EP1356143B1 - Method for spinning and winding pet filaments - Google Patents

Abstract

The present invention relates to a process for producing and winding POY filaments not less than 90% by weight PET, based on the total weight of the POY, at spinning takeoff speeds above 3 800 m/min, which comprises a) setting the spinline extension ratio in the range from 50 to 250, b) passing the filaments directly upon exit from the spinneret through a quench delay zone 20 mm to 300 mm in length, c) quenching the filaments to below the solidification temperature, d) converging the filaments at a distance between 500 mm and 2 500 mm from the underface of the spinneret, e) using at least one oiler pin per yarn to add spin finish to a standard deviation of less than 90 digits for the finish application variation, f) using oiler pins and yarn converging and yarn guiding elements that have low-friction surfaces, g) setting the yarn tension above the takeoff godets between 0.07 cN/dtex and 0.5 cN/dtex, h) entangling the yarn at a yarn tension between 0.05 cN/dtex and 0.20 cN/dtex and air pressure between 1.0 bar and 5.5 bar to a node count of at least 10 n/m with a coefficient of variation of less than 100%, i) winding the yarn at a yarn tension between 0.03 cN/dtex and 0.20 cN/dtex by driving the contact roll of the winder at an at least 0.3% higher frequency than the winding chuck and varying the angle of wind between a minimum of 3.5° and a maximum of 7.5° over the winding time.

Description

The present invention relates to methods for spinning and winding of preoriented, non-crystalline filaments containing at least 90% by weight based on the total weight of the polyethylene terephthalate filament (PET).

Usually, preoriented, non-crystalline PET filaments are also used referred to as POY, depending on the titre to be produced at take-off speeds produced from 2500 to 3500 m / min. Such filaments have elongation at break values of 90 - 165%, which are advantageous for the Be further processing in a stretch or draw texturing process have proven. In the mentioned speed range, no crystallization in the PET filaments are produced, such as Fig. 2 from man-made fibers / textile industry, January 1980, page 27 can be found.

However, if one attempts as in the production of spinning-oriented, crystalline PET filaments, which are also known as FOY or HOY, the Further increase takeoff speed, then be due to the lower thermal and mechanical stability of the POY yarns higher fractions, uneven characteristics and / or errors in further processing, especially observed in stretch texturing.

First approaches to solving these problems are in the patent applications WO 99/51799, WO 99/07927 and WO 93/19229. WO 99/51799 discloses a method for spinning continuous filaments in which the freshly spun filaments by means of an accelerated refrigerant gas in one Tube to be cooled. By such a procedure, a Increasing the spinning take-off speed up to 4530 m / min, without reducing the elongation at break of the filaments. Information regarding the Fractions can not be found in the publication.

WO 99/07927 relates to a process for the preparation of Preoriented filaments of polyester-based polymer blends. In the Presence of a certain amount of an additive copolymer is also included high spin-off speeds up to 6000 m / min PET filaments with obtained high elongation at break values. Information regarding the fractions can not be taken from this document.

In contrast, WO 93/19229 describes a method for spinning and Cooling of continuous filaments by means of a spinning device with nozzle plates containing spinning heads and Abkühlschächten with air-permeable wall, through which a stream of air is sucked into the interior of the Abkühlschächte. there become even with a small number of spinning breaks uniform PET filaments produced. However, at high speeds from 4200 to 5700 m / min significantly lower elongation at break of 85 to 54%. such Values are characteristic of spin-oriented, crystalline filaments.

infolge von mechanischer und/oder thermischer Fadenbeschädigung werden fehlerhafte Filamente erhalten;

• die Effizienz der Verfahren wird durch Schlaufenbildungen und Fadenbrüche deutlich reduziert;
• weiterhin wird eine Sattelbildung auf dem Spulkörper und Fadenabschläger, d. h. ein Herunterrutschen von Einzel- oder Gesamtfilamenten von der Spulkörperkante, beobachtet.

Although these processes enable spinning and winding of preoriented, non-crystalline filaments at high spin-off speeds, they are still in need of improvement in the production of POY. Disadvantages include the following points:

as a result of mechanical and / or thermal thread damage, defective filaments are obtained;

• the efficiency of the process is significantly reduced by looping and yarn breaks;
• Furthermore, a saddle formation on the bobbin and Fadenabschläger, ie a slipping of single or total filaments of the Spulkörperkante observed.

In view of the prior art, it was now the task of the present Invention, a method for spinning and winding of pre-oriented, not crystalline filaments which are at least 90 wt .-% based on the Total weight of the filament made of PET, to provide which does not manufacture and wind up the pre-oriented crystalline PET filaments at high spinning speeds with low number of errors allows. In particular, the pre-oriented should not crystalline PET filaments yield values in the range of 90% - 165% and a high uniformity with respect to the filament characteristics and the Have preparation order.

Another object of the present invention was a method for spinning and winding preoriented, non-crystalline PET filaments indicate that is industrially and inexpensively feasible. The inventive method should be as high as possible Spin-off speeds, preferably greater than 3800 m / min, in particular in the range of 4200 to 8000 m / min, with the lowest possible Spinning error rate allow. Furthermore, a good coil design should be adjustable be high yarn weights on the bobbin of more than 4 kg and a to allow good coil drainage behavior in further processing.

An object of the present invention was also to be seen in that the obtainable by the process according to the invention POYs with a very good staining and processing level with the lowest possible Material error rate Allow stretching or stretch texturing.

These are solved as well as other tasks that are not explicitly mentioned however, from the contexts discussed hereinbefore without further ado derivable or developable by a method of spinning and Winding with all features of claim 1. Expedient Modifications of the method according to the invention are in the on claim 1 backed dependent claims under protection.

a) der Spinnverzug im Bereich von 50 bis 250 eingestellt wird,

b) die Filamente direkt nach Austritt aus der Spinndüse eine Abkühlungsverzögerungszone von 20 mm bis 300 mm Länge durchlaufen,

c) die Filamente unter die Erstarrungstemperatur abgekühlt werden,

d) die Filamente in einem Abstand zwischen 500 mm und 2500 mm von der Düsenunterseite gebündelt werden,

e) Spinnpräparation mittels mindestens einem Ölerstift pro Faden mit einer Präparationsauftragsschwankung der Standardabweichung von weniger als 90 Digits zudosiert wird,

f) mit reibungsarmen Oberflächen ausgeführte Ölerstifte, Fadenbündelungs-und Fadenführungselemente einsetzt werden,

g) die Fadenspannung vor den Abzugsgaletten zwischen 0,07 cN/dtex und 0,5 cN/dtex eingestellt wird,

h) der Faden mit einer Fadenspannung zwischen 0,05 cN/dtex und 0,20 cN/dtex und einem Luftdruck zwischen 1,0 bar und 5,5 bar verwirbelt wird, wobei eine Knotenanzahl von mindestens 10 n/m bei einem Variationskoeffizienten der Knotenanzahl unterhalb von 100 % eingestellt wird,

i) der Faden mit einer Fadenspannung zwischen 0,03 cN/dtex und 0,20 cN/dtex aufgespult wird, wobei der Antrieb der Tastwalze des Wicklers mit einer von mindestens 0,3 % höheren Frequenz als der Antrieb des Spuldorns angesteuert wird und der Fadenverlegewinkel über die Spulenlaufzeit zwischen minimal 3,5° und maximal 7,5° variiert wird,

gelingt es auf nicht ohne weiteres vorhersehbare Weise, vororientierte, nicht kristalline PET-Filamente bei hoher Spinnabzugsgeschwindigkeit mit geringer Bruchzahl herzustellen und aufzuspulen. Dabei weisen die vororientierten, nicht kristallinen PET-Filamente Reißdehnungswerte im Bereich von 90 % - 165 % und eine hohe Gleichmäßigkeit bezüglich der Filament-Kennwerte und des Präparationsauftrages auf.By providing a process for the production and winding of preoriented, non-crystalline PET filaments with spin-off speeds greater than 3800 m / min, which is characterized in that

a) the spinning delay is set in the range from 50 to 250,

b) the filaments go through a cooling delay zone of 20 mm to 300 mm length directly after leaving the spinneret,

c) the filaments are cooled below the solidification temperature,

d) the filaments are bundled at a distance of between 500 mm and 2500 mm from the nozzle base,

e) dope preparation is metered in by means of at least one oiler stick per thread with a sample application variation of the standard deviation of less than 90 digits,

f) Ölerstifte executed with low-friction surfaces, thread bundling and thread guide elements are used,

g) the thread tension in front of the take-off godets is set between 0.07 cN / dtex and 0.5 cN / dtex,

h) the yarn is intermingled with a yarn tension between 0.05 cN / dtex and 0.20 cN / dtex and an air pressure between 1.0 bar and 5.5 bar, with a number of knots of at least 10 n / m with a coefficient of variation of Number of nodes is set below 100%,

i) the thread is wound with a thread tension between 0.03 cN / dtex and 0.20 cN / dtex, wherein the drive of the contact roller of the winder is driven with a frequency of at least 0.3% higher than the drive of the spool and the Thread laying angle is varied over the coil running time between a minimum of 3.5 ° and a maximum of 7.5 °,

succeeds in not easily predictable way to produce pre-oriented, non-crystalline PET filaments at high spinning deduction speed with a small fraction and spool. In this case, the preoriented, non-crystalline PET filaments have elongation at break values in the range of 90% to 165% and a high degree of uniformity with regard to the filament characteristics and the preparation application.

⇒ Das erfindungsgemäße Verfahren ist auf einfache Art und Weise, großtechnisch und kostengünstig durchführbar. Insbesondere erlaubt das Verfahren das Spinnen und Aufspulen bei hohen Abzugsgeschwindigkeiten von größer 3800 m/min, insbesondere zwischen 4200 und 8000 m/min, und die Herstellung hoher Fadengewichte auf dem Spulkörper von mehr als 4 kg.

⇒ Die durch das Verfahren erhältlichen Spulkörper von vororientierten, nicht kristallinen PET-Filamente können somit auf einfache Art und Weise, mit geringsten Ablaufmängeln in einem Streck- bzw. einem Strecktexturierprozeß weiterverarbeitet werden.

⇒ Aufgrund der hohen Gleichmäßigkeit der durch das Verfahren erhältlichen vororientierten, nicht kristallinen Filamente wird eine gleichmäßige und nahezu fehlerfreie Anfärbung und Weiterverarbeitung des vororientierten Polyester-Filaments ermöglicht.

At the same time, the inventive method has a number of other advantages. These include:

⇒ The method according to the invention can be carried out in a simple manner, on an industrial scale and at low cost. In particular, the method allows spinning and winding at high take-off speeds of greater than 3800 m / min, in particular between 4200 and 8000 m / min, and the production of high thread weights on the bobbin of more than 4 kg.

⇒ The bobbins of preoriented, non-crystalline PET filaments obtainable by the process can thus be further processed in a simple manner with the least amount of run-off defects in a stretch or draw texturing process.

⇒ Due to the high degree of uniformity of the pre-oriented, non-crystalline filaments obtainable by the process, a uniform and virtually error-free dyeing and further processing of the preoriented polyester filament is made possible.

The present invention relates to a process for the production and for winding preoriented, noncrystalline filaments that are too at least 90 wt .-% based on the total weight of the filament Polyethylene terephthalate (PET) consist, for example, by Polycondensation in a known manner from terephthalic acid and Ethylene glycol is available.

The polyethylene terephthalate can be both a homo- and a copolymer be. Suitable copolymers are in particular those in addition to the above mentioned recurring units still up to 15 mol% based on all repeat units of the PET repeat units are more common Comonomers, such as. B. 1,3-propanediol, 1,4-butanediol, diethylene glycol, Triethylene glycol, 1,4-cyclohexanedimethanol, polyethylene glycol, isophthalic acid and / or adipic acid. In the context of the present invention however, PET homopolymers are preferred.

Furthermore, the PET can also be a small proportion, preferably up to 0.5 Wt .-% based on the total weight of the filament, on Branching components. To the inventively preferred Branching components include polyfunctional acids, such as Trimellitic acid, pyromellitic acid, or tri- to hexavalent alcohols, such as Trimethylolpropane, pentaerythritol, dipentaerythritol, glycerol, or the like Hydroxy acids.

1. Ein Copolymer, welches folgende Monomereinheiten enthält:

A = Acrylsäure, Methacrylsäure oder CH₂ = CR - COOR', wobei R ein H-Atom oder eine CH₃-Gruppe und R' ein C_1-15-Alkylrest oder ein C_5-12-Cycloalkylrest oder ein C_6-14-Arylrest ist,

B = Styrol oder C_1-3-alkylsubstituierte Styrole,

wobei das Copolymer aus 60 bis 98 Gew.-% A und 2 bis 40 Gew.-% B, vorzugsweise aus 83 bis 98 Gew.-% A und 2 bis 17 Gew.-% B, und besonders bevorzugt aus 90 bis 98 Gew. -% A und 2 bis 10 Gew.-% B (Summe = 100 Gew.-%) besteht.

2. Ein Copolymer, welches folgende Monomereinheiten enthält:

C = Styrol oder C_1-3-alkylsubstituierte Styrole,

D = eines oder mehrere Monomere der Formel I, II oder III

wobei R¹, R² und R³ jeweils ein H-Atom oder ein C_1-15-Alkylrest oder ein C_6-14-Arylrest oder ein C _5-12-Cycloalkylrest sind,

wobei das Copolymer aus 15 bis 95 Gew.-% C und 2 bis 80 Gew.-% D, vorzugsweise aus 50 bis 90 Gew.-% C und 10 bis 50 Gew.-% D und besonders bevorzugt aus 70 bis 85 -% C und 15 bis 30 Gew.-% D besteht, wobei die Summe aus C und D zusammen 100 Gew.-% ergibt.

3. Ein Copolymer, welches folgende Monomereinheiten enthält:

E = Acrylsäure, Methacrylsäure oder CH₂ = CR - COOR', wobei R ein H-Atom oder eine CH₃-Gruppe und R' ein C_1-15-Alkylrest oder ein C_5-12Cycloalkylrest oder ein C_6-14-Arylrest ist,

F = Styrol oder C_1-3-alkylsubstitutierte Styrole,

G = eines oder mehrere Monomere der Formel I, II oder III

wobei R¹, R² und R³ jeweils ein H-Atom oder ein C_1-15-Alkylrest oder ein C_5-12-Cycloalkylrest oder ein C_6-14-Arylrest sind,

H = eines oder mehrerer etyhlenisch ungesättigter mit E und/oder mit F und/oder G copolymerisierbarer Monomerer aus der Gruppe, welche aus α-Methylstyrol, Vinylacetat, Acrylsäureestern, Methacrylsäureestern, die von E verschieden sind, Vinylchlorid, Vinylidenchlorid, halogensubstituierten Styrolen, Vinylethern, Isopropenylethern und Dienen besteht,

wobei das Copolymer aus 30 bis 99 Gew.-% E, 0 bis 50 Gew.-% F, >0 bis 50 Gew.-% G und 0 bis 50 Gew.-% H, vorzugsweise aus 45 bis 97 Gew.-% E, 0 bis 30 Gew.-% F, 3 bis 40 Gew.-% G und 0 bis 30 Gew.-% H und besonders bevorzugt aus 60 bis 94 Gew.-% E, 0 bis 20 Gew.-% F, 6 bis 30 Gew.-% G und 0 bis 20 Gew.-% H besteht, wobei die Summe aus E, F, G und H zusammen 100 Gew.-% ergibt.

4. Ein Polymer aus folgender Monomereinheit:

   wobei R¹ und R² Substituenten bestehend aus den optionalen Atomen C, H, O, S, P und Halogenatomen sind und die Summe des Molekulargewichts von R¹ und R² mindestens 40 beträgt. Beipielhafte Monomereinheiten umfassen Acrylsäure, Methacrylsäure, und CH₂ = CR - COOR', wobei R ein H-Atom oder eine CH₃-Gruppe und R' ein C_1-15-Alkylrest oder ein C_5-12-Cycloalkylrest oder ein C_6-14-Arylrest ist, sowie Styrol und C_1-3-alkylsubstituierte Styrole.

In addition, in the context of the present invention, it may be expedient to add up to 2.5% by weight, based on the total weight of the filament, of additive polymer to the PET as strain-increasing agent. Particularly suitable additive polymers according to the invention include the following polymers and / or copolymers:

1. A copolymer containing 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 radical is,

B = styrene or C _1-3 alkyl-substituted styrenes,

wherein the copolymer of 60 to 98 wt .-% A and 2 to 40 wt .-% B, preferably from 83 to 98 wt .-% A and 2 to 17 wt .-% B, and particularly preferably from 90 to 98 wt % A and 2 to 10% by weight B (total = 100% by weight).

2. A copolymer containing the following monomer units:

C = styrene or C _1-3 alkyl-substituted styrenes,

D = one or more monomers of the formula I, II or III

wherein R ¹ , R ² and R ^{3 are} each H or C _1-15 alkyl or C _6-14 aryl or C _5-12 cycloalkyl,

wherein the copolymer consists of 15 to 95% by weight C and 2 to 80% by weight D, preferably from 50 to 90% by weight C and 10 to 50% by weight D and particularly preferably from 70 to 85% C and 15 to 30 wt .-% D, wherein the sum of C and D together gives 100 wt .-%.

3. A copolymer containing 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 radical is,

F = styrene or C _1-3 alkyl-substituted styrenes,

G = one or more monomers of the formula I, II or III

where R ¹ , R ² and R ^{3 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 esters, methacrylates other than E, 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, preferably from 45 to 97 wt .-% E, 0 to 30 wt .-% F, 3 to 40 wt .-% G and 0 to 30 wt .-% H and particularly preferably from 60 to 94 wt .-% E, 0 to 20 wt .-% F, 6 to 30 wt .-% G and 0 to 20 wt .-% H, wherein the sum of E, F, G and H together gives 100 wt .-%.

4. A polymer of the following monomer unit:

wherein 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 weight of R ¹ and R ^{2 is} at least 40. Exemplary monomer units include acrylic acid, methacrylic acid, and CH ₂ = CR - COOR 'where R is H or CH ₃ and R' is C _1-15 alkyl or C _5-12 cycloalkyl or C _{6 -14} -aryl, as well as styrene and C _1-3 alkyl-substituted styrenes.

Details of the preparation of these substances and mixing the Additive polymers with the PET are disclosed in WO 99/07 927 described. In addition, with respect to the metered addition and dispersion of the additive in PET to the document DE 100 22 889.5.

In the context of the present invention, additive polymers and / or Copolymers which are amorphous and insoluble in the polyester matrix are preferred. Preferably, they have a glass transition temperature of 90 to 200 ° C, wherein the glass transition temperature in a known manner, preferably by Differential scanning calorimetry is determined. More details can Prior art, for example, the document WO 99/07927 taken are, the disclosure of which is hereby incorporated by reference.

According to the invention, the additive polymer and / or copolymer is such selected that the ratio of the melt viscosities of the additive polymer and / or copolymer and the matrix polymer 0.8: 1 to 10: 1, preferably 1.5: 1 to 8: 1. The melt viscosity is in a known manner by means of Oscillation Rheometer at an oscillation frequency of 2.4 Hz and a Temperature equal to the melting temperature of the matrix polymer plus 34 ° C is, measured. For polyethylene terephthalate, the measuring temperature for the Melt viscosity at 290 ° C. Further details can turn the Publication WO 99/07927 be removed. The melt viscosity of the Additive polymer and / or copolymer is preferably higher than that of Matrix polymer, and it has been found that the choice of a specific Viscosity range for the additive polymer and / or copolymer and the choice the viscosity ratio to optimize the properties of the produced Thread contributes. At an optimized viscosity ratio is a minimization the amount of the additive additive polymer and / or copolymer is possible, which, among other things, improves the economic efficiency of the process becomes. The polymer mixture to be spun preferably contains 0.05 to 2.5 % By weight of additive polymer and / or copolymer.

By choosing the favorable viscosity ratio to achieve a close Distribution of particle sizes of the additive polymer and / or copolymer in the Polymer matrix with the desired fibril structure of the additive polymer and / or copolymer in the thread. The high compared to the matrix polymer Glass transition temperature of the additive polymer and / or copolymer provides a rapid solidification of this fibril structure in the filament safely. The maximum particle sizes of the additive polymer and / or copolymer immediately after exiting the spinneret at about 1000 nm, while the average particle size is 400 nm or less. After the spinning delay of the Thread reaches the favorable Fibrillenstruktur, in which the threads at least 60% by weight of the additive polymer and / or copolymer in the form of fibrils with lengths in the range of 0.5 to 20 microns and diameters in the range of 0.01 to 0.5 microns included.

The polyethylene terephthalate according to the invention may contain conventional amounts, preferably 0 to 5 wt .-%, preferably 0 to 1 wt .-%, each based on the total weight of the filament of further additives as admixtures, such as catalysts, stabilizers, antistatic agents, antioxidants, Flame retardants, dyes, dye-uptake modifiers, Light stabilizers, organic phosphites, optical brighteners and Matting agents included.

The PET is inventively with a take-off speed greater than 3800th m / min, suitably at least 4200 m / min, preferably greater than 4600 m / min, in particular at least 6000 m / min, more preferably greater 6000 m / min, spun into preoriented non-crystalline filaments and wound. A very particular in the context of the present invention preferred range is between 4200 and 8000 m / min, in particular between 4600 and 6000 m / min.

For the purposes of the present invention, preoriented, non-crystalline Filaments such filaments having an elongation at break between 90 and 165%, exhibit.

It may be expedient for the inventive method, a spinning-cooling device to use when stress-induced crystallization at high spinning take-off speeds is reduced. In a special preferred embodiment of the present invention is a spinning-cooling device can be used, as in the publication WO 99/51799 is described. On the disclosure of this document is in this Context explicitly referred to.

The usable within the meaning of the invention PET preferably has a intrinsic viscosity (intrinsic viscosity) in the range of 0.55 dl / g to 0.75 dl / g.

In the method according to the invention is a melt of the PET means Spinning pumps at constant speed, the speed according to known Calculating profile is set so that the desired yarn titer is obtained, pressed into nozzle packages and through the nozzle holes of the nozzle plate of the package extruded into molten filaments.

The melt can, for example, in an extruder of polymer chips It is necessary to prepare the chips beforehand Water content ≤ 100 ppm, in particular to a water content ≤ 50 ppm dry. The direct feed of the PET melt from the final reactor of a Polycondensation plant in the spinning is preferred.

T_m:

Schmelzpunkt von PET, ca. 260°C

T_Sp:

Spinntemperatur [°C].

The temperature of the melt, commonly referred to as the spinning temperature and measured in front of the spin pump, depends on the melting point of the PET. It is preferably in the range given by formula 1: Formula 1: T m + 19 ° C ≤ T sp ≤ T m + 49 ° C With

T _m:

Melting point of PET, approx. 260 ° C

T _Sp :

Spinning temperature [° C].

The homogeneity of the melt has a direct influence on the Material properties of the spun filaments. Preferably used Therefore, a static mixer with at least two elements, the before and / or after the spin pump is installed, for homogenizing the Melt. By way of example, a spinning pump of the type Promix the company Barmag / D with integrated mixer can be used.

The temperature dependent on the spinning temperature of the nozzle plate is through regulated their so-called heat tracing. Come as a heat For example, a "Diphyl" heated spinning beam or additional Convection, induction or radiant heater in question. Usually lies the temperature of the nozzle plates at the level of the spinning temperature.

An increase in temperature at the nozzle plate can be due to the pressure gradient in the Nozzle package can be achieved. Known derivatives, such as K. Riggert "Progress in the production of polyester tire cord yarn" Chemiefasern 21, page 379 (1971), describe a temperature increase of about 4 ° C per 100 bar pressure drop.

Furthermore, it is possible to increase the nozzle pressure by using loose filter media, in particular of steel sand with a mean grain size between 0.10 mm and 1.2 mm, preferably between 0.12 mm and 0.75 mm and / or filter blanks, made of metal fabrics or non-wovens with a fineness ≤ 40 μm, preferably 5 to 20 microns, can be made to control.

In addition, the pressure drop in the nozzle hole contributes to the total pressure. Of the Nozzle pressure is preferably between 80 bar and 450 bar, in particular set between 100 bar and 250 bar, the latter an increase in the Melting temperature immediately before the extrusion of 4 - 10 ° C corresponds.

δ:

Dichte der Schmelze [g/cm³]; für PET = 1,22 g/cm³

D:

Düsenlochdurchmesser [cm]

dpf:

Titer des Einzelfilamentes [den]

The spinning distortion i _Sp , ie the quotient of take-off speed and injection speed, is calculated according to US Pat. No. 5,250,245 via formula 2 with the density of the PET, the nozzle hole diameter and the titer of the single filament: Formula 2: i sp = 2.25 • 105 • (δ • π) • D 2 (Cm) / dpf (denier) With

δ:

Density of the melt [g / cm ³ ]; for PET = 1.22 g / cm ³

D:

Nozzle hole diameter [cm]

dpf:

Titre of the individual filament

In the context of the present invention, the spinning delay is between 50 and 250, preferably between 70 and 170.

The length / diameter ratio of the nozzle hole is preferably chosen between 1.5 and 6, in particular between 1.5 and 4.

The extruded filaments pass through a cooling delay zone. Directly below the nozzle package this is formed as a return zone, in the emerging from the nozzle holes filaments before the direct Influence of the cooling gas to be preserved and in default or cooling be delayed. An active part of the return is considered offset of the Nozzle package executed in the spinning beam inside, so that the filaments of surrounded by heated walls. A passive part is going through Insulation layers and unheated frames formed. The lengths of the active Recesses are between 0 to 300 mm, those of the passive part between 20 to 150 mm, with a total length of 20 - 300 mm is maintained.

As an alternative to the active recess may be below the spinner Be installed reheater. In contrast to the active return points then this zone of cylindrical or rectangular cross section at least a heating independent of the spinning beam.

For radial, concentric surrounding the thread porous cooling systems, Can the cooling delay with the help of cylindrical covers be achieved.

Subsequently, the filaments are at temperatures below their Solidification temperature cooled. According to the invention denotes the Solidification temperature is the temperature at which the melt in the solid State of aggregation passes.

Means for cooling the filaments are those skilled in the art from the Technique known. The use has proven particularly useful according to the invention of cooling gases, in particular cooled air. The cooling air points preferably a temperature of 12 ° C to 35 ° C, especially 16 ° C to 26 ° C. on. The speed of the cooling air is advantageously in the range of 0.20 m / sec to 0.55 m / sec.

For example, monofilament systems can be used to cool the filaments used, consisting of individual cooling tubes with perforated wall consist. Through active cooling air supply or by using the Selbstansaugungseffekts from the filaments and / or by suction of the Cooling air is achieved a cooling of each filament. alternative to the individual pipes are also the known Querstromanblasungssysteme used.

A special embodiment of the cooling and drafting area exists therein, the filaments emerging from the retarding zone in a zone of the Length in the range of 10 to 175 cm, preferably in a zone of length in Range of 10 - 80 cm to supply cooling air. It is for filaments with a Titer when winding ≤ 1.5 dtex per filament a zone length in the range of 10-40 cm and for filaments with a titer between 1.5 and 9.0 dtex per Filament a zone length in the range of 20 - 80 cm particularly suitable.

Afterwards, the filaments and their accompanying air pass through passed a cross-section reduced channel together, wherein by the Control of cross-sectional taper and sizing in Thread direction a ratio of the air speed to the thread speed Stripping from 0.2 to 20: 1, preferably 0.4 to 5: 1, is set.

After cooling the filaments to temperatures below the Solidification temperature, they are bundled into a thread. Of the According to the invention suitable distance of the bundling of the nozzle bottom can by methods known to those skilled in the online measurement of the Thread speed and / or thread temperature, for example with a Laser Doppler anemometer from TSI / D or an infrared camera of the company Manufacturer Goratec / D type IRRIS 160, to be determined. He is 500 to 2500 mm. In this case, single filaments with a spin titer ≤ 4.5 dtex preferably at a smaller distance ≤ 1500 mm, thicker filaments preferably bundled at a greater distance.

In the context of the present invention, it is expedient that preferably all surfaces that come into contact with the spun filament out particularly low-friction materials are made. In this way linting can be largely avoided, it will be obtained higher quality filaments. As especially suitable for this purpose have low friction surfaces of the specification "TriboFil" of the Company Ceramtec / D proven.

The bundling of the filaments takes place in a Ölerstift, the thread the the desired amount of spin finish uniformly. A special suitable Ölerstift is characterized by an inlet part, the thread channel with oil inlet opening and the outlet part. The inlet part is funnel-shaped extended so that contact with the still-dry filaments avoided becomes. The impact point of the filaments takes place within the thread channel the inflow of the preparation. Thread channel and oil inlet opening are in the Width adapted to the thread titer and the number of filaments. Particularly well proven have openings and widths in the range of 1.0 mm to 4.0 mm. Of the Outlet part of Ölerstiftes is designed as a homogenization distance, the preferably has oil reservoirs. For example, suitable oiler pens from the company Ceramtec / D, type TriboFil, from the company Goulston / USA, type LuroJet, from the company Kyocera / J, type SF, and from the company Rauschert / D, Type PN can be obtained.

The uniformity of the oil application is according to the invention of great importance. It can, for example, with a Rossa meter according to the in Chemical fibers / textile industry, 42./94, Nov. 1992 on page 896 described Method to be determined. The amount of oil application amount and their Fluctuation is given in relative units called digits. in the Within the scope of the present invention, in such Procedure Values for the standard deviation of the oil application of less obtained as 90 digits, in particular less than 60 digits. Values for the invention are particularly preferred Standard deviation of the oil application of less than 45 digits, in particular of less than 30 digits. A value for the standard deviation corresponds to this of 45 digits, about 3.1% of the coefficient of variation.

In the context of the present invention, it has proven to be particularly advantageous proved, preparation lines and pumps to avoid gas bubbles self-degassing interpret, as this to a considerable oil application fluctuation being able to lead. It is in a very particularly preferred Embodiment of the present invention, a preparation pump of the type Profin of the company Barmag / D used.

According to the invention, the filaments are vortexed before being wound up. there conventional systems have proved to be of little use because of due to the high speed and thus the increased air pressure a considerable loop and fluff formation is observed. Furthermore they require high winding voltages, which make the coil assembly negative affect and saddle formation, slipping and Fadenabschlägern on lead the bobbin.

In the context of the present invention, these disadvantages advantageously by using nozzles with closed Gamkanälen avoided, since in such systems entanglements of the thread in the insertion slot even at low yarn tension and high air pressure can be avoided. The Entangling nozzles are preferably arranged between godets, wherein the Outlet yarn tension by means of different speed of the inlet and Outlet Galette is regulated. It should not exceed 0.20 cN / dtex and priority should be the infeed tension values between 0.05 cN / dtex and 0.18 cN / dtex. The air pressure of Entanglingluft is here between 1.0 and 5.5 bar.

Node numbers of at least 10 n / m are set. There are maximum opening lengths less than 100 cm and values for the Coefficients of variation of the number of nodes below 100% of particular Interest. Advantageously, when using air pressures ≥ 3.0 bar Node numbers ≥ 15 n / m achieved by a high uniformity characterized in that the coefficient of variation is less than or equal to 70% and the maximum opening length is 50 cm.

In practice, LD type systems from Temco / D, the Double system of the company Slack & Parr / USA, or nozzles of the type Polyjet of the Company Heberlein proved to be particularly suitable.

Particularly positive effects on lint reduction are achieved when before the actual Entangling a migration nozzle is applied. at Air pressures of less than 1 bar will further homogenize the applied spin finish or a mixing of individual filaments reached. These nozzles are used before the first take-off godet, preferably directly after the oil pen.

The peripheral speed of the first godet unit is called Discharge speed called. Other godet systems can be applied before the thread in the winding unit to Spulkörpem (Coils) is wound on sleeves.

Stable, error-free bobbins are a prerequisite for error-free Peel off the thread and for a flawless further processing. Therefore, in the context of the present method, a winding tension in Range of 0.03 cN / dtex - 0.20 cN / dtex, preferably in the range of 0.05 cN / dtex - 0.15 cN / dtex.

Preferably, the winder with a Flügelradchangierung to Thread laying and driven feeler roller for controlling the speed of the in turn driven Spuldorns on which the winding tube is attached, Mistake. To avoid Fadenabschlägern it is advantageous to the drive the touch roller with at least 0.3% higher frequency than the drive of To head for Spuldorns.

Furthermore, it is extremely useful by a Spiegelstörverfahren, the Laying angle in increments of at least 1 ° to vary to slipping To avoid thread layers especially in mirror areas. A variation of the Installation angle over the coil travel between 3.5 ° and 7.5 ° According to the invention for stabilizing the coil structure particularly preferred. It is considered perpendicular to the bobbin tube, the angle between the Thread running direction on the bobbin and the perpendicular to the bobbin as Designation angle called.

With the help of Entangling- and Wicklerbedingungen invention Stable winding produced.

An important parameter of the method according to the invention is the adjustment the thread tension before the withdrawal godets. As is well known, this is Voltage essentially from the actual orientation voltage Hamana, the friction tension on the thread guides and the oil pen and the Thread-air friction tension together. In the context of the present Invention, the yarn tension in front of the godets is in the range of 0.07 cN / dtex to 0.50 cN / dtex, preferably between 0, 07 cN / dtex and 0.20 cN / dtex.

Too low a tension below 0.07 cN / dtex does not yield the desired level of preorientation. If the stress exceeds 0.50 cN / dtex, So thread damage occurs by frictional heat, the Lead to deterioration of the thread characteristics.

According to the invention, the tension is determined by the spinning take-off speed, the oil pen distance from the nozzle, the friction surfaces and the length of the The distance between the oil pen and the departure godet is regulated. This track length is advantageously not more than 6.0 m, preferably less than 2.5 m, the spinning and the extraction machine by parallel design such are arranged that a straight line run is guaranteed.

For adjusting the winding tension according to the invention, the Winding speed of the POYs advantageously 0 - 2% below the Off speed. Preferably, a winding speed that is 0 - 1% below the spinning take-off speed is selected.

Advantageously, during the implementation of the inventive Method in the vicinity of the winding machine a temperature ≤ 35 ° C, especially between 12 and 28 ° C, and a relative humidity between 40 - 90% set. Furthermore, it is expedient the POY coils at least 4 Hours at 12 to 28 ° C and a relative humidity between 40 - 90% store the further processing.

Method for determining the specified material parameters are the Professional well known. You can use the specialized literature, for example the Publication WO 99/07927, the disclosure of which is hereby incorporated by reference is taken.

The characteristics of the Verwitbelns be with a node counter of the type ITEMAT from Enka-Technica / D at a speed of 100 m / min and a set level no. 1 determined.

For online fluff detection when spinning a Fraytec device of the company ENKA Tecnica / D used. The lint detection sensor must have a direct Trigger downstream video camera whose image is saved and so on makes possible errors evaluable and classifiable. Incorrect measurements, e.g. through oil droplets or vibrations can be done by such an approach be avoided. The evaluation allows in particular, texturierrelevante To determine errors. These filament tufts looking like mistakes made by Postponement of fractures could be caused by application of the inventive method to 0 per hour at a Spin deduction speed of 5000 m / min can be reduced.

The invention will be explained in more detail by way of example, without that the invention should be limited to this example.

A melt of polyethylene terephthalate was from a reactor with a intrinsic viscosity of 0.64 dl / g according to a melt viscosity 290 ° C of 250 Pas and a temperature of 282 ° C discharged and by means of a pressure booster pump with a pressure of 205 bar and a quantity of 302.4 kg / h conveyed through the melt line. The melt flowed through Filter with 20 micron fineness and a heat exchanger, the melt temperature cooled from 292 ° C to the spinning temperature of 290 ° C.

This filtered partial stream 1 of the amount 302.4 kg / h was in the second Partial flow of the amount 13.98 kg / h, corresponding to 4.62 wt .-% of the first Stream, and the third part of the flow split 288.42 kg / h and branched.

For dosing and transport of the second partial flow and the Additivstromes was a left-handed operated 6-speed planetary gear pump the company Mahr GmbH, Göttingen / DE used. It is a 6-fold Spinning pump, by reversing the sense of rotation and thus the Flow direction, each having equal volume flows of 6 input channels in an output channel combined.

The second partial flow was divided equally between 5 and 6 inputs counterclockwise operated 6-speed planetary gear pump from Mahr GmbH, Göttingen / DE, fed.

A copolymeric additive of the 3rd substance group containing 9% by weight of styrene, 89% by weight of methyl methacrylate and 2% by weight of N-cyclohexylmaleimide chosen with a viscosity ratio of 5.8.

The dried to a residual moisture content of <0.1 wt .-% additive was in melted at an extruder and at a melt temperature of 265 ° C. at 2.33 kg / h, corresponding to 0.77% by weight of the first Partial flow, the remaining input channel of the 6-fold planetary gear pump fed.

This additive flow was in the outlet channel of the planetary gear with the Polyester stream from one of the 5 polyester-fed input channels brought together and by means of a static premixer of the type SMXS DN 12 of the Sulzer AG, Zurich / CH, with an inner diameter of 12.9 mm and 3 times the length of the inner diameter premixed before the Polyester streams of the 4 remaining input channels in this premix Outlet of the planetary gear pump were supplied.

The residence time of the additive melt until merging with the further polymers was about 70 sec.

The subsequent treatment of the first polymer mixture with a Additive content of 16.7 wt .-% was carried out in a first static Main mixer type SMXS DN 17 from Sulzer AG, Zurich / CH, with one Inner diameter of 17.8 mm and 9 times the length of the Inner diameter.

This first mixture was added to the third part stream and after a Flow path L of 4 times the inner diameter of the first main mixer a second main mixer of type SMX from Sulzer AG with a Inner diameter of 52.5 mm and a length of 10 times the diameter supplied there homogenized and dispersed.

The residence time of the additive melt until contact with the 3rd substream was about 100 sec.

The polymer mixture was distributed by means of product lines to 12 spinning positions per position containing 6 spinneret packs. Each spin pack contained a round die with 34 holes of 0.25 mm diameter and 2 times the diameter. Furthermore, the spin pack above the nozzle plate contained a spin filter package consisting of a steel sand packing of 30 mm height and a grain size of 0.35 to 0.50 mm and a very fine mesh of 40 microns and a steel nonwoven filter of 20 microns pore diameter. The cross-sectional area of the spin filter pack was 45 cm ² . The flow rate of the melt mixture resulted in a nozzle pressure of 150 bar. The residence time of the melt in the filter pack was about 1.5 min. The surface of the spinneret was 30 mm above the lower edge of the heating box (active return). The total return was 110 mm. The heating of the spin pack was adjusted by means of HTM heat transfer oil to 290 ° C.

The molten filaments extruded from the die holes became by means of blown air, which is horizontal to the threadline over a length of 1500 mm a velocity of 0.5 m / sec and a temperature of 19 ° C had, cooled and at a distance of 1400 mm from the nozzle plate in an oil pen of the company CeramTec of the type TriboFil to a thread bundled, wherein the diameter of the oil passage was 1 mm, and with Spin finish of Goulston coated, with an order of 0.35% had been set. The standard deviation of the oil application was 38 digits.

An S-shaped pair of godets pulled the thread with one Speed of 5000 m / min, with the spinning delay ratio to 141 and the yarn tension before the first godet was set to 28 cN. Between the godets was a closed at normal threadline Vortex nozzle of the company Temco, type LD installed at an air pressure of 4.0 bar the thread a Verwirbelungsknotenzahl of 22 n / m at a CV value of 53.9%. The thread tension at the inlet of the Vortex nozzle was set at 16 cN, the outlet at 18 cN. The Thread guides were of the surface type "Low Friction" from Barmag / D.

In each case six threads of a spinning position became winding packages in a winder coiled, with the speed of 4985 m / min being chosen such the yarn tension prior to winding was 12 cN. The elevation of Tast roller opposite the Spuldorn was 0.6%. The laying angle was varies between 4.3 ° and 6.5. The flow meter detected the production of a 19kg spool no filament tufts.

Preoriented (POY) filaments were obtained which were characterized by a titer of 141 dtex, a breaking strength of 25 cN / tex and an elongation at break of 117% were marked. The POY coils were in a Barmag texturing machine Type FK6 with a speed of 900 m / min drawtexturized. The draw ratio was 1.70. The first heater had a temperature of 210 ° C, the second of 170 ° C.

The textured yarn had a titer of 88 dtex, a tenacity of 42 cN / tex and an elongation at break of 22% and was by a good Staining uniformity characterized. The inventive method characterized here in particular by a small number of Yarn breaks both during spinning and during texturing.

In the spinning mill, 98% were full 19 kg spools, 92% in stretch texturing full 5 kg spools made.

Claims (5)

1. Method of producing and winding pre-oriented non-crystalline filaments composed of at least 90% by weight of PET as a percentage of the total weight of the filament, at spinning takeoff speeds of above 3800 m/min, characterised in that

   a) the spinline extension ratio is set in the range from 50 to 250,

   b) directly on exit from the spinneret capillary, the filaments pass through a cooling delay zone from 20 to 300 mm in length,

   c) the filaments are cooled to below the solidification temperature,

   d) the filaments are converged at a distance of between 500 mm and 2500 mm from the underside of the capillary,

   e) at least one oiler pin per filament is used to meter on spin finish to a standard deviation of less than 90 digits for the variation in the application of the finish,

   f) use is made of oiler pins, filament-converging elements and filament-guiding elements that have low-friction surfaces,

   g) the filament tension upstream of the takeoff godets is set at between 0.07 cN/dtex and 0.5 cN/dtex,

   h) the filament is entangled at a filament tension of between 0.05 cN/dtex and 0.20 cN/dtex and an air pressure of between 1 bar and 5.5 bars, a node count of at least 10 n/m being set with a coefficient of variation of less than 100% for the node count,

   i) the filament is wound up at a filament tension of between 0.03 cN/dtex and 0.20 cN/dtex, the drive of the contact roll of the winder being operated at a frequency at least 0.3% higher than the drive of the winding chuck and the angle of wind being varied between a minimum of 3.5° and a maximum of 7.5° over the winding time.
2. Method according to claim 1, characterised in that the spinning takeoff speed is set in the range from 4200 to 8000 m/min and in particular in the range from 4600 to 6000 m/min.
3. Method according to claim 1 and/or 2, characterised in that the PET used is one with which up to 2.5% by weight of additive polymer, as a percentage of the total weight of the polymer, is admixed as an extensibility enhancer.
4. Method according to at least one of the foregoing claims, characterised in that the filaments are cooled by means of a cooling device which reduces stress-induced crystallisation at high spinning speeds.
5. Method according to at least one of the foregoing claims, characterised in that the PET used is one with which up to 2.5% by weight of additive polymer, as a percentage of the total weight of the polymer, is admixed as an extensibility enhancer and the filaments are cooled by means of a cooling device which reduces stress-induced crystallisation at high spinning speeds.