.8 4.5 2600 68 43113 5 95 11.2 5.1 2520 67 42114 10 90 12.9 6.0 2480 67 41115 20 80 13.4 7.1 2390 65 40116 30 70 14.0 7.9 2360 61 37__________________________________________________________________________
Examples 117 to 121
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 529 C, Bayer AG) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been prepared in accordance with the procedure of Example 70:
__________________________________________________________________________Rubber particle size d.sub.50 0.5 .mu.mBlock rubber content (Buna BL 6533, Bayer AG) 17.0% by weightAdditionally adducted polystyrene 6.2% by weightViscosity of the polystyrene 74.0 dl/gAdditionally adducted polyphenylene ether 1.5% by weightLimiting viscosity of the polyphenylene ether 0.53 dl/gViscosity of the PSAN matrix 77.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17117 -- 100 12.1 4.1 2600 68 42118 5 95 12.9 5.0 2540 67 41119 10 90 13.4 5.6 2500 66 40120 20 80 13.4 6.1 2470 65 38121 30 70 14.1 7.6 2430 60 36__________________________________________________________________________
Examples 122 to 126
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 529 C, Bayer AG) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been prepared in accordance with the procedure of Example 42:
__________________________________________________________________________Rubber particle size d.sub.5 0.4 .mu.mBlock rubber content (Buna BL 6533, Bayer AG) 17.0% by weightAdditionally adducted polystyrene 6.2% by weightViscosity of the polystyrene 74.0 ml/gAdditionally adducted polycyclohexyl 1.5% by weightmethacrylateViscosity of the polycyclohexyl methacrylate 55.0 ml/gViscosity of the PSAN matrix 77.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17122 -- 100 12.1 4.3 2550 68 44123 5 95 12.7 5.2 2500 67 42124 10 90 13.3 5.7 2460 66 40125 20 80 13.4 6.4 2410 66 39126 30 70 13.9 7.8 2380 60 36__________________________________________________________________________
Examples 127 to 131
Component A employed was a solution ABS having the following properties:
______________________________________Rubber particle size d.sub.50 4.0 .mu.mRubber content (Buna HX 529 C, Bayer AG) 17.0% by weightViscosity of the PSAN matrix 79.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight______________________________________
Component B was a molding material according to the invention which had been prepared in accordance with the procedure of Example 87:
__________________________________________________________________________Rubber particle size d.sub.50 0.4 .mu.mBlock rubber content (Buna BL 6533, Baysr AG) 16.0% by weightHomopolybutadiene (Buna HX 500, Bayer AG) 3.9% by weightAdditionally adducted polystyrene 9.0% by weightViscosity of the polystyrene 74.0 ml/gViscosity of the PSAN matrix 77.4 ml/gStyrene content of the PSAN matrix 75.0% by weightAcrylonitrile content of the PSAN matrix 25.0% by weight__________________________________________________________________________ Notched impact Modulus SurfaceComponent Component strength of elas- gloss A B 23.degree. C. -40.degree. C. ticity Cond. A Cond. BEx. [parts by wt.] [parts by wt.] [kJ/m.sup.2 ] [kJ/m.sup.2 ] [N/mm.sup.2 ] [%] [%]__________________________________________________________________________101 100 -- 17.7 12.5 1750 49 17127 -- 100 14.9 6.2 2520 68 43128 5 95 16.8 7.2 2490 67 42129 10 90 17.1 7.8 2430 67 40130 20 80 17.0 8.5 2380 65 38131 30 70 17.2 9.3 2340 60 32__________________________________________________________________________

Number	Date	Country	Kind
4017680	Jun 1990	DEX
4030351	Sep 1990	DEX

Number	Name	Date	Kind
4118348	Bennett et al.	Oct 1978
4283511	Ueno et al.	Aug 1981

Number	Date	Country
1117692	Feb 1982	CAX
0111588	Jun 1984	EPX
0167707	Jan 1986	EPX

ABS molding materials

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