DE10210018A1 - A tension increasing agent for spinning processes containing an additive/polymer and a flow aid useful for production of staple fibers and commercial yarns - Google Patents

Abstract

A tension increasing agent for spinning processes containing (sic) an additive-polymer and a flow aid independently containing a polymer obtained by polymerisation of monomers of given formula and 3 copolymers containing specific monomer units is new. A tension increasing agent for spinning processes containing (sic) an additive-polymer and a flow aid independently containing: (a) a polymer obtained by polymerization of monomers of formula (I): where R<1> and R<2> = substituents containing the optional atoms C,H, O,S, and P, and halogen atoms, and the sum of the molecular weights of R<1> and R<2> is at least 40, (b) a copolymer, containing the monomer units: A = (meth)acrylic acid or CH2=CR-COOR', where R = H or Me, R' = 1-15C alkyl, 5-12C cycloalkyl, or 6-14C aryl, B = styrene or 1-3C alkyl substituted styrene, where the polymer contains (wt.%): A (60-98) and B (2-40) (sum = 100 wt.%), (c) = a copolymer containing the monomers units: C = styrene or 1-3 alkyl substituted styrene, D = one or more monomers of formula (II, (III), or (IV), where R<3>,R<4>, and P<5> = H, 1-15C alkyl, 6-14C aryl, or 5-12C cycloalkyl, where the polymer comprises C (15-95) and D (2-80), where the sum of C and D = 100 wt.%, or (d ) a copolymer containing the monomer units: E = (meth)acrylic acid or CH2 =CR-COOR', where R = H or ME and R' = 1-15C alkyl,5-12C cycloalkyl, or 6-14C aryl, F = styrene or 1-3C alkyl substituted styrene, G = one or more monomers of formula II, III, or IV, where R<3>, R<4>, and R<5> = 1-15C alkyl, 5-12C cycloalkyl, or 6-14C aryl, H = one or more ethylenically unsaturated with E, and/or with F, and/or with G polymerisable monomers from the group: alpha-methylstyrene, vinyl acetate, (meth)acrylic acid esters, different from E, acrylonitrile, (meth)acrylamide, vinyl chloride, vinylidene chloride, halogen substituted styrenes, vinyl ethers, isopropenyl ethers, and dienes, where the polymer comprises (wt.%): E (30-99), F (0-50), G (0-50), and H (0-50), where the sum of E, F, G, and H = 100 wt.%, and the additive polymer has a mean particle diameter of 0.1-1.0 mm and the flow aid has a mean particle diameter of 0.1-100 micron. Independent claims are included for: (1) A process for preparation of synthetic fibers from a fiber forming matrix of polymers based melt/mixture, in which the fiber forming matrix of polymers contains a tension increasing agent in accordance with at least one of the above claims, in amount 0.05-5 wt.% relative to the total weight of fiber forming polymer matrix to which the tension increasing agent is added; (2) a synthetic fiber obtained by the above process; and (3) further treatment of the synthetic fiber in stretching or stretch texturing process.

Description

The present invention relates to an elongation enhancer comprising Additive polymer and a trickle aid. The stretching agent can be in Process for the production of synthetic threads from a fiber-forming Polymer-based mixture used and the resulting threads can on the one hand used as continuous filaments or processed into staple fibers become.

The spinning of polymer blends into synthetic threads is already known. It aims to be higher at a certain spinning speed To obtain elongation at break in the spun thread than without modification by additional Polymer. This is intended to produce a higher draw ratio for the production of the End yarns may be possible, which result in higher productivity of the spinning unit should.

The increase in production aims to improve the profitability of the Manufacturing process. This is due to production difficulties and more expensive To a certain extent, high-speed equipment was reduced again.

The additional costs for the additive polymer are of major influence, so that depending on the amount added, there is even a zero point for the Economy there. The availability of the additive polymers also plays a role Market an important role. For these reasons, a large number of those in the Literature described additives for large-scale implementation.  

The producer or process provider must cover the entire production chain and can take into account the increase in production of a sub-step (e.g. the spinning mill). The subsequent processes must not be impaired become. In particular, it is a primary object of this invention that Not to reduce processing conditions in the subsequent steps, preferred to improve, despite the increased spinning speed.

For example, for the production of POYs in the prior art for Polymer blends very high elongations at break, even for high ones Called spinning speeds, which greatly reduces the Mark degrees of orientation. Such spun threads are known to be not stable in storage and can be used in stretch texturing processes at high Do not create and process speeds. At high In turn, the elongation at break specified for the spinning speeds is <70% to a significant degree of crystallization, which the achievable strengths in Texturing process reduced.

The first approaches to solving these problems are described in EP 0 047 464 B (Teijin), DE 197 07 447 (Zimmer), DE 199 37 727 (Zimmer), DE 199 37 728 (Zimmer) and WO 99/07 927 (Degussa ) disclosed. EP 0 047 464 B relates to an undrawn polyester yarn, the addition of 0.2-10% by weight of a polymer of the type - (- CH ₂ -R ₂ -) _n -, such as poly (4-methyl-1 - pentene) or polymethyl methacrylate, improved productivity is obtained by increasing the elongation at break of the filament at speeds between 2500-8000 m / min and correspondingly higher draw ratios. A fine and uniform dispersion of the additive polymer by mixing is necessary, the particle diameter having to be ≦ 1 μm in order to avoid fibril formation. The decisive factor for the effect is the interaction of three properties - the chemical additive structure, which hardly allows the additive molecules to stretch, the low mobility and the compatibility of polyester and additive. The measures serve to increase productivity. Requirements for stretch texturing are not disclosed. The reworkability of the technical teaching within the framework of WO 99/07927 resulted in a high additive consumption and associated impairment of the quality and processability.

DE 197 07 447 (Zimmer) relates to the production of polyester or polyamide Filaments with an elongation at break ≦ 180%. The addition of 0.05 to 5% by weight a copolymer of 0 to 90% by weight of (meth) acrylic acid alkyl ester, 0 to 40 % By weight of maleic acid (anhydride) and 5 to 85% by weight of styrene to the polyester or Polyamide enables a significant increase in the spinning take-off speed.

The publication DE 199 37 727 (Zimmer) describes the production of polyester Staple fibers made from a polymer blend disclosed containing 0.1 to 2.0% by weight of a contains incompatible, amorphous, polymeric additive, which a Glass transition temperature in the range of 90 to 170 ° C. In doing so the ratio of the melt viscosity of the polymeric additive to Melt viscosity of the polyester component 1: 1 to 10: 1.

DE 199 37 728 (Zimmer) relates to a process for the production of HMLS threads made of polyester, polymeric additive and optionally additives with a spinning take-off speed of 2500 to 4000 m / min. It should polymeric additive a glass transition temperature in the range of 90 to 170 ° C. have and the ratio of the melt viscosity of the polymeric additive to Melt viscosity of the polyester component 1: 1 to 7: 1.

WO 99/07 927 relates to the production of POYs by spinning polymer mixtures based on polyester with a take-off speed v of at least 2500 m / min. wherein a second, amorphous, thermoplastically processable copolymer with a glass transition temperature of more than 100 ° C. is added to the polyester. The ratio of the melt viscosity of the copolymer to the melt viscosity of the polyester is 1: 1 to 10: 1. At least 0.05% by weight of copolymer is added to the polyester and the maximum amount M of the copolymer added to the polyester depends on the take-off speed v and is

Although the latter procedures (Zimmer AG) are already good and practical thread breakage rates during the spinning of such Polymer blends show, however, are processes for Spinning polymer blends with an even smaller number of Thread breaks required to further increase the efficiency of the spinning process. Furthermore, the further processing behavior of the synthetic threads, especially in stretch texturing.

In the processes mentioned, the means of elongation increase used usually granulated before metering in to the polyester To increase the flow properties of the additive polymer. However, that can also be done Granulated additive polymer only relatively due to its large grain size dose poorly and unevenly. This leads to a deterioration in Yarn characteristics, in particular the uniformity of the synthetic threads (e.g. Dyeing behavior).

The costly granulation step can be achieved by using conventional pouring aids, such as water-insoluble, hydrophobic or moisture adsorbing powders of diatomaceous earth, pyrogenic silicas, tricalcium phosphate, calcium silicates, Al ₂ O ₃ , MgO, MgCO ₃ , ZnO, stearates, fatty amines (see CD Römpp Chemie Lexicon - Version 1.0, Stuttgart / New York: Georg Thieme Verlag 1995), cannot be avoided, since such trickle aids are disadvantageous for the spinning process. On the one hand, they can deposit in the spinning device and in this way lead to blockages in the lines and nozzles and thus to malfunctions. There is also the danger of the "foreign substances" deteriorating the material properties of the resulting synthetic threads and increasing the thread breakage rate during spinning.

In view of the prior art, it was now the task of the present Invention to provide an elongation enhancer for spinning processes represent the manufacture of synthetic threads with constant Yarn properties made possible in a simple manner. In particular, should the elongation enhancer according to the invention no granules and thus less expensive than those known from the prior art Elongation enhancer.

Another object of the present invention was to provide a method to indicate the spinning of synthetic threads, the industrial and is inexpensive to carry out. The inventive method should Production of POYs with the highest possible withdrawal speeds, preferably allow ≧ 2500 m / min.

According to the synthetic threads should be simple can be processed further. In particular, the should according to the invention POYs available further processing in a stretching or Stretch texturing process, preferably at high processing speeds, with constant yarn properties.

These and other tasks not explicitly mentioned are solved, however can easily be derived from the contexts discussed in the introduction or can be developed by a stretching agent for spinning processes with all the features of claim 1. Appropriate modifications of Elongation-increasing agents according to the invention are described in claim 1  back-related subclaims placed under protection. The procedure for Manufacture of synthetic threads is described in the process claims described, whereas the synthetic thread obtainable by the method is claimed in independent product claim 9. Further processing of the synthetic thread in a drawing or drawing texturing process protected in claim 10, whereas claim 11 relates to use of the synthetic thread for the production of staple fibers.

By providing an elongation enhancer for spinning processes comprising an additive polymer and a trickle aid, the additive polymer and the trickle aid each being independent of one another

• 1. a.) A polymer obtained by polymerizing monomers of the general formula (I):
  is available, where R ¹ and R ^{2 are} substituents consisting of the optional atoms C, H, O, S, P and halogen atoms and the sum of the molecular weights of R ¹ and R ^{2 is} at least 40,
• 2. b.) A copolymer which contains the following monomer units:
  A = acrylic acid, methacrylic acid or CH ₂ = CR-COOR ', where R is an H atom or a CH ₃ group and R' is a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 Aryl residue is
  B = styrene or C _1-3 alkyl-substituted styrenes, the copolymer consisting of 60 to 98% by weight of A and 2 to 40% by weight of B, preferably of 83 to 98% by weight of A and 2 to 17% by weight. % B, and particularly preferably consists of 90 to 98% by weight A and 2 to 10% by weight B (total = 100% by weight),
• 3. c.) A copolymer which contains the following monomer units:
  C = styrene or C _1-3 alkyl-substituted styrenes,
  D = one or more monomers of the formula II, III or IV
  where R ³ , R ⁴ and R ^{5 are} each an H atom or a C _1-15 alkyl radical or a C _6-14 aryl radical or a C _5-12 cycloalkyl radical,
  the copolymer consisting of 15 to 95% by weight of C and 2 to 80% by weight of D, preferably of 50 to 90% by weight of C and 10 to 50% by weight of D and particularly preferably of 70 to 85% C and 15 to 30 wt .-% D, the sum of C and D together making 100 wt .-%, or
• 4. d.) A copolymer which contains the following monomer units:
  E = acrylic acid, methacrylic acid or CH ₂ = CR-COOR ', where R is an H atom or a CH ₃ group and R' is a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 Aryl residue is
  F = styrene or C _1-3 alkyl-substituted styrenes,
  G = one or more monomers of the formula II, III or IV
  where R ³ , R ⁴ and R ^{5 are} each an H atom or a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 aryl radical,
  H = one or more ethylenically unsaturated monomers copolymerizable with E and or with F and / or G from the group consisting of α-methylstyrene, vinyl acetate, acrylic acid esters, methacrylic acid esters other than E, acrylonitrile, acrylamide, methacrylamide, vinyl chloride, vinylidene chloride, halogen-substituted styrenes, vinyl ethers, isopropenyl ethers and dienes,
  wherein the copolymer consists of 30 to 99% by weight E, 0 to 50% by weight F, 0 to 50% by weight G and 0 to 50% by weight H, preferably 45 to 97% by weight E. , 0 to 30% by weight of F, 3 to 40% by weight of G and 0 to 30% by weight of H and particularly preferably from 60 to 94% by weight of E, 0 to 20% by weight of F, 6 up to 30% by weight G and 0 to 20% by weight H, the sum of E, F, G and H together giving 100% by weight,

are and the elongation means is characterized in that the Additive polymer has an average particle diameter of 0.1 to 1.0 mm and  the trickle aid has an average particle diameter of 0.1 to 100 µm exhibit, it succeeds in a manner that is not readily predictable To provide elongation enhancers for spinning processes which the production of synthetic threads with a lower thread breakage rate and with allows constant yarn properties in a simple manner. The expansion agent according to the invention for the Melt spinning of synthetic threads cannot be granulated.

At the same time, the elongation-increasing agent according to the invention has a number of further advantages. These include:

• - The elongation means according to the invention is spinning and winding of synthetic threads in a simple manner, Can be carried out on an industrial scale and at low cost. In particular, it allows that Spinning and winding at high take-off speeds.
• - Due to the high uniformity of using the Elongation-increasing agents according to the invention obtainable synthetic Fadens is a simple way to get a good bobbin build adjust the, a uniform and almost flawless staining and Further processing of the synthetic thread allowed.
• - The method according to the invention is in particular for the production of POYs based on polyester with elongation at break values in the range of 90% -165%, a high degree of uniformity with regard to the filament characteristics and low degree of crystallization.
• - The using the elongation enhancer according to the invention available synthetic threads can be easily, can be processed on an industrial scale and at low cost. For example  can the POYs according to the invention at high speeds in one Stretching or a stretch texturing process with uniform Yarn properties are processed further.

The present invention relates to an elongation enhancer for Spinning process comprising an additive polymer and a flow aid, the Additive polymer and the trickle aid each independently a polymer of the above type a.) or a copolymer of the above Type b.), C.) Or d.). Mixtures of several of the polymers mentioned and / or copolymers are conceivable.

According to the invention, exemplary monomer units of the general formula (I) which can be used to synthesize the polymer of type a.) Include acrylic acid, methacrylic acid and CH ₂ = CR-COOR ', where R is an H atom or a CH ₃ group and R 'is a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 aryl radical, and also styrene and C ₁₃ alkyl-substituted styrenes.

Component H of the copolymer of type d.) Is a optional component. Although the advantages to be achieved according to the invention already by copolymers, which components from groups E to 6 have, can be achieved occur those to be achieved according to the invention Advantages also if the structure of the copolymer of type d.) More Group H monomers are involved.

Component H is preferably selected so that it does not disadvantage Effect on the properties of the type d.) Copolymer.

Component H can u. a. therefore used to the properties to modify the copolymer as desired, for example by Increases or improvements in flow properties when the copolymer is heated to the melting temperature, or to reduce a residual color in the  Copolymer or by using a polyfunctional monomer to make up this way some degree of crosslinking in the copolymer introduce.

In addition, H can also be chosen so that a copolymerization of Components E to G are possible or supported in the first place, as in the case of MSA and MMA, which do not copolymerize per se, but when one is added third component such as styrene copolymerize easily.

Suitable monomers for this purpose include u. a. Vinyl esters, esters acrylic acid, for example methyl and ethyl acrylate, esters of Methacrylic acid, which differ from methyl methacrylate, for example Butyl methacrylate and ethylhexyl methacrylate, acrylonitrile, acrylamide, Methacrylamide, vinyl chloride, vinylidene chloride, styrene, α-methylstyrene and the various halogen-substituted styrenes, vinyl and isopropenyl ether, dienes, such as 1,3-butadiene and divinylbenzene. The color reduction of the For example, copolymers can be used particularly preferably by using a electron-rich monomers, such as a vinyl ether, vinyl acetate, Styrene or α-methylstryrene can be achieved.

Are particularly preferred among the compounds of component H. aromatic vinyl monomers, such as styrene or α-methylstyrene.

The production of said polymers and copolymers is of type a.) To d.) known per se. You can in substance, solution, suspension or Emulsion polymerization can be produced. Helpful hints can be found with regard to bulk polymerization in Houben-Weyl, Volume E20, Part 2 (1987), page 114ff. Information on solution polymerization can be found there on page 1156ff. The suspension polymerization technique is just there on page 1149ff, while the emulsion polymerization is on the page  1150ff is executed and explained. If necessary, the resulting Polymers are still ground.

The imidized types of copolymers c.) And d.) Can be derived from the monomers be prepared using a monomeric imide as well subsequent complete or preferably partial imidization of the corresponding copolymer containing maleic acid derivative. Be preserved these polymers for example by complete or preferably partial Implementation of the corresponding copolymer in the melt phase with ammonia or a primary alkyl or arylamine, for example aniline (Encyclopedia of Polymer Science and Engineering Vol. 16 [1989], Wiley-Verlag, page 78). The resulting polymers may still have to be ground.

All of the copolymers according to the invention and, if present, not theirs imidized starting copolymers are commercially available or after one for the process familiar to the skilled worker can be produced.

According to the invention, the additive polymer has a medium one Particle diameter from 0.1 to 1.0 mm and the flow aid a medium one Particle diameter from 0.1 to 100 microns. The determination of particle size can be carried out using methods known from the prior art. The average particle diameter (grain diameter) is preferably the Spinning fiber additive polymers via a sieve analysis, for example with a Alpine air jet screening machine type A 200 LS, determined. The middle one Particle diameter (grain diameter) of the trickle aid is preferably about Laser diffraction spectroscopy, for example with a Mastersizer Microplus Malvern company (measuring range: 0.05-555 µm).

In the context of the present invention, stretching agents with viscosity numbers in the range from 70 to 130 cm ³ / g are preferred for textile applications, such as polyester POYs, because these are suitable for spinning polymer mixtures of polyethylene terephthalate with an intrinsic viscosity number of about 0.55 to 0 , 75 dl / g have proven to be particularly useful. The elongation-increasing agent according to the invention has a significantly improved flowability compared to the pure additive polymer. This improvement can be determined, for example, in accordance with DIN 53492 "Determination of the Flowability of Granular Plastics", November 1992, for example using a Coesfeld trickle funnel with a diameter of the outlet nozzle of 10 mm. In this case, pouring times t _{R10 of} less than 20 seconds, expediently between 10 and 20 seconds, in particular between 10 and 15 seconds, are preferably determined for the elongation-increasing agent according to the invention, whereas pouring times t _R10 <20 seconds up to not for the pure additive polymer without addition of a pouring aid be kept pourable.

Within the scope of the present invention, elongation-increasing means have been found especially proven, which is largely an additive polymer and a trickle aid identical chemical composition included.

The flow aid and the additive polymer used advantageously at least 50% by weight, suitably at least 60% by weight, preferably at least 70% by weight, in particular at least 80 wt .-%, each based on the total weight of the trickle aid or used additive polymer, the same repeat units. In In this context, the repetition units characterize the the recurring monomers derived from the monomers originally used Units in the polymer.

Results which are particularly advantageous according to the invention can be achieved if at least 90% by weight of the flow aid and the additive polymer used, preferably at least 95% by weight, in particular at least 97% by weight, each based on the total weight of the trickle aid or the used  Additive polymers that have the same repeat units. All in one particularly preferred embodiment of the present invention the polymer composition of the flow aid and that of the additive used Polymer completely match.

In the context of the present invention, it is also expedient to have a Use trickle aid that has a similar weight average molecular weight as the additive polymer used. This preferably gives way Weight average molecular weight of the trickle aid of less than 50%, expediently by less than 30%, in particular by less than 20%, from that of the additive polymer used.

The preferred concentration range of the flow aid is in the additive polymer at 0.05 to 5.0 wt .-%, preferably at 0.05 to 1.0 wt .-%, each based on the total weight of additive polymer and pouring aid, and depends on the Surface and thus on the average diameter of the additive polymers. at a bead polymer with an average grain size of 0.7 mm becomes a Concentration of the flow aid from 0.05 to 0.3% by weight is preferred. With decreasing diameter of the pearls takes for the flow-promoting effect required concentration of the trickle aid. If the concentration is too low Trickle aid, the flow-promoting effect is incomplete, while at too high Concentrations of the flow aid no further improvement in flow behavior is achieved, but a strong, technically undesirable dust formation the excess, finely divided trickle aid powder enters.

Advantageously, the additive polymer and the Trickle aid dried to remove residual volatile compounds in the additive polymer or remove in the trickle aid. The drying process itself known way. In particular, the additive polymer has Proven drying on a fluid bed dryer. The trickle aid will preferably produced by an emulsion polymerization process and by  Spray drying isolated. Exemplary descriptions of spray drying are DE 33 20 67 or Ullmann's Encyclopedia of Industrial Chemistry, 5th edition (1988), B 2, page 4-23. Depending on the spray unit (single-component nozzle, Two-substance nozzle or atomizer disc) particles with a medium Grain diameter of 20 to 300 microns obtained.

The mixing of additive polymer and flow aid to produce a The most even (homogeneous) elongation enhancer can be on known way. Further details are, for example, in Ullmanns Encyclopedia of technical chemistry, 5th edition (1988) and in Römpps Chemistry lexicon (CD) - Version 1.0, Stuttgart / New York: Georg Thieme Verlag 1995 described.

In the context of the present invention, it has also proven to be extremely proven expedient, preferably using a fluidized bed Dryer-dried additive polymer and the spray-dried pouring aid mix using a fluid bed dryer. Details on Fluidized bed processes can also be found in the specialist literature, for example Ullmanns Encyclopedia of technical chemistry, 5th edition (1988) and Römpps Chemie Lexicon (CD) - Version 1.0, Stuttgart / New York: Georg Thieme Verlag 1995 be removed.

The elongation-increasing agent according to the invention can be particularly advantageous Way of producing synthetic threads from a fiber-forming Mixture based on matrix polymers can be used. Designate it in the context of the present invention synthetic threads all types of threads, the mixtures of synthetic polymers are available. Among other things, they include staple fibers (Staple fibers), textile filaments such as plain yarns, POYs, FOYs, and technical Filaments.  

Further details on synthetic threads and the groups mentioned, especially regarding their material properties and the usual ones Manufacturing conditions can, for example, from the prior art Fourne "Synthetic Fibers: Manufacture, Machines and Apparatus, Characteristics; Manual for plant planning, machine construction and Company "Munich, Vienna; Hanser Verlag 1995, as well as the printed matter DE 199 37 727 (staple fibers), DE 199 37 728 and DE 199 37 729 (technical yarns) and WO 99/07 927 (POYs) can be found. On the revelation content of this Scriptures are therefore explicitly referred to.

In the context of a particularly preferred embodiment of the present Invention is the inventive method for the production of Staple fibers, plain yarns, POYs, FOYs or technical filaments are used. It was particularly suitable for the production of POYs proved.

According to the invention, the synthetic threads are produced from a fiber-forming matrix polymer-based melt mixture that the contains stretching agents according to the invention.

The spinning can be done both by a direct spinning process, in which the Elongation means in the form of a melt to melt the matrix Polymers is metered in, as well as by an extruder spinning process which the elongation enhancer as a solid to the matrix polymer metered in and then melted. more details to the methods mentioned can the prior art, for example Documents EP 0 047 464 B, WO 99/07 927, DE 100 49 617 and DE 100 22 889 are taken, to the disclosure of which herewith explicitly refer is taken.  

Thermoplastic processable come as fiber-forming matrix polymers Polymers, preferably polyamides, such as polyamide-6 and polyamide-6,6 and Polyester in question. Mixtures of different polymers are also conceivable. in the However, polyesters are preferred in the context of the present invention, especially polyethylene terephthalate (PET), polyethylene naphthalate, Polytrimethylene terephthalate (PTMT) and polybutylene terephthalate (PBT). In a particularly preferred embodiment of the present invention is Matrix polymer polyethylene terephthalate, polytrimethylene terephthalate or Polybutylene terephthalate, especially polyethylene terephthalate.

Homopolymers are preferred according to the invention. But it also comes Copolymers, preferably polyester copolymers in a proportion up to about 15 mol% of conventional comonomers, such as. B. diethylene glycol, triethylene glycol, 1,4-cyclohexanedimethanol, polyethylene glycol, isophthalic acid and / or Adipic acid, in question.

The polymers according to the invention can contain additives as further constituents contain, as they are common for thermoplastic molding compositions and for Improve polymer properties. As such named for example: antistatic agents, antioxidants, flame retardants, Lubricants, dyes, light stabilizers, polymerization catalysts and auxiliaries, adhesion promoters, matting agents and / or organic phosphites. These additives are used in the usual amount, preferably in amounts of up to 10% by weight, preferably <1% by weight, based on 100% by weight of the Polymer mixture used.

If a polyester is used in the process according to the invention, this can also a small proportion (maximum 0.5% by weight) of branching components included, e.g. B. polyfunctional acids, such as trimellitic acid, pyromellitic acid, or tri- to hexavalent alcohols, such as trimethylolpropane, pentaerythritol, Dipentaerythritol, glycerin, or corresponding hydroxy acids.  

According to the invention, the matrix polymer becomes the one according to the invention Elongation enhancer in an amount of at least 0.05% by weight added, the elongation enhancer amorphous and in the matrix Polymer must be largely insoluble. Essentially, they are Elongation enhancer and the matrix polymer are not compatible with each other and form two phases that can be distinguished microscopically. Furthermore, the elongation means must have a glass transition temperature (determined by DSC with 10 ° C / min heating rate) of more than 100 ° C and be processable thermoplastically.

The melt viscosity of the elongation-increasing agent should be selected so that that the ratio of its melt viscosity extrapolated to the measuring time zero, measured at an oscillation rate of 2.4 Hz and a temperature that is the same the melting temperature of the matrix polymer is plus 34.0 ° C (for Polyethylene terephthalate 290 ° C) relative to that of Elongation medium, measured under the same conditions, between 1: 1 and 10: 1. I.e. the melt viscosity of the elongation enhancer is at least equal to or preferably higher than that of the matrix polymer. The ratio of the melt viscosity of the Elongation enhancer to that of the matrix polymer among the above Conditions between 1.4: 1 and 8: 1. A ratio is particularly preferred melt viscosities between 1.7: 1 and 6.5: 1. Under these conditions the average particle size of the additive polymer is 140-350 nm.

The amount of elongation enhancer to be added to the matrix polymer is between 0.05% and 5% by weight, based on the total weight the polymer mixture. For many applications, for example for the The production of POYs is sufficient for addition quantities of less than 1.5% Take-off speeds over 3500 and up to 6000 m / min and more, even often less than 1.0%, which is a significant cost advantage.  

Mixing of the elongation enhancer with the matrix polymer is on known. It is described, for example, in WO 99/07 927 and DE 100 49 617 and DE 10 02 2889, the disclosure of which is hereby explicitly described is referenced. The 2 stretching agent is added for example in extruder spinning by adding it as a solid to the matrix Polymer chips in the extruder inlet with chip mixer or gravimetric Dosing or alternatively by melting the elongation-increasing agent, Dosing by means of a gear pump and feeding into the melt flow of the Matrix polymer. Then a homogeneous is produced Distribution by mixing in the extruder and / or by means of static or dynamic mixer.

The polymer mixture is spun at temperatures, depending on Matrix polymer, in the range of 220 to 320 ° C.

The production of the synthetic threads from the inventive Polymer blends by melt spinning are done using themselves known spinning devices, such as those found in the publications DE 199 37 727 (staple fibers), DE 199 37 728 and DE 199 37 729 (technical yarns) and WO 99/07 927 (POYs). On the revelation content these writings are therefore explicitly referred to.

Since the inventive method for the production of POYs as a whole has proven particularly expedient, will be a special in the following preferred embodiment of the process according to the invention for the production described by POYs. The transfer of the teaching according to the invention A person skilled in the art is familiar with processes for producing other synthetic threads immediately obvious.

POYs are preferably melt spun at Spinning take-off speeds of at least 2500 m / min. Here is the  Filter package according to the known prior art with filter devices and / or loose filter media (e.g. steel sand).

The melted polymer mixture is after shear and Filtration treatment in the nozzle pack through the holes in the nozzle plate pressed. In the subsequent cooling zone, the melt threads are Cooling air cooled below its softening temperature, so that sticking or Upset on the following thread guide is avoided. Training The cooling zone is not critical, provided the filament bundle is homogeneous uniformly penetrating air flow is guaranteed. So can directly An air-free zone below the nozzle plate to delay cooling be provided. The cooling air can be blown from one side by transverse or radial blowing Air conditioning system are supplied or by means of a cooling pipe from the environment can be removed by self-priming.

After cooling, the filaments are bundled and spinning oil is applied to them. For this purpose, oil stones are used, to which the spinning oil is an emulsion of Metering pumps is supplied. The prepared thread runs through advantageously an entangling device (devouring device) for Improvement in thread closure. Also handling and Safety devices must be attached before the thread reaches the winding unit and there is wound onto packages on cylindrical bobbins. The The peripheral speed of the thread package is automatically regulated and is equal to the winding speed. The thread pull-off speed can be 0.2-2.5% higher than that due to its traversing movement Winding speed. Optionally, after preparation or before Winding driven godets are applied. The The peripheral speed of the first godet system is called Withdrawal speed. Additional godets can be used for stretching or relax.  

The incompatibility of the elongation enhancer and the matrix polymer causes the elongation enhancer to form radially symmetrical elongated particles in the matrix polymer predominantly in the direction of the thread immediately after the polymer mixture emerges from the spinneret. The length / diameter ratio is preferably <2. The diameter (d) is determined perpendicularly and the length parallel to the thread running direction. The best conditions were obtained when the mean particle diameter (arithmetic mean) d ₅₀ ≦ 400 nm and the proportion of particles <1000 nm in a sample cross-section was below 1%.

The influence of these particles by the spin delay could be analytical be detected. Examinations of the filaments after the TEM (transmission electron microscopy) methods have shown that there there is a fibril-like structure. The average diameter of the fibrils was estimated to be around 40 nm. The length / diameter ratio of the Fibrils were <50. Are these fibrils not formed or are they Stretching agent particles after exiting the spinneret in the Diameter too large or the size distribution is too uneven, which at insufficient viscosity ratio is the case, so the effect lost.

The role effect described in the literature could with the Elongation-increasing means according to the invention cannot be traced. The Evaluation of microscopic examinations of fiber cross and longitudinal sections suggests that the spinning delay tension is directed to the fibrils that are forming and the polymer matrix warps with little tension. This takes place Deformation of the matrix under conditions that reduce the Orientation and suppression of spin-induced crystallization results. It makes sense to evaluate the effect on the spinning thread formation and processing behavior.  

Furthermore, for the effectiveness of the elongation enhancer according to this Invention a flow activation energy of the copolymers of at least 80 kJ / mol, i.e. a higher flow activation energy than that of the polymer matrix extremely useful. Under this condition, it is possible that the fibrils solidify in front of the polyester matrix and a significant proportion of the adjacent ones Take up spinning tension. This makes it possible to get the one you want To achieve an increase in capacity of the spinning system.

The preferred embodiment of the invention described above The procedure is the same for fast spinning POY threads with one POY filament titer from <3 dtex to 20 dtex and more, as well as from POY filament titles <3 dtex, in particular microfilaments with 0.2 to 2.0 dtex suitable.

In the method according to the invention is due to the used Elongation-increasing means the thread breakage rate compared to that of the prior art Technically known methods significantly reduced. In a preferred one Embodiment of the present invention is in the manufacture of POYs with a titer <3 dtex, the thread break rate is less than 1 break per ton Polymer mixture, expediently less than 0.9 breaks per ton Polymer mixture, preferably less than 0.8 fractions per ton Polymer mixture, in particular less than or equal to 0.75 fractions per ton Polymer mixture.

The synthetic threads obtainable by the process according to the invention can be used directly in the present form or on known per se Be processed further. In a particularly preferred Embodiment of the present invention they are used to manufacture Staple fibers used. Further details on the production of Staple fibers of the prior art, for example the publication DE 199 37 727 and the documents cited therein can be found.  

In a further particularly preferred embodiment of the present Invention are POYs produced by the inventive method stretched or stretch textured. It is for the further processing of the Spinning thread in the drawing texturing process at high speeds the following important: spinning threads according to this invention as roving for the Stretch texturing - usually referred to as POY - is preferred with Take-off speeds ≧ 500 m / min. preferably <3500 m / min, especially preferably <4000 m / min. manufactured. These yarns must be physical Have structure that by a specific degree of orientation and low crystallization is characterized. Have proven themselves to this Characterization of the parameters elongation at break, birefringence, Degree of crystallization and shrinkage. The polymer mixture according to the invention polyester-based is characterized by an elongation at break of the polymer Spinning threads (POY) of at least 85% and a maximum of 180%. The cooking shrink is 32-69%, the birefringence is between 0.030 and 0.075, the Crystallinity is less than 20% and the tensile strength is at least 17 cN / tex. The elongation at break of the polymer filaments is preferably between 85 and 160%. Particularly favorable conditions exist when the elongation at break the polymer filament is between 109 and 146%, the tensile strength at the same time at least 22 cN / tex and the Uster value is a maximum of 0.7%.

The POYs available in this way are for further processing in a stretch or stretch texturing process particularly suitable. It can also with the Further processing a lower number of thread breaks can be observed. The stretch texturing takes place depending on the filament title type with different Speeds, whereby for normal titer filaments ≧ 2 dtex per filament (Final titer) speeds 750 m / min. preferably ≧ 900 m / min. applied become. For microfilaments and fine titers (final titers) <2 dtex Speeds between 400 and 750 m / min preferred. The procedure leaves  advantageously refer to these titers and in particular microfilaments between Use 0.15 and 1.10 dtex (final titer) per filament.

The draw ratios to be used for the specified spun threads are between 1.35 and 2.2, with draw ratios in the upper region and vice versa preferably being used for a lower degree of orientation. In stretch texturing, the stretching ratio is influenced by tension fluctuations (surging) as a function of the working speed. Stretching ratios according to the formula are therefore particularly preferred:
Draw ratio = 5.10 ^-4 .w (m / min) + b
in which
w = stretch texturing speed in m / min
b = constant which is between 1.15 and 1.50,
apply.

In the following, the invention is illustrated by example and comparative example explained in more detail without restricting the invention to this example shall be. The specified property values, as well as the Values given above, determined as follows:

The residual monomer content of methyl methacrylate and styrene was determined using the gas chromatographic headspace analysis, a method of determination Vaporizable components in liquids and solids (including from Monomers in thermoplastics). The residual monomer content of N- Cyclohexylmaleimide was gas chromatographed on a solution of Polymers determined in dichloromethane.  

The average grain diameter of the staple fiber additive beads was over a Screen analysis determined with an Alpine air jet screening machine (type A 200 LS).

The mean grain diameter of the spray-dried trickle aid was over Laser diffraction spectroscopy with a Mastersizer Microplus from Malvern (Measuring range: 0.05-555 µm).

The pourability was determined according to DIN 53492 "Determination of the pourability of granular plastics ", November 1992 Trickle funnel from Coesfeld with a diameter of the outlet nozzle of 10 mm inserted.

The intrinsic viscosity was determined on a solution of 0.5 g polyester in 100 ml a mixture of phenol and 1,2-dichlorobenzene (3: 2 parts by weight) at 25 ° C. certainly.

The viscosity number VZ (also Staudinger function) is the concentration-related relative viscosity change of a 0.5% solution of the copolymer in chloroform based on the solvent, whereby the throughput times in the Ubbelohde viscometer with hanging ball level, Schott type no. 53203 and capillary 0c according to DiN -Norm 51562 at 25 ° C were determined. Chloroform was used as the solvent.

in which
t = throughput time of the polymer solution in seconds
t _o = throughput 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 ≦ 1000 ppm (polyester ≦ 50 ppm). The granules were then introduced into the temperature-controlled measuring plate in a cone-plate rheometer, type UM100, Physica Meßtechnik GmbH, Stuttgart / DE, while blanketing with nitrogen. The measuring cone (MK210) was positioned on the measuring plate after the sample had melted, ie after approx. 30 seconds. The measurement was started after a further heating-up period of 60 seconds (measuring time = 0 seconds). The measurement temperature was 290 ° C. for polyethylene terephthalate and additive polymers to which polyethylene terephthalate is added, or was equal to the melting temperature (method according to this) of the polymer concerned plus 34.0 ° C. The measuring temperature thus determined corresponds to the typical processing or spinning temperature of the respective polymer. The amount of sample was chosen so that the rheometer gap was completely filled. The measurement was carried out in oscillation with the frequency 2.4 Hz (corresponding to a shear rate of 15 sec ^-1 ) and a deformation amplitude of 0.3, and the amount of the complex viscosity was determined as a function of the measurement time. The initial viscosity was then converted to zero measurement time by linear regression.

For the determination of the melting temperature of the polymer, the Polymer sample first melted at 310 ° C for 1 min and immediately quenched to room temperature. Then the Melting temperature by DSC measurement (differential scanning calorimetry) a heating rate of 10 ° C / min determined. Pretreatment and measurement took place under nitrogen blanketing.

The titer was measured with a precision weight and a weighing device in determined in a known manner. The preload was expediently for pre-oriented filaments (POYs) 0.05 cN / dtex and for textured yarn (DTY) 0.2 cN / dtex.  

The tensile strength and the elongation at break were measured in a Statimat measuring device determined the following conditions; the clamping length was 200 mm for POY or 500 mm for DTY, the measuring speed was 2000 mm / min for POY or 1500 mm / min for DTY, the pretension was 0.05 cN / dtex for POY or 0.2 cN / dtex for DTY. By dividing the values for the maximum tear load the tensile strength was determined by the titer and the elongation at break was determined evaluated at maximum load.

example a.) Production of the elongation enhancer

A bead polymer based on MMA / styrene / N-cyclohexylmaleimide prepared in suspension was used as the additive polymer. This was a terpolymer composed of 89.2% by weight of methyl methacrylate, 8.8% by weight of styrene and 2% by weight of N-cyclohexylmaleimide, the terpolymer having a viscosity number VZ of approximately 101 cm ³ / g and a Melt viscosity (at 290 ° C) of about 1400 Pa.s.

The MMA / styrene / N-cyclohexylmaleimide additive polymer with VZ 101 cm ³ / g was obtained as follows:
A mixture of 525 kg of completely deionized water, 0.071 kg of KHSO ₄ and 13 kg of a 13% aqueous solution of a polyacrylic acid was heated to 40 ° C. in a 10001 polymerization vessel with a heating / cooling jacket equipped with a stirrer, reflux condenser and thermometer. With stirring, 525 kg of a mixture of 88.68 parts by weight of methyl methacrylate (MMA), 8.75 parts by weight of styrene, 1.99 parts by weight of N-cyclohexylrnaleinimide, 0.14 parts by weight of 2-ethylhexyl thioglycolate, 0.09 parts by weight of t-dodecyl mercaptan, 0.05 part by weight of stearic acid and 0.3 part by weight of dilauroyl peroxide were added. The mixture was polymerized for 130 minutes at 80 ° C. and 60 minutes at 98 ° C. and then cooled to room temperature. The polymer beads were filtered off, washed thoroughly with demineralized water and dried in a fluidized bed dryer at 80.degree.

The dried polymer beads are then mixed with 0.1 part by weight a spray-dried MMA / styrene emulsion polymer and approx. 5 minutes mixed in a fluid bed dryer.

The MMA / styrene emulsion polymer, which acts as an antistatic agent or flow aid, was obtained as follows:
80 kg of fully demineralized water, 0.016 kg of 75% sodium diisooctyl sulfosuccinate and 0.056 kg of sodium peroxodisulfate were placed in a 500 l polymerization vessel with a heating / cooling jacket equipped with a stirrer, reflux condenser and thermometer and heated to an internal temperature of 92 ° C. In a second reactor equipped with a stirrer, an emulsion of 182.4 kg methyl methacrylate, 17.6 kg styrene, 0.080 kg thioglycolic acid 2-ethylhexyl ester in 120 kg demineralized water containing 0.8 kg sodium diisooctylsulfosuccinate and 0.12 kg Contained sodium peroxodisulfate. This emulsion was metered at a rate of 1.2 kg / minute into the polymerization vessel, which was kept at a polymerization temperature of about 92 ° C. by heating or cooling. After the end of the metering, the reactor contents were reheated for 30 minutes at an internal temperature of 92 ° C.

The polymer dispersion obtained was then spray-dried in a spray tower from Niro, equipped with an atomizing disc rotating at 15,000 rpm. The air supplied had a temperature of 180 to 190 ° C; the emerging air had a temperature of 75 to 80 ° C. The dried MMA / styrene copolymer had an average grain size of d ₅₀ = 14 μm.

The VZ of the spray-dried MMA / styrene copolymer was 97 cm ³ / g.

The spray dried MMA / styrene copolymer was the same as above described in a concentration of 0.1% by weight with the MMAIStyroI / N- Cyclohexylmaleinimide in a fluid bed dryer at room temperature 5 Minutes mixed.

510 kg of polymer beads were obtained with a viscosity number according to DIN 7745 of 101 cm ³ / g, a residual methylinethacrylate content of 0.47% by weight and an average grain diameter of 0.75 mm. The residual styrene content was below the detection limit of 0.05% by weight. The residual N-cyclohexylnialeinimide content was below the detection limit of 0.1% by weight. The results of the trickle tests according to DIN 53492 are summarized in Table 1 below.

Table 1

Flowability of the example according to DIN 53492

b.) Production of a synthetic thread

Polyethylene terephthalate chips with a water content of less than 35 ppm, the intrinsic viscosity of 0.64 dl / g and a melt viscosity (at 290 ° C) of 250 Pa.s were passed into the feed of an extruder. Perpendicular to Direction of conveyance of the extruder screw and centric to the extruder feed there was a downpipe through which the dried Elongation enhancer using a gravimetric type dosing system K2G from K-TRON AG / Switzerland in the catchment area above the Extruder screw to the polyester chips evenly and continuously was added.

The elongation enhancer was used in a concentration of 0.77% by weight, based on the total amount of the polymer mixture of polyester and Elongation enhancer, which is caused by the spinning system fed by the extruder was removed, added. The total amount taken off Polymer mixture was operated by the number of spinning pumps operated spinning system described below and by the throughput of the respective Spinning pump defined. When all the spinning pumps were in operation, a lot became of a total of 304.5 kg / h of polymer mixture removed from the spinning system and the stretching agent was applied at a rate of 2.34 kg / h dosed gravimetrically into the extruder feed.

The wave movement of the Extruder screw for premixing the additive beads with the Polyester chips. The polyester chips and the additive beads were in the Extruder, an LTM-24D / E8 spinning extruder from Barmag AG, Remscheidt / DE, melted and mixed together. This first polymer blend was at a temperature of 290 ° C with a pressure of 180 bar, as Melt flow of 304.5 kg / h transported through the melt line and one Filtration with a 20 µm filter candle.  

The filtered first polymer blend became a static mixer of the type SMX from Sulzer AG with an inner diameter of 52.5 mm and a length of 525 mm, there homogenized to a second polymer mixture and dispersed.

This second polymer mixture was brought up to twelve by means of the product line Spinning positions, each position containing six spin packs, distributed, the average residence time of the second polymer mixture from the exit from the static mixer was five minutes before entering the spin pack. each Spin pack contained a round nozzle with 34 holes with a diameter of 0.25 mm and the length of twice the diameter. The spin pack contained above the nozzle plate a spinning filter package, consisting of a steel sand pack from 30 mm high and a grain size of 0.5 to 0.85 mm, as well as a mesh of 40 µm and a steel fleece filter of 20 µm pore diameter. The The diameter of the spin filter pack was 85 mm. The residence time of the melt in the filter pack was about 1.5 minutes. The heating of the spin pack was set to 290 ° C. The surface of the spinneret was 30 mm above the limitation of the heating box. In the throughput of the melt mixture posed a nozzle pressure of 150 bar. The mean dwell time of the Polymer blend of polyester and elongation melt from Extruder exit to exit from the spin packs was approximately ten Minutes.

The molten filaments extruded from the die holes became by means of blowing air of one speed flowing horizontally to the thread course cooled from 0.55 m / s and a temperature of 18 ° C and at a distance of 1250 mm bundled from the nozzle plate in an oiling stone to the thread and coated with spin finish.  

An S-shaped pair of godets pulled the thread with one Speed of 5000 m / min, with a spinning delay ratio of 141 was set.

Between the godets there was a closed one with normal thread running Swirling nozzle installed with an air pressure of 4.5 bar the thread impressed a swirl knot number of 13 knots / m. The inlet tension in the inlet of the swirling nozzle was set to 0.16 g / den.

Six threads each of a spinning position were wound packages in a winder spooled, the spool speed of 4985 m / min chosen in this way was that the thread tension before winding was 0.1 g / den. There were receive pre-oriented (POY) threads, characterized by a titer of 126 den, an elongation at break of 116% and a tensile strength of 2.4 g / den.

During the seven-day production period, the breakage rate at Operation of the spinning system averaged 0.75 breaks per tonne Polymer mixture.

The POY coils obtained were processed using a FK6 texturing machine Barmag AG / Germany at a speed of 900 m / min drawtexturized. The draw ratio became 1.77 and the Heater temperatures 1 and 2 selected at 210 and 170 ° C, respectively. The breakage rate was an average of 21 breaks per ton of textured yarn. The textured yarn had a titer of 74 den, a tensile strength of 4.5 g / den, an elongation at break of 18.3% and was characterized by a good uniformity of staining.

Comparative example

The pourability of the aforementioned MMA / styrene / N- Cyclohexylmaleimide additive polymer with no additive added was also  determined according to DIN 53492. The results obtained are in Table 2 summarized.

Table 2

Flowability of the comparative example according to DIN 53492

A production of synthetic threads analogous to the example according to the invention failed because the additive polymer was used without a flow aid using a gravimetric dosing system type K2 G from K-TRON AG / Switzerland in Feed area above the extruder screw not to the polyester chips could be metered in evenly and continuously.

Claims (12)

1. Elongation-increasing agent for spinning processes comprising an additive polymer and a trickle aid, the additive polymer and the trickle aid in each case independently of one another

• 1. a.) A polymer obtained by polymerizing monomers of the general formula (I):
  is available, where R ¹ and R ^{2 are} substituents consisting of the optional atoms C, H, O, S, P and halogen atoms and the sum of the molecular weights of R ¹ and R ^{2 is} at least 40,
• 2. b.) A copolymer which contains the following monomer units:
  A = acrylic acid, methacrylic acid or CH ₂ = CR-COOR ', where R is an H atom or a CH ₃ group and R' is a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 - is aryl residue,
  B = styrene or C _1-3 alkyl-substituted styrenes,
  the copolymer consisting of 60 to 98% by weight of A and 2 to 40% by weight of B (total = 100% by weight),
• 3. c.) A copolymer which contains the following monomer units:
  C = styrene or C _1-3 alkyl-substituted styrenes,
  D = one or more monomers of the formula II, III or IV
  where R ³ , R ⁴ and P ^{5 are} each an H atom or a C _1-15 alkyl radical or a C _6-14 aryl radical or a C _5-12 cycloalkyl radical,
  wherein the copolymer consists of 15 to 95% by weight of C and 2 to 80% by weight of D, the sum of C and D together making up 100% by weight, or
• 4. d.) A copolymer which contains the following monomer units:
  E = acrylic acid, methacrylic acid or CH ₂ = CR-COOR ', where R is an H atom or a CH ₃ group and R' is a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 - is aryl residue,
  F = styrene or C _1-3 alkyl-substituted styrenes,
  G = one or more monomers of the formula II, III or IV
  where R ³ , R ⁴ and R ^{5 are} each an H atom or a C _1-15 alkyl radical or a C _5-12 cycloalkyl radical or a C _6-14 aryl radical,
  H = one or more ethylenically unsaturated monomers copolymerizable with E and / or with F and / or G from the group consisting of α-methylstyrene, vinyl acetate, acrylic acid esters, methacrylic acid esters other than E, acrylonitrile, acrylamide, methacrylamide, vinyl chloride, Vinylidene chloride, halogen-substituted styrenes, vinyl ethers, isopropenyl ethers and dienes,
  wherein the copolymer of 30 to 99 wt .-% E, 0 to 50 wt .-% F, 0 to 50 wt .-% G and 0 to 50 wt .-% H, the sum of E, F, G and H together gives 100% by weight,

are characterized in that the additive polymer have an average particle diameter of 0.1 to 1.0 mm and the flow aid have an average particle diameter of 0.1 to 100 µm. 2. Elongation-increasing means according to claim 1, characterized in that that it is 99.95 to 95.0% by weight additive polymer and 0.05 to 5.0% by weight  Trickle aid, each based on the total weight of the Stretching agent. 3. Elongation increasing means according to claim 1 and / or 2, characterized characterized in that the flow aid and the additive polymer too at least 50% by weight, expediently at least 60% by weight, preferably at least 70% by weight, in particular at least 80 wt .-%, each based on the total weight of the trickle aid or Additive polymers that have the same repeat units. 4. Elongation increasing means according to at least one of the preceding Claims, characterized in that the trickle aid and the additive Polymer at least 90% by weight, preferably at least 95% by weight, in particular at least 97% by weight, based in each case on the Total weight of the flow aid or the additive polymer, the same Have repeating units. 5. Elongation increasing means according to at least one of the preceding Claims, characterized in that the trickle aid and the additive Completely agree polymer in their composition. 6. Elongation increasing means according to at least one of the preceding Claims, characterized in that the weight average of Molecular weight of the trickle aid by less than 50%, expediently by less than 30%, in particular by less than 20% deviates from that of the additive polymer. 7. Process for the production of synthetic threads from a fiber-forming matrix polymer-based melt mixture, characterized in that the fiber-forming matrix polymer at least one elongation enhancer according to at least one of the  preceding claims in an amount of 0.05 to 5 wt .-%, based on the total weight of fiber-forming matrix polymer this stretching agent. 8. The method according to claim 7, characterized in that the Spinning take-off speed set to at least 3000 m / min. 9. Synthetic thread obtainable by a method according to claim 7 and / or 8. 10. Further processing of the synthetic thread according to claim 9 in one Stretching or stretch texturing process. 11. Use of the synthetic thread according to claim 9 for the production of staple fibers. 12. Use of the synthetic thread according to claim 9 as a technical Yarn.