Description

The present invention relates to an improved process for the preparation of acrylonitrile- butadiene-styrene (ABS) molding compositions which can be performed at a large scale and leads to advantageous copolymer products.

It is well known that ABS polymer products with high surface quality require a low amount of salt specks on the surface. Salt specks often stem from deposits on the extruder screw of the ABS process, which typically is a single step process to produce ABS materials out of SAN, which is fed, in particular as melt, as granule or powder feed, to the extruder, and rubber coming from precipitation, eventually sintering and centrifugation.

Therefore, some ABS producers add another process step before the ABS extrusion process, which is a rubber drying in a rotary dryer, flash dryer and/or fluid bed dryer. Typically, these pre-drying steps keep the precipitating agent, e.g. magnesium sulphate, within the rubber, however as a finely dispersed powder which does not result in strongly visible surface defects. As a flipside, such a process consumes extra energy and extra assets, hence is more expensive than a single ABS extrusion step using ABS rubber not being pre-dried. Another, very important reason against the rubber pre-drying step is the danger of ignition. Finely dispersed, reactive polymers like polybutadiene are destined to ignite if not properly protected by a large amount of stabilizer and/or protective atmos phere, such as nitrogen. ABS processes not requiring a pre-drying step are in the focus of the present invention.

According to DE-A 2037784, graft rubber moist after centrifuging can be introduced into an SAN melt with evaporation of the water, and a thermoplastic composition containing up to 60% of graft rubber can be obtained. This process requires a relatively large amount of electrical energy, and rubber particles and assistant residues are entrained with the evaporating water and have to be disposed of as special waste. The water stripped off in the form of steam and contaminated by rubber components must be re garded, together with the cooling water required for condensation, as waste water which requires treatment. Moreover, deposits of auxiliaries which may occur in the extruders may contaminate the product. US 5,151,026 and US 5,232,649 are directed to the removal of liquids from solids, in particular from polystyrene.

It is an object of the present invention to provide a process which substantially avoids the stated disadvantages and to provide an effective water removal in the extruder.

It is known from general rubber technology that moist or more or less partially dewatered rubber can be obtained from slurries by pressing out the water mechanically in presses, including screw presses. This is frequently carried out by using apparatuses which have strainer barrels through which the water can flow away in the same way as through a sieve. However, these strainer barrels tend to become blocked. The rubber obtained in this manner, which still has a certain residual moisture content, is then pressed to form bales or is granulated.

Obtaining thermoplastics from an aqueous environment has also led to similar solutions.

Thus, JP S61 53362 (B2, Toshiba, 1986) describes a process for obtaining polymers from polymers which have not been dried or from slurries. An example is the dewatering of a poly-SAN slurry having a solids content of about 40% and a particle size of 0.3 mm in a twin-screw extruder which is provided with two strainer barrels and three devolati lization orifices. The devolatilization is effected under reduced pressure.

JP S59 27776 (B2, Toray, 1984) describes a process for dewatering and plastificating ABS polymers in an extruder, the water being removed in a direction opposite to the transport direction, with subsequent two-stage devolatilization, or, in another embodi ment, by means of a special screw. Such screw designs are available only as expensive specially produced products.

EP-A 0534235 describes the preparation of toughened thermoplastics by incorporating mechanically partially dewatered rubber in a thermoplastic above the softening point of the thermoplastic, the rubber being partially dewatered prior to incorporation in an ex truder and the remaining residual water being removed during the incorporation by de volatilization apparatuses which may be arranged before or after the mixing-in point. This process likewise has the disadvantage that a large amount of water still has to be evaporated, two machines furthermore being required, i.e. a main extruder and a side extruder, and likewise concentrates of only limited use being obtained. US 5,817,266 discloses that the essentially mechanical dewatering of water-moist rubber can be carried out in a single twin-screw continuous kneader and compounder having commercial components to give a compacted, externally dry rubber, compact material, if a machine having a pair of double-thread or preferably triple-thread screws rotating in the same direction is used, to the feed section of which the precipitated, previously de- watered but water-moist rubber is fed, the extruder possessing, in succession in the con veying direction, at least two back-up zones and two associated dewatering orifices and subsequently at least one kneading zone and thereafter at least one devolatilization zone and finally a discharge zone whose orifice may, if required, be closed by a die lip. US 6,165,399 describes a process which permits the preparation of an impact-resistant thermoplastic comprising at least one water-moist elastomer component and one or more thermoplastic, brittle polymers in a technically simple manner, as far as possible in one process step. It further describes a process by means of which polymer blends can be prepared in one process step by mixing of the thermoplastic with further polymers. In particular, a process is described which has the flexibility to permit the blending of even the most different polymers with one another and also the blending of greatly varying quantity mixing ratios of thermoplastic polymer and elastomer component, which give the toughened thermoplastics having low to very high rubber contents, and which at the same time is reliable in operation. However, the document does not disclose how to effectively reduce the salt concentration.

According to WO-A1 2015/000873, a thermoplastic compositions can be prepared with reduced salt concentration, which have a smooth surface with low amount of visible salt specks.

However, it is not only important to reduce salt specks in order to achieve a high surface quality. In patent literature there are numerous documents showing that large ABS par ticles, especially those in mass-ABS, have a negative impact on surface quality, espe cially on gloss. The large rubber particles on the surface scatter the light and therefore, the respective ABS part appears dull / gloss reduced. The invention relates to a process for a producing thermoplastic ABS molding composi tion, comprising 30 - 80 wt.-%, based on the weight of the molding composition, of at least one thermoplastic copolymer matrix A (component A), with components based on the dry weight of A:

A1 : 50 - 80 wt.-% of styrene and/or a-methylstyrene and/or p-methyl-styrene A2: 20 - 40 wt.-% of (meth)acrylonitrile, in particular acrylonitrile, A3: 0 - 20 wt.-% of one or more co-polymerizable monomers, preferably Ci-

Cs-acrylates and/or methyl-methacrylate,

19.99 - 60 wt.-%, based on the weight of the molding composition, of at least one ABS-copolymer B (component B), with components based on the dry weight of B: B1 : 30 - 90 wt.-% of one or more rubber component(s) as graft basis, having a glass transition temperature of less than 0°C, made from, based on the dry weight of B1,

B11 : 50 - 100 wt.-% of one or more of butadiene or isoprene, in partic ular butadiene, and B12: optionally, 0 - 50 wt.-% of further monomers, in particular from the group of styrene, methyl methacrylate, DCPA, butanediol diacrylate, ethylene glycol diacryate and tris-allyl-cyanurate; preferably styrene,

B2: 10 - 70 wt.-% of one or more graft stages, polymerized after the graft basis, with, based on the dry weight of B2, B21 : 50 - 90 wt.-% of styrene, a-methylstyrene and/or p-methyl-styrene,

B22: 5 - 40 wt.- % of (meth)acrylonitrile, in particular acrylonitrile,

B23: 0 - 40 wt.-% of one or more co-polymerizable monomers, prefer ably Ci-Cs-acrylates and/or methyl-methacrylate, 0 - 40 wt.-%, in particular 0 - 20 wt.-%, based on the weight of the molding compo sition, of one or more polymers C (component C) selected from the group of poly carbonates, polyesters, polyestercarbonates and polyamides,

0.01 - 20 wt.-%, in particular 0.3 - 5 wt.-%, based on the weight of the molding composition, of one or more additives D (component D), in particular from the group of thermal stabilizers, UV stabilizers, dispersants, pigments, lubricants, dye stuff, colorants, inorganic fillers and organic fillers, where the process for producing the thermoplastic ABS molding composition comprises (or consists of) the following steps: a) mixing the components A, B and D and optionally C, by using at least one ex truder comprising: a first feeding zone FZ1 , in which component B and at least part of component D are fed to the at least one extruder; a preheating zone PZ, in which component B is heated to a temperature of 100°C or below; a mechanical dewatering zone DZ, in which component B, having a water content of more than 20 wt.-%, in particular more than 25 wt.-%, based on the total weight of component B, is mechanically dewatered at a dewatering temperature T _dw in a range from 50°C to 200°C, preferably from 50°C to 180°C, more preferably from 50°C to 160°C, more preferably from 50°C to 120°C, more preferably from 50°C to 100°C, whereby the water content in component B is reduced by 10 wt.-% to 90 wt.-%, based on the water comprised in component B when fed to the first feeding zone FZ1, and wherein: the mechanical dewatering zone DZ comprises at least one dewatering aperture, in particular for liquid water; in a second feeding zone FZ2, at least part of component A and optionally part of component D are fed, preferably in melt and/or solid form, more preferably in melt form, to the at least one extruder, where component A is brought in contact with component B; in at least one degassing zone DG, preferably in two or more degassing zones DG, component A and/or component B are degassed; in an optional third feeding zone FZ3, part of component A, component C and/or part of component D are optionally fed to the extruder together or separately from one another; and b) removing the thermoplastic ABS molding composition from a discharge zone CZ of the extruder.

Components A, B and D and optionally C are mixed in the at least one extruder and the thermoplastic ABS molding composition is produced. Many different thermoplastic ABS molding compositions can be produced by the process according to the present inven tion. At least two extruders can be operated in parallel, wherein preferably each extruder comprises a first feeding zone FZ1, a preheating zone PZ, a mechanical dewatering zone DZ, a second feeding zone FZ2, at least one degassing zone DG, optionally a third feeding zone FZ3 and a discharge zone CZ. Further, the at least one extruder can com prise one or more first feeding zones FZ1, one or more preheating zones PZ, one or more mechanical dewatering zones DZ, one or more second feeding zones FZ2, one or more degassing zones DG, optionally one or more third feeding zones FZ3 and one or more discharge zones CZ. Up to ten, preferably up to five, feeding zones are possible. Preferably, the zones of the at least one extruder are arranged in the given order in downstream conveying direction. In particular, the preheating zone PZ is located up stream of the mechanical dewatering zone DZ and directly followed in conveying direc tion by the mechanical dewatering zone DZ. Preferably, each of the one or more me chanical dewatering zone DZ comprises at least one dewatering aperture. More prefer ably, each of the one or more mechanical dewatering zone DZ comprises exactly one dewatering aperture.

In a preferred embodiment, the at least one extruder comprises two or more degassing zones DG and in the two or more degassing zones DG component A and/or component B are degassed, wherein at least one of the two or more degassing zones DG is operated at a first degassing pressure P _di , at least a further one of the two or more degassing zones DG is operated at a second degassing pressure P _d 2 and the first degassing pres sure P _di is higher than the second degassing pressure P _d 2 and wherein the first degas sing pressure P _di is higher than 0.8 bar absolute and the second degassing pressure P _d 2 is lower than 1.2 bar absolute. In particular, the first degassing pressure P _di is applied upstream of the second degassing pressure P _d 2.

In a more preferred embodiment, the at least one extruder comprises a first degassing zone DG1 and a second degassing zone DG2 and in the first degassing zone DG1 and the second degassing zone DG2 component A and/or component B are degassed, wherein the first degassing zone DG1 is operated at a first degassing pressure P _e n , the second degassing zone DG2 is operated at a second degassing pressure P _d 2 and the first degassing pressure P _di is higher than the second degassing pressure P _d 2 and wherein the first degassing pressure P _di is higher than 0.8 bar absolute and the second degassing pressure P _d 2 is lower than 1.2 bar absolute. In particular, the first degassing zone DG1 is located upstream of the second degassing zone DG2.

In the entry of the at least one extruder in the first feeding zone FZ1 component B is preferably present in a premix with at least part of component D. The part of component D, which is fed to the at least one extruder in the first feeding zone FZ1 comprises or consists of in particular a stabilizer such as a thermal stabilizer and/or UV stabilizer.

In the preheating zone PZ, the temperature of component B and part of component D is raised. Preferably, component B is heated to a maximum of 200°C, more preferably of 180°C, even more preferably of 160°C, even more preferably of 120°C and even more preferably of 100°C. Preferably, component B is heated to a temperature of at least 30°C, more preferably at least 45°C in the preheating zone PZ. The preheating can be achieved by active heating and/or by shear energy of extruder elements, preferably by shear en- ergy of extruder elements. In a preferred embodiment, the preheating zone PZ comprises at least one kneading block and/or counterflow conveying element.

Due to the at least one kneading block and/or at least one counterflow conveying ele ment, higher shear energy is introduced compared to conveying elements, which heats component B to release the water more easily in the subsequent mechanical dewatering zone DZ. Preferably, the preheating zone PZ comprises at least one kneading block and/or at least one counterflow conveying element, which are arranged upstream, refer ring to the conveying direction, of the mechanical dewatering zone DZ, in particular up stream, referring to the conveying direction, of the at least one dewatering aperture, which can also be referred to as dewatering orifice or dewatering opening.

In a preferred embodiment, a conveying element is arranged between the preheating zone PZ and the mechanical dewatering zone DZ and/or forms a transition from the preheating zone PZ to the mechanical dewatering zone DZ. In particular, the preheating zone PZ and the mechanical dewatering zone DZ are separated from each other by at least one conveying element.

It is preferred that the preheating zone PZ is free of dewatering and/or degassing aper- tures, which can also be referred to as orifices or openings. Further preferably, the pre heating zone PZ comprises or consists of closed, in particular in radial direction, barrels.

Due the preheating of component B, the subsequent mechanical dewatering is improved as the preheated component B is easier releasing the water. If component B is too cold in the mechanical dewatering zone DZ, significant amounts of water are hold back in the component B and cannot be removed in the mechanical dewatering zone. The preheat ing and mechanical dewatering is preferably supported by an increased pressure.

In the mechanical dewatering zone DZ, the water content in component B is reduced from more than 20 wt.-%, in particular more than 25 wt.-%, based on the total weight of component B, by 10 wt.-% to 90 wt.-%, based on the water comprised in component B. The total weight of component B denotes the sum of the dry weight of component B and the weight of the water comprised therein. Water is removed from component B through the at least one dewatering aperture, in particular in a liquid state. In order to determine the water content of component B in and/or after the mechanical dewatering zone DZ, the amount of water withdrawn in the mechanical dewatering zone DZ can be measured. The temperature of component B can be further enhanced in the mechanical dewatering zone DZ. The mechanical de- watering zone DZ serves for dewatering component B and a part of residual water con tained in component B is mechanically removed (squeezing).

The mechanical dewatering zone DZ preferably contains at least a first retarding ele ment, kneading block and/or counterflow conveying element and at least one dewatering aperture, which can also be referred to as dewatering orifice, which is present upstream of the first retarding element, kneading block and/or counterflow conveying element, pref erably by a distance corresponding to at least one screw diameter Ds. The material, here in particular component B, is typically conveyed against at least one retarding element, kneading block and/or counterflow conveying element, which acts as an obstacle and is present, as a rule, at the end of the mechanical dewatering zone DZ. This builds up a pressure, which forces water out of component B. The pressure can be built up by dif ferent arrangements of screw elements, kneading elements or other retarding elements. Examples of possible retarding elements are given in US 6,165,399 and are included in this patent. Preferably, sealings are arranged between the screw elements in the me chanical dewatering zone DZ.

Preferably, a dewatering pressure P _dw in the mechanical dewatering zone DZ is at least 10 bar.

However, in addition to US 6,165,399, the dewatering apertures used can comprise screens or mesh filters, but preferably the dewatering apertures are not Seiher housings. The temperature of the outcoming water is in general from 20°C to 99°C, preferably from 25°C to 80°C, measured at the at least one dewatering aperture. In the case, where at least two dewatering apertures are present in at least one dewatering zone DZ, the tem perature of the outcoming water at a first dewatering aperture is preferably at least 10°C lower, more preferably at least 20°C lower, than the temperature of the outcoming water at a second dewatering aperture, wherein the first dewatering aperture is located up stream of the second dewatering aperture.

In a further particular embodiment, one or more further plastication sections PS are pre sent before, thus upstream of, the second feeding zone FZ2, in which component A, preferably in melt and/or solid form, is fed in, ie. downstream of a last mechanical de watering zone DZ. In this plastication section PS, the very substantially dewatered com ponent B, for example the rubber powder, is first homogenized and plasticated, in par ticular alone. Component A and, if required, components C and/or D are accordingly introduced into a viscous melt of component B in this embodiment. In this case, a possi ble further plastication section PS downstream of the mixing of component A serves merely for homogenizing the mixture of the components already present in the plastic state.

Component A is partly or completely fed to the at least one extruder in the second feeding zone FZ2, where component A is in particular mixed with component B already present in the at least one extruder. The at least part of component A fed to the at least one extruder in the second feeding zone FZ2 can comprise part of component D. The second feeding zone FZ2 is preferably directly or indirectly followed by the at least one degassing zone DG, in particular the first degassing zone DG1 and the second de gassing zone DG2, each of which is provided with one or more degassing apertures. In the at least one degassing zone DG, the remaining residual water which was not me- chanically removed in the mechanical dewatering zone DZ is partially or completely re moved. Because the temperatures of the present components are here usually above 100°C, the water generally leaves the at least one extruder mainly as steam. The energy required for evaporating the water has, as a rule, already been introduced into the plas- tication sections PS. However, it is also possible to supply the energy in a conventional manner by heating the extruder barrel.

The at least one degassing aperture is preferably present at the top of the extruder. A lateral arrangement (on one side or both sides of the extruder) of the at least one degas sing aperture is like-wise preferred.

Part of component A can further be fed to the at least one extruder in the third feeding zone FZ3, where also component C can be fed to the at least one extruder. In addition, the part of component A fed in the third feeding zone FZ3 can comprise part of compo nent D. Components A, C and D can be fed in the third feeding zone FZ3 together or separately from one another.

In a preferred embodiment, the third feeding zone FZ3 is arranged between the at least one degassing zone DG, in particular a last of the at least one degassing zone DG, and the discharge zone CZ, thus the at least one degassing zone DG is preferably positioned between the second feeding zone FZ2 and the third feeding zone FZ3. Alternatively, the third feeding zone FZ3 can be arranged between two of the two or more degassing zones DG, in particular between the first degassing zone DG1 and the second degassing zone DG2. The total amount of component D is preferably the sum of the parts of D, which are fed in the first feeding zone FZ1 , optionally the second feeding zone FZ2 and optionally the third feeding zone FZ3. The total amount of component A is preferably the sum of the at least part of A, which is fed in the second feeding zone FZ2 and optionally the part of A, which is fed in the third feeding zone FZ3.

The total amount of component B is preferably fed to the at least one extruder in the first feeding zone FZ1.

In the discharge zone CZ, the thermoplastic ABS molding composition, comprising com ponents A, B, D and optionally C, is conveyed out of the at least one extruder. The dis charge zone CZ can comprise further conveying elements. The discharge zone CZ is preferably the last section of the extruder and preferably comprises or consists of a con veying screw and a closed barrel part, which ends into a defined discharge orifice. The discharge zone CZ is preferably heated.

The water content of the thermoplastic ABS molding composition in the discharge zone CZ is as a rule from 0.05 wt.-% to 2 wt.-%, in particular from 0.05 wt.-% to 1.5 wt.-%, based on the dry thermoplastic ABS molding composition, present in the discharge zone CZ. The temperature of the thermoplastic ABS molding composition coming out of the discharge orifice is as a rule from 150°C to 350°C, preferably from 180°C to 330°C, de pending on the type of polymers used.

Component B, when fed to the at least one extruder, is in particular a moist solid. Com ponent B is fed to the first feeding zone FZ1 as a substantially wet component B. Pref erably, component B is fed to the first feeding zone FZ1 with a water content of not more than 70 wt.-%, more preferably not more than 50 wt.-%, based on the total weight of component B, and where component B has a grafting degree of not more than 60%, more preferably not more than 50%, in particular not more than 45%, wherein the grafting degree is the percentage ratio of the weight of component B2 related to the sum of the weight of components B1 and B2, respectively present in component B.

Preferably, the weight-based particle size distribution of the rubber particles in compo nent B has >90 wt.-% of all rubber particles in the range of 50 nm to 950 nm.

Preferably, component B has a bimodal weight-based particle size distribution with par ticles <70 wt.-%, more preferably <65 wt.-%, of all rubber particles in ^nm to 150 nm. More preferably, component B has a bimodal weight-based particle size dis tribution and the rubber B1 is made from butadiene and optionally 1 wt.-% to 20 wt.-%, based on the weight of the rubber B1 , of further monomers, in particular from the group of styrene, methyl methacrylate, DCPA, butanediol diacrylate, ethylene glycol diacrylate and tris-allyl-cyanurate, preferably styrene.

Preferably, component A has a content of acrylonitrile of less than 40 wt.-%, more pref erably less than 36 wt.-%, based on the dry weight of component A, and the rubber B1 of component B is made of butadiene or of butadiene and styrene.

Preferably, the graft basis B1 particles in component B have a gel content of 60% or more, more preferably 65% or more, even more preferably 70% or more, and a swelling index of 45 or less, more preferably 40 or less. In a preferred embodiment, the graft basis B1 particles in component B have a gel content of 90% or less, more preferably 85% or less and the swelling index is 15 or more, more preferably 20 or more. It was found that with this gel content in combination with the given swelling index, improved surface qual ities for the thermoplastic ABS molding composition, based on smaller emulsion parti cles, are achieved. In particular, dull / gloss reduced surfaces under certain circum stances are avoided, even though when subjected to a shear rate typically observed in injection molding and extrusion.

The thermoplastic ABS molding composition prepared according to the process of the invention leads to molded parts with low Yellowness Index and low content of volatile components (VOC).

Preferably, the graft rubber particles in component B have been prepared by using either an inorganic peroxide, in particular persulfate, or an organic compound, in particular an organic peroxide or azobisisobutyronitrile, as initiator. Alternatively, the graft rubber par ticles in component B can be prepared without addition of an initiator.

The use of a melt pump, of an extruder (ie. side extruder) or of a metering pump as a metering means for the components C and/or D is preferred. Preferably, the second feeding zone FZ2 and/or the third feeding zone FZ3 comprise at least one side extruder attached thereto.

Preferably, the third feeding zone FZ3 comprises at least one liquid inlet and at least one mixing element downstream of the liquid inlet. Preferably, at least one dewatering aperture of the mechanical dewatering zone DZ com prises at least one stuffer screw with preferably two shafts. Preferably, the at least one stuffer screw comprises screw elements with U-shape. With the U-shaped form of the screw element an improved dewatering performance can be achieved as less water is retained as compared to for example closely intermeshing el ements. Preferably, at least one dewatering aperture of the mechanical dewatering zone DZ is equipped with a metal-wire-mesh composite sheet (MWC), a finely perforated metal sheet, and/or a slit diaphragm.

Preferably, the mechanical dewatering zone DZ comprises one or more elements from the group of screw elements, extruder shafts, barrels and liners of barrels, where at least one element is made of a stainless steel material, where the stainless steel material comprises more than 10 wt.-% of chrome (Cr), based on the stainless steel material. Preferably, the stainless steel material further comprises at least one metal or transition metal from the group consisting of vanadium (V), copper (Cu), nickel (Ni) and molyb- denum (Mo).

More preferably, the sum of the weight of Cr and optionally V, Cu, Ni and/or Mo, in par ticular the sum of the weight of Cr and optionally V, Cu and/or Ni, comprised in the stain less steel material is more than 15 wt.-%, based on the total weight of the stainless steel material. Due to the harsh conditions in the mechanical dewatering zone DZ originating from the presence of aqueous salt solutions at high temperatures, the defined stainless steel material leads to longer life times of the extruder.

With the chosen material, the runtime of the equipment for the process is elongated, in particular the lifetime of the extruder under the respective process conditions is im proved.

The term weight of the molding composition corresponds to the weight of the produced thermoplastic ABS molding composition. Examples for component B, based on SAN-grafted polybutadiene are described, for ex ample, in EP-A 0 258 741 and EP-A 0 062 901. The at least one ABS-copolymer B (component B) can be constructed from: B1 : 40 to 85 wt.-%, based on the dry weight of B, of the graft basis B1 obtainable by (a) polymerizing: (B11): 0 to 21 wt.-%, based on the dry weight of B1, of at least one vinylaromatic monomer, in particular styrene, and B12: 79 to 100 wt.-%, based on the dry weight of B1 , of one or more of butadiene or isoprene, where (B11) and (B12) sum to 100 wt.-%; and

(b) agglomerating component B1 by adding (BC): 0.01 to 5 parts by weight, based on 100 parts by weight of component B1, in each case based on the solids content, corre sponding to the dry weight, of an agglomerating copolymer (BC) of: (BC1): 80 to 99.9 wt.-% of one or more hydrophobic Ci to C12 alkyl acrylates or Ci to C12 alkyl methacry lates and (BC2): 0.1 to 20 wt.-% of one or more hydrophilic comonomers selected from the group consisting of methacrylamide, acrylamide, methylacrylamide, ethylacrylamide and n-butylacrylamide, where (BC1) and (BC2) sum to 100 wt.-%; and

B2: 15 to 60 wt.-%, based on the dry weight of B, of one or more graft stages obtainable by reacting the agglomerated component B1 with a mixture of: (B21) 70 to 90 wt.-%, based on the dry weight of B2, of styrene and/or a-methylstyrene, in particular styrene, and (B22) 10 to 30 wt.-%, based on the dry weight of B2, of acrylonitrile and/or methyl methacrylate, in particular acrylonitrile, where component B1 and component B2 sum to 100 wt.-% in total.

The agglomerating copolymer (BC) has preferably a (i) weight median particles size D50 value of from 100 to 150 nm and (ii) the agglomerated component B1 has preferably a bimodal particle size distribution of a fraction x) of nonagglomerated particles having a D50 value of not more than 150 nm, more preferably in the range of from 80 to 120 nm and a fraction y) of agglomerated particles having a D50 value in the range of from 300 to 550 nm. The weight median particle size D50 is the diameter which divides the population exactly into two equal parts. 50 wt.-% of the particles are larger than the weight median particle size D50 and 50 wt.-% are smaller. The particle size distribution, the weight mean average particle diameter Dw and the weight median particle size D50 value can be determined using a ultracentrifuge (for example as described in W. Scholtan, H. Lange: Kolloid Z. u. Z. Polymere 250, pp. 782 to 796 (1972)) or a disc centrifuge (for example DC 24000 by CPS Instruments Inc.). The weight mean average particle diameter Dw (or De Broucker mean particle diameter) is an average size based on unit weight of particle. The definition for the weight mean average particle size diameter Dw can be given as: Dw = sum ( n, ^* Di ⁴ ) / sum ( n, ^* D, ³ ) n,: number of particles with the diameter D,

See G. Lagaly, O. Schulz, R. Ziemehl: Dispersionen und Emulsionen: Eine Einfuhrung in die Kolloidik feinverteilter Stoffe einschlieBlich der Tonminerale, Darmstadt, Steinkopf- Verlag 1997, ISBN 3-7985-1087-3, page 282, formula 8.3b. The summation is normally performed from the smallest to largest diameter of the particles size distribution. It should be mentioned that for a particles size distribution of particles with the same density the volume mean average particle size diameter Dv is equal to the weight mean average particle size diameter Dw.

Graft basis B1

Component B12 employed may be for example isoprene and/or butadiene, preferably butadiene.

Component B11 employed may be a -methylstyrene and/or styrene, preferably only sty rene.

The graft basis B1 generally employs component B12 in an amount of from 79 to 100 wt.-%, preferably 90 to 98 wt.-%, and component B11 in an amount of from 0 to 21 wt-

%, preferably 2 to 10 wt.-%.

Preference is given to a graft basis B1 composed of butadiene and styrene in the above- mentioned composition. B1 as graft basis has preferably a glass transition temperature of less than 0°C measured by dynamical mechanical analysis with an applied frequency of 1 Hz.

The graft basis B1 is preferably produced by polymerizing the components B12 and op tionally B11 in aqueous emulsion according to processes known to those skilled in the art generally at temperatures of 20°C to 100°C, preferably 50°C to 90°C and at pressures between 0 and 18, preferably 0 and 15 bar(g) (gauge pressure). The polymerization may employ the customary emulsifiers such as alkali metal salts of alkyl- or arylsulfonic acids, alkyl sulfates, fatty alcohol sulfonates, salts of higher fatty acids comprising 10 to 30 carbon atoms or resin soaps. It is preferable to employ the sodium or potassium salts of alkylsulfonates or fatty acids comprising 10 to 18 carbon atoms. The emulsifiers are fa vorably employed in an amount of from 0.5 to 5 wt.-%, preferably from 0.5 to 2 wt.-%, based on the total weight of the monomers used for the graft basis B1. A water/monomer ratio of from 2:1 to 0.7:1 is generally employed.

Polymerization initiators employed are in particular the commonly used persulfates such as sodium or potassium peroxodisulfate, or mixtures thereof, though redox systems are also suitable. The amounts of initiators, for example 0.1 to 1 wt.-%, based on the total weight of the monomers used for producing the graft basis B1, depends on the molar weight desired.

Polymerization assistants that may be employed include preferably the customary buffer substances used to adjust the pH to the preferred range of from 6 to 10, for example sodium bicarbonate, sodium carbonate and sodium pyrophosphate, or mixtures thereof and also generally 0.1 to 3 wt.-% of a molecular weight regulator such as mercaptan, e.g. tert.-dodecylmercaptan or n-dodecyclmercaptan, terpinol or dimeric a-methylsty- rene. The molecular weight regulators can be added at once at the beginning of the polymerization or in several portions at the beginning and/or during the polymerization or continuously from the beginning until the end of the polymerization with constant or variable feed rates.

The feeding time for the components B12 and optionally B11 is at least 6 hours, preferred 8 hours, and less than 20 hours, preferred less than 16 hours. The solids content in the aqueous dispersion after the polymerization is preferably from 25 to 50 wt.-%, particularly preferably from 30 to 45 wt.-%.

The precise polymerization conditions, in particular type, feed modus and amount of the emulsifier are preferably selected within the abovementioned ranges such that the graft basis B1 has a D50 value as defined herein below, as is described, for example, in DE- A1 102005022632, examples S11 to S13, or for example WO-A1 2014/170406, exam ples A1 to A3. The graft basis B1 generally has a D50 value of not more than 150 nm, preferably in the range of from 80 to 120 nm, particularly preferably 80 to 110 nm. Small particle sizes enhance the biaxial impact strength of the thermoplastic ABS molding composition. The polydispersity U of the particles size distribution which is defined in this context as U = (D90 - D ₁₀ )/D ₅ O of the graft basis B1 is preferably less than 0.35, in particular less than

0.33. Preference is given to a graft substrate having a D50 value in the range of from 80 to 120 nm and a polydispersity U of less than 0.35, in particular less than 0.33. D10 and D90 values are defined as follows: D10 is the diameter at which 10 wt.-% of the particles are smaller than this value and D90 is the diameter at which 90 wt.-% of the particles are smaller than this value.

Agglomerating Copolymer (BC)

Agglomeration of the graft basis B1 is preferably achieved by employing an agglomerat- ing copolymer BC, a copolymer of (BC1) one or more hydrophobic Ci to C12 alkyl acry lates or Ci to C12 alkyl methacrylates and (BC2) one or more hydrophilic comonomers selected from the group consisting of methacrylamide, acrylamide, methylacrylamide, ethylacrylamide and n-butylacrylamide. The agglomerating component (BC) has prefer ably a D50 value of from 100 to 150 nm.

The composition of the copolymer (BC) is generally as follows:

(BC1) 80 to 99.9, preferably 90 to 99.9 wt.-% of the component (BC1) and (BC2) 0.1 to 20, preferably 0.1 to 10 wt.-% of the component (BC2), where the sum of monomers (BC1) and (BC2) is precisely 100 wt.-%.

The monomers (BC1) employed are preferably C1-C4 alkyl acrylates or else mixtures thereof. The monomer (BC1) is preferably ethyl acrylate. The monomer (BC2) is prefer ably methacrylamide.

Preference is given to a copolymer BC of ethyl acrylate and methacrylamide. Particular preference is given to a copolymer BC of 92 to 98 wt.-%, based on the total applied monomers in BC, corresponding the sum of the dry weight of components BC1 and BC2, of ethyl acrylate and 2 to 8 wt.-%, based on the total applied monomers in BC, of meth- acrylamide. Very particular preference is given to a copolymer BC of 93 to 97 wt.-%, based on the total applied monomers in BC, of ethyl acrylate and 3 to 7 wt.-%, based on the total applied monomers in BC, of methacrylamide.

Preference is given to copolymers BC having a weight-average molar mass (Mw) of from 30,000 to 300,000 g/mol, measured by gel permeations chromatography (GPC) with tet- rahydrofuran as solvent.

Particular preference is given to a copolymer BC described hereinabove and having a core constructed from at least one of the hydrophobic monomers cited as component BC1 , preferably from ethyl acrylate, wherein this core is covered with a copolymer con structed from the components BC1 and BC2.

It is particularly preferable when the copolymer BC is constructed from (BC11) 5 to 20 wt.-%, based on the total amount of the copolymer BC, of one or more hydrophobic monomers (BC1), preferably ethyl acrylate, as the core and (BC12) 80 to 95 wt.-%, based on the total amount of the copolymer BC, of a shell polymerized onto the core and constructed from (BC121) 93 to 97 wt.-%, based on the total amount of the monomers forming the shell, of at least one hydrophobic monomer (BC1), preferably ethyl acrylate and (BC122) 3 to 7 wt.-%, based on the total amount of the monomers forming the shell, of at least one hydrophilic monomer (BC2), preferably methacrylamide.

It is very particularly preferable when the copolymer BC is constructed from (BC11) 8 to 12 wt.-%, based on the total amount of the copolymer BC, of ethyl acrylate as the core, and (BC12) 88 to 92 wt.-%, based on the total amount of the copolymer BC, of a shell polymerized onto the core and constructed from (BC121) 93 to 97 wt.-%, based on the total amount of the monomers forming the shell, of ethyl acrylate and (BC122) 3 to 7 wt- %, based on the total amount of the monomers forming the shell, of methacrylamide.

Preference is accordingly given to a process for producing the agglomerating copolymer BC comprising monomer components BC1 and BC2, in particular ethyl acrylate and methacrylamide, said process comprising initially polymerizing a portion of BC1, in par ticular ethyl acrylate, (formation of the substrate) and subsequently adding the remaining portion of BC1 , in particular ethyl acrylate, and BC2, in particular methacrylamide, as a mixture. The portions correspond preferably to the ratios described hereinabove. The production of the agglomerating copolymer BC employed is carried out according to processes known to those skilled in the art, particularly advantageously by emulsion polymerization, and the emulsifiers cited hereinabove for the graft basis B1 may be em ployed. It is preferable to employ the sodium and potassium salts of alkylsulfonates com- prising 10 to 18 carbon atoms. The emulsifiers are advantageously employed in an amount of from 0.5 to 5 wt.-%, preferably 0.5 to 2 wt.-%, based on the total monomer content of the copolymer BC.

Polymerization initiators employed are in particular the commonly used persulfates such as sodium or potassium peroxodisulfate, or mixtures thereof, though redox systems are also suitable. The amounts of initiators, for example 0.1 to 1 wt.-%, based on the total weight of the monomers used for producing the copolymer BC, depends on the molar weight desired. Polymerization assistants that may be employed include preferably the customary buffer substances and/or basic substances used to adjust the pH to the preferred range of from 4 to 10. As buffer substances can be used for example sodium bicarbonate, sodium carbonate and sodium pyrophosphate, or mixtures thereof; as basic substances can be used for example sodium hydroxide, potassium hydroxide, or mixtures thereof. If desired molecular weight regulator such as mercaptan, e.g. tert.-dodecylmercaptan or n-dode- cy cl mercaptan, terpinol or dimeric a-methylstyrene can be used. The molecular weight regulators can be added at once at the beginning of the polymerization or in several portions at the beginning and/or during the polymerization or continuously from the be ginning until the end of the polymerization with constant or variable feed rates.

The copolymer BC is preferably produced by aqueous emulsion polymerization accord ing to processes known to those skilled in the art generally at temperatures of 20°C to 100°C, preferably 50°C to 90°C and at pressures between 0 and 6 bar(g), preferably 0 and 3 bar(g) (gauge pressure). The solids content in the aqueous dispersion after the polymerization is preferably 3 to 60 wt.-%, more preferably from 7 to 50 wt.-%, particu larly preferably from 10 to 45 wt.-%.

The process for producing the core/shell copolymers BC described hereinabove is an emulsion polymerization comprising the steps of: (I) emulsion polymerizing at least one monomer BC1 as defined hereinabove in a first step and (II) adding a monomer mixture comprising monomers (BC1+BC2) in a further step, wherein the steps (I) and (II) are performed in the presence of at least one emulsifier which is employed in an amount of from 0.05 to 1.0 wt.-%, preferably 0.05 to 0.5 wt.-%, in step (I) and in an amount of from 0.45 to 4.5 wt.-%, preferably 0.45 to 1.8 wt.-%, in step (II), in each case based on the total monomer content.

The copolymer BC is preferably employed as an aqueous dispersion, as a so-called ag glomeration latex. The agglomerating copolymer BC can have different values of the polydispersity U of the particles size distribution, e.g. the particles size distribution can be broad with values of polydispersity U larger than 0.27 or narrow with a polydispersity U of 0.27 or less. Preferably the polydispersity U is broad and in the range of larger than 0.27. In another embodiment preferably the polydispersity U is narrow and in the range of from 0.27 to 0.20, in particular in the range of from 0.25 to 0.21.

The agglomerating copolymer BC preferably has a D50 value of from 110 to 150 nm, particularly preferably from 115 to 140 nm.

A preferred embodiment employs an agglomerating copolymer BC having a polydisper sity U of 0.27 or less, in particular of less than 0.25, and a D50 value of from 110 to 150 nm, in particular of 115 to 140 nm.

A further preferred embodiment employs an agglomerating copolymer BC having a pol ydispersity U in the range of from 0.27 to 0.20, in particular in the range of from 0.25 to 0.21, and a D50 value of from 100 to 150 nm, preferably 110 to 150 nm, in particular of 115 to 140 nm.

Agglomeration of the Graft Basis B1

The agglomeration of the graft basis B1 is generally achieved by adding a dispersion of the copolymer BC described hereinabove. The concentration of the copolymer BC in the dispersion used for agglomeration shall generally be between 3 to 60 wt.-%, preferably between 7 to 50 wt.-%. The agglomeration generally employs from 0.1 to 5 parts by weight, preferably from 0.5 to 3 parts by weight, of the dispersion of the copolymer BC per 100 parts of the graft basis B1 , in each case reckoned on solids. The agglomeration is generally carried out at a temperature of from 20°C to 120°C, pref erably from 30°C to 100°C, more preferably from 30°C to 75°C and at pressures between 0 and 6 bar(g), preferably 0 and 3 bar(g) (gauge pressure). The addition of copolymer BC may be effected in one go or portion wise, continuously or with a feed profile over a particular time period. According to a preferred embodiment the addition of copolymer BC is effected such that 1/1 to 1/100 of the total amount of copolymer BC is introduced per minute. The agglomeration time, i.e. the time from the beginning of the addition of copolymer BC to the start of the subsequent graft copolymerization, is preferably from one minute to two or more hours, for example to 2 hours, particularly preferably from 10 to 60 minutes.

Basic electrolytes may optionally be added to the agglomeration in an amount of from 1 to 50 wt.-% (based on 100wt.-% of the solids content of the copolymer BC). Useful basic electrolytes include organic or inorganic hydroxides. Inorganic hydroxides especially are useful. Particular preference is given to using lithium hydroxide, sodium hydroxide or potassium hydroxide. According to one of the particularly preferred embodiments KOH is used as the basic electrolyte. According to another preferred embodiment NaOH is used as the basic electrolyte. However, it is also possible to employ mixtures of two or more basic electrolytes.

This may be advantageous, for example, when the growth of the rubber particles is to be precisely controlled. Hence it may be useful, for example, to employ mixtures of LiOH with KOH or mixtures of LiOH with NaOH. It is likewise possible to use mixtures of KOH and NaOH and this constitutes a further preferred embodiment. The electrolytes are gen- erally dissolved prior to addition. A preferred solvent is the aqueous phase. Preference is given to using diluted solutions, for example solutions having a concentration in the range of from 0.001 to 0.1, in particular from 0.001 to 0.05, preferably less than 0.03, for example less than 0.025 g of basic electrolyte/ml of solvent. The addition of the basic electrolytes may be effected prior to the addition of copolymer BC, simultaneously there- with or separately therefrom or after addition of B1.

It is also possible to premix the basic electrolytes in the dispersion of copolymer BC. According to a preferred embodiment the addition of the basic electrolytes is effected prior to the addition of the agglomerating copolymer BC. The basic electrolyte is gener ally employed in an amount in the range of from 0.01 to 4 wt.-%, preferably 0.05 to 2.5, in particular 0.1 to 1.5 wt.-% based on component B (solids).

The pH during the agglomeration is generally from 6 to 13. According to a preferred embodiment the pH is from 8 to 13.

Agglomerated Graft Basis B1

The graft basis B1 obtained after the agglomeration has preferably a bimodal particle size distribution of fractions x) and y) where x) is a fraction of nonagglomerated particles and y) is a fraction of agglomerated particles having a D50 value in the range of from 300 to 550 nm, particularly preferably 350 to 480 nm. In case that narrow sized agglomerating copolymer BC with a polydispersity U of 0.27 or less is used for the agglomeration, the polydispersity U of the agglomerated fraction is less than 0.28, more preferably less than 0.27 and more preferably less than 0.26. The nonagglomerated particles of the fraction x) generally have a D50 value of not more than 150 nm, preferably in the range of from 80 to 120 nm.

The weight fraction of the particles of the fraction x) of the agglomerated graft basis B1 is generally 15 to 40 wt.-%, preferably 20 to 30 wt.-%, and the fraction of the particles of the fraction y) is generally 60 to 85 wt.-%, preferably 70 to 80 wt.-%, based on the total mass of the particles, x) and y) generally summing to 100 wt.-%.

The obtained dispersion of the agglomerated graft basis B1 is relatively stable and may be readily stored and transported without onset of visible coagulation. The agglomerated graft basis B1 is used to produce ABS-copolymer B.

ABS-copolymer B

To produce the ABS-copolymer B (component B), the agglomerated graft basis B1 is polymerized with the monomers B21 and B22. Component B generally comprises 40 to 85 wt.-%, based on the solids content of com ponent B, of a graft basis (B1) and 15 to 60 wt.-%, based on the solids content of com ponent B, of one or more graft stages B2 (component B2). B1 and B2 sum to 100 wt.-%.

Component B2 may be obtained by reaction of (B21) 70 to 90 wt.-%, preferably 75 to 85 wt.-%, of styrene and/or a-methylstyrene, in particular styrene, and (B22) 10 to 30 wt- %, preferably 15 to 25 wt.-%, of acrylonitrile, methacrylonitrile and/or methyl methacry late, in particular acrylonitrile, in the presence of the agglomerated graft basis B1. B21 and B22 sum to 100 wt.-%. Preferred components B2 are constructed from: B21 copol ymers of styrene and acrylonitrile, B22 copolymers of a-methylstyrene and acrylonitrile. Particular preference is given to B21 copolymers of styrene and acrylonitrile. Particularly preferred components B2 are obtained by reaction of from 75 to 85 wt.-% of styrene and from 15 to 25 wt.-% of acrylonitrile.

Component B2 is preferably prepared by an emulsion polymerization process after per forming the above described agglomeration of the graft basis B1.

The graft copolymerization for preparing component B2 may be performed in the same system as the emulsion polymerization for producing the graft basis B1 and further emul sifiers and assistants may be added if necessary. The monomer mixture to be polymer ized onto the graft basis according to one embodiment may be added to the reaction mixture all at once, spread over a plurality of stages - for example to construct a plurality of graft superstrates - or in continuous fashion during the polymerization. The monomers B21 and B22 (in particular styrene and acrylonitrile) may preferably be added simultane ously with constant feed rates and with a constant ratio of the feed rates of B21 and B22. It is also preferable to use variable feed rates for the monomers B21 and B22 and vari able ratios of the feed rates for the monomers B21 and B22 according to the teaching of the application WO-A1 2015/165810. In general, the time for feeding the monomers B21 and B22 is in the range of 1 to 10 hours, preferably in 1.5 to 6 hours.

In accordance with another embodiment, the component B2 is polymerized from a mon omer mixture composed of the components B21 and B22, in particular styrene and ac rylonitrile, in the presence of the agglomerated graft basis B1 obtained according to the above described process. The monomers may be added individually or in mixtures with one another. For example it is possible to initially graft B21 alone and subsequently graft a mixture of B21 and B22. This graft copolymerization is advantageously again per formed in aqueous emulsion under the customary conditions described hereinabove for the graft substrate.

Particulars pertaining to the performance of the graft reaction are known to those skilled in the art and are disclosed, for example, in DE-A 24 27 960, EP-A 0 062 901 or WO-A1 2014/170406 (see “Pfropfcopolymer B, Allgemeine Vorgehensweise”, pp 34-35).

Preference is given to the following embodiments:

Component B is preferably produced by polymerizing the components B21 and B22 in aqueous emulsion according to processes known to those skilled in the art generally at temperatures of 20°C to 100°C, preferably 50°C to 90°C and at pressures between 0 and 18 bar(g), preferably 0 and 15 bar(g) (gauge pressure). The polymerization may employ the customary emulsifiers such as alkali metal salts of alkyl- or arylsulfonic acids, alkyl sulfates, fatty alcohol sulfonates, salts of higher fatty acids comprising 10 to 30 carbon atoms or resin soaps. It is preferable to employ the sodium or potassium salts of alkylsulfonates or fatty acids comprising 10 to 18 carbon atoms. The emulsifiers are fa vorably employed in an amount of from 0.1 to 3 wt.-%, preferably from 0.2 to 1 wt.-%, based on the total weight of component B.

Polymerization initiators employed are in particular the commonly used persulfates such as sodium or potassium peroxodisulfate, or mixtures thereof, though redox systems are also suitable. The amounts of initiators, for example 0.1 to 1 wt.-%, based on the total dry weight of component B, depends on the molar weight desired.

Polymerization assistants that may be employed include the customary buffer sub stances used to adjust the pH to the preferred range of from 6 to 10, for example sodium bicarbonate, sodium carbonate and sodium pyrophosphate, or mixtures thereof and also optionally 0.01 to 0.3 wt.-% of a molecular weight regulator such as mercaptan, e.g. tert.- dodecylmercaptan or n-dodecyclmercaptan, terpinol or dimeric a-methylstyrene based on the total dry weight of component B. The molecular weight regulators can be added at once at the beginning of the polymerization or in several portions at the beginning and/or during the polymerization or continuously from the beginning until the end of the polymerization with constant or variable feed rates. The solids content in the aqueous dispersion after the polymerization is preferably from 25 to 50 wt.-%, particularly preferably from 30 to 45 wt.-%.

Preference is given to component B constructed from: B1 : 40 to 85 wt.-%, based on the solids content, corresponding to the dry weight, of component B, of a graft basis B1 obtainable by (a) polymerizing:

(B12): 0 to 21 wt.-%, based on the graft basis B1, of styrene, and (B11): 79 to 100 wt.-%, based on the graft basis B1, of butadiene, where (B11) and (B12) sum to 100 wt.-%; and (b) agglomerating the obtained graft basis B1 by adding (BC): 0.01 to 5 parts by weight, based on 100 parts by weight of the graft basis B1 , in each case based on the solids content, of an agglomerating copolymer (BC) of:

(BC1): 80 to 99.9 wt.-% of ethyl acrylate and (BC2): 0.1 to 20 wt.-% of methacrylamide, where (BC1) and (BC2) sum to 100 wt.-%; and

B2: 15 to 60 wt.-%, based on the solids content of component B, of component B2 ob tainable by reacting the agglomerated graft basis B1 with a mixture of:

(B21) 70 to 90 wt.-%, based on component B2, of styrene, and

(B22) 10 to 30 wt.-%, based on component B2, of acrylonitrile, where the graft basis B1 and component B2 sum to 100 wt % in total; and where the agglomerating copolymer (BC) has a D50 value of from 100 to 150 nm, preferably of from 110 to 140 nm and a polydispersity U larger than 0.27 or of 0.27 or less, preferably less than 0.27, preferably in the range of from 0.26 to 0.20, and the agglomerated graft basis B1 has a bimodal particle size distribution of a fraction x) of nonagglomerated particles in an amount of 15 to 40 wt.-%, having a D50 value of not more than 150 nm, preferably in the range of from 80 to 120 nm and a fraction y) of agglomerated particles in an amount of 60 to 85 wt.-%, having a D50 value in the range of from 300 to 550 nm, preferably with a polydispersity U of less than 0.28 and x) and y) generally summing to 100 wt.-%.

Component B may be further used as it is obtained in the reaction mixture, for example as a latex emulsion or latex dispersion. Alternatively, however, it may also be worked up in a further step. A stabilizer dispersion is preferably added to the component B before the workup measures take place. Workup measures are known in principle to those skilled in the art. Examples of workup steps include the isolation of component B from the reaction mixture, for example by spray drying, shearing or by precipitation with strong acids or using other precipitants, for example from inorganic compounds such as mag nesium sulfate. The solids content of the dispersion of component B is about 40 wt.-%. Preferably, component B is precipitated before being fed to the at least one extruder of the process according to the present invention, in particular, separately or together with parts of one or several other components, in an aqueous precipitation step, wherein the aqueous composition used for precipitation contains less than 5.0%, more preferred less than 4.0%, even more preferred less than 3.5% , for example 2.5%, by dry weight of salt(s), relating to the dry weight of component B. In general, a precipitation of component B is feasible with a bi-valent salt concentration (in a solution of 20% component B in water) between 0.3 and 0.7% which corresponds to between 1.5% and 3.5% by weight of salt per dry weight of component B. Concentrations below these values can be applied e.g. for tri-valent salts. In a further preferred embodiment the aqueous composition for precipitation comprises about 20 wt- % solid content, (e.g. 18 to 22%) wherein the solid is component B, and about 0.8 wt.-% of salt, what corresponds to 4 wt.-%of salt relating to the dry weight of the component B, in a solution with 20 wt.-%of solid content. Preferably, the salt used for the precipitation step is chosen from a group comprising anhydrous magnesium sulfate, magnesium sul fate with crystal water, anhydrous aluminum sulfate, aluminum sulfate with crystal water, calcium chloride, magnesium chloride, magnesium hydroxide and bi-valent salts and tri- valent salts, in particular magnesium and calcium, with sulphuric acid and combinations thereof.

The aqueous precipitation step is preferably directly or indirectly followed by a sintering step, wherein the precipitated component B is agglomerated to larger particles, charac terized by using a temperature from 100° to 125°C, preferred below 120°C, more pre ferred below 115°C and in other cases from 100° to 110°C. In particular, the sintering step is effectuated at a pressure above atmospheric pressure. Component B can be treated in one or more sintering steps. In general, the residence time for the sintering step is 180 minutes or less, preferably less than 60 min and more preferably from 30 to 40 minutes. The total residence time for the precipitation step and the sintering step is preferably between 45 and 90 minutes, in particular about 60 minutes. In the precipitation step as well as in the sintering step, the water contains preferably between 15 wt.-% to 25 wt.-%, more preferably 18 wt.-% to 22 wt.-% of solid components, what mainly corre sponds to the dry weight of component B.

In a preferred embodiment, component B is washed directly or indirectly after the sinter ing step with an amount of water, which corresponds to 1 to 90 wt.-%, more preferred 10 to 50 wt.-% of water, relating to the dry weight of component B. In a preferred embodi ment, component B is washed with water after the sintering step and during and/or after a centrifugation step, whereas the amount of washing water is > 1 wt.-%, preferred >5 wt.-%, especially preferred >10 wt.-% based on total 100 wt.-% dry component B.

After the sintering step, the sintered component B is preferably treated in a further step to remove some of the water. Partial dewatering may be effected, for example, by filtra tion, settling out, pressing out, decanting, centrifugation or thermal drying. Preferably, one or more centrifugation steps are used. Component B is preferably partially de watered to a residual water content of up to 60 wt.-%, often up to 40 wt.-% and compo nent B containing residual water is fed to the first feeding zone FZ1 of the extruder. The first feeding zone FZ1 usually comprises automatic metering means and the actual me tering orifice or a plurality of metering orifices. The metering means are for example in the form of a conveying screw which conveys or forces the conveyed material into the metering orifice. It is also possible for component B to be metered by suitable gravimetric or volumetric metering means and to be metered under gravity into the metering orifice of the extruder.

In a possible embodiment, a vent section VeS is located upstream in the direction oppo site the conveying direction of the extruder. Typically, it has one or more vent orifices through which occluded air in component B can escape.

A preferred process is provided for producing the above-described component B by:

(i) polymerizing the monomers B12 and B11 in aqueous emulsion to afford a particulate graft basis B1 ,

(ii) agglomerating the particulate graft basis B1 which is in the form of an emulsion using an agglomerating copolymer (BC), wherein the copolymer (BC) has a polydispersity U larger than 0.27 or of 0.27 or less, preferably less than 0.27, preferably in the range of from 0.26 to 0.20, and a D50 value of from 100 to 150 nm to afford an agglomerated particulate graft basis B1 and subsequently (iii) polymerizing the monomers B21 and B22 of component B2 in aqueous emulsion in the presence of the agglomerated particulate graft basis B1. B, B1, B11, B12, BC, B21 and B22 are preferably as defined above.

In accordance with the process, the obtained particulate graft basis B1 generally has a D50 value of not more than 150 nm, preferably of from 80 to 120 nm.

The thermoplastic ABS molding composition comprises component B and the at least one thermoplastic copolymer matrix A, additives D and optionally one or more polymers C. Preference is given to a thermoplastic ABS molding composition composed of or con sisting of component A, component B, component D and optionally component C.

Preferably the molding compound (thermoplastic ABS molding composition) comprises: A: 30 to 80 wt.-% of at least one thermoplastic copolymer matrix A obtainable from: A1: 69 to 80 wt.-%, based on the dry weight of A, of styrene or a-methylstyrene or a mixture of styrene and a-methylstyrene and A2: 20 to 31 wt.-%, based on A, of acrylonitrile and B: 19.99 to 60 wt.-% of component B; and

K: 0.01 to 40 wt.-% of further components K, comprising additives D and optionally pol ymers C, where the components A, B and K sum to 100 wt.-%.

Copolymer matrix A

The copolymer matrix A (component A) is preferably produced from the components acrylonitrile and styrene and/or a-methylstyrene by bulk polymerization or in the pres ence of one or more solvents. Preference is given to component A having weight-aver age molar masses Mw of from 50,000 to 300,000 g/mol, where the weight molar masses may be determined, for example, by means of GPC with tetrahydrofuran as solvent and with UV detection. Component A forms the matrix of the thermoplastic ABS molding composition. The number-averaged molar masses (Mn) of component A is preferably from 15,000 to 100,000 g/mol (determined by GPC with tetrahydrofuran as solvent and with UV detection). The viscosity of component A (determined according to DIN 53726:1983-09 at 25°C in a 0.5 wt.-% solution in DMF) is, for example, from 50 to 120 ml/g. Component A may in particular comprise or consist of:

(Aa) polystyrene-acrylonitrile, produced from, based on (Aa), 69 to 80 wt.-% of styrene and 20 to 31 wt.-% of acrylonitrile, or

(Ab) poly-a-methylstyrene-acrylonitrile, produced from, based on (Ab), 69 to 80 wt.-% of a-methylstyrene and 20 to 31 wt.-% of acrylonitrile, or

(Ac) a mixture of the copolymer matrix (Aa) and the copolymer matrix (Ab).

Component A may also be obtained by copolymerization of acrylonitrile, styrene and a- methylstyrene. However, it is also possible in principle to employ polymer matrices con- taining further monomer building blocks.

Component A may be produced by bulk polymerization/solution polymerization in, for example, toluene or ethylbenzene according to a process such as is described, for ex ample, in Kunststoff-Handbuch, Vieweg-Daumiller, Vol V, (Polystyrol), Carl-Hanser-Ver- lag, Munich 1969, pages 122 f., lines 12 ff.

As previously described hereinabove component A is preferably a polystyrene-acryloni trile, poly-a-methylstyrene-acrylonitrile or mixtures thereof. In a preferred embodiment after production component A is isolated according to processes known to those skilled in the art and preferably processed into pellets.

Polymers C

Further, the thermoplastic ABS molding composition can additionally comprise one or more further, in particular thermoplastic, polymer (C) (component C) selected from the group of polycarbonates, polyester carbonates, polyesters and polyamides. Suitable ex amples include, in particular, semicrystalline polyamides, semiaromatic copolyamides, polyesters, polyoxyalkylene, polyarylene sulfides, polyether ketones, polyvinyl chlorides, and/or polycarbonates.

Suitable polycarbonates are known per se. They are in particular obtainable by interfacial polycon-densation, for example by the processes of DE-B 1 300266, or by reacting di phenyl carbonate with bisphenols according to the process of DE-A 1495730. Suitable polyamides are known homopolyamides, copolyamides and mixtures of such polyamides. They may be semi-crystalline and/or amorphous polyamides. Preferred pol yamides are very generally those having an aliphatic semicrystalline or partly aromatic and amorphous structure of any type, and blends thereof. Appropriate products are avail- able, for example, under the trade name Ultramid.RTM. (from BASF). Suitable semi crystalline polyamides are polyamide-6, polyamide-6,6, mixtures and corresponding co polymers of those components.

Suitable, in particular thermoplastic, polyesters are preferably polyalkylene tereph- thalates, that is to say reaction products of aromatic dicarboxylic acids or reactive deriv atives thereof (e.g. dimethyl esters or anhydrides) and aliphatic, cycloaliphatic or arylali- phatic diols, and mixtures of such reaction products. Preferred polyalkylene tereph- thalates may be prepared from terephthalic acids (or reactive derivatives thereof) and aliphatic or cycloaliphatic diols having from 2 to 10 carbon atoms according to known methods (Kunststoff-Handbuch, Volume VIII, p. 695 ff, Carl Hanser Verlag, Munich 1973).

It is also possible to employ mixtures of two or more of the cited polymers (C). The ther moplastic ABS molding composition may comprise, based on thermoplastic ABS mold- ing composition, from 0 to 40 wt.-%, preferably 0 to 30 wt.-%, particularly preferably 0 to 20 wt.-% of the abovementioned polymers (C).

Additives D As additives D (component D), the thermoplastic molding compound may comprise one or more components selected from the group consisting of dispersants, fillers and added substances DS.

As the component D, the thermoplastic ABS molding composition may further also com- prise 0 to 5 wt.-% of fibrous or particulate fillers or mixtures thereof, in each case based on the thermoplastic ABS molding composition. Preferred examples of fillers or reinforc ers that may be employed include glass fibers that may be finished with a sizing and a coupling agent, glass beads, mineral fibers, aluminum oxide fibers, mica, quartz flour or wollastonite. It is also possible to admix with the molding compounds metal flakes, metal powder, metal fibers, metal-coated fillers, for example nickel-coated glass fibers, and other additive substances that shield electromagnetic waves. It is also possible to add carbon fibers, carbon black, in particular conductivity carbon black, or nickel-coated car bon fibers.

Various additives, as component D, may be added to the molding compounds in amounts of from 0.01 to 20 wt.-% as assistants and processing additives. Suitable additives in clude all substances customarily employed for processing or finishing the polymers.

Examples for component D include, for example, dyes, pigments, lubricants, in particular which are useful for production of molded bodies/articles, colorants, antistatic agents, flame retardants, antioxidants, stabilizers, for example stabilizers for improving thermal stability, stabilizers for increasing photostability, light stabilizers, stabilizers for enhancing hydrolysis resistance and chemical resistance; matting agents, antidrip agents and anti- thermal decomposition agents. These additves may be in part admixed at any stage of the manufacturing operation, but preferably at an early stage in order to profit early on from the stabilizing effects (or other specific effects) of the additves. For further custom ary assistants and added substances, see, for example, “Plastics Additives Handbook”, Ed. Gachter and Muller, 4th edition, Hanser Publ., Munich, 1996.

Examples of suitable pigments include titanium dioxide, phthalocyanines, ultramarine blue, iron oxides or carbon black, and also the entire class of organic pigments.

Examples of suitable colorants include all dyes that may be used for the transparent, semi-transparent, or non-transparent coloring of polymers, in particular those suitable for coloring styrene copolymers.

Examples of suitable flame retardants that may be used include the halogen-containing or phosphorus-containing compounds known to the person skilled in the art, magnesium hydroxide, and also other commonly used compounds, or mixtures thereof.

Examples of suitable antioxidants include sterically hindered monocyclic or polycyclic phenolic antioxidants which may comprise various substitutions and may also be bridged by substituents. These include not only monomeric but also oligomeric compounds, which may be constructed of a plurality of phenolic units. Hydroquinones and hydroqui- none analogs are also suitable, as are substituted compounds, and also antioxidants based on tocopherols and derivatives thereof. It is also possible to use mixtures of dif ferent antioxidants. It is possible in principle to use any compounds which are customary in the trade or suitable for styrene copolymers, for example antioxidants from Irganox® range. In addition to the phenolic antioxidants cited above by way of example, it is also possible to use so-called costabilizers, in particular phosphorus- or sulfur-containing costabilizers. These phosphorus- or sulfur-containing costabilizers are known to those skilled in the art.

Examples of suitable light stabilizers include various substituted resorcinols, salicylates, benzotriazoles and benzophenones.

Suitable matting agents include not only inorganic substances such as talc, glass beads or metal carbonates (for example MgCCh, CaCCh) but also polymer particles, in particu lar spherical particles having diameters D50 greater than 1 pm, based on, for example, methyl methacrylate, styrene compounds, acrylonitrile or mixtures thereof. It is further also possible to use polymers comprising copolymerized acidic and/or basic monomers.

Examples of suitable antidrip agents include polytetrafluoroethylene (Teflon) polymers and ultrahigh molecular weight polystyrene (weight-average molar mass Mw above 2,000,000 g/mol).

Examples of fibrous or pulverulent fillers include carbon or glass fibers in the form of glass fabrics, glass mats, or filament glass rovings, chopped glass, glass beads, and wollastonite, particular preference being given to glass fibers. When glass fibers are used they may be finished with a sizing and a coupling agent to improve compatibility with the blend components. The glass fibers incorporated may either take the form of short glass fibers or else continuous filaments (rovings).

Examples of suitable particulate fillers include carbon black, amorphous silica, magne sium carbonate, powdered quartz, mica, bentonites, talc, feldspar or, in particular, cal cium silicates, such as wollastonite, and kaolin.

Examples of suitable antistatic agents include amine derivatives such as N,N-bis(hydrox- yalkyl)alkylamines or -alkyleneamines, polyethylene glycol esters, copolymers of eth- ylene oxide glycol and propylene oxide glycol (in particular two-block or three-block co polymers of ethylene oxide blocks and propylene oxide blocks), and glycerol mono- and distearates, and mixtures thereof. Examples of suitable stabilizers include hindered phenols but also vitamin E or com pounds having analogous structures and also butylated condensation products of p-cre- sol and dicyclopentadiene. HALS stabilizers (Hindered Amine Light Stabilizers), benzo- phenones, resorcinols, salicylates, benzotriazoles are also suitable. Other suitable com pounds include, for example, thiocarboxylic esters. Also usable are C6-C2o-alkyl esters of thiopropionic acid, in particular the stearyl esters and lauryl esters. It is also possible to use the dilauryl ester of thiodipropionic acid (dilauryl thiodipropionate), the distearyl ester of thiodipropionic acid (distearyl thiodipropionate) or mixtures thereof. Examples of further additives include HALS absorbers, such as bis(2,2,6,6-tetramethyl-4-piperidyl) sebacate or UV absorbers such as 2H-benzotriazol-2-yl-(4-methylphenol). Such addi- tives are typically used in amounts of from 0.01 to 2 wt.-%, based on the thermoplastic ABS molding composition.

Suitable lubricants (demolding agents) include stearic acids, stearyl alcohol, stearic es ters, amide waxes (bisstearylamide), polyolefin waxes and/or generally higher fatty ac- ids, derivatives thereof and corresponding fatty acid mixtures comprising 12 to 30 carbon atoms. Also particularly suitable is ethylenebisstearamide. The amounts of these addi tions are in the range of from 0.05 to 5 wt.-%, based on the thermoplastic ABS molding composition. Also suitable additives are silicone oils, oligomeric isobutylene or similar substances. Typical amounts, when employed, are from 0.001 to 3 wt.-%, based on the thermoplastic ABS molding composition. Also usable are pigments, dyes, optical brighteners, such as ultramarine blue, phthalocyanines, titanium dioxide, cadmium sulfides, derivatives of perylenetetracarboxylic acid.

Processing assistants and stabilizers such as UV stabilizers, heat stabilizers (for exam ple butylated reaction products of p-cresol and dicyclopentadiene, Wingstay L from Om- nova, or else the dilauryl ester of thiodipropionic acid, Irganox PS 800 from BASF), lub ricants and antistatic agents (for example ethylene oxide-propylene oxide copolymers such as Pluronic from BASF), when employed, are typically used in amounts of from 0.01 to 5 wt.-%, based on the thermoplastic ABS molding composition.

The individual added substances are generally used in the respective customary amounts.

Preferable when the components of the thermoplastic ABS molding composition are blended by melt mixing by conjoint extrusion, kneading or rolling of the components, this is preferably done at temperatures in the range of from 160°C to 400°C, more preferably from 180°C to 280°C. In a preferred embodiment, component B is first partially isolated from the aqueous dispersion obtained in the respective production steps.

In an extruder, the drive power is converted to temperature increase and pressurization. An extruder usually comprises the following process zones: solids intake, melting (plas- tification), possibly further materials intake, dispersion, homogenization, devolatilization and discharge (see also “Aufbereiten von Polyolefinen”, VDI-Verlag, 1984, pp.185 ff).

The extruder in particular comprises and is preferably composed of the following sections or zones, preferably in downstream conveying direction: the first feeding zone FZ1 , in which component B and at least part of component D are fed to the at least one extruder; the preheating zone PZ, in which component B is heated to a temperature of 100°C or below; the mechanical dewatering zone DZ, in which component B is mechanically dewatered at a dewatering temperature T _dW in a range from 50°C to 200°C, preferably from 50°C to 180°C, more preferably from 50°C to 160°C, even more preferably from 50°C to 120°C, even more preferably from 50°C to 100°C, whereby the water content in component B is reduced from more than 20 wt.-%, in particular more than 25 wt.-%, based on the total weight of component B, by 10 wt.-% to 90 wt.-%, based on the water comprised in com ponent B when fed to the first feeding zone FZ1, the second feeding zone FZ2, in which at least part of component A and optionally part of component D are fed, preferably in melt and/or solid form, to the extruder, where com ponent A is brought in contact with component B; the at least one degassing zone DG, in which component A and/or component B are degassed, optionally the third feeding zone FZ3, in which part of component A, component C and/or part of component D are optionally fed to the extruder together or separately from one another; and the discharge zone CZ, in which the thermoplastic ABS molding composition is removed from the extruder.

In the first feeding zone FZ1 solid is usually conveyed and compacted, and entrained air is also removed.

Further, the extruder can comprise at least one melting section S, where polymers (com ponents) are usually melted and fillers are usually predispersed. This can be followed by a melt-conveying zone, for example a distributive mixing zone, in which solids and fluids are distributed in the melt and the temperature of the composition is homogenized. In a dispersive mixing zone is it possible to disperse solid polymer particles and liquid drop lets.

The at least one degassing zone DG serves in particular for the removal of water, resid ual monomers and solvents. In particular, air, water and/or volatile organic compounds (VOC) escape through the at least one degassing zone DG. In principle, high melt tem perature, high rotation rate and optionally addition of entrainer (e.g. water), and also ap plication of a vacuum, serve to optimize degassing or devolatilization.

Preferably, at least one devolatilization aperture is present in each of the at least one degassing zone DG, in particular in each of the first degassing zone DG1 and the second degassing zone DG2, and more preferably has a suction-removal system utilizing the Venturi effect. It is preferable that the at least one devolatilization aperture is equipped with a retention screw. Retention screws, also known as stuffing or stuffer screws, can prevent the escape of the thermoplastic ABS molding composition through the at least one devolatilization aperture. Other retention elements can also be used.

The at least one devolatilization aperture can be operated under atmospheric pressure, under vacuum or under superatmospheric pressure, respectively. The discharge zone CZ usually comprises a pressure-increase zone, in order to gener ate the pressure needed in downstream assemblies such as filters.

Component A and optionally component C are preferably fed, in particular in melt and/or solid form, downstream of the first feeding zone FZ1 in conveying direction, in particular in the second feeding zone FZ2 and/or the third feeding zone FZ3, respectively. The at least one melting section S can be combined with at least one mixing section M in a section of the extruder. Further, the at least one extruder comprises at least one screw. In a preferred embodi ment, the external diameter of the at least one screw is 30 mm to 230 mm, in particular 60 mm to 220 mm. A preferred rate of rotation of the at least one screw is 200 to 1500 rpm. The at least one extruder preferably has two screws, in particular each of the at least one extruder has two screws. The throughput of thermoplastic ABS molding com- position in the at least one extruder is preferably 400 kg/h to 10000 kg/h.

Some preferred embodiments of the process steps and the at least one extruder are described in US 6,165,399. In a preferred embodiment, the at least one extruder is a twin-screw extruder. However, it is also possible to use an extruder having three or more screws or an extruder having a main screw of large diameter and, arranged around this, small screws (planetary arrangement). The screws of the at least one extruder, further more, preferably rotate in the same direction. However, rotation in opposite directions is also possible. Particular preference is given to a twin-screw extruder having screws ro tating in the same direction.

Preferably, the screw elements (the at least one screw) of the at least one extruder have a flight depth ration DS,extemai/DS, internal of from 1.2 to 1.8 and contain 3-flight, 2-flight, and 2-flight high volume elements. Depending on the type and amounts of the components of the composition, screws having a smaller flight depth or screws having a larger flight depth (ie. Deep-flighted screws) may be used in the extruder. Preference is given to the use of screws having a flight depth ration DS,extemai/DS, internal of from 1.2 to 1.8, preferably from 1.4 to 1.6, and particularly preferably from 1.45 to 1.48, for example 1.55, ie. a large flight depth. In another embodiment, screws having a medium flight depth, particularly those having a flight depth ratio of from 1.4 to 1.48, are used. This embodiment of the extruder may be advantageous for certain components and certain amounts of the com ponents. Screws with flight depth ratios of more than 2 are also suitable.

The thermoplastic ABS molding composition is preferably conveyed to a melt pump. The absolute pressure of the thermoplastic ABS molding composition during conveying from the at least one degassing zone DG, in particular the last of the at least one degassing zone DG, to the melt pump is preferably below 40 bar, more preferably below 30 bar and in particular below 15 bar.

The absolute pressure of the thermoplastic ABS molding composition is increased in the melt pump (SP), preferably to at least 50 bar, more preferably to at least 65 bar and with particular preference to at least 70 bar.

The absolute pressure can be measured in each case by conventional pressure-meas urement equipment. The method of checking can be based on direct measurement of the mechanical pressure or on measurement of the pressure on a membrane, a piezo element, a sensor, or other conventional components that are used by the person skilled in the art for checking pressure in technical systems.

The temperature of the ABS molding composition can be measured via a thermometer extending into the melt to a substantial depth within an adapter, and/or by using a com mercially available insertion thermometer on the polymer strand.

In contrast to further extruder sections in which conveying elements are used to increase pressure, the melt pump which serves for pressure increase and for discharge of the thermoplastic ABS molding composition from the extruder conveys the thermoplastic ABS molding composition without any great additional temperature increase. The melt pump is preferably configured as gear pump.

Preferably, the at least one extruder comprises a gear pump and optionally at least one melt filter after the discharge zone CZ.

During conveying from the degassing the temperature of the thermoplastic ABS molding composition is preferably below 300°C. The temperature is preferably below 280°C and in particular below 265°C. The temperature of the thermoplastic ABS molding composi tion downstream of the at least one degassing zone DG, in particular downstream of the second degassing zone DG2, in conveying direction is usually at least 200°C.

The thermoplastic ABS molding composition can be conveyed from the at least one de volatilization aperture to the melt pump by way of at least one screw element and/or by way of an adapter. The adapter comprises no conveying elements and no mixing ele ments.

Preferably, step b) is followed by a pelletizing process for the thermoplastic ABS molding composition.

The thermoplastic ABS molding composition can be introduced from the extruder, in par ticular from the melt pump, into a melt-pelletization procedure, in particular an underwa ter pelletization procedure. Appropriate devices are known. It is preferable that the ther moplastic ABS molding composition emerging from a pelletizing die or other die attached after the melt pump is cooled, whereupon the thermoplastic ABS molding composition solidifies, and is optionally pelletized.

The thermoplastic ABS molding composition can moreover be conveyed via at least one melt filter, in particular after the melt pump, in conveying direction. These filters are known to the person skilled in the art. The at least one melt filter can also be configured as melt sieve.

It is preferable that there is at least one melt filter arranged after the melt pump in con veying direction. It is preferable that the melt pump has connection to a device for the underwater pelletization procedure.

The invention further relates to a thermoplastic ABS molding composition produced by the process described above, and to moldings made from such ABS compositions (the thermoplastic ABS molding composition).

The described thermoplastic ABS molding composition can be used for the production of molded articles (moldings) such as sheets, semifinished products, films, fibers or foams. Processing may be carried out using the known processes for thermoplastic processing, in particular production may be effected by thermoforming, extruding, injection molding, calandaring, blow molding, compression molding, press sintering, deep drawing or sin tering, preferably by injection molding.

In the context of the present application the abovementioned embodiments may be com bined with one another.

The following examples, figures 1 and 2 and claims further describe the invention.

Figure 1 shows an extruder applicable in the invention, comprising a first feeding zone FZ1, a preheating zone PZ, a mechanical dewatering zone DZ, a second feeding zone FZ2, two degassing zones DG1 , DG2, a third feeding zone FZ3 and a discharge zone CZ and also a melt pump SP, which has an adapter AD. The preheating zone PZ is located upstream of the mechanical dewatering zone DZ and directly followed in con veying direction by the mechanical dewatering zone DZ. Further, there is a melt filter SF arranged after the melt pump SP in conveying direction, followed by a device for an underwater pelletization procedure UW.

Component B and at least part of component D are fed to the first feeding zone FZ1 , at least part of component A is fed to the second feeding zone FZ2 and optionally part of component A, component C and/or part of component D are fed to the third feeding zone FZ. In the preheating zone PZ, component B is heated and in the mechanical dewatering zone DZ, water W is removed from component B.

Figure 2 shows screw elements SE with U-shape.

Examples

In the following, examples for the inventive production of thermoplastic ABS molding compositions are given.

Component A is polymerized based on 20.5 wt.-% acrylonitrile, 64.5 wt.-% stryrene and 15 wt.-% ethyl-benzene (EB), based on the applied amounts of acrylonitrile, styrene and ethyl-benzene. A reaction temperature of 163°C, a pressure of 2.4 bar gauge and a res idence time of 2.3 hours are used in the reactor. Non reacted monomers and EB are removed from the reaction mixture by degassing to obtain component A having a pol ymerized composition comprising 76 wt.-% of styrene and 24 wt.-% of acrylonitrile, based on the total weight of component A, and a viscosity number of 64 dl/g.

The degassing is performed using a tube bundle heat exchanger.

The base rubber component B1 is produced by emulsion polymerization using a feed stream addition process. The monomers are introduced into the reactor in the following order: Demineralized water, potassium stearate, potassium persulfate and sodium hy- drogencarbonate are provided first and the temperature is set to 67°C. Initially, styrene is added in an amount of 7 wt.-%, based on the total monomer amount, over 20 minutes. Following the styrene addition, a first portion of 1,3-butadiene is added in an amount of 7 wt.-%, based on the total monomer amount, over 25 minutes. The remaining portion of

1,3-butadiene which amounts to 86 wt.-%, based on the total monomer amount, is sub sequently added over 8.5 hours tert.-dodecylmercaptane is added in an amount of 41 wt.-% based on the total amount of tert.-dodecylmercaptane at the start of the first portion of 1 ,3-butadiene, another amount of 41 wt.-% is added after 4 hours after start of styrene feed and 18 wt.-% is added after 8 hours after start of styrene feed. The applied amounts are: 3180 parts styrene, 4693 parts 1,3-butadiene (first portion), 37554 parts 1,3-butadi- ene (second, remaining portion), 454 parts tert.-dodecylmercaptane, 111.9 parts potas sium persulfate, 338 parts potassium stearate and 159.5 parts sodium hydrogencar- bonate. After the end of the feeding of the second, remaining portion of 1 ,3-butadiene, a temperature of 67°C and a maximum pressure of 7.8 bar are applied for a residence time of 2 hours. The pressure is then released to 2.5 bar and an amount of 1900 parts 1,3- butadiene is distilled of by reducing the pressure from 2.5 bar to 0.4 bar and the distilled 1,3-butadiene is recovered and introduced into the next polymerization batch. The final latex B1 has a solid content of 44.0 to 45.0 wt.-%, based on the total weight of component B1.

Component B1 showed a weight based particle size D50 of 109.9 ± 6.9 nm, a swelling index of 26.7 ± 4.2 and a gel content of 76.7 ± 3.4. The agglomerating copolymer is produced by emulsion polymerization. First, 62.0 parts of Mersolat H30 (Lanxess Deutschland GmbH, emulsifier, Ci2-Ci8-SC>3 K ⁺ , CAS Registry Number: 68188-18-1, solids content 30.0 wt-%) are dissolved in 7280.8 parts of demin eralized water and heated to 60°C with stirring under a nitrogen atmosphere. 1428.0 parts of a sodium persulfate solution with 3.0 wt.-% in demineralized water is added to this solution with continued stirring. After 15 minutes, 1397 parts of ethyl acrylate are introduced over 18 minutes with a concomitant temperature increase from 60°C to 80°C. The following three feeds are then introduced over 180 minutes: a) 11101.6 parts of ethyl acrylate, b) 1.1277 parts of sodium persulfate as 3 wt.-% solution in demineralized water, c) solution of 549.6 parts of Mersolat H30 (Lanxess Deutschland GmbH) and 549.6 parts of methacrylamide in 6458.9 parts of demineralized water.

Once addition of the feeds a) to c) is complete, the polymerization is continued for 60 minutes at 80°C with stirring. This is followed by cooling to room temperature and addi tion of 2800 parts of demineralized water. The solids content of the latex of the agglom erating copolymer BC1 is 40.5 wt.-%. The weight mean average particle diameter Dsois 118 to 124 nm. The polydispersity U is in the range of 0.21 to 0.25. The agglomerated graft basis B1 is produced according to the following procedure. First, 46025.9 parts of the latex of the graft basis B1 , based on the solids content of the latex, are initially charged at a temperature of 68°C and stirred. 1118 parts of the latex of the agglomerating copolymer (BC) (based on the latex solids) are diluted with 7988.2 parts of demineralized water. This diluted latex is then added over 25 minutes with stirring to agglomerate the graft basis B1. After 5 minutes 419.4 parts of potassium stearate dis solved in demineralized water and further demineralized water (total amount: in 31969 parts) having a temperature of 68°C are added to the agglomerated latex of the graft basis B1 with continued stirring. The particle size distribution of the agglomerated graft basis B1 is measured. Only a fraction of the particles in the latex of the graft base B1 is agglomerated to larger parti cles. The agglomeration yield is the fraction of the agglomerated particles in wt.-%based on the total amount of the particles. The agglomeration yield is determined from the cu mulative distribution curve of the particle size measurement. The weight median particle size D50 of the fraction of agglomerated particles (fraction y)) in the obtained agglomerated latex of the graft base B is determined: D50: 340 to 360 nm, fraction y: 60 to 80 wt- %. Once the agglomeration step is complete, 54.5 parts of potassium persulfate dissolved in 2442 parts of demineralized water are added to the agglomerated latex of the graft basis B1 at 68°C with continued stirring. A monomer mixture of 24228 parts of styrene and 6057 parts of acrylonitrile is added over 2 hours and 44 minutes while stirring is continued. The temperature is increased to 80°C over this time period of addition of the styrene/acrylonitrile mixture. Once the addition of the styrene/acrylonitrile mixture is complete, 54.5 parts of potassium persulfate dissolved in 2442 parts of demineralized water are added under continued stirring. The polymerization is continued for 80 minutes at 80°C and then 72.9 parts dispersion of a stabilizer (Wingstay L, Phenol, 4-methyl-, reaction products with dicyclopentadiene and isobutene, CAS No.: 68610-51-5, based on solids of the dispersion having a solids content of 50 wt.-%) are added to the obtained graft latex with a solid content of 39.0 to 41.5 wt.-%. The term parts is based on weight in the context of the present application.

Component B2 showed a bimodal particle size distribution with a particle size D50 (small) of 131.0 ± 13.5 nm and a particle size D50 (large) of 346.9 ± 42.8 nm.

The latex of component B was then precipitated in a continuous process with an aqueous magnesium sulfate solution at a temperature of 88°C in a first stirred reactor, sintered at a temperature of 110°C in a second stirred reactor and centrifuged at up to 1.800 rpm, resulting in a water content of 25.8 to 29.6 wt.-% based on the total weight of component B.

Subsequently, component B was fed to an extruder (ZSK 133 SC from Coperion) according to the invention and mixed with component A, resulting in a thermoplastic ABS molding composition. The setup of the extruder (ZSK 133 SC from Coperion) was as shown in figure 1. The thermoplastic ABS molding composition showed a flowability M VR (220°C) of 18.7 ± 2.0 ml/10 min, a charpy notched impact strength of 22.5 ± 2.0 kJ/m ² , a Vicat S.T (B/50) of 97 ± 1.0 °C and a yellowness ( on granules) of 16.1 ± 2.0. Further, the thermoplastic ABS molding composition only comprised residual monomers in total of 450 to 1100 ppm, based on the total weight of the thermoplastic ABS molding composition, and more specific 350 to 900 ppm styrene and 75 to 200 ppm ethyl-ben zene.

Production example 1

The test extruder was equipped with two main shafts made out of the preferred stainless steel material, namely stainless steel AISI 630 (DIN EN 10088-3:2014-12 1.4542), wherein the stainless steel material comprised more than 10 wt.-% of chrome (Cr), based on the stainless steel material and the sum of the weight of Cr, V, Cu and Ni comprised in the stainless steel material was more than 15 wt.-%, based on the total weight of the stainless steel material. In the preheating zone PZ four 45° kneading blocks, each of them 60 mm long, were used. The dewatering zone DZ had two dewatering apertures to remove liquid water.

1.7 t/h of wet component B, having a water content of 26 wt.-%, based on the total weight of component B, comprising water and the dry weight of component B, and a first part of component D (2.5 kg/h) were fed to the first feeding zone FZ1. 0.7 t/h of component A were fed to the second feeding zone FZ2. 1.46 t/h of component A and the remaining part of D (6.5 kg/h) were fed to the third feeding zone FZ3.

At a first dewatering aperture in the mechanical dewatering zone DZ, a temperature of 85°C of the mixture of B and D in the extruder was measured. At a second dewatering aperture in the mechanical dewatering zone DZ, a temperature of 140°C was measured. At the fist dewatering aperture 110 l/h of water was released, at the second dewatering aperture 147 l/h water were released.

No corrosion was observed on the main shafts after two years of operation. The runtime of the equipment was improved.

Production example 2 Example 2 corresponds to example 1 with the difference that the test extruder was equipped with two main shafts made out of steel AISI D2 (DIN EN ISO 4957 1.2379), wherein the sum of the weight of Cr, V, Cu and Ni comprised in the steel material was less than 15 wt.-%, based on the total weight of the stainless steel material.

After two years of operation, the shaft showed significant corrosion in the area of the dewatering zone DZ.

Production example 3

Example 3 corresponds to example 1 with the difference that no preheating zone PZ was present at the extruder. Only conveying elements were used upstream of the mechanical dewatering zone DZ. The temperature of the product in the extruder at the first dewater ing aperture was 41 °C, a very reduced amount of water is removed at this position. Op- eration of the extruder was improved by reducing the throughput of wet component B by 40% to avoid plugging of the outlet of the degassing zone DG1 by polymer foam.

The analytical methods used to characterize the polymers are briefly summarized: a) Charpy notched impact strength [kJ/m ² ]:

The notched impact strength is determined on test specimens (80x10x4 mm, produced by injection molding at a compound temperature of 240°C and a mold temperature of 70°C) at 23°C according to ISO 179-1 A:2010-11. b) Flowability (MVR [ml/10 min]):

The flowability is determined on a polymer melt at 220°C with a load of 10 kg according to ISO 1133:2012-03. c) Particle size [nm]: The weight mean average particle diameter DW of the rubber dis- persions of the graft basis B1 and the agglomerated graft basis B1 was measured using a CPS Instruments Inc. DC 24000 disc centrifuge. Measurement was performed in 17.1 ml of an aqueous sugar solution with a sucrose density gradient of from 8 to 20 wt.-% to achieve stable flotation behavior of the particles. A polybutadiene latex having a narrow distribution and an average particle size of 405 nm was used for calibration. The meas- urements were taken at a disk rotational speed of 24000 rpm by injection of 0.1 ml of a diluted rubber dispersion (aqueous 24 wt.-% sucrose solution, comprising about 0.2 to 2 wt.-% of rubber particles) into the disc centrifuge containing the aqueous sugar solution having a sucrose density gradient of from 8 to 20 wt.-%.

The weight mean average particle diameter DW of the agglomerating copolymer (BC) was measured with the CPS Instruments Inc. DC 24000 disc centrifuge using 17.1 ml of an aqueous sugar solution having a sucrose density gradient of from 3.5 to 15.5 wt.-% to achieve stable sedimentation behavior of the particles. A polyurethane latex (particle density 1.098 g/ml) having a narrow distribution and an average particle size of 155 nm was used for calibration. The measurements were taken at a disk rotational speed of 24 000 rpm by injection of 0.1 ml of a diluted dispersion of the copolymer BC (produced by diluting with water to a content of 1 to 2%) into the disk centrifuge containing the aqueous sugar solution having a sucrose density gradient of from 3.5 to 15.5 wt.-%.

The weight mean average particle diameter Dw was calculated using the formula:

Dw = sum ( n, * Di ⁴ ) / sum ( n, * D, ³ ) ni: number of particles with the diameter Di d) The solids contents were measured after drying the samples at 180°C for 25 min in a drying cabinet. e) Swelling index Ql and gel content [%]:

The gel content values were determined with the wire cage method in toluene (see Hou- ben-Weyl, Methoden der Organischen Chemie, Makromolekulare Stoffe, part 1 , page 307 (1961) Thieme Verlag Stuttgart). A film was produced from the aqueous dispersion of the graft substrate by evaporation of the water. 0.2 g of this film was admixed with 50 g of toluene. After 24 hours the toluene was removed from the swelled sample and the sample was weighed. After 16 hours of drying in vacuum at 110°C the sample was weighed again.

The swelling index is determined by:

Swelling index Ql = (Swelled gel with toluene prior to drying) / (gel after drying) The gel content is determined by: Gel content = (mass of sample dried in vacuum) / (weight of sample prior to swelling) * 100% f) Yellowness index Yl The Yl value was determined on platelets having dimensions of 60x40x2 mm and pro duced by injection molding at a compound temperature of 240°C and a mold temperature of 70°C according to ASTM method E313-96 (illuminant/observer combination C/2°).