Title of Invention	"A PROCESS FOR THE PRODUCTION OF PREORIENTED FILAMENTS"
Abstract	Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula.

Title of Invention

"A PROCESS FOR THE PRODUCTION OF PREORIENTED FILAMENTS"

Abstract

Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula.

Full Text	1A This invention relates to a process for the production of preorientated filaments. The present invention relates to a process for the production of preorientated filaments from polyester-based polymer mixtures prepared in the melt, with the addition of an amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100OC, by spinning the molten polymer mixtures with a draw-off speed v of at least 2500 m/min. Spinning of polymer mixtures is known from a number of publications: EP 0 035 796 A (Teijin) describes synthetic fibres, inter alia of polyester or polyamide, which comprise 1 - 15 wt. % of a polysulphone polymer having a high glass transition point, of TG > 150 °C. The additive remains in the matrix in a spheroidal form and influences the surface structure of the filaments and the thread friction. The spinning speed is 2000 - 5500 m/min. EP 0 041 327 B (ICI) discloses fibres of PET or PA-6.6 which comprise 0.1 - 10 wt.% of a further polymer having anisotropic properties (LCP types). The spinning speeds are 1000 to 5000 m/min. A speed suppression (WUSS) is achieved by a higher elongation at break of the strand and therefore higher stretching ratios and an increase in productivity. EP 0 080 274 B (ICI) relates to fibres of PET, PA-6.6 or PP which comprise 0.1 - 10 wt.% of a further polymer which is present in the melt with an average particle size of 0.5 -3 m and is deformed to fibrils during melt spinning. The spinning speeds are 2000 to 6000 m/min, a speed suppression (WUSS: wind up speed suppression) of at least 20 % being achieved by a higher elongation at break or lower birefringence of the (PET) strand, and therefore higher stretching ratios and an increase in productivity. Preferred additive polymers are polyethylene glycol or 2 PA-6.6 for PET or polyolefins for PA-6.6. The effect reacts markedly to production parameters, such as throughput, spinning temperature, type of mixing or type of extruder. A transfer to production plants of different capacity, types of equipment or titre programmes is made difficult by this sensitivity. We attribute the negative behaviour to an unsuitable additive with too low a viscosity, too low a glass transition point and the tendency to crystallize. JP 56-91013 A (Teijin) discloses a non-stretched polyester yarn, in which, by addition of 0,5 - 10 wt.-% of a styrene polymer, an improved productivity is achieved by increasing the elongation at break of the strand at speeds of between 850 - 8000 m/min, preferably > 2500 m/min, with correspondingly higher stretching ratios. No requirements are disclosed for the polymer mixture and the non-stretched yarn for the stretch texturizing. EP 0 047 464 B (Teijin) relates to a non-stretched polyester yarn, in which, by addition of 0,2 - 10 wt.-% of a polymer of the type (CH2-CR1R2 )nsuch as poly(4-methyl-l-pentene) or polymethyl methacrylate, an improved productivity is obtained by increasing the elongation at break of the strand at speeds of between 2500 - 8000 m/min, with correspondingly higher stretching ratios. A fine and uniform dispersion of the additive polymer by mixing is needed, it being necessary for the particle diameter to be EP 0 631 638 B (AKZO) describes fibres of predominantly PET which contains 0.1 - 5 wt.% of a polymethacrylic acid alkyl ester imidized to the extent of 50 - 90 %. The fibres obtained at speeds of 500 - 10,000 m/min and subsequently finally stretched have a higher initial modulus. Spinning at very high speeds (such as 8000 m/min) is said to be possible with conventional thread breakage counts. Up to 8000 m/min partly orientated yarns which are not yet stretched to the final elongation and can be processed e. g. to texturized yarns are obtained. In the examples of industrial yarns, the influence on the modulus cannot be readily reconstructed; in gen. the strengths achieved are lower, which is a considerable disadvantage for this product. For textile applications, only stretched yarns are described. The associated unstretched yarns at a spinning speed of from 6000 m/min show elongations at break of Spinning of polymer mixtures to synthetic fibres has the aim of obtaining a higher elongation at break in the strand at a particular spinning speed than without modification by an additive polymer. As a result, a higher stretching ratio for production of the final yarn is said to be possible, which is said to have the effect of a higher productivity of the spinning unit. According to EP 0 041 327 B, for example, a where E/E' are the non-modified/modified elongations at break, is to be expected. Investigation of the formula shows that the effect is the greatest at high increases in elongation (E' - E) . However, elongations which are too high and therefore a reduced degree of orientation of the strand are unsuitable for processing in high-speed stretch texturizing processes. 4 Another way of increasing productivity is described in EP 0 080 274 B by the parameter WUSS > 20 %. At a spinning speed which is at least 20 % higher, the same elongation at break in the strand is obtained as at the correspondingly lower speed with non-modified polymer. No running properties in the spinning mill at a higher speed and during further processing or properties of the final yarns produced there are disclosed. It has been found that the average particle sizes claimed, of > 0.5 \|im, are unsuitable for commercial processing of the mixture, since such particle distributions lead to many capillary and thread breakages. Increasing production is targeted at improving the profitability of the production process. This is curtailed again to a certain extent by production difficulties and expensive high-speed equipment. The additional costs for the additive polymer have a substantial influence, so that, depending on the amount added, there is even a zero point for the profitability. The availability of the additive polymers on the market also plays an important role. For these reasons, a large number of the additives described in the literature are eliminated from large-scale industrial conversion. The producer or processor must take into account the entire production chain, and cannot stop at increasing production of a component step (e. g. spinning). The secondary processes should not be impaired. In particular, one of the main aims of this invention is not to curtail and preferably to improve the further processing conditions in the secondary steps, in spite of an increased spinning speed. Very high elongations at break are thus mentioned in the prior art for polymer mixtures also for high spinning speeds, these characterizing a marked reduction in the degree of orientation. As is known, such strands are not storage-stable, and cannot be spread and processed at high speeds in friction texturizing processes. Elongations at break of The object of the present invention is to provide a process for processing polymer mixtures based on polyester at a draw-off speed of > 2500 m/min to preorientated filaments, which are preferably suitable for stretch texturizing, in which the abovementioned disadvantages do not occur. In particular, the costs of the additive added to the polyester should be as low as possible, i. e. the additive must be inexpensive, and the amount added must be kept low. Spinning of the polymer mixture must lead to an increase in production compared with the non-modified matrix polymer and allow processing of the strand at a high speed in the stretch texturizing process. According to the invention, this object is achieved by a process according to the statements in the patent claims. This process is characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1 : 1 to 10 : 1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% (based on the polyester) and not more than an amount M, where M is given by the formula According to the invention, a copolymer is added to the polyester in an amount of at least 0.05 wt.%, where the copolymer must be amorphous and largely insoluble in the polyester matrix. The two polymers are substantially incompatible with one another and form two phases which can be distinguished under the microscope. Furthermore, the 6 copolymer must have a glass transition temperature {determined by DSC with a heating up rate of 10 oC/min) of more than 100 BC and must be thermoplastically processable. The melt viscosity of the copolymer here is to be chosen such that the ratio of its melt viscosity, extrapolated to the measurement time of zero and measured at an oscillation rate of 2.4 Hz and a temperature equal to the melting temperature of the polyester plus 34.0 OC {for polyethylene terephthalate 290 2C), in relation to that of the polyester, measured under the same conditions, is between 1 : 1 and 10 : 1. I. e. the melt viscosity of the copolymer is at least equal to or preferably higher than that of the polyester. Only by the choice of a specific viscosity range for the additive {copolymer) or by the choice of a specific viscosity ratio of the additive and polyester is the optimum degree of action achieved. With a viscosity ratio optimized in this way, it is possible to minimize the amount of additive added, as a result of which the profitability of the process becomes particularly high and particularly favourable processing properties are achieved. Surprisingly, the viscosity ratio determined according to the invention as ideal for use of polymer mixtures for the production of synthetic filament yarns is above the range identified in the literature as favourable for the mixing of two polymers. In contrast to the prior art, polymer mixtures with high molecular weight copolymers had an excellent spinnability. Due to the high flow activation energy of the additive polymers, the viscosity ratio further increases drastically in the region of thread formation after discharge of the polymer mixture from the spinneret. By the choice of a favourable viscosity ratio, a particularly narrow particle size distribution of the additive in the polyester matrix is achieved, and by combination of the viscosity ratio with a flow activation energy of significantly more than that of the polyester (PET about 60 kJ/mol), i. e. of more than 7 80 kJ/mol, preferably more than 100 kJ/mol, the required fibril structure of the additive in the strand is obtained. The glass transition temperature, which is high compared to the polyester, ensures a rapid consolidation of this fibril structure in the strand. The maximum particle sizes of the additive polymer here immediately after discharge from the spinneret are about 1000 nm, while the average particle size is 400 nm or less. The ratio of the melt viscosity of the copolymer to that of the polyester under the abovementioned conditions is preferably between 1.4 : 1 and 8 : 1. A ratio of the melt viscosities of between 1.7 : 1 and 6.5 : 1 is particularly preferred. Under these conditions, the average particle size of the additive polymer is 220 - 350 nm. The amount of copolymer to be added to the polyester is at least 0.05 wt.%. For many applications, amounts added of less than 1.5 % are sufficient at draw-off speeds above 3500 and up to 6000 m/min and more, even often less than 1.0 %, which is a considerable cost advantage. The maximum amount of additive polymer to be added according to this invention in relation to that of the polyester corresponds to the amount M, where M is defined as a function of the spinning draw-off speed v by the following formula: Maximum amounts added of 1.39 to 2.95 wt.% thus result in the spinning speed range from 3500 to 6000 m/min. Preferably, to achieve a particularly good profitability, the upper limit of the amount of additive to be added for draw-off speeds of more than 2900 m/min is defined by the parameter M, where 8 Amounts added of between 0.39 and 1.91 wt.% thus result for spinning speeds of 3500 to 6000 m/min. For draw-off speeds of more than 4200 m/min, the amount of additive polymer to be added to the polyester is preferably at least equal to the parameter N, but at least equal to 0.05 wt.%, where For draw-off speeds of 4200 to 6000 m/min, the minimum amount is thus between 0.057 and 0.57 wt.%. If the abovementioned preferred viscosity ratio of additive polymer to polyester is adhered to, the amount of copolymer to be added relative to that of the polyester preferably corresponds to the parameter P, where P = P ± 0.2 wt.%, but is at least 0.05 wt.%, and where, for draw-off speeds of more than 3900 m/min The amount of additive to be added in this preferred case is thus between 0.07 wt.% and 1.39 wt.% for spinning speeds of 3900 to 6000 m/min. For spinning speeds between 2500 m/min and the minimum spinning speeds specified here for M, N and P, only the minimum and maximum amounts stated in claim 1 apply, while for higher spinning speeds, the abovementioned ranges of amounts are preferably additionally used. These formulae of course also apply to spinning speeds of more than 6000 m/min up to about 12000 m/min. 9 Possible fibre-formimg matrix polymers are thermoplastically processable polyesters, such as polyethylene terephthalate (PET), polyethylene naphthalate, polypropylene terephthalate and polybutylene terephthalate. The homopolymers are preferred. However, copolymers of these polyesters with a content of up to about 15 mol% of conventional comonomers, such as e. g diethylene glycol, triethylene glycol, 1,4-Cyclohexanedimethanol, polyethylene glycol, isophthalic acid and/or adipic acid, are also possible. The polymers can additionally comprise additives, such as catalysts, stabilizers, optical brighteners and matting agents. The polyester can also comprise a small amount (not more than 0.5 wt.%) of branching components, that is to say e. g. polyfunctional acids, such as trimellitic acid or pyromellitic acid, or tri- to hexavalente alcohols, such as trimethylolpropane, pentaerythritol, dipentaerythritol or glycerol, or corresponding hydroxy acids. Mixing of the additive polymer (copolymer) with the matrix polymer is carried out by addition as a solid to the matrix polymer chips in the extruder intake with a chips mixer or gravimetric metering, or alternatively by melting the additive polymer, metering it by means of a gear pump and feeding it into the melt stream of the matrix polymer. A homogeneous distribution is then established by mixing in the extruder and/or by means of static or dynamic mixers. By a specific choice of the mixer and of the duration of the mixing operation, a defined particle distribution is advantageously established before the melt mixture is passed on through product distribution lines to the individual spinning stations and spinnerets. Mixers having a shear rate of 16 to 128 sec-1 and a residence time in the mixer of at least 8 sec have proved suitable. The product of the shear rate {s-1) and the 0.8th power of the residence time {in sec) here should be 250 to 2500, preferably 300 to 600. 10 The shear rate is defined here by the shear rate in the empty pipe (s-1) times the mixer factor, the mixer factor being a characteristic parameter of the mixer type. For Sulzer-SMX types, for example, this factor is about 7-8. The shear rate y in the empty pipe is calculated according to and the residence time x (s) according to wherein F = amount of polymer conveyed (g/tnin) V2 = internal volume of the empty pipe (cm3) R = diameter of the empty pipe (mm) £ = empty volume content (for Sulzer-SMX types 0.84 to 0.88) 5 = nominal density of the polymer mixture in the melt (about 1.2 g/cm3) Both the mixing of the two polymers and the subsequent spinning of the polymer mixture are carried out at temperatures, depending on the matrix polymer, in the range from 220 to 320 2C. The production of synthetic filaments from the polymer mixtures according to the invention by high-speed spinning with draw-off speeds of > 2500 m/min is carried out using spinning devices which are known per se. The filter package here is equipped according to the known prior art with filter devices and/or loose filter media (e. g. steel grit). 11 After the shear and filtration treatment has taken place, the molten polymer mixture is forced through the bores of the die plate in the die package. In the subsequent cooling zone, the melt threads are cooled to below their softening point by means of cooling air, so that sticking or backing-up at the following thread guide organ is avoided. The construction of the cooling zone is not critical, as long as a homogeneous stream of air which penetrates the filament bundle uniformly is ensured. A still air zone can therefore be provided directly below the die plate to delay cooling. The cooling air can be fed in by blowing transversely or radially from an air-conditioning system, or can be taken from the environment by automatic suction by means of a cooling pipe. After cooling, the filaments are bundled and charged with spinning oil. Oiler stones to which the spinning oil is fed as an emulsion by metering pumps are used for this. The prepared thread advantageously passes through an entangling device (entwisting device) to improve the thread compactness. Handling and safety organs may also be appropriate, before the thread arrives at the winding unit and is wound up there to packages on cylindrical bobbins. The circumferential speed of the thread package is regulated automatically and is the same as the winding-up speed. The draw-off speed of the thread can be 0.2 - 2.5 % higher than the winding-up speed because of its changing movement. Driven godets can optionally be used after the preparation or before the winding up. The circumferential speed of the first godet system is designated the draw-off speed. Further godets can be used for stretching or relaxing. The incompatibility of the two polymers has the effect that the additive polymer forms spheroidal or longitudinally shaped particles in the matrix polymer immediately after i discharge of the polymer mixture from the spinneret. The length/diameter ratio is preferably > 2. The best 12 conditions resulted when the average particle size (arithmetic mean) d50 was 1000 nm in a sample cross-section was below 1 %. It was possible to demonstrate the influence of the spinning draft on these particles analytically. New studies on the strands by the TEM (transmission electron microscopy) method have shown that a fibril-like structure exists there. The average diameter of the fibrils has been estimated at approx. 40 nm. The length/diameter ratio of the fibrils here was > 50. If these fibrils are not formed, or if the additive particles are too large in diameter after discharge from the spinneret, or if the size distribution is too non-uniform, which is the case with an inadequate viscosity ratio, the effect of the action is lost. The rolling action described in the literature could not be reconstructed with the additive polymer according to the invention. The evaluation of microscope studies of the fibre cross- and longitudinal sections suggest that the spinning draft tension is passed to the additive fibrils which form and the polymer matrix distorts with little stress. The deformation of the matrix consequently takes place under conditions which result in a reduction of the orientation and suppression of spinning-induced crystallization. The effect is appropriately evaluated by the strand construction and the processing properties. Furthermore, for the effectiveness of the additives according to this invention, a flow activation energy of the copolymers of at least 80 kJ/mol, that is to say a higher flow activation energy than that of the polyester matrix, is necessary. Only under this proviso is it possible for the additive fibrils to solidify before the polyester matrix and to absorb a considerable proportion of the enclosed spinning tension. As a result, it is possible 13 to achieve the desired increase in capacity of the spinning unit. As is known, the strand structure is substantially formed in the draft zone below the spinneret. The length of the draft zone is varied by the thread draw-off speed in the case of non-modified polymer. Typical values for roving yarns with conventional draw-off speeds of at least 2500 m/min are lengths of about 300 mm, preferably for POY ^ 250 mm to The process according to the invention is similarly suitable for high-speed spinning of POY threads with a POY filament titre of > 3 dtex to 20 dtex and more, and also POY filament titres of For further processing of the strand in the stretch texturizing process at high speeds, the following is important: Strands according to this invention as roving yarn for stretch texturizing - usually called POY - are produced with draw-off speeds of > 2500 m/min, preferably > 3500 m/min, particularly preferably > 4000 m/min. These yarns must have a physical structure which is characterized by a specific degree of orientation and a low crystallization. The parameters of elongation at break, birefringence, degree of crystallization and shrinkage at the boil have proved appropriate for its characterization. The polymer mixture according to the invention is characterized by an elongation at break of the PET strands (POY) of at least 85 % and not more than 180 %. The shrinkage at the boil is 32 - 69 %, the birefringence is 14 between 0.03 0 and 0.075, the crystallinity is less than 20 % and the tear strength is at least 17 cN/tex. The elongation at break of the PET strands is preferably between 85 and 160 %. Particularly favourable circumstances exist if the elongation at break of the PET strands is between 109 and 146 %, the tear strength at the same time is at least 22 cN/tex and the Uster value is not more than 0.7 %. Stretch texturizing is carried out at different speeds, depending on the filament titre type, speeds of > 750 m/min, preferably > 900 m/min, being used for normal-titre filaments of > 2 dtex per filament (final titre) . For microfilaments and fine titres (final titre) of The stretching ratios to be applied are between 1.35 and 2.2 for the strands specified, stretching ratios in the upper range preferably being used for a lower degree of orientation and vice versa. During the stretch texturizing, the stretching ratio is influenced by variations in tension (surging) as a function of the operating speed. Particularly preferred stretching ratios are therefore those according to the formula: stretching ratio = 5 o 10~4 o w (m/min) + b wherein w = stretch texturizing speed in m/min b = constant which lies between 1.15 and 1.50, to be applied. The additive polymers to be added according to the invention to the polyester can have a varying chemical 15 composition, as long as they have the abovementioned properties. Three different copolymer types are preferred, that is to say 1. A copolymer which comprises the following monomer units: A = acrylic acid, methacrylic acid or CH2 = CR - COOR, wherein R is an H atom or a CH3 group and R is a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical, B = styrene or C1-3-alkyl-substituted styrenes, wherein the copolymer comprises 60 to 98 wt.% A and 2 to 40 wt.% B, preferably 83 to 98 wt.% A and 2 to 17 wt.% B, and particularly preferably 90 to 98 wt.% A and 2 to 10 wt.% B (total = 100 wt.%). 2. A copolymer which comprises the following monomer units: C = styrene or C1-3-alkyl-substituted styrenes, D = one or more monomers of the formula I, II or III wherein R1, R2 and R3 are each an H atom or a C1-15_alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical, wherein the copolymer comprises 15 to 95 wt.% C and 2 to 80 wt.% D, preferably 50 to 90 wt.% C and 5 to 50 wt.% D, and particularly preferably 70 to 85 wt.% C 16 and 15 to 30 wt.% D, the total of C and D together giving 100 %. A copolymer which comprises the following monomer units: E = acrylic acid, methacrylic acid or CH2 = CR - COOR, wherein R is an H atom or a CH3 group and R' is a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical, F = styrene or C1-3-alkyl-substituted styrenes, G = one or more monomers of the formula I, II or III wherein Rl R2 and R3 are each an H atom or a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical, H = one or more ethylenically unsaturated monomers, which can be copolymerized with E and/or with F and/or G, from the group which consists of a-methy1styrene, vinyl acetate, acrylic acid esters, methacrylic acid esters which differ from E, vinyl chloride, vinylidene chloride, halogen-substituted styrenes, vinyl ethers, isopropenyl ethers und dienes, the copolymer comprising 30 to 99 wt.% E, 0 to 50 wt.% F, >0 to 50 wt.% G and 0 to 50 wt.% H, preferably 45 to 97 wt.% E, 0 to 30 wt.% F, 3 to 40 wt.% G and 0 to 30 wt.% H, and particularly preferably 60 to 94 wt.% E, 0 to 20 wt.% F, 6 to 17 30 wt.% G and 0 to 20 wt.% H, the total of E, F, G and H together giving 100 %. Component H is an optional component. Although the advantages to be achieved according to the invention can already be achieved by copolymers which contain components from groups E to G, the advantages to be achieved according to the invention also arise if further monomers from group H participate in the building up of the copolymer to be employed according to the invention. Component H is preferably chosen such that it has no adverse effect on the properties of the copolymers to be used according to the invention. Component H can be employed, inter alia, to modify the properties of the copolymer in a desired manner, for example by increases or improvements in the flow properties when the copolymer is heated to the melting temperature, or to reduce a residual colour in the copolymer, or, by using a polyfunctional monomer, to introduce a certain degree of crosslinking into the copolymer in this manner. In addition, H can also be chosen such that copolymerization of components E to G is rendered possible at all or is assisted, such as in the case of MAA and MMA, which do not in themselves copolymerize, but copolymerize without problems on addition of a third component, such as styrene. Monomers which are suitable for this purpose include, inter alia, vinyl esters, esters of acrylic acid, for example methyl und ethyl acrylate, esters of methacrylic acid which differ from methyl methacrylate, for example butyl methacrylate and ethylhexyl methacrylate, vinyl chloride, vinylidene chloride, styrene, tx-methylstyrene and the various halogen-substituted styrenes, vinyl und isopropenyl ether, dienes, such as, for example, 1,3-butadiene, and 18 divinylbenzene. The reduction in the colour of the copolymer can particularly preferably be achieved, for example, by using an electron-rich monomer, such as, for example, a vinyl ether, vinyl acetate, styrene or methylstyrene. Particularly preferred compounds of component H are aromatic vinyl monomers, such as, for example, styrene or -methylstyrene, The preparation of the copolymers to be used according to the invention is known per se. They can be prepared by bulk, solution, suspension or emulsion polymerization. Helpful notes in respect of bulk polymerization are to be found in Houben-Weyl, volume E20, part 2 (1987), page 1145 et seq. Notes on solution polymerization are likewise to be found there on page 1156 et seq. The suspension polymerization technique is likewise described there on page 1149 et seq., while emulsion polymerization is likewise described and explained there on page 1150 et seq. Bead polymers, the particle size of which lies in a particularly favourable range, are particularly preferred in the context of the invention. The copolymers to be used according to the invention, for example, by mixing into the melt of the fibre polymers are particularly preferably in the form of particles having an average diameter of 0.1 to 1.0 mm. However, larger or smaller beads or granules can also be employed. The polymers according to the invention can comprise, as_ further constituents, additives such as are usual for thermoplastic moulding compositions and contribute towards improving the polymer properties. Examples of these which may be mentioned are: antistatics, antioxidants, flameproofing agents, lubricants, dyestuffs, light stabilizers, polymerization catalysts and auxiliaries, adhesion promoters, matting agents and/or organic 19 phosphites. These additives are employed in the usual amount, preferably in amounts of up to 10 wt.%, preferably The imidized copolymer types 2 and 3 can be prepared both from the monomers using a monomeric imide and by subsequent complete or, preferably, partial imidation of a copolymer comprising the corresponding maleic acid derivative. These additive polymers are obtained, for example, by complete or, preferably, partial reaction of the corresponding copolymer with ammonia or a primary alkyl- or arylamine, for example aniline, in the melt phase (Encyclopedia of Polymer Science and Engineering vol. 16 [1989], Wiley-Verlag, page 78). All the copolymers according to the invention, as well as their non-imidized starting copolymer, where appropriate, are commercially obtainable or can be prepared by a process familiar to the expert. For polymer mixtures of polyethylene terephthalate with an intrinsic viscosity of about 0.55 to 0.75 dl/g and copolymers of type 1, 2 or 3, copolymers having viscosity numbers in the range from 70 to 130 cm3/g are preferred. The process according to the invention enables the draw-off speed during strand production to be increased substantially compared with the prior art by the addition of a copolymer to the polyester, while the stretching ratio during the stretch texturizing can be kept constant, corresponding to the non-modified polyester. The capacity of the production unit therefore increases directly proportionally to the draw-off speed. Since the capacity of the spinning station is proportional to the product of the stretching ratio and draw-off speed, the gain in capacity in the spinning mill is: wherein 20 VV1 = stretching ratio with additive VVo = stretching ratio without additive V1 = winding up speed of the strand with additive Vo = winding up speed of the strand without additive Typically v0 is in the range from 2500 to 3500 m/min and VVo is between 1.35 and 2.2, corresponding to the spinning speed according to the known prior art. The dependent variables M, M, P and N according to the invention state that the amount of additive added may not be chosen independently of the draw-off speed if the aim of producing, from polymer mixtures, preorientated filaments of low crystallinity which are suitable for stretch texturizing is to be achieved. It is necessary to avoid here on the one hand the degree of preorientation being too low, i. e. e. g. the elongation at break will be too high, and on the other hand a noticeable spinning-induced crystallization occurring at too high a degree of orientation. The stretching ratio during stretch texturizing has been determined for filaments produced at various draw-off speeds and additive concentrations. The relationships of M7 P and N here are represented as lines of constant stretching ratio. This results in a particular advantage of this process. The filament producer can choose and adjust the amount of additive at any desired draw-off speed such that he obtains a stretching ratio which is optimum for his further processing conditions. Stretch texturizing is therefore carried out under optimum, selectable conditions. The values for properties stated in the following examples and in the above text were determined as follows: Distribution of the additive particles: Melt strands or pellet samples were broken down with a sharp chisel in 21 liquid nitrogen. The broken surfaces were investigated by-means of scanning electron microscopy and subsequent evaluation by image analysis, taking as the basis an elliptical form (spheroidal), the length, width and, calculated therefrom, average diameter being evaluated. Thread speeds were determined by means of laser Doppler anemometry using a diode laser of 10 mW output, TSI GmbH, Aachen/DE, type LS50M. In this method, a laser beam is divided and the two component beams are made to intersect on the object to be measured. The interference frequency is measured in the backscatter region and the object speed is calculated from the shift in the interference frequency. The thread speed was measured at several distances underneath the spinneret. The change in speed until the speed defined by the draw-off device is reached characterizes the spinning draft zone. The length between the speed points of 1000 m/min and 90 % of the final speed in [mm] was defined as the measure. This draft length is usually several 100 mm. At high spinning speeds, it can be shortened to about 100 mm, a constriction (necking) of the thread occurring; the change in thread speed in the region from about 1750 m/min is then almost punctiform. The intrinsic viscosity was determined on a solution of 0.5 g polyester in 100 ml of a mixture of phenol and 1,2-dichlorobenzene (3 : 2 parts by wt.) at 25 BC. The viscosity number VN (also Staudinger function) is the concentration-related relative change in the viscosity of a 0.5% solution of the copolymer in chloroform, based on the solvent, the flow-through times being determined in an Ubbelohde viscometer with a suspended ball level, Schott type no. 53203 and capillary 0c in accordance with DIN standard 51562 at 25 aC. Chloroform was used as the solvent. 22 wherein t = flow-through time of the polymer solution in seconds t0 = flow-through time of the solvent in seconds c = concentration in g/100 ccm To determine the melt viscosity (initial viscosity), the polymer was dried in vacuo to a water content of plate rheometer, type UM100, Physica MeStechnik GmbH, Stuttgart/DE, with masking with nitrogen. After the sample had melted, i. e. after approx. 30 seconds, the measuring ball (MK210) was positioned on the measuring plate. The measurement was started after a further heating up period of 60 seconds (measurement time = 0 seconds). The measurement temperature was 290 aC for polyethylene terephthalate and additive polymers added to polyethylene terephthalate, or was the same as the melting temperature (method follows) of the polyester in question plus 34.0 SC. The measurement temperature specified in this way corresponds to the typical processing or spinning temperature of the particular polyester. The amount of sample was chosen such that the rheometer gap was filled completely. The measurement was carried out in oscillation with a frequency of 2.4 Hz (corresponding to a shear rate of 15 sec"1) and a deformation amplitude of 0.3, and the value of the complex viscosity was determined as a function of the measurement time. Thereafter, the initial viscosity was converted to the measurement time zero by linear regression. 23 For the determination of the melting temperature of the polyester, the polyester sample was first melted at 310 EC for 1 min and quenched to room temperature immediately thereafter. The melting temperature was then determined by DSC measurement (differential scanning calorimetry) at a heating up rate of 10 2C/min. The pretreatment and measurement were carried out with masking with nitrogen. The flow activation energy (E) is a measure of the rate of change of the zero viscosity as a function of the change in measurement temperature, the zero viscosity being the viscosity extrapolated to the shear rate 0. The zero viscosity was measured at temperatures in the range from 240 to 280 eC with a high-pressure capillary rheometer, type Rheograph 2002, Gottfert GmbH, Buchen/DE, and the results were evaluated by the three parameter plot of Carreau-Winter. Thereafter/ the flow activation energy was determined by means of the Arrhenius plot from the zero viscosity in accordance with the method of M. Pahl et al. , Praktische Rheologie der Kunststoffe und Elastomere [Practical rheology of plastics and elastomers], VDI-Verlag, Dusseldorf (1995), pages 256 et seq. The strength properties were determined with a tensile tester at a clamped length of 200 mm, a pretension force of 0.05 cN/dtex and a test speed of 2000 mm/min. The shrinkage at the boil was determined on fibres which had been conditioned at room temperature and treated beforehand for 10 min in water of 95 ± 1 2C. The birefringence was measured as described in DE 195 19 898 A and the Uster-values were measured as described in EP 0 346 641 B. The stretching force was determined with a Dynafil M apparatus from Textechno, M6nchengladbach/DE at a heating tube temperature of 200 2C and a test speed of 100 m/min. 24 The crystallinity (C) was calculated from the density p according to the density being determined on short knotted pieces of thread at 23 2C by the density gradient method (in CCl4/n-heptane) . The crimping parameters of the texturized filament yarns (nominal titre to 500 dtex) were determined in accordance with DIN 53840, part 1. The depth of dyeing was determined on a circular knitted piece dyed with Terasil navy blue GRL-C 200 % (Ciba-Geigy, Basel/CH) by comparative measurement of the colour reflection with a reflectance photometer in accordance with DIN 54001. Example 1: (comparison) Polyethylene terephthalate having an intrinsic viscosity intr = 0.64 dl/g (corresponds to an initial viscosity of 250 Pa's) and a residual water content of The strands emerging from the bores of the die plate were cooled in a conventional blowing shaft with transverse blowing, the air speed being adjusted to 0.45 m/sec. At a distance of 1200 mm below the spinneret, the cooled strands were bundled by means of an oiler pin and provided 25 with a spinning oil-water emulsion, the amount of preparation applied to the thread being 0.35 %, based on the thread weight. The thread bundle was drawn off by means of two driven godets entwined in s-shaped form and wound on empty bobbins to yarn packages in a winding unit from Barmag AG, Remscheid/DE, type SW7, with birotor changing. The spinning draw-off speed was defined by the circumferential speed of the godets. The winding speed was set about 1 % lower, so that a tension of 10 cN resulted between the godets and winder. The nominal titre of the thread produced in this way was 84/34 dtex. The take-off speed was adjusted to 3200 m/min, an amount of polymer of 41.1 g/min being fed to the spinneret. The strand characteristic data are summarized in table 1. Table 1: Reference POY No. Comparison experiment CV: coefficient of variation 26 Example 2: The spinning system according to example 1 was supplemented by a metering device comprising a compounding extruder and a gear metering pump. Using this metering system, the additive, with a residual water content of The spinning draw-off speed, however, was adjusted to a constant speed,of 5000 m/min. The polymer throughput was 63 g/min, which resulted in an average residence time of the melt of about 7.5 min before entry into the spinneret package. In another comparison experiment (no. 3), the additive Delpet 80N was metered in a concentration of 1.8 wt.% into the PET melt stream and spun under the same conditions. In further experiments (no. 4-9), polymer mixtures according to the invention were spun under the same conditions, but the amount of the particular copolymer added was only 0.65 wt.%. The additives were products from Degussa AG, Hanau/DE, that is to say copolymers with, in the polymer, 8.8 wt.% styrene (S) and 91.2 wt.% methyl methacrylate (MMA) and various viscosity numbers (according to table 2). In experiment no. 9, under otherwise the same conditions, a polymer mixture was prepared and spun at a temperature of only 286 SC. The strand characteristic data for this and 27 the abovementioned experiments are summarized in table 2a and 2b. Table 2a: 28 Table 2b: number Viscosity :1 1.7 2.4 4.4 4.5 5.1 4.4 ratio* E** kJ/mol 110 Titre dtex 130 129 130 129 129 130 Draw-off m/min 5000 5000 5000 5000 5000 5000 speed Spinning 2C 296 296 296 296 296 286 temperature Elongation at % 96.4 112.1 115.1 123.4 113.2 116.1 break Melt viscosity of the additive polymer to melt viscosity of the polyester (=1) * Flow activation energy When the viscosity number of the additive polymer added is increased, an increase in the elongation at break is initially found, i. e. a maximum improvement in the profitability is observed on addition of the copolymer with a viscosity number of about 105 ccm/g. When the additive with an even higher viscosity number is added, the profitability of the process decreases again slowly. Compared with the additive disclosed in EP 47 464 B, about the same capacity-increasing effect is achieved with the copolymers according to the invention with viscosity numbers in the range from 91 to 118 ccm/g, with a drastically reduced amount of additive. 29 This reduction in the amount of additive not only is advantageous economically, but also means a considerable technological advantage. Impairments in the further processing properties, such as e. g. sticking of additive inclusions on the thread surface to the hot metal surfaces of the heaters(of texturizing units, are reduced considerably if it is possible - as in the context of this invention - to decrease the amount of additive added. Furthermore, the boundary between additive inclusions and polyester matrix represents a defective point in the transfer of mechanical stresses in the yarn, because of the incompatibility of the two materials, which at high additive concentrations can lead to capillary breakages. This effect is the more pronounced the higher the amount of additive, and impairs the texturizing properties and the tear strength of the texturized yarn. In experiments.no. 6 and 9, in spite of the drastically changed pre-exposure of the melt mixture to heat by using a spinning temperature of 286 2C and 296 2C respectively, virtually the same elongations at break are achieved, i. e. the additive according to the invention is distinguished by a good heat stability in the temperature range relevant on a large industrial scale. Example 3: In further experiments further polymer mixtures were spun under the same conditions as in example 2, the amount of the particular additive added being 0.72 wt.%. The additives were copolymers from Degussa AG, Hanau/DE with, in the polymer, 8.8 wt.% styrene, 86.2 wt.% MMA and 5 wt.% N-cyclohexylmaleimide and various viscosity numbers, as shown in table 3, which also contain the strand characteristic data. 30 Table 3: Experiment No. 10 11 12 13 14 15 16 17 Additive wt. % 0.72 0.72 0.72 0.72 0.72 0.72 0.72 0.72 concentration Viscosity ccm/g 61 72 88 99.4 99.6 113.7 128.6 174 number Viscosity :1 0.8 2.0 3.2 4.0 4.2 5.6 9.6 11.2 ratio* E** kJ/mol 120 Titre dtex 129 129 131 131 129 131 129 129 Draw-off m/min 5000 5000 5000 5000 5000 5000 5000 5000 speed Spinning fiC 296 296 296 296 296 296 296 296 temperature Elongation at % 70.1 85.5 106.7 125.9 127.6 133 125.1 49.2 break (* and ** see table 2b) Comparison experiments no. 10 and 17 and experiments no. 11 to 16 again confirm the existence of a pronounced optimum of the additive viscosity with regard to the capacity-increasing effect and the elongation at break. In the range of viscosity numbers from 61 to about 100 ccm/g, the profitability of the process initially increases virtually linearly with the viscosity number. In the .range from VN = 100 ccm/g up to the viscosity number of about 115 ccm/g the profitability then improves further only slightly. Above this optimum, the profitability again is reduced slightly up to the viscosity number of about 130 ccm/g. At VN = 174 ccm/g, a distinctly negative effect in respect of capacity occurs. Experiment no. 11 gives a POY with a lower elongation at break than the other experiments and therefore lies in the limit region of the invention. 31 Example 4: In experiment no. 18, a die package with a die plate with 17 bores instead of 34 bores was employed in the spinning system from example 2. Under otherwise unchanged conditions, 0.65 wt.% of the additive according to the invention was mixed in with 8.8 wt.% styrene and 91.2 wt.% MMA of viscosity number VN = 98.5 ccm/g, and the polymer mixture was spun to a thread with a nominal titre of 84/17 dtex at an amount of polymer of 63 g/min, a spinning draw-off speed of 5000 m/min and a spinning temperature of 296 eC. In another experiment (no. 19), under otherwise unchanged conditions, a spinneret plate with 72 bores, bore diameter 0.10 mm, L = 2D, was employed and a polymer mixture with the same additive as in experiment no. 18 was spun at a spinning speed iof 5000 m/min to a thread of nominal titre 84/72 dtex. Finally, a spinneret plate with 120 bores, bore diameter 0.13 mm, 1 = 2D, was employed and with an addition of 0.65 wt.% of the same additive as before, an amount of polymer of 58 g/min and a spinning speed of 4500 m/min, a thread of nominal titre 84/120 dtex was spun (experiment no. 20). The characteristic data of all the strands are summarized in table 4. 32 Table 4: Comparison example 5: Polyethylene terephthalate having an intrinsic viscosity intr = 0.64 dl/g (corresponding to an initial viscosity of 250 Pa.s) and a residual water content of At the discharge of this spinning pump, the melt was divided into 6 component streams with throughputs the same as one another. Each of these component streams was fed through a spinneret adapter with 2 static mixers, type SMX DN 10, from Sulzer AG, Zurich/CH, to a spinneret package. 33 The die package comprised, viewed in the melt flow direction, defined shear and filtration means of the following construction: Steel grit volume of particle size 350 to 500 m, support plate, second fabric filter of 20 pin, spinneret plate with 34 bores, bore diameter 0.25 mm, L = 2D and a diameter of the plate of 80 mm, corresponding to a filter area of 40 cm2. With a varied polymer throughput, a pressure of 110 - 190 bar is established. The strands emerging from the bores of the spinneret were cooled in a conventional blowing shaft with transverse blowing, the .air speed being adjusted to 0.55 m/min. At a distance of 1500 mm below the spinneret, the cooled strands were bundled by means of an oiler pin and provided with a spinning oil-water emulsion, the amount of preparation applied to the threads being about 0.35 %. The thread bundle was drawn off by means of two driven godets entwined in s-shaped form and wound on 6 empty bobbins to yarn packages in a winding unit from Barmag AG, Remscheid/DE, type CW8 T-920/6, with birotor changing. The spinning draw-off speed was defined by the circumferential speed of the godets. The winding speed was set about 1 % lower, so that. a tension of about 10 cN resulted between the godet and winder. The nominal titre of the threads produced in this way was 84/34 dtex. The draw-off speed was adjusted to 3200 m/min, an amount of polymer per spinneret of 44 g/min being established, resulting in an average residence time of the melt before entry into the-spinning pump of about 15 min. In a second experiment, the draw-off speed was increased to 5000 m/min and at the same time an amount of polymer of 63 g/min per spinneret with an average residence time of about 11 min was established. The characteristic data of the strands are 34 summarized in table 5 as the mean of all 6 bobbins of each individual experiment. Table 5: Comparison experiment No. El E2 ratio The strands from comparison experiments no. El and no. E2 were further processed in a converted Barmag stretch texturizing machine, type FK6-S-900, equipped with the Barmag disc unit, type 7, with polyurethane discs PU, H6, 35 configuration 1-4-1, D/Y = 1.84, heater temperatures 1 and 2 = 195 / 160 2C at a speed of 800 m/min and heater temperatures 1 and 2 = 210 / 160 -C at a speed of 1000 m/min. The stretching ratio, determined from the ratio of the discharge speed to the intake speed, was adjusted to match the characteristic data of the strand, and is summarized in table 6 with the characteristic data achieved for the texturized yarn as the mean of all 6 bobbins of each individual experiment. Table 6: Results of the stretch texturizing of experiment no. El -E2 (+ = positive; 0 = limited processability; - = negative) Comparison example El corresponds to the prior art both as regards the properties of the strand and in the stretch texturizing. When the spinning speed is increased to 5000 m/min, problems arise in the stretch texturizing in the form of breakages and thread tension defects, and the stretching ratio to be used must be greatly reduced. The strength which can be achieved is also lower. The reason lies in the increased degree of crystallization of the POY strand, and is characterized by a correspondingly lower 36 elongation at break and necking behaviour in the spinning draft. Example 6: In the spinning system according to example 5 and under the same spinning conditions, an additive polymer according to the invention with a residual water content of The additive polymer was a product of Degussa AG, Hanau/DE, type Degalan® PVPMS, corresponding to a copolymer according to the invention of the following composition: 8.8 wt.% styrene, 91.2 wt.% MMA; viscosity number VN = 98.5 ccm/g The ratio of the melt viscosities of additive to polyester according to this invention was 4.8 and the residence time of the polymer mixture in the mixing zone (7 mixing elements, as example 5) was 8 s. The spinning draw-off speed was adjusted to a constant speed of 5000 m/min. The polymer throughput per spinneret was 63 g/min. The die pressure was in the range from 145 to 150 bar. Table 7 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment. In comparison examples E3 and E4, the amount of additive is lower than the parameter N defined above, and is therefore so low that although there is a significant difference to non-modified yarn, the amount of additive is not sufficient 37 to reduce the crystallinity and the necking to the required extent so that good further processing properties are ensured. In contrast, experiments no. E5 to E8 are according to the invention. Table 7: Experiment No. E3 E4 E5 E6 E7 E8 Residence time min 11 11 11 11 11 11 Number of SMX 7 7 7 7 7 7 elements Spinning temperature 2C 290 290 290 290 290 290 Draw-off speed m/min 5000 5000 5000 5000 5000 5000 Additive wt. % 0.12 0.17 0.41 0.77 0.97 1.47 concentration Spinning titre dtex 129.7 128.6 128.7 127.2 129.3 129.4 Elongation at break % 70.4 73.4 90.3 118.1 139.9 167.0 CV elongation at % 3.1 3.5 2.5 2.2 2.5 2.6 break Tear strength cN/tex 34.9 34.7 30.6 25.6 22.8 17.0 CV breaking load % 3.1 2.6 2.4 2.3 3.0 2.7 Birefringence X 10"3 86.3 81.4 72.5 58.1 36.5 Shrinkage at the % 4.7 7.8 50.8 60.7 57.3 61 38 The strands according to the invention were subjected to stretch texturizing as in example El at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 8 as the mean of all 6 bobbins of each individual experiment. Table 8: Results of the stretch texturizing of experiments E5 - E8 {+ = positive; 0 = limited processability; - = negative) The additive amount in experiment E6 was most appropriate for the spinning conditions. The best properties of the stretch-texturized yarn were achieved here. It was also possible to increase the texturizing speed to 1000 m/min with positive processing properties without problems, while the comparison yarn according to the prior art from example El had already showed a deterioration in the processing properties when the texturizing speed was increased from 800 to 1000 m/min (tab. 6). Good stretch texturizing results were also to be achieved in examples E5, E7 and E8. However, the amount of additive in these experiments is no longer in the particularly preferred range. This manifests itself in a slight but still non-critical reduction in the tear strength and elongation at break, in particular in example E8, where the 39 amount of additive deviated the most from the particularly-preferred range. Example 7: In the metering system and spinning system according to example 6 and under the same spinning conditions, the same additive polymer as in example 6 was added to the polyethylene terephthalate chips, again in various concentrations. In this case, the spinning draw-off speed was adjusted to a constant speed of 4350 m/min. The polymer throughput per spinneret was 55 g/min. The die pressure was in the range from 130 to 145 bar. Table 9 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment. 40 ratio The strands were subjected to stretch texturizing as in experiment El at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 10 as the mean of all 6 bobbins of each individual experiment. In experiment E10, the additive concentration was particularly appropriate for the spinning speed, so that firstly particularly preferred properties of the strand resulted, and secondly the best yarn properties and the 41 best processing properties were also achieved in the stretch texturizing. Stretch-texturized yarns of good quality were also produced in experiments Ell and E12. In experiment Ell, the amount 'of additive metered in is no longer in the particularly preferred range. As a result, the elongation at break of the strand also lies outside the preferred range, and in comparison with experiment E10, a slight reduction in the tear strength and elongation at break of the stretch-texturized yarn can be seen. This trend continues in experiment E12, where the amount of additive is also outside the preferred range of addition. Table 10: Results of the stretch texturizing of experiment no. E10 -E12 (+ = positive; 0 = limited processability; - = negative) Example 8: In the metering and spinning system according to example 6 and under otherwise the same conditions, the spinning speed was varied between 3200 m/min and 6000 m/min. The amount of additive metered in was adjusted here such that elongations at break of between 115 % and 133 % resulted in the POY yarn. 42 Table 11 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment. For comparison, the data of experiment no. El contained in table 5 are listed again. ratio Table 11: 43 The strands were subjected to stretch texturizing as in example 5 at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 12 as the mean of all 6 bobbins of each individual experiment. Table 12: Results of the stretch texturizing of experiment no. El, E6, E10, E13, E14 Experiment No. El E13 E10 E6 E14 Speed m/min 1000 1000 1000 1000 1000 Stretching ratio 1: 1.79 1.86 1.73 1.72 1.72 Tension Fl / F2 cN 32/31 31/28 35/21 32/29 31/28 Elongation at % 19.2 18.6 20.6 21.5 20.1 break Tear strength cN/tex 45.3 44.7 45.5 45.2 43.8 Dyeing level 1-2 1-2 1-2 1-2 1-2 Processing 0 + + + + properties {+ = positive; 0 = limited processability; - = negative) In all the experiments according to this invention, the amount of additive added was ideally appropriate for the spinning speed. Strands with preferred properties which also gave outstanding results in the stretch texturizing resulted. Example 9: The spinning system according to example 2 was modified to the extent that the number of static mixers used for mixing in the additive was reduced from 15 to 9 and 3 respectively, corresponding to residence times of 44, 26 and 9 s. The same spinning conditions were otherwise maintained. SEM investigations were carried out on pellet 44 samples of the modified polyester emerging from the spinneret, to evaluate the distribution of the additive. The result is summarized in table 13, together with the elongation at break of the resulting POY yarn. If the additive is mixed in inadequately (experiment Ml) , its effectiveness - recognizable by the decreasing elongation at break - is reduced considerably. The reason for the reduced effectiveness of the additive is the increasing content of additive particles of > 1000 ran diameter and the poorer distribution over the yarn cross-section. This is visible in SEM photographs and in graph plots of the particle size against the number of particles. Table 13: Influence of the mixer design (nominal width DN 15) Experiment No. Ml M2 M3 Elongation at break % 77 109.2 116.2 POY Number of mixing 3 9 15 elements Average particle run 0.22 0.21 0.19 diameter Content of particles % 1.5 0.5 0 > 1000 nm Example 10: Preparation examples for copolymers 1. A mixture of 4750 g completely desalinated water and 118 g Degapas® 8105 S was heated to 40 eC in a 10 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 4750 g of a mixture of 86.2 parts by weight methyl methacrylate (MMA), 8.8 parts by weight styrene, 5 parts by weight cyclohexylmaleimide, 0.14 part by weight 2-ethylhexyl thioglycollate, 0.09 part by 45 weight t-dodecylmercaptan, 0.05 part by weight stearic acid and 0.25 part by weight dxlauroyl peroxide were then added, while stirring. The batch was polymerized at 80 eC for 165 minutes and at 90 CC for 60 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 eC in a fluidized bed drier. 4710 g of clear polymer beads with a viscosity number of 99.6 ccm/g were obtained. 2. A mixture of 2400 g completely desalinated water and 46 g of a 6 per cent aqueous solution of a methacrylic acid copolymer was heated to 40 aC in a 5 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 2400 g of a mixture of 90.65 parts by weight methyl methacrylate (MMA), 8.75 parts by weight styrene, 0.15 part by weight 2-ethylhexyl thioglycollate, 0.1 part by weight t-dodecylmercaptan, 0.05 part by weight stearic acid and 0.3 part by weight dilauroyl peroxide were then added, while stirring. The batch was polymerized at 80 aC for 150 minutes and at 90 CC for 30 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 2C in a fluidized bed drier. 2283 g clear polymer beads with a viscosity number of 98.5 ccm/g were obtained. 3. A mixture of 2400 g completely desalinated water and 46 g of a 6 per cent aqueous solution of a methacrylic acid polymer was heated to 40 CC in a 5 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 2400 g of a mixture of 90.715 parts by weight methyl methacrylate {MMA), 8.75 parts by weight styrene, 0.115 part by weight 2-ethylhexyl thioglycollate, 0.07 part by weight t-dodecylmercaptan, 0.05 part by weight stearic acid 46 and 0.3 part by weight dilauroyl peroxide were then added, while stirring. The batch was polymerized at 80 eC for 150 minutes and at 90 eC for 60 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 2C in a fluxdized bed drier. 2299 g clear polymer beads with a viscosity number of 118.4 ccm/g were obtained. -47-WE CLAIM 1. Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastfcalfy processable coporymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula. 2. Process as claimed in claim 1, wherein the ratio of the melt viscosity of the copofymer to the mett viscosity of (he polyester is 1.4 : 1 to 8 :1. 3. Process as claimed in claim 1 or 2, wherein the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester Is 1.7 :1 to 6.5 :1. 4. Process as claimed in claim 1, 2 or 3 wherein the copolymer comprises the following monomer units: A= acrylic acid, methacryfic acid or CH2 = CR - COOR', wherein R is an H atom or a CH3 group and R1 is a C1-15 -alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical. -48-B = styrene or C1-3 -alky1-substituted styrenes, wherein the copolymer comprises 60 to 98 wt.% A and 2 to 40 wt.% B (total = 100 wt%). 5. Process as claimed in claim 4 wherein the copolymer comprises 83 to 98 wt. % A and 2 to 17 wt. % B (total = 100 wt. /.) . 6. Process as claimed in claim 4 or 5 wherein the copolymer comprises 90 to 98 wt.% A and 2 to 10 wt.% B (total = 100 wt.%). 7. Process as claimed in claims 1, 2 or 3, wherein the copolymer comprises the follawing monomer units: C = styrene orC - alkyl-substituted styrenes, 1-3 D = one or more monomers of the formula I, II or III wherein R , R and R are each an H atom or a C - alkyl radical or a C - cycloalkyl radical 1-15 5-12 or a C - aryl radical, 6-14 and wherein the copolymer comprises 15 to 95 wt. % C and 2 to 80 wt. % D, the total of C and D together giving 100%. 8. Process as claimed in claim 7, wherein the copolymer comprises 50 to 90 wt. % C and 5 to 50 wt. % D, the total of C and D together giving 100%. -49- 9. Process as claimed in claims 7 or 8, wherein the copolymer comprises 70 to 85 wt.% C and 30 to 15 wt. % D, the total of C and D together giving 100 %. 10. Process as claimed in claims 1, 2 or 3, wherein the copolymer comprises the following monomer units: E = acrylic acid, methacrylic acid or CH - CR - COOR', wherein 2 R is an H atom or a CH group, and R is a C -alkyl 3 1-15 radical or a C cycloalkyl radical or a C -aryl 5-12 6-14 radical, F = styrene or C 1-3 - alkyl - substituted styrenes, G = one or more monomers of the formula I, II or III wherein R1 , R2 , R3 are each an H atom or a C1-15 - alkyl radical or a C5-12 - cycloalkyl radical or a C 6-14, - aryl radical H = one or more ethylenically unsaturated monomers, which can be copolymerized with E and/or with F and/or 6, from the group which consists of -methylstyrene, vinyl acetate, acrylic acid esters, methacrylic acid esters which differ from E, vinyl chloride, vinyl idene chloride, halogen-substituted styrenes, vinyl esters, isopropenyl ethers und dienes, -50- wherein the copolymer comprises 30 to 99 wt.% E, 0 to 50 wt.% F, >0 to 50 wt. % of G and 0 to 50 wt.% of H, the total of E, F, G and H together giving 100%. 11. Process as claimed in claim 10 wherein the copalymer comprises 45 to 97 wt-% E, 0 to 30 wt- % of F, 3 to 40 wt.% of G and 0 to 30 wt.% of H, the total of E, F, G and H together giving 100%. 12. Process as claimed in claim 10 or 11, wherein the copolymer comprises 60 to 94 wt. % of E, 0 to 20% wt.% of F, 6 to 30 wt- % of G and 0 to 20 wt.% of H, the total of E, F, B and H together giving 100 %. 13. Process as claimed in one or more claims 1 to 12, wherein the copolymer comprises additives in an amount of in each case 14. Process as claimed in one or more of claims 1 to 13, wherein the polymer mixture is prepared, after melting of the polyester and copolymer, in a static mixer, the diameter of which - 1 is chosen such that the shear rate is between 16 and 128 s and the product of the shear rate and the 0.8th power of the residence time in seconds is greater than 250. 15. Process as claimed in one or more of claims 1 to 14, wherein the mixture is subjected to shear treatment during mixing isuch that the average particle size of the copolymer immediately -51- after discharge from the spinneret is not more than 400 nm, that less than 1 % of the copolymer particles contained in the mixture have a particle size of > 1 m, and that the length/diameter ratio of the copolymer particles is > 2, the copolymer particles being present in the polymer matrix in the filaments in the form of fibrils after the spinning draft and the length/diameter ratio of the fibrils being > 50. 16. Process as claimed in one or more of claims 1 to 15, wherein the polyester is a thermoplastically processable polyester, such as polyethylene terephthalate, polyethylene naphthalate, polypropylene terephthalate or polybutylene tere- phthalate, it being possible for the polyester optionally to comprise up to 15 mol % of a comonomer and/or up to 0.5 wt. % of a polyfunctional branching component. 17. Process as claimed in one or more of claims 1 to 16, wherein the filaments are initially wound up after the spinning and are then subjected to a stretch tsxturizing, the stretching ratio being between 1: 1.35 and 1: 2.20. 18. Process as claimed in claim 17 wherein the textured filaments with a capillary titre of more than 2 dtex are produced at a processing speed of at least 750 m/min and the texturezed filaments with a capillary titre of less than 2 dtex are produced at a processing speed of at least 400 m/min. -52- 19. Preorientated filaments produced according to the process as claimed in one or more of claims 1 to 16 wherein they have an elongation at break of 85 to 180%, a tear strength of at least 17 cN/tex, a shrinkage at the boil of 32 to 69/,, a birefringence of 0.030 to 0.075 and a crystal 1inity of less than 20%. 20. Preorientated filaments as claimed in claim 19, wherein they have an elongation at break of 109 to 146%, a tear strength of at least 22 cN/tex and a normal Uster of 21. Texturised filaments wherein they are produced from the preorientated filaments as claimed in claims 19 and 20 in accordance with the process as claimed in claims 17 and 18. Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula.

Full Text

1A

This invention relates to a process for the production of preorientated filaments.
The present invention relates to a process for the production of preorientated filaments from polyester-based polymer mixtures prepared in the melt, with the addition of an amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100OC, by spinning the molten polymer mixtures with a draw-off speed v of at least 2500 m/min.
Spinning of polymer mixtures is known from a number of publications:
EP 0 035 796 A (Teijin) describes synthetic fibres, inter alia of polyester or polyamide, which comprise 1 - 15 wt. % of a polysulphone polymer having a high glass transition point, of TG > 150 °C. The additive remains in the matrix in a spheroidal form and influences the surface structure of the filaments and the thread friction. The spinning speed is 2000 - 5500 m/min.
EP 0 041 327 B (ICI) discloses fibres of PET or PA-6.6 which comprise 0.1 - 10 wt.% of a further polymer having anisotropic properties (LCP types). The spinning speeds are 1000 to 5000 m/min. A speed suppression (WUSS) is achieved by a higher elongation at break of the strand and therefore higher stretching ratios and an increase in productivity.
EP 0 080 274 B (ICI) relates to fibres of PET, PA-6.6 or PP which comprise 0.1 - 10 wt.% of a further polymer which is present in the melt with an average particle size of 0.5 -3 m and is deformed to fibrils during melt spinning. The spinning speeds are 2000 to 6000 m/min, a speed suppression (WUSS: wind up speed suppression) of at least 20 % being achieved by a higher elongation at break or lower birefringence of the (PET) strand, and therefore higher stretching ratios and an increase in productivity. Preferred additive polymers are polyethylene glycol or

2
PA-6.6 for PET or polyolefins for PA-6.6. The effect reacts markedly to production parameters, such as throughput, spinning temperature, type of mixing or type of extruder. A transfer to production plants of different capacity, types of equipment or titre programmes is made difficult by this sensitivity. We attribute the negative behaviour to an unsuitable additive with too low a viscosity, too low a glass transition point and the tendency to crystallize.
JP 56-91013 A (Teijin) discloses a non-stretched polyester yarn, in which, by addition of 0,5 - 10 wt.-% of a styrene polymer, an improved productivity is achieved by increasing the elongation at break of the strand at speeds of between 850 - 8000 m/min, preferably > 2500 m/min, with correspondingly higher stretching ratios. No requirements are disclosed for the polymer mixture and the non-stretched yarn for the stretch texturizing.
EP 0 047 464 B (Teijin) relates to a non-stretched polyester yarn, in which, by addition of 0,2 - 10 wt.-% of a polymer of the type (CH2-CR1R2 )nsuch as poly(4-methyl-l-pentene) or polymethyl methacrylate, an improved productivity is obtained by increasing the elongation at break of the strand at speeds of between 2500 - 8000 m/min, with correspondingly higher stretching ratios. A fine and uniform dispersion of the additive polymer by mixing is needed, it being necessary for the particle diameter to be EP 0 631 638 B (AKZO) describes fibres of predominantly PET which contains 0.1 - 5 wt.% of a polymethacrylic acid alkyl ester imidized to the extent of 50 - 90 %. The fibres

obtained at speeds of 500 - 10,000 m/min and subsequently finally stretched have a higher initial modulus. Spinning at very high speeds (such as 8000 m/min) is said to be possible with conventional thread breakage counts. Up to 8000 m/min partly orientated yarns which are not yet stretched to the final elongation and can be processed e. g. to texturized yarns are obtained. In the examples of industrial yarns, the influence on the modulus cannot be readily reconstructed; in gen. the strengths achieved are lower, which is a considerable disadvantage for this product. For textile applications, only stretched yarns are described. The associated unstretched yarns at a spinning speed of from 6000 m/min show elongations at break of Spinning of polymer mixtures to synthetic fibres has the aim of obtaining a higher elongation at break in the strand at a particular spinning speed than without modification by an additive polymer. As a result, a higher stretching ratio for production of the final yarn is said to be possible, which is said to have the effect of a higher productivity of the spinning unit. According to EP 0 041 327 B, for example, a

where E/E' are the non-modified/modified elongations at break, is to be expected. Investigation of the formula shows that the effect is the greatest at high increases in elongation (E' - E) . However, elongations which are too high and therefore a reduced degree of orientation of the strand are unsuitable for processing in high-speed stretch texturizing processes.

4
Another way of increasing productivity is described in EP 0 080 274 B by the parameter WUSS > 20 %. At a spinning speed which is at least 20 % higher, the same elongation at break in the strand is obtained as at the correspondingly lower speed with non-modified polymer. No running properties in the spinning mill at a higher speed and during further processing or properties of the final yarns produced there are disclosed. It has been found that the average particle sizes claimed, of > 0.5 |im, are unsuitable for commercial processing of the mixture, since such particle distributions lead to many capillary and thread breakages.
Increasing production is targeted at improving the profitability of the production process. This is curtailed again to a certain extent by production difficulties and expensive high-speed equipment. The additional costs for the additive polymer have a substantial influence, so that, depending on the amount added, there is even a zero point for the profitability. The availability of the additive polymers on the market also plays an important role. For these reasons, a large number of the additives described in the literature are eliminated from large-scale industrial conversion.
The producer or processor must take into account the entire production chain, and cannot stop at increasing production of a component step (e. g. spinning). The secondary processes should not be impaired. In particular, one of the main aims of this invention is not to curtail and preferably to improve the further processing conditions in the secondary steps, in spite of an increased spinning speed.
Very high elongations at break are thus mentioned in the prior art for polymer mixtures also for high spinning speeds, these characterizing a marked reduction in the degree of orientation. As is known, such strands are not

storage-stable, and cannot be spread and processed at high speeds in friction texturizing processes. Elongations at break of The object of the present invention is to provide a process for processing polymer mixtures based on polyester at a draw-off speed of > 2500 m/min to preorientated filaments, which are preferably suitable for stretch texturizing, in which the abovementioned disadvantages do not occur. In particular, the costs of the additive added to the polyester should be as low as possible, i. e. the additive must be inexpensive, and the amount added must be kept low. Spinning of the polymer mixture must lead to an increase in production compared with the non-modified matrix polymer and allow processing of the strand at a high speed in the stretch texturizing process.
According to the invention, this object is achieved by a process according to the statements in the patent claims. This process is characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1 : 1 to 10 : 1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% (based on the polyester) and not more than an amount M, where M is given by the formula

According to the invention, a copolymer is added to the polyester in an amount of at least 0.05 wt.%, where the copolymer must be amorphous and largely insoluble in the polyester matrix. The two polymers are substantially incompatible with one another and form two phases which can be distinguished under the microscope. Furthermore, the

6
copolymer must have a glass transition temperature {determined by DSC with a heating up rate of 10 oC/min) of more than 100 BC and must be thermoplastically processable.
The melt viscosity of the copolymer here is to be chosen such that the ratio of its melt viscosity, extrapolated to the measurement time of zero and measured at an oscillation rate of 2.4 Hz and a temperature equal to the melting temperature of the polyester plus 34.0 OC {for polyethylene terephthalate 290 2C), in relation to that of the polyester, measured under the same conditions, is between 1 : 1 and 10 : 1. I. e. the melt viscosity of the copolymer is at least equal to or preferably higher than that of the polyester. Only by the choice of a specific viscosity range for the additive {copolymer) or by the choice of a specific viscosity ratio of the additive and polyester is the optimum degree of action achieved. With a viscosity ratio optimized in this way, it is possible to minimize the amount of additive added, as a result of which the profitability of the process becomes particularly high and particularly favourable processing properties are achieved. Surprisingly, the viscosity ratio determined according to the invention as ideal for use of polymer mixtures for the production of synthetic filament yarns is above the range identified in the literature as favourable for the mixing of two polymers. In contrast to the prior art, polymer mixtures with high molecular weight copolymers had an excellent spinnability.
Due to the high flow activation energy of the additive polymers, the viscosity ratio further increases drastically in the region of thread formation after discharge of the polymer mixture from the spinneret. By the choice of a favourable viscosity ratio, a particularly narrow particle size distribution of the additive in the polyester matrix is achieved, and by combination of the viscosity ratio with a flow activation energy of significantly more than that of the polyester (PET about 60 kJ/mol), i. e. of more than

7
80 kJ/mol, preferably more than 100 kJ/mol, the required fibril structure of the additive in the strand is obtained. The glass transition temperature, which is high compared to the polyester, ensures a rapid consolidation of this fibril structure in the strand. The maximum particle sizes of the additive polymer here immediately after discharge from the spinneret are about 1000 nm, while the average particle size is 400 nm or less.
The ratio of the melt viscosity of the copolymer to that of the polyester under the abovementioned conditions is preferably between 1.4 : 1 and 8 : 1. A ratio of the melt viscosities of between 1.7 : 1 and 6.5 : 1 is particularly preferred. Under these conditions, the average particle size of the additive polymer is 220 - 350 nm.
The amount of copolymer to be added to the polyester is at least 0.05 wt.%. For many applications, amounts added of less than 1.5 % are sufficient at draw-off speeds above 3500 and up to 6000 m/min and more, even often less than 1.0 %, which is a considerable cost advantage.
The maximum amount of additive polymer to be added according to this invention in relation to that of the polyester corresponds to the amount M, where M is defined as a function of the spinning draw-off speed v by the following formula:

Maximum amounts added of 1.39 to 2.95 wt.% thus result in the spinning speed range from 3500 to 6000 m/min.
Preferably, to achieve a particularly good profitability, the upper limit of the amount of additive to be added for draw-off speeds of more than 2900 m/min is defined by the parameter M*, where

8
Amounts added of between 0.39 and 1.91 wt.% thus result for spinning speeds of 3500 to 6000 m/min.
For draw-off speeds of more than 4200 m/min, the amount of additive polymer to be added to the polyester is preferably at least equal to the parameter N, but at least equal to 0.05 wt.%, where

For draw-off speeds of 4200 to 6000 m/min, the minimum amount is thus between 0.057 and 0.57 wt.%.
If the abovementioned preferred viscosity ratio of additive polymer to polyester is adhered to, the amount of copolymer to be added relative to that of the polyester preferably corresponds to the parameter P, where P = P* ± 0.2 wt.%, but is at least 0.05 wt.%, and where, for draw-off speeds of more than 3900 m/min

The amount of additive to be added in this preferred case is thus between 0.07 wt.% and 1.39 wt.% for spinning speeds of 3900 to 6000 m/min.
For spinning speeds between 2500 m/min and the minimum spinning speeds specified here for M*, N and P, only the minimum and maximum amounts stated in claim 1 apply, while for higher spinning speeds, the abovementioned ranges of amounts are preferably additionally used. These formulae of course also apply to spinning speeds of more than 6000 m/min up to about 12000 m/min.

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Possible fibre-formimg matrix polymers are thermoplastically processable polyesters, such as polyethylene terephthalate (PET), polyethylene naphthalate, polypropylene terephthalate and polybutylene terephthalate. The homopolymers are preferred. However, copolymers of these polyesters with a content of up to about 15 mol% of conventional comonomers, such as e. g diethylene glycol, triethylene glycol, 1,4-Cyclohexanedimethanol, polyethylene glycol, isophthalic acid and/or adipic acid, are also possible. The polymers can additionally comprise additives, such as catalysts, stabilizers, optical brighteners and matting agents. The polyester can also comprise a small amount (not more than 0.5 wt.%) of branching components, that is to say e. g. polyfunctional acids, such as trimellitic acid or pyromellitic acid, or tri- to hexavalente alcohols, such as trimethylolpropane, pentaerythritol, dipentaerythritol or glycerol, or corresponding hydroxy acids.
Mixing of the additive polymer (copolymer) with the matrix polymer is carried out by addition as a solid to the matrix polymer chips in the extruder intake with a chips mixer or gravimetric metering, or alternatively by melting the additive polymer, metering it by means of a gear pump and
feeding it into the melt stream of the matrix polymer. A
homogeneous distribution is then established by mixing in
the extruder and/or by means of static or dynamic mixers. By a specific choice of the mixer and of the duration of the mixing operation, a defined particle distribution is advantageously established before the melt mixture is passed on through product distribution lines to the individual spinning stations and spinnerets. Mixers having a shear rate of 16 to 128 sec-1 and a residence time in the mixer of at least 8 sec have proved suitable. The product of the shear rate {s-1) and the 0.8th power of the residence time {in sec) here should be 250 to 2500, preferably 300 to 600.

10
The shear rate is defined here by the shear rate in the empty pipe (s-1) times the mixer factor, the mixer factor being a characteristic parameter of the mixer type. For Sulzer-SMX types, for example, this factor is about 7-8. The shear rate y in the empty pipe is calculated according to

and the residence time x (s) according to

wherein
F = amount of polymer conveyed (g/tnin)
V2 = internal volume of the empty pipe (cm3)
R = diameter of the empty pipe (mm)
£ = empty volume content (for Sulzer-SMX types 0.84 to 0.88)
5 = nominal density of the polymer mixture in the melt (about 1.2 g/cm3)
Both the mixing of the two polymers and the subsequent spinning of the polymer mixture are carried out at temperatures, depending on the matrix polymer, in the range from 220 to 320 2C.
The production of synthetic filaments from the polymer mixtures according to the invention by high-speed spinning with draw-off speeds of > 2500 m/min is carried out using spinning devices which are known per se. The filter package here is equipped according to the known prior art with filter devices and/or loose filter media (e. g. steel grit).

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After the shear and filtration treatment has taken place, the molten polymer mixture is forced through the bores of the die plate in the die package. In the subsequent cooling zone, the melt threads are cooled to below their softening point by means of cooling air, so that sticking or backing-up at the following thread guide organ is avoided. The construction of the cooling zone is not critical, as long as a homogeneous stream of air which penetrates the filament bundle uniformly is ensured. A still air zone can therefore be provided directly below the die plate to delay cooling. The cooling air can be fed in by blowing transversely or radially from an air-conditioning system, or can be taken from the environment by automatic suction by means of a cooling pipe.
After cooling, the filaments are bundled and charged with spinning oil. Oiler stones to which the spinning oil is fed as an emulsion by metering pumps are used for this. The prepared thread advantageously passes through an entangling device (entwisting device) to improve the thread compactness. Handling and safety organs may also be appropriate, before the thread arrives at the winding unit and is wound up there to packages on cylindrical bobbins. The circumferential speed of the thread package is regulated automatically and is the same as the winding-up speed. The draw-off speed of the thread can be 0.2 - 2.5 % higher than the winding-up speed because of its changing movement. Driven godets can optionally be used after the preparation or before the winding up. The circumferential speed of the first godet system is designated the draw-off speed. Further godets can be used for stretching or relaxing.
The incompatibility of the two polymers has the effect that the additive polymer forms spheroidal or longitudinally shaped particles in the matrix polymer immediately after i discharge of the polymer mixture from the spinneret. The length/diameter ratio is preferably > 2. The best

12
conditions resulted when the average particle size (arithmetic mean) d50 was 1000 nm in a sample cross-section was below 1 %.
It was possible to demonstrate the influence of the spinning draft on these particles analytically. New studies on the strands by the TEM (transmission electron microscopy) method have shown that a fibril-like structure exists there. The average diameter of the fibrils has been estimated at approx. 40 nm. The length/diameter ratio of the fibrils here was > 50. If these fibrils are not formed, or if the additive particles are too large in diameter after discharge from the spinneret, or if the size distribution is too non-uniform, which is the case with an inadequate viscosity ratio, the effect of the action is lost.
The rolling action described in the literature could not be reconstructed with the additive polymer according to the invention. The evaluation of microscope studies of the fibre cross- and longitudinal sections suggest that the spinning draft tension is passed to the additive fibrils which form and the polymer matrix distorts with little stress. The deformation of the matrix consequently takes place under conditions which result in a reduction of the orientation and suppression of spinning-induced crystallization. The effect is appropriately evaluated by the strand construction and the processing properties.
Furthermore, for the effectiveness of the additives according to this invention, a flow activation energy of the copolymers of at least 80 kJ/mol, that is to say a higher flow activation energy than that of the polyester matrix, is necessary. Only under this proviso is it possible for the additive fibrils to solidify before the polyester matrix and to absorb a considerable proportion of the enclosed spinning tension. As a result, it is possible

13
to achieve the desired increase in capacity of the spinning unit.
As is known, the strand structure is substantially formed in the draft zone below the spinneret. The length of the draft zone is varied by the thread draw-off speed in the case of non-modified polymer. Typical values for roving yarns with conventional draw-off speeds of at least 2500 m/min are lengths of about 300 mm, preferably for POY ^ 250 mm to The process according to the invention is similarly suitable for high-speed spinning of POY threads with a POY filament titre of > 3 dtex to 20 dtex and more, and also POY filament titres of For further processing of the strand in the stretch texturizing process at high speeds, the following is important: Strands according to this invention as roving yarn for stretch texturizing - usually called POY - are produced with draw-off speeds of > 2500 m/min, preferably > 3500 m/min, particularly preferably > 4000 m/min. These yarns must have a physical structure which is characterized by a specific degree of orientation and a low crystallization. The parameters of elongation at break, birefringence, degree of crystallization and shrinkage at the boil have proved appropriate for its characterization. The polymer mixture according to the invention is characterized by an elongation at break of the PET strands (POY) of at least 85 % and not more than 180 %. The shrinkage at the boil is 32 - 69 %, the birefringence is

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between 0.03 0 and 0.075, the crystallinity is less than 20 % and the tear strength is at least 17 cN/tex. The elongation at break of the PET strands is preferably between 85 and 160 %. Particularly favourable circumstances exist if the elongation at break of the PET strands is between 109 and 146 %, the tear strength at the same time is at least 22 cN/tex and the Uster value is not more than 0.7 %.
Stretch texturizing is carried out at different speeds, depending on the filament titre type, speeds of > 750 m/min, preferably > 900 m/min, being used for normal-titre filaments of > 2 dtex per filament (final titre) . For microfilaments and fine titres (final titre) of The stretching ratios to be applied are between 1.35 and 2.2 for the strands specified, stretching ratios in the upper range preferably being used for a lower degree of orientation and vice versa. During the stretch texturizing, the stretching ratio is influenced by variations in tension (surging) as a function of the operating speed. Particularly preferred stretching ratios are therefore those according to the formula:
stretching ratio = 5 o 10~4 o w (m/min) + b wherein
w = stretch texturizing speed in m/min b = constant which lies between 1.15 and 1.50, to be applied.
The additive polymers to be added according to the invention to the polyester can have a varying chemical

15
composition, as long as they have the abovementioned properties. Three different copolymer types are preferred, that is to say
1. A copolymer which comprises the following monomer
units:
A = acrylic acid, methacrylic acid or CH2 = CR -
COOR, wherein R is an H atom or a CH3 group and R is a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical,
B = styrene or C1-3-alkyl-substituted styrenes,
wherein the copolymer comprises 60 to 98 wt.% A and 2 to 40 wt.% B, preferably 83 to 98 wt.% A and 2 to 17 wt.% B, and particularly preferably 90 to 98 wt.% A and 2 to 10 wt.% B (total = 100 wt.%).
2. A copolymer which comprises the following monomer
units:
C = styrene or C1-3-alkyl-substituted styrenes,
D = one or more monomers of the formula I, II or III

wherein R1, R2 and R3 are each an H atom or a C1-15_alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical,
wherein the copolymer comprises 15 to 95 wt.% C and 2
to 80 wt.% D, preferably 50 to 90 wt.% C and 5 to
50 wt.% D, and particularly preferably 70 to 85 wt.% C

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and 15 to 30 wt.% D, the total of C and D together giving 100 %.
A copolymer which comprises the following monomer units:
E = acrylic acid, methacrylic acid or CH2 = CR -
COOR, wherein R is an H atom or a CH3 group and R' is a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical,
F = styrene or C1-3-alkyl-substituted styrenes,
G = one or more monomers of the formula I, II or III

wherein Rl R2 and R3 are each an H atom or a C1-15-alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical,
H = one or more ethylenically unsaturated monomers, which can be copolymerized with E and/or with F and/or G, from the group which consists of a-methy1styrene, vinyl acetate, acrylic acid esters, methacrylic acid esters which differ from E, vinyl chloride, vinylidene chloride, halogen-substituted styrenes, vinyl ethers, isopropenyl ethers und dienes,
the copolymer comprising 30 to 99 wt.% E, 0 to 50 wt.% F, >0 to 50 wt.% G and 0 to 50 wt.% H, preferably 45 to 97 wt.% E, 0 to 30 wt.% F, 3 to 40 wt.% G and 0 to 30 wt.% H, and particularly preferably 60 to 94 wt.% E, 0 to 20 wt.% F, 6 to

17
30 wt.% G and 0 to 20 wt.% H, the total of E, F, G and H together giving 100 %.
Component H is an optional component. Although the advantages to be achieved according to the invention can already be achieved by copolymers which contain components from groups E to G, the advantages to be achieved according to the invention also arise if further monomers from group H participate in the building up of the copolymer to be employed according to the invention.
Component H is preferably chosen such that it has no adverse effect on the properties of the copolymers to be used according to the invention.
Component H can be employed, inter alia, to modify the properties of the copolymer in a desired manner, for example by increases or improvements in the flow properties when the copolymer is heated to the melting temperature, or to reduce a residual colour in the copolymer, or, by using a polyfunctional monomer, to introduce a certain degree of crosslinking into the copolymer in this manner.
In addition, H can also be chosen such that
copolymerization of components E to G is rendered possible at all or is assisted, such as in the case of MAA and MMA, which do not in themselves copolymerize, but copolymerize without problems on addition of a third component, such as styrene.
Monomers which are suitable for this purpose include, inter alia, vinyl esters, esters of acrylic acid, for example methyl und ethyl acrylate, esters of methacrylic acid which differ from methyl methacrylate, for example butyl methacrylate and ethylhexyl methacrylate, vinyl chloride, vinylidene chloride, styrene, tx-methylstyrene and the various halogen-substituted styrenes, vinyl und isopropenyl ether, dienes, such as, for example, 1,3-butadiene, and

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divinylbenzene. The reduction in the colour of the copolymer can particularly preferably be achieved, for example, by using an electron-rich monomer, such as, for example, a vinyl ether, vinyl acetate, styrene or methylstyrene.
Particularly preferred compounds of component H are aromatic vinyl monomers, such as, for example, styrene or -methylstyrene,
The preparation of the copolymers to be used according to the invention is known per se. They can be prepared by bulk, solution, suspension or emulsion polymerization. Helpful notes in respect of bulk polymerization are to be found in Houben-Weyl, volume E20, part 2 (1987), page 1145 et seq. Notes on solution polymerization are likewise to be found there on page 1156 et seq. The suspension polymerization technique is likewise described there on page 1149 et seq., while emulsion polymerization is likewise described and explained there on page 1150 et seq.
Bead polymers, the particle size of which lies in a particularly favourable range, are particularly preferred in the context of the invention. The copolymers to be used according to the invention, for example, by mixing into the melt of the fibre polymers are particularly preferably in the form of particles having an average diameter of 0.1 to 1.0 mm. However, larger or smaller beads or granules can also be employed.
The polymers according to the invention can comprise, as_ further constituents, additives such as are usual for thermoplastic moulding compositions and contribute towards improving the polymer properties. Examples of these which may be mentioned are: antistatics, antioxidants, flameproofing agents, lubricants, dyestuffs, light stabilizers, polymerization catalysts and auxiliaries, adhesion promoters, matting agents and/or organic

19
phosphites. These additives are employed in the usual amount, preferably in amounts of up to 10 wt.%, preferably The imidized copolymer types 2 and 3 can be prepared both from the monomers using a monomeric imide and by subsequent complete or, preferably, partial imidation of a copolymer comprising the corresponding maleic acid derivative. These additive polymers are obtained, for example, by complete or, preferably, partial reaction of the corresponding copolymer with ammonia or a primary alkyl- or arylamine, for example aniline, in the melt phase (Encyclopedia of Polymer Science and Engineering vol. 16 [1989], Wiley-Verlag, page 78). All the copolymers according to the invention, as well as their non-imidized starting copolymer, where appropriate, are commercially obtainable or can be prepared by a process familiar to the expert.
For polymer mixtures of polyethylene terephthalate with an intrinsic viscosity of about 0.55 to 0.75 dl/g and copolymers of type 1, 2 or 3, copolymers having viscosity numbers in the range from 70 to 130 cm3/g are preferred.
The process according to the invention enables the draw-off speed during strand production to be increased substantially compared with the prior art by the addition of a copolymer to the polyester, while the stretching ratio during the stretch texturizing can be kept constant, corresponding to the non-modified polyester. The capacity of the production unit therefore increases directly proportionally to the draw-off speed.
Since the capacity of the spinning station is proportional to the product of the stretching ratio and draw-off speed, the gain in capacity in the spinning mill is:

wherein

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VV1 = stretching ratio with additive
VVo = stretching ratio without additive
V1 = winding up speed of the strand with additive
Vo = winding up speed of the strand without additive
Typically v0 is in the range from 2500 to 3500 m/min and VVo is between 1.35 and 2.2, corresponding to the spinning speed according to the known prior art.
The dependent variables M, M*, P and N according to the invention state that the amount of additive added may not be chosen independently of the draw-off speed if the aim of producing, from polymer mixtures, preorientated filaments of low crystallinity which are suitable for stretch texturizing is to be achieved. It is necessary to avoid here on the one hand the degree of preorientation being too low, i. e. e. g. the elongation at break will be too high, and on the other hand a noticeable spinning-induced crystallization occurring at too high a degree of orientation. The stretching ratio during stretch texturizing has been determined for filaments produced at various draw-off speeds and additive concentrations. The relationships of M*7 P* and N here are represented as lines of constant stretching ratio. This results in a particular advantage of this process. The filament producer can choose and adjust the amount of additive at any desired draw-off speed such that he obtains a stretching ratio which is optimum for his further processing conditions. Stretch texturizing is therefore carried out under optimum, selectable conditions.
The values for properties stated in the following examples and in the above text were determined as follows:
Distribution of the additive particles: Melt strands or pellet samples were broken down with a sharp chisel in

21
liquid nitrogen. The broken surfaces were investigated by-means of scanning electron microscopy and subsequent evaluation by image analysis, taking as the basis an elliptical form (spheroidal), the length, width and, calculated therefrom, average diameter being evaluated.
Thread speeds were determined by means of laser Doppler anemometry using a diode laser of 10 mW output, TSI GmbH, Aachen/DE, type LS50M. In this method, a laser beam is divided and the two component beams are made to intersect on the object to be measured. The interference frequency is measured in the backscatter region and the object speed is calculated from the shift in the interference frequency. The thread speed was measured at several distances underneath the spinneret. The change in speed until the speed defined by the draw-off device is reached characterizes the spinning draft zone. The length between the speed points of 1000 m/min and 90 % of the final speed in [mm] was defined as the measure. This draft length is usually several 100 mm. At high spinning speeds, it can be shortened to about 100 mm, a constriction (necking) of the thread occurring; the change in thread speed in the region from about 1750 m/min is then almost punctiform.
The intrinsic viscosity was determined on a solution of 0.5 g polyester in 100 ml of a mixture of phenol and 1,2-dichlorobenzene (3 : 2 parts by wt.) at 25 BC.
The viscosity number VN (also Staudinger function) is the concentration-related relative change in the viscosity of a 0.5% solution of the copolymer in chloroform, based on the solvent, the flow-through times being determined in an Ubbelohde viscometer with a suspended ball level, Schott type no. 53203 and capillary 0c in accordance with DIN standard 51562 at 25 aC. Chloroform was used as the solvent.

22

wherein
t = flow-through time of the polymer solution in seconds
t0 = flow-through time of the solvent in seconds c = concentration in g/100 ccm
To determine the melt viscosity (initial viscosity), the polymer was dried in vacuo to a water content of plate rheometer, type UM100, Physica MeStechnik GmbH, Stuttgart/DE, with masking with nitrogen. After the sample had melted, i. e. after approx. 30 seconds, the measuring ball (MK210) was positioned on the measuring plate. The measurement was started after a further heating up period of 60 seconds (measurement time = 0 seconds). The measurement temperature was 290 aC for polyethylene terephthalate and additive polymers added to polyethylene terephthalate, or was the same as the melting temperature (method follows) of the polyester in question plus 34.0 SC. The measurement temperature specified in this way corresponds to the typical processing or spinning temperature of the particular polyester. The amount of sample was chosen such that the rheometer gap was filled completely. The measurement was carried out in oscillation with a frequency of 2.4 Hz (corresponding to a shear rate of 15 sec"1) and a deformation amplitude of 0.3, and the value of the complex viscosity was determined as a function of the measurement time. Thereafter, the initial viscosity was converted to the measurement time zero by linear regression.

23
For the determination of the melting temperature of the polyester, the polyester sample was first melted at 310 EC for 1 min and quenched to room temperature immediately thereafter. The melting temperature was then determined by DSC measurement (differential scanning calorimetry) at a heating up rate of 10 2C/min. The pretreatment and measurement were carried out with masking with nitrogen.
The flow activation energy (E) is a measure of the rate of change of the zero viscosity as a function of the change in measurement temperature, the zero viscosity being the viscosity extrapolated to the shear rate 0. The zero viscosity was measured at temperatures in the range from 240 to 280 eC with a high-pressure capillary rheometer, type Rheograph 2002, Gottfert GmbH, Buchen/DE, and the results were evaluated by the three parameter plot of Carreau-Winter. Thereafter/ the flow activation energy was determined by means of the Arrhenius plot from the zero viscosity in accordance with the method of M. Pahl et al. , Praktische Rheologie der Kunststoffe und Elastomere [Practical rheology of plastics and elastomers], VDI-Verlag, Dusseldorf (1995), pages 256 et seq.
The strength properties were determined with a tensile tester at a clamped length of 200 mm, a pretension force of 0.05 cN/dtex and a test speed of 2000 mm/min.
The shrinkage at the boil was determined on fibres which had been conditioned at room temperature and treated beforehand for 10 min in water of 95 ± 1 2C.
The birefringence was measured as described in
DE 195 19 898 A and the Uster-values were measured as
described in EP 0 346 641 B.
The stretching force was determined with a Dynafil M apparatus from Textechno, M6nchengladbach/DE at a heating tube temperature of 200 2C and a test speed of 100 m/min.

24
The crystallinity (C) was calculated from the density p according to

the density being determined on short knotted pieces of thread at 23 2C by the density gradient method (in CCl4/n-heptane) .
The crimping parameters of the texturized filament yarns (nominal titre to 500 dtex) were determined in accordance with DIN 53840, part 1.
The depth of dyeing was determined on a circular knitted piece dyed with Terasil navy blue GRL-C 200 % (Ciba-Geigy, Basel/CH) by comparative measurement of the colour reflection with a reflectance photometer in accordance with DIN 54001.
Example 1: (comparison)
Polyethylene terephthalate having an intrinsic viscosity intr = 0.64 dl/g (corresponds to an initial viscosity of 250 Pa's) and a residual water content of The strands emerging from the bores of the die plate were cooled in a conventional blowing shaft with transverse blowing, the air speed being adjusted to 0.45 m/sec.
At a distance of 1200 mm below the spinneret, the cooled strands were bundled by means of an oiler pin and provided

25
with a spinning oil-water emulsion, the amount of preparation applied to the thread being 0.35 %, based on the thread weight.
The thread bundle was drawn off by means of two driven godets entwined in s-shaped form and wound on empty bobbins to yarn packages in a winding unit from Barmag AG, Remscheid/DE, type SW7, with birotor changing. The spinning draw-off speed was defined by the circumferential speed of the godets. The winding speed was set about 1 % lower, so that a tension of 10 cN resulted between the godets and winder. The nominal titre of the thread produced in this way was 84/34 dtex.
The take-off speed was adjusted to 3200 m/min, an amount of polymer of 41.1 g/min being fed to the spinneret. The strand characteristic data are summarized in table 1.
Table 1: Reference POY

No.
Comparison experiment

CV: coefficient of variation

26
Example 2:
The spinning system according to example 1 was supplemented by a metering device comprising a compounding extruder and a gear metering pump. Using this metering system, the additive, with a residual water content of The spinning draw-off speed, however, was adjusted to a constant speed,of 5000 m/min. The polymer throughput was 63 g/min, which resulted in an average residence time of the melt of about 7.5 min before entry into the spinneret package.
In another comparison experiment (no. 3), the additive Delpet 80N was metered in a concentration of 1.8 wt.% into the PET melt stream and spun under the same conditions.
In further experiments (no. 4-9), polymer mixtures according to the invention were spun under the same conditions, but the amount of the particular copolymer added was only 0.65 wt.%. The additives were products from Degussa AG, Hanau/DE, that is to say copolymers with, in the polymer, 8.8 wt.% styrene (S) and 91.2 wt.% methyl methacrylate (MMA) and various viscosity numbers (according to table 2).
In experiment no. 9, under otherwise the same conditions, a polymer mixture was prepared and spun at a temperature of only 286 SC. The strand characteristic data for this and

27
the abovementioned experiments are summarized in table 2a and 2b.
Table 2a:

28
Table 2b:

number
Viscosity :1 1.7 2.4 4.4 4.5 5.1 4.4 ratio*
E** kJ/mol 110
Titre dtex 130 129 130 129 129 130
Draw-off m/min 5000 5000 5000 5000 5000 5000 speed
Spinning 2C 296 296 296 296 296 286 temperature
Elongation at % 96.4 112.1 115.1 123.4 113.2 116.1 break
*Melt viscosity of the additive polymer to melt viscosity of the polyester (=1)
** Flow activation energy
When the viscosity number of the additive polymer added is increased, an increase in the elongation at break is initially found, i. e. a maximum improvement in the profitability is observed on addition of the copolymer with a viscosity number of about 105 ccm/g. When the additive with an even higher viscosity number is added, the profitability of the process decreases again slowly.
Compared with the additive disclosed in EP 47 464 B, about the same capacity-increasing effect is achieved with the copolymers according to the invention with viscosity numbers in the range from 91 to 118 ccm/g, with a drastically reduced amount of additive.

29
This reduction in the amount of additive not only is advantageous economically, but also means a considerable technological advantage. Impairments in the further processing properties, such as e. g. sticking of additive inclusions on the thread surface to the hot metal surfaces of the heaters(of texturizing units, are reduced considerably if it is possible - as in the context of this invention - to decrease the amount of additive added. Furthermore, the boundary between additive inclusions and polyester matrix represents a defective point in the transfer of mechanical stresses in the yarn, because of the incompatibility of the two materials, which at high additive concentrations can lead to capillary breakages. This effect is the more pronounced the higher the amount of additive, and impairs the texturizing properties and the tear strength of the texturized yarn.
In experiments.no. 6 and 9, in spite of the drastically changed pre-exposure of the melt mixture to heat by using a spinning temperature of 286 2C and 296 2C respectively, virtually the same elongations at break are achieved, i. e. the additive according to the invention is distinguished by a good heat stability in the temperature range relevant on a large industrial scale.
Example 3:
In further experiments further polymer mixtures were spun under the same conditions as in example 2, the amount of the particular additive added being 0.72 wt.%. The additives were copolymers from Degussa AG, Hanau/DE with, in the polymer, 8.8 wt.% styrene, 86.2 wt.% MMA and 5 wt.% N-cyclohexylmaleimide and various viscosity numbers, as shown in table 3, which also contain the strand characteristic data.

30 Table 3:
Experiment No. 10 11 12 13 14 15 16 17
Additive wt. % 0.72 0.72 0.72 0.72 0.72 0.72 0.72 0.72 concentration
Viscosity ccm/g 61 72 88 99.4 99.6 113.7 128.6 174 number
Viscosity :1 0.8 2.0 3.2 4.0 4.2 5.6 9.6 11.2 ratio*
E** kJ/mol 120
Titre dtex 129 129 131 131 129 131 129 129
Draw-off m/min 5000 5000 5000 5000 5000 5000 5000 5000
speed
Spinning fiC 296 296 296 296 296 296 296 296
temperature
Elongation at % 70.1 85.5 106.7 125.9 127.6 133 125.1 49.2
break
(* and ** see table 2b)
Comparison experiments no. 10 and 17 and experiments no. 11 to 16 again confirm the existence of a pronounced optimum of the additive viscosity with regard to the capacity-increasing effect and the elongation at break. In the range of viscosity numbers from 61 to about 100 ccm/g, the profitability of the process initially increases virtually linearly with the viscosity number. In the .range from VN = 100 ccm/g up to the viscosity number of about 115 ccm/g the profitability then improves further only slightly. Above this optimum, the profitability again is reduced slightly up to the viscosity number of about 130 ccm/g. At VN = 174 ccm/g, a distinctly negative effect in respect of capacity occurs. Experiment no. 11 gives a POY with a lower elongation at break than the other experiments and therefore lies in the limit region of the invention.

31
Example 4:
In experiment no. 18, a die package with a die plate with 17 bores instead of 34 bores was employed in the spinning system from example 2.
Under otherwise unchanged conditions, 0.65 wt.% of the additive according to the invention was mixed in with 8.8 wt.% styrene and 91.2 wt.% MMA of viscosity number VN = 98.5 ccm/g, and the polymer mixture was spun to a thread with a nominal titre of 84/17 dtex at an amount of polymer of 63 g/min, a spinning draw-off speed of 5000 m/min and a spinning temperature of 296 eC.
In another experiment (no. 19), under otherwise unchanged conditions, a spinneret plate with 72 bores, bore diameter 0.10 mm, L = 2D, was employed and a polymer mixture with the same additive as in experiment no. 18 was spun at a spinning speed iof 5000 m/min to a thread of nominal titre 84/72 dtex.
Finally, a spinneret plate with 120 bores, bore diameter 0.13 mm, 1 = 2D, was employed and with an addition of 0.65 wt.% of the same additive as before, an amount of polymer of 58 g/min and a spinning speed of 4500 m/min, a thread of nominal titre 84/120 dtex was spun (experiment no. 20).
The characteristic data of all the strands are summarized in table 4.

32
Table 4:

Comparison example 5:
Polyethylene terephthalate having an intrinsic viscosity intr = 0.64 dl/g (corresponding to an initial viscosity of 250 Pa.s) and a residual water content of At the discharge of this spinning pump, the melt was divided into 6 component streams with throughputs the same as one another. Each of these component streams was fed through a spinneret adapter with 2 static mixers, type SMX DN 10, from Sulzer AG, Zurich/CH, to a spinneret package.

33
The die package comprised, viewed in the melt flow direction, defined shear and filtration means of the following construction: Steel grit volume of particle size 350 to 500 m, support plate, second fabric filter of 20 pin, spinneret plate with 34 bores, bore diameter 0.25 mm, L = 2D and a diameter of the plate of 80 mm, corresponding to a filter area of 40 cm2. With a varied polymer throughput, a pressure of 110 - 190 bar is established.
The strands emerging from the bores of the spinneret were cooled in a conventional blowing shaft with transverse blowing, the .air speed being adjusted to 0.55 m/min.
At a distance of 1500 mm below the spinneret, the cooled strands were bundled by means of an oiler pin and provided with a spinning oil-water emulsion, the amount of preparation applied to the threads being about 0.35 %.
The thread bundle was drawn off by means of two driven godets entwined in s-shaped form and wound on 6 empty bobbins to yarn packages in a winding unit from Barmag AG, Remscheid/DE, type CW8 T-920/6, with birotor changing. The spinning draw-off speed was defined by the circumferential speed of the godets. The winding speed was set about 1 % lower, so that. a tension of about 10 cN resulted between the godet and winder. The nominal titre of the threads produced in this way was 84/34 dtex.
The draw-off speed was adjusted to 3200 m/min, an amount of polymer per spinneret of 44 g/min being established, resulting in an average residence time of the melt before entry into the-spinning pump of about 15 min. In a second experiment, the draw-off speed was increased to 5000 m/min and at the same time an amount of polymer of 63 g/min per spinneret with an average residence time of about 11 min was established. The characteristic data of the strands are

34
summarized in table 5 as the mean of all 6 bobbins of each individual experiment.
Table 5:
Comparison experiment No. El E2

ratio
The strands from comparison experiments no. El and no. E2 were further processed in a converted Barmag stretch texturizing machine, type FK6-S-900, equipped with the Barmag disc unit, type 7, with polyurethane discs PU, H6,

35
configuration 1-4-1, D/Y = 1.84, heater temperatures 1 and 2 = 195 / 160 2C at a speed of 800 m/min and heater temperatures 1 and 2 = 210 / 160 -C at a speed of 1000 m/min.
The stretching ratio, determined from the ratio of the discharge speed to the intake speed, was adjusted to match the characteristic data of the strand, and is summarized in table 6 with the characteristic data achieved for the texturized yarn as the mean of all 6 bobbins of each individual experiment.
Table 6:
Results of the stretch texturizing of experiment no. El -E2

(+ = positive; 0 = limited processability; - = negative)
Comparison example El corresponds to the prior art both as regards the properties of the strand and in the stretch texturizing. When the spinning speed is increased to 5000 m/min, problems arise in the stretch texturizing in the form of breakages and thread tension defects, and the stretching ratio to be used must be greatly reduced. The strength which can be achieved is also lower. The reason lies in the increased degree of crystallization of the POY strand, and is characterized by a correspondingly lower

36
elongation at break and necking behaviour in the spinning draft.
Example 6:
In the spinning system according to example 5 and under the same spinning conditions, an additive polymer according to the invention with a residual water content of The additive polymer was a product of Degussa AG, Hanau/DE, type Degalan® PVPMS, corresponding to a copolymer according to the invention of the following composition:
8.8 wt.% styrene, 91.2 wt.% MMA; viscosity number VN = 98.5 ccm/g
The ratio of the melt viscosities of additive to polyester according to this invention was 4.8 and the residence time of the polymer mixture in the mixing zone (7 mixing elements, as example 5) was 8 s.
The spinning draw-off speed was adjusted to a constant speed of 5000 m/min. The polymer throughput per spinneret was 63 g/min. The die pressure was in the range from 145 to 150 bar. Table 7 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment.
In comparison examples E3 and E4, the amount of additive is lower than the parameter N defined above, and is therefore so low that although there is a significant difference to non-modified yarn, the amount of additive is not sufficient

37
to reduce the crystallinity and the necking to the required
extent so that good further processing properties are
ensured. In contrast, experiments no. E5 to E8 are
according to the invention.
Table 7:
Experiment No. E3 E4 E5 E6 E7 E8
Residence time min 11 11 11 11 11 11
Number of SMX 7 7 7 7 7 7
elements
Spinning temperature 2C 290 290 290 290 290 290
Draw-off speed m/min 5000 5000 5000 5000 5000 5000
Additive wt. % 0.12 0.17 0.41 0.77 0.97 1.47
concentration
Spinning titre dtex 129.7 128.6 128.7 127.2 129.3 129.4
Elongation at break % 70.4 73.4 90.3 118.1 139.9 167.0
CV elongation at % 3.1 3.5 2.5 2.2 2.5 2.6
break
Tear strength cN/tex 34.9 34.7 30.6 25.6 22.8 17.0
CV breaking load % 3.1 2.6 2.4 2.3 3.0 2.7
Birefringence X 10"3 86.3 81.4 72.5 58.1 36.5
Shrinkage at the % 4.7 7.8 50.8 60.7 57.3 61

38
The strands according to the invention were subjected to stretch texturizing as in example El at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 8 as the mean of all 6 bobbins of each individual experiment.
Table 8:
Results of the stretch texturizing of experiments E5 - E8

{+ = positive; 0 = limited processability; - = negative)
The additive amount in experiment E6 was most appropriate for the spinning conditions. The best properties of the stretch-texturized yarn were achieved here. It was also possible to increase the texturizing speed to 1000 m/min with positive processing properties without problems, while the comparison yarn according to the prior art from example El had already showed a deterioration in the processing properties when the texturizing speed was increased from 800 to 1000 m/min (tab. 6).
Good stretch texturizing results were also to be achieved in examples E5, E7 and E8. However, the amount of additive in these experiments is no longer in the particularly preferred range. This manifests itself in a slight but still non-critical reduction in the tear strength and elongation at break, in particular in example E8, where the

39
amount of additive deviated the most from the particularly-preferred range.
Example 7:
In the metering system and spinning system according to example 6 and under the same spinning conditions, the same additive polymer as in example 6 was added to the polyethylene terephthalate chips, again in various concentrations.
In this case, the spinning draw-off speed was adjusted to a constant speed of 4350 m/min. The polymer throughput per spinneret was 55 g/min. The die pressure was in the range from 130 to 145 bar. Table 9 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment.

40

ratio
The strands were subjected to stretch texturizing as in experiment El at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 10 as the mean of all 6 bobbins of each individual experiment.
In experiment E10, the additive concentration was particularly appropriate for the spinning speed, so that firstly particularly preferred properties of the strand resulted, and secondly the best yarn properties and the

41
best processing properties were also achieved in the stretch texturizing.
Stretch-texturized yarns of good quality were also produced in experiments Ell and E12. In experiment Ell, the amount 'of additive metered in is no longer in the particularly preferred range. As a result, the elongation at break of the strand also lies outside the preferred range, and in comparison with experiment E10, a slight reduction in the tear strength and elongation at break of the stretch-texturized yarn can be seen. This trend continues in experiment E12, where the amount of additive is also outside the preferred range of addition.
Table 10:
Results of the stretch texturizing of experiment no. E10 -E12

(+ = positive; 0 = limited processability; - = negative)
Example 8:
In the metering and spinning system according to example 6 and under otherwise the same conditions, the spinning speed was varied between 3200 m/min and 6000 m/min. The amount of additive metered in was adjusted here such that elongations at break of between 115 % and 133 % resulted in the POY yarn.

42
Table 11 contains the strand characteristic data as the mean of all 6 bobbins of each individual experiment. For comparison, the data of experiment no. El contained in table 5 are listed again.

ratio
Table 11:

43
The strands were subjected to stretch texturizing as in example 5 at a processing speed of 1000 m/min. The textile characteristic data are summarized in table 12 as the mean of all 6 bobbins of each individual experiment.
Table 12:
Results of the stretch texturizing of experiment no. El, E6, E10, E13, E14
Experiment No. El E13 E10 E6 E14
Speed m/min 1000 1000 1000 1000 1000
Stretching ratio 1: 1.79 1.86 1.73 1.72 1.72
Tension Fl / F2 cN 32/31 31/28 35/21 32/29 31/28
Elongation at % 19.2 18.6 20.6 21.5 20.1 break
Tear strength cN/tex 45.3 44.7 45.5 45.2 43.8
Dyeing level 1-2 1-2 1-2 1-2 1-2
Processing 0 + + + +
properties
{+ = positive; 0 = limited processability; - = negative)
In all the experiments according to this invention, the amount of additive added was ideally appropriate for the spinning speed. Strands with preferred properties which also gave outstanding results in the stretch texturizing resulted.
Example 9:
The spinning system according to example 2 was modified to the extent that the number of static mixers used for mixing in the additive was reduced from 15 to 9 and 3 respectively, corresponding to residence times of 44, 26 and 9 s. The same spinning conditions were otherwise maintained. SEM investigations were carried out on pellet

44
samples of the modified polyester emerging from the
spinneret, to evaluate the distribution of the additive.
The result is summarized in table 13, together with the
elongation at break of the resulting POY yarn.
If the additive is mixed in inadequately (experiment Ml) , its effectiveness - recognizable by the decreasing elongation at break - is reduced considerably. The reason for the reduced effectiveness of the additive is the increasing content of additive particles of > 1000 ran diameter and the poorer distribution over the yarn cross-section. This is visible in SEM photographs and in graph plots of the particle size against the number of particles.
Table 13:
Influence of the mixer design (nominal width DN 15)
Experiment No. Ml M2 M3
Elongation at break % 77 109.2 116.2 POY
Number of mixing 3 9 15
elements
Average particle run 0.22 0.21 0.19 diameter
Content of particles % 1.5 0.5 0 > 1000 nm
Example 10: Preparation examples for copolymers
1. A mixture of 4750 g completely desalinated water and 118 g Degapas® 8105 S was heated to 40 eC in a 10 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 4750 g of a mixture of 86.2 parts by weight methyl methacrylate (MMA), 8.8 parts by weight styrene, 5 parts by weight cyclohexylmaleimide, 0.14 part by weight 2-ethylhexyl thioglycollate, 0.09 part by

45
weight t-dodecylmercaptan, 0.05 part by weight stearic acid and 0.25 part by weight dxlauroyl peroxide were then added, while stirring. The batch was polymerized at 80 eC for 165 minutes and at 90 CC for 60 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 eC in a fluidized bed drier.
4710 g of clear polymer beads with a viscosity number of 99.6 ccm/g were obtained.
2. A mixture of 2400 g completely desalinated water and
46 g of a 6 per cent aqueous solution of a methacrylic acid copolymer was heated to 40 aC in a 5 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 2400 g of a mixture of 90.65 parts by weight methyl methacrylate (MMA), 8.75 parts by weight styrene, 0.15 part by weight 2-ethylhexyl thioglycollate, 0.1 part by weight t-dodecylmercaptan, 0.05 part by weight stearic acid and 0.3 part by weight dilauroyl peroxide were then added, while stirring. The batch was polymerized at 80 aC for 150 minutes and at 90 CC for 30 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 2C in a fluidized bed drier.
2283 g clear polymer beads with a viscosity number of 98.5 ccm/g were obtained.
3. A mixture of 2400 g completely desalinated water and
46 g of a 6 per cent aqueous solution of a methacrylic acid polymer was heated to 40 CC in a 5 1 polymerization vessel equipped with a stirrer, reflux condenser and thermometer. 2400 g of a mixture of 90.715 parts by weight methyl methacrylate {MMA), 8.75 parts by weight styrene, 0.115 part by weight 2-ethylhexyl thioglycollate, 0.07 part by weight t-dodecylmercaptan, 0.05 part by weight stearic acid

46
and 0.3 part by weight dilauroyl peroxide were then added, while stirring. The batch was polymerized at 80 eC for 150 minutes and at 90 eC for 60 minutes and then cooled to room temperature. The polymer beads were filtered off, washed out thoroughly with completely desalinated water and dried at 80 2C in a fluxdized bed drier.
2299 g clear polymer beads with a viscosity number of 118.4 ccm/g were obtained.

-47-WE CLAIM
1. Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastfcalfy processable coporymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula.

2. Process as claimed in claim 1, wherein the ratio of the melt viscosity of the
copofymer to the mett viscosity of (he polyester is 1.4 : 1 to 8 :1.
3. Process as claimed in claim 1 or 2, wherein the ratio of the melt viscosity
of the copolymer to the melt viscosity of the polyester Is 1.7 :1 to 6.5 :1.
4. Process as claimed in claim 1, 2 or 3 wherein the copolymer comprises
the following monomer units:
A= acrylic acid, methacryfic acid or CH2 = CR - COOR', wherein R is an H atom or a CH3 group and R1 is a C1-15 -alkyl radical or a C5-12-cycloalkyl radical or a C6-14-aryl radical.

-48-B = styrene or C1-3 -alky1-substituted styrenes,

wherein the copolymer comprises 60 to 98 wt.% A and 2
to 40 wt.% B (total = 100 wt%).
5. Process as claimed in claim 4 wherein the copolymer comprises 83 to 98 wt. % A and 2 to 17 wt. % B (total = 100 wt. */.) .
6. Process as claimed in claim 4 or 5 wherein the copolymer comprises 90 to 98 wt.% A and 2 to 10 wt.% B (total = 100 wt.%). 7. Process as claimed in claims 1, 2 or 3, wherein the copolymer comprises the follawing monomer units:
C = styrene orC - alkyl-substituted styrenes,
1-3 D = one or more monomers of the formula I, II or III

wherein R , R and R are each an H atom or a
C - alkyl radical or a C - cycloalkyl radical
1-15 5-12
or a C - aryl radical,
6-14 and wherein the copolymer comprises 15 to 95 wt. % C and 2 to 80
wt. % D, the total of C and D together giving 100%.
8. Process as claimed in claim 7, wherein the copolymer comprises 50 to 90 wt. % C and 5 to 50 wt. % D, the total of C and D together giving 100%.

-49-
9. Process as claimed in claims 7 or 8, wherein the copolymer comprises 70 to 85 wt.% C and 30 to 15 wt. % D, the total of C and D together giving 100 %.
10. Process as claimed in claims 1, 2 or 3, wherein the copolymer comprises the following monomer units:
E = acrylic acid, methacrylic acid or CH - CR - COOR', wherein
2
R is an H atom or a CH group, and R is a C -alkyl
3 1-15
radical or a C cycloalkyl radical or a C -aryl
5-12 6-14
radical,
F = styrene or C
1-3 - alkyl - substituted styrenes,
G = one or more monomers of the formula I, II or III

wherein R1 , R2 , R3 are each an H atom or a
C1-15 - alkyl radical or a C5-12 - cycloalkyl radical or
a C 6-14, - aryl radical
H = one or more ethylenically unsaturated monomers, which can be
copolymerized with E and/or with F and/or 6, from the group which
consists of -methylstyrene, vinyl acetate, acrylic acid
esters, methacrylic acid esters which differ from E, vinyl
chloride, vinyl idene chloride, halogen-substituted styrenes,
vinyl esters, isopropenyl ethers und dienes,

-50-
wherein the copolymer comprises 30 to 99 wt.% E, 0 to 50 wt.% F, >0 to 50 wt. % of G and 0 to 50 wt.% of H, the total of E, F, G and H together giving 100%.
11. Process as claimed in claim 10 wherein the copalymer
comprises 45 to 97 wt-% E, 0 to 30 wt- % of F, 3 to 40 wt.% of G
and 0 to 30 wt.% of H, the total of E, F, G and H together giving
100%.
12. Process as claimed in claim 10 or 11, wherein the
copolymer comprises 60 to 94 wt. % of E, 0 to 20% wt.% of F, 6 to
30 wt- % of G and 0 to 20 wt.% of H, the total of E, F, B and H
together giving 100 %.
13. Process as claimed in one or more claims 1 to 12, wherein
the copolymer comprises additives in an amount of in each case
14. Process as claimed in one or more of claims 1 to 13,
wherein the polymer mixture is prepared, after melting of the
polyester and copolymer, in a static mixer, the diameter of which
- 1
is chosen such that the shear rate is between 16 and 128 s and the product of the shear rate and the 0.8th power of the residence time in seconds is greater than 250.
15. Process as claimed in one or more of claims 1 to 14,
wherein the mixture is subjected to shear treatment during mixing
isuch that the average particle size of the copolymer immediately

-51-
after discharge from the spinneret is not more than 400 nm, that less than 1 % of the copolymer particles contained in the mixture have a particle size of > 1 m, and that the length/diameter ratio of the copolymer particles is > 2, the copolymer particles being present in the polymer matrix in the filaments in the form of fibrils after the spinning draft and the length/diameter ratio of the fibrils being > 50.
16. Process as claimed in one or more of claims 1 to 15,
wherein the polyester is a thermoplastically processable
polyester, such as polyethylene terephthalate, polyethylene
naphthalate, polypropylene terephthalate or polybutylene tere-
phthalate, it being possible for the polyester optionally to
comprise up to 15 mol % of a comonomer and/or up to 0.5 wt. % of
a polyfunctional branching component.
17. Process as claimed in one or more of claims 1 to 16,
wherein the filaments are initially wound up after the spinning
and are then subjected to a stretch tsxturizing, the stretching
ratio being between 1: 1.35 and 1: 2.20.
18. Process as claimed in claim 17 wherein the textured filaments with a capillary titre of more than 2 dtex are produced at a processing speed of at least 750 m/min and the texturezed filaments with a capillary titre of less than 2 dtex are produced at a processing speed of at least 400 m/min.

-52-
19. Preorientated filaments produced according to the
process as claimed in one or more of claims 1 to 16 wherein they
have an elongation at break of 85 to 180%, a tear strength of at
least 17 cN/tex, a shrinkage at the boil of 32 to 69*/,, a
birefringence of 0.030 to 0.075 and a crystal 1inity of less than
20%.
20. Preorientated filaments as claimed in claim 19, wherein
they have an elongation at break of 109 to 146%, a tear strength
of at least 22 cN/tex and a normal Uster of 21. Texturised filaments wherein they are produced from the
preorientated filaments as claimed in claims 19 and 20 in
accordance with the process as claimed in claims 17 and 18.
Process for the production of preorientated filaments comprising the steps of preparing a polymer mixture by melting and mixing together polyester based polymer with the amorphous, thermoplastically processable copolymer having a glass transition temperature of more than 100°C, and spinning the molten polymer mixtures with a draw-off speed v of at least 2, 500 m/min to form the filaments characterized in that the ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1:1 to 10:1, in that the amount of copolymer added to the polyester corresponds to at least 0.05 wt.% and not more than an amount M, where M is given by the formula.

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Patent Number

209426

Indian Patent Application Number

01364/CAL/1998

PG Journal Number

35/2007

Publication Date

31-Aug-2007

Grant Date

30-Aug-2007

Date of Filing

03-Aug-1998

Name of Patentee

ZIMMER AKTIENGESELLACHAFT

Applicant Address

BORSIGALLEE 1, DE-60388, FRANKFURT,

Inventors:

#	Inventor's Name	Inventor's Address
1	DR. ULRICH THIELE	HEINRICH-VON-BRENTANO-STRASSE 2, DE-63486 BRUCHKOBEL, GERMANY
2	DR. ALEXANDER KLEIN	IM BIENENGARTEN 4, DE-55218 INGELHEIM, GERMANY
3	DR. HEINZ-DIETER SCHUMANN	ADALBERT-STIFTER-STRASSE 37, DE-63477 MAINTAL GERMANY
4	DR. HELMUT SCHWIND	TREUENERSTRASSE 5, DE-63457 HANAU
5	WOLFGANG JANAS	AM BORNGRABEN 6, DE-63826 GEISELBACH
6	DR. KLAUS DORN	TREUENERSTRASSE 6, DE-63457 HANAU , GERMANY
7	PETER KEMPF	NORDRING 11, DE-63517 RODENBACH, GERMANY
8	DIETMAR WANDEL	JOHANNES-MACHERM-STRASSE 8, DE-63456 HANAU, GERMANY
9	DR. JOACHIM CZIOLLEK	WALLSTRASSE 78, DE-55122 MAINZ, GERMANY

PCT International Classification Number

D 01 F 6/92

PCT International Application Number

N/A

PCT International Filing date

PCT Conventions:

#	PCT Application Number	Date of Convention	Priority Country
1	197 33 799.6	1997-08-05	Germany
2	19747867.0	1997-10-30	Germany