EP1330564B1 - Procede pour filer et enrouler des filaments de polyester en utilisant des additifs de filage, filaments de polyester obtenus par ce procede de filage, texturation par etirage des filaments de polyester et filaments de polyester gonflants obtenus par cette texturation par etirage - Google Patents

Procede pour filer et enrouler des filaments de polyester en utilisant des additifs de filage, filaments de polyester obtenus par ce procede de filage, texturation par etirage des filaments de polyester et filaments de polyester gonflants obtenus par cette texturation par etirage Download PDF

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Publication number
EP1330564B1
EP1330564B1 EP01992808A EP01992808A EP1330564B1 EP 1330564 B1 EP1330564 B1 EP 1330564B1 EP 01992808 A EP01992808 A EP 01992808A EP 01992808 A EP01992808 A EP 01992808A EP 1330564 B1 EP1330564 B1 EP 1330564B1
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European Patent Office
Prior art keywords
filaments
polyester
filament
break
winding
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EP01992808A
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German (de)
English (en)
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EP1330564A1 (fr
Inventor
Dietmar Wandel
Achim Dulling
Ulrich Mirwaldt
Alexander Klein
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Roehm GmbH Darmstadt
LL Plant Engineering AG
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ZiAG Plant Engineering GmbH
Roehm GmbH Darmstadt
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    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
    • D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
    • D01F6/88—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polycondensation products as major constituent with other polymers or low-molecular-weight compounds
    • D01F6/92—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polycondensation products as major constituent with other polymers or low-molecular-weight compounds of polyesters
    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
    • D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
    • D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
    • D01F6/62—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyesters

Definitions

  • the present invention relates to methods for spinning and winding of preoriented polyester filaments using spin additives, which at least 90% by weight based on the total weight of the polyester filament of polybutylene terephthalate (PBT) and / or Polytrimethylene terephthalate (PTMT), preferably from PTMT, as well as the preoriented polyester filaments obtainable by the process.
  • spin additives which at least 90% by weight based on the total weight of the polyester filament of polybutylene terephthalate (PBT) and / or Polytrimethylene terephthalate (PTMT), preferably from PTMT, as well as the preoriented polyester filaments obtainable by the process.
  • PBT polybutylene terephthalate
  • PTMT Polytrimethylene terephthalate
  • the present invention also relates to methods for Stretch texturing of spun and wound polyester filaments as well the bulky polyester filaments obtainable by stretch texturing.
  • polyester filaments in particular of Polyethylene terephthalate (PET) filaments
  • PET Polyethylene terephthalate
  • PET and PBT or PTMT are due to structural and Attribute differences, such as those in Chemical Fibers Int., P. 53, vol. 50 (2000) and theme on the 39th Int. Man made Fiber Congress, from 13 to 15 Sept. in Dornbirn. So will assume that different chain formations for the Property differences are responsible.
  • WHERE 99/27168 discloses a polyester fiber comprising at least 90% by weight Polytrimethylene terephthalate and a boiling shrinkage between 5% and 16% and an elongation at break of 20% to 60%.
  • the production of in WO 99/27168 described polyester fiber is made by spinning and Stretching. This spin spinning speeds of at most 2100 m / min specified. The procedure is due to the low Spinning speed uneconomical.
  • the obtained Polyester fibers, as the indicated figures show, strongly crystalline and thus only partially suitable for draw texturing.
  • European patent EP 0,731,196 B1 claims a method for spinning, Stretching and winding a synthetic thread, with the thread after the stretching and before winding to reduce the Shrinkage is subjected to a heat treatment.
  • usable Synthetic fibers also include polytrimethylene terephthalate fibers.
  • the heat treatment is carried out in that the synthetic Thread in close proximity but substantially without contact along an elongated heating surface is performed.
  • the application of a Heat treatment makes the process more expensive and also supplies synthetic threads with high crystallinity, which are only partially suitable for draw texturing.
  • the tensile strength of the Polytrimethylene terephthalate fibers is 26.5 cN / tex (Texturing speed of 450 m / min) or 29.15 cN / tex (Texturing speed of 850 m / min) and the elongation at break of 38.0% (Texturing speed of 450 m / min) or 33.5% (Texturing speed of 850 m / min) specified.
  • Figure 1 describes the change in boiling shrinkage for three PTMT-POY coils depending on the storage time under normal climatic conditions. in this connection was the change in the POY cooking shrinkage for three coils with different initial value over the storage time at normal Climatic conditions examined.
  • the spools No. 16 and 17 with high Initial value> 40% show after 4 weeks a boiling shrinkage above 30%, preferably above 40%. If the initial value of the boiling shrinkage However, less than 40%, so the coil 18 shows that this after 4 weeks Storage time, however, falls below the critical value of 30%.
  • the shrinkage is a measure of the processability and the Degree of crystallization of the fibers.
  • the fibers described in WO 01/04393 have Plastics with a higher degree of crystallization, which is essential worse and only at lower draw ratio and / or lower Process the texturing speed.
  • Another object of the present invention was a method for spinning and winding of preoriented polyester filaments, which is industrially and inexpensively feasible.
  • the invention Procedure should be as high take-off speeds, preferably greater 2200 m / min and high thread weights on the bobbin of more than 4 kg, allow.
  • the pre-oriented polyester filaments should be simple and manner in a stretch texturing process, especially at high Texturing speeds, preferably greater than 450 m / min, further processed can be.
  • the filaments obtainable by stretch texturing should have excellent material properties, for. B. a high tensile strength of more than 26 cN / tex and a high elongation at break of more than 30% for HE filaments or more than 36% for SET filaments.
  • the present invention relates to a process for the production and for winding preoriented polyester filaments which are at least 90 Wt .-% based on the total weight of the filament
  • Polybutylene terephthalate (PBT) and / or polytrimethylene terephthalate (PTMT) consist.
  • Polybutylene terephthalate (PBT) and / or polytrimethylene terephthalate (PTMT) are known in the art.
  • Polybutylene terephthalate can by Polycondensation of terephthalic acid with equimolar amounts of 1,4-butanediol, Polytrimethylene terephthalate by polycondensation of Terephthalic acid with equimolar amounts of 1,3-propanediol can be obtained. Also mixtures of the two polyesters are conceivable. According to the invention preferred becomes PTMT.
  • the polyesters can be both homopolymers and copolymers.
  • copolymers In particular, those in addition to recurrent PTMT and / or PBT units still up to 15 mol% based on all Repeating units of polyester repeating units more usual Comonomers, such as.
  • polyester homopolymers prefers.
  • the polyesters according to the invention can be customary amounts other additives than 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 polyesters Preferably, contain 0 to 5 wt .-% based on the total weight of the filament of additives.
  • the polyesters can also a small proportion, preferably up to 0.5 wt .-% based on the total weight of the filament, on Branching components, included.
  • 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.
  • additive polymers and / or copolymers in Fonn of bead polymers particularly preferred whose particle size in a particularly favorable range.
  • the invention are for example by mixing into the melt of the fiber polymers using additive polymers and / or copolymers in the form of particles with an average diameter of 0.1 to 1.0 mm. There are, however larger or smaller beads or granules can be used.
  • the additive polymers and / or copolymers may also already be included in chips of the matrix polymer be, so that a metering is omitted.
  • additive polymers and / or copolymers which are amorphous and are insoluble in the polyester matrix.
  • they Preferably, they have one Glass transition temperature of 90 to 200 ° C, the glass transition temperature in a known manner, preferably by differential scanning calorimetry, is determined. Further details may be in the state of the art, for example the Publication WO 99/07927, the disclosure of which hereby is explicitly referred to.
  • the additive polymer and / or copolymer is selected such 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 is.
  • 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 28 ° C is, measured. For PTMT, the measurement temperature for the melt viscosity is included 255 ° C. Further details can in turn be found in document WO 99/07927 be removed.
  • the melt viscosity of the additive polymer and / or Copolymer is preferably higher than that of the matrix polymer and it has shown that the choice of a specific viscosity range for the additive polymer and / or copolymer and the choice of the viscosity ratio to Optimization of the properties of the yarn produced contributes.
  • a optimized viscosity ratio is a minimization of the amount of additive Additive polymer and / or copolymer possible, whereby, inter alia, the Profitability of the method is improved.
  • the to be spun Polymer mixture preferably contains 0.05 to 2.5 wt .-%, especially preferably 0.25 to 2.0 wt .-% additive polymer and / or copolymer.
  • the threads at least 60 wt .-% 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 ranging from 0.01 to 0.5 microns included.
  • polyesters are preferably thermoformable and can be spun into filaments and spooled become.
  • such polyesters are particularly advantageous, the one Intrinsic viscosity in the range of 0.70 dl / g to 0.95 dl / g.
  • a polymer melt for example, directly from the Endreaktor a Polycondensation be removed or from solid polymer chips in a melt extruder are made,
  • the spin additive can in known manner, inter alia, in molten or solid form metered into the matrix polymer, homogeneously distributed in this and to fine particles are dispersed.
  • a device may be used according to DE 100 22 889.
  • the melt or melt mixture the polyester by means of spinning pumps at a constant speed the speed is set according to known formula, that the desired yarn titer is obtained, pressed into nozzle packages and through the nozzle holes of the nozzle plate of the package is extruded into molten filaments.
  • the melt can be made for example in an extruder of polymer chips are, where it is particularly favorable, the chips previously on a water content ⁇ 30 ppm, in particular to a water content of ⁇ 15 ppm.
  • the specified parameters serve to limit the hydrolytic and / or thermal viscosity degradation, the expediently as possible should be low.
  • a viscosity reduction less than 0.12 dl / g, in particular less than 0.08 dl / g, desirable.
  • the homogeneity of the melt has a direct influence on the Material properties of the spun filaments.
  • a static mixer with at least one element, which after the Spinning pump is installed, for homogenization of the melt.
  • 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 or radiant heater in question.
  • the temperature is the nozzle plates at the level of spinning temperature.
  • a temperature increase at the nozzle plate can be achieved by the pressure gradient in the nozzle package.
  • Known derivations such as K. Riggert "Advances in the production of polyester tire cord” Chemiefasern 21 , page 379 (1971), describe a temperature increase of about 4 ° C per 100 bar pressure drop.
  • 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, the made of metal fabrics or non-wovens with a fineness ⁇ 40 ⁇ can control.
  • 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, the made of metal fabrics or non-wovens with a fineness ⁇ 40 ⁇ can control.
  • the pressure drop in the nozzle hole contributes to the total pressure.
  • the Nozzle pressure is preferably between 80 bar and 450 bar, in particular set between 100 bar and 250 bar.
  • the spinning delay is between 70 and 500, preferably between 100 and 250.
  • the length / diameter ratio of the nozzle hole is preferably between 1.5 and 6 selected, in particular between 1.5 and 4.
  • the extruded filaments pass through a cooling delay zone. Directly below the nozzle package this is designed as a return zone in which the emerging from the nozzle holes filaments are preserved from the direct action of the cooling gas and delayed in delay or cooling.
  • An active part of the return is performed as an offset of the nozzle package in the spinning beam in, so that the filaments are surrounded by heated walls.
  • a passive part is formed by insulation layers and unheated frames. The lengths of the active recess are between 0 to 100 mm, that of the passive part between 20 to 120 mm, with a total length of 30 - 200 mm, preferably 30 - 120 mm is maintained.
  • this zone of cylindrical or rectangular cross section at least a heating independent of the spinning beam.
  • the filaments are at temperatures below their Solidification temperature cooled.
  • 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.
  • 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 Self-priming effect of the filaments becomes a cooling each achieved single filament.
  • Alternative to the single tubes are also the known Querstromanblasungssysteme used.
  • suitable distance of the bundling of the nozzle bottom can by methods known to those skilled in the art for online measurement of 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, preferably 500 to 1800 mm.
  • This filaments are with a Titer ⁇ 3.5 dtex, preferably at a smaller distance ⁇ 1500 mm, thicker Filaments are preferably bundled at a greater distance.
  • the bundling of the filaments takes place in an oiler stone, the thread the the desired amount of spin finish uniformly.
  • a special suitable ⁇ lerstein 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.
  • the Outlet part of the oiler is designed as a homogenization distance, the preferably has oil reservoirs.
  • Such oilers can, for example, from the Company Cermatec / D or Goulston / USA.
  • the uniformity of the oil application can according to the invention of great importance be. 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.
  • a Rossa meter according to the in Chemical fibers / textile industry, 42./94, Nov. 1992 on page 896 described Method to be determined.
  • Particular preference is given to values for the standard deviation of the oil application less than 45 digits, in particular less than 30 digits. there corresponds to a value for the standard deviation of 90 digits or 45 digits about 6.2% and 3.1% of the coefficient of variation, respectively.
  • an entangling is particularly preferred before being wound up Thread.
  • nozzles with closed yarn channels as special proved suitable, since in such systems entanglements of the thread in the Insertion slot avoided even with low thread tension and high air pressure become.
  • the Entanglingdüsen are preferably between godets arranged, wherein the exit thread tension by means of different Speed of the inlet and outlet galette is regulated. It should be .20 cN / dtex and primarily values between 0.05 cN / dtex and 0.15 cN / dtex.
  • the air pressure of Entanglingluft is between 0.5 and 5.5 bar, at winding speeds up to 3500 m / min at a maximum of 3.0 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.
  • nodal 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.
  • systems have become of the type LD of the company Temco / D, the double system of the company Slack & Parr / USA, or nozzles of the type Polyjet of Heberlein as proved particularly suitable.
  • the peripheral speed of the first godet unit is called Discharge speed called.
  • Other godet systems can be used be before the thread in the winding unit to winding bodies (coils) on Sleeves is wound up.
  • Stable, error-free filament wound bodies are a prerequisite for error-free removal of the thread and for as error-free as possible Further processing. Therefore, in the context of the present process, a Winding tension in the range of 0.025 cN / dtex - 0.15 cN / dtex, preferably in Range of 0.03 cN / dtex - 0.08 cN / dtex.
  • Thread tension before and between the withdrawal godets is this voltage essentially from the actual orientation voltage Hamana, the friction tension on the yarn guides and the oiler and the Thread-air friction tension together.
  • this voltage essentially from the actual orientation voltage Hamana, the friction tension on the yarn guides and the oiler and the Thread-air friction tension together.
  • the thread tension before and between the withdrawal godets in Range from 0.05 cN / dtex to 0.20 cN / dtex, preferably between 0.08 cN / dtex and 0.15 cN / dtex.
  • the tension is determined by the oiler distance from the nozzle, the Friction surfaces and the length of the distance between oiler and withdrawal godet regulated.
  • This route length is advantageously not more than 6.0 m, preferably less than 2.0 m, with the spinning and drawing machine are arranged by parallel construction such that a straight yarn path is guaranteed.
  • the geometric parameters also change the conditioning time of the thread between bundling point and Aufspulung described.
  • the fast-running Relaxation during this time affects the quality of the coil construction.
  • the conditioning time defined in this way is between 50 and 200 ms selected.
  • the winding speed of the POYs is between 2200 according to the invention m / min and 6000 m / min. Preferably, a speed between 2500 m / min and 6000 m / min. Particularly preferred are the Polymer blends at speeds in the range of 3500 m / min to 6000 wound up in m / min.
  • the POY coils at least 4 hours at 12 to 35 ° C and a relative humidity of 40-85% before Store further processing.
  • normal conditions is known to those skilled in and over the Standard DIN 53802 defined. Under “normal conditions” according to DIN 53802 the temperature is 20 ⁇ 2 ° C and the relative humidity 65 ⁇ 2%.
  • the intrinsic viscosity is in the capillary viscometer from Ubbelohde at 25 ° C and calculated according to known formula.
  • a solvent is a Mixture of phenol / 1,2-dichlorobenzene in the weight ratio 3: 2 used.
  • the Concentration of the solution is 0.5 g of polyester per 100 ml of solution.
  • the crystallization and the glass transition temperature a calorimeter DSC device from Mettler is used. Here is the Sample first heated to 280 ° C and melted and then quenched. The DSC measurement is carried out in the range of 20 ° C to 280 ° C with a heating rate of 10 K / min. The temperature variables are determined by the processor.
  • the determination of the density of filaments is carried out in a density-gradient column at a temperature of 23 ⁇ 0.1 ° C.
  • the reagent used is n-heptane (C 7 H 16 ) and tetrachloromethane (CCl 4 ).
  • the result of the density measurement can be used to calculate the degree of crystallinity, based on the density of the amorphous polyester D a and the density of the crystalline polyester D k .
  • the titer is known with a precision grape and a weighing device in Determined way.
  • the bias is suitably for Preoriented filaments (POYs) 0.05 cN / dtex and for textured yarn (DTY) 0.2 cN / dtex.
  • Tear strength and elongation at break are included in a Statimat meter the following conditions are determined; the clamping length is 200 mm for POY or 500 mm for DTY, the measuring speed is 2000 mm / min for POY or 1500 mm / min for DTY, the preload is 0.05 cN / dtex for POY or 0.2 cN / dtex for DTY. By dividing the values for the maximum breaking load the titer determines the tear strength and the elongation at break is added evaluated maximum load.
  • Strands of filaments are used to determine the boiling shrinkage de-energized in water at 95 ⁇ 1 ° C for 10 ⁇ 1 min.
  • the strands are tempered with a bias of 0.05 cN / dtex for POY or 0.2 cN / dtex for DTY produced; the length measurement of the strands before and after the temperature treatment takes place at 0.2 cN / dtex. From the Length difference is calculated in a known manner of boiling shrinkage.
  • the crimp characteristics of the textured filaments are in accordance with DIN 53840, Part 1 with the texturates of the company Stein / D at 120 ° C development temperature measured.
  • the normal Uster values are determined with the Uster tester 4-CX and as Uster% values indicated. It is at a test speed of 100 m / min the test time 2.5 min.
  • the POY according to the invention can be further processed in a simple manner, in particular stretch texturized.
  • the stretch texturing preferably takes place at a texturing speed of at least 500 m / min, more preferably in one Texturing speed of at least 700 m / min.
  • the draw ratio is preferably at least 1: 1.35, in particular at least 1: 1.40. It has become Stretch texturing on a high temperature heater type machine, such as For example, the AFK the company Barmag, proved to be particularly useful.
  • the bulky filaments thus produced have a low number Lint and after staining under cooking conditions with a Dispersion dye without carrier excellent color depth and Color uniformity on.
  • Bulky SET filaments produced according to the invention preferably have a tensile strength of more than 26 cN / tex and an elongation at break of more than 36%.
  • the tear strength is preferably more than 26 cN / tex and the elongation at break more than 30%.
  • the chips were melted in a 3E4 extruder from Barmag, see above that the temperature of the melt was 255 ° C.
  • This melt was various amounts of polymethyl methacrylate commercial type Plexiglas 7N the company Röhm GmbH / D added as strain increase additive, which previously dried to a residual moisture of less than 0.1%.
  • the additive polymer was for this purpose by means of a melting extruder melted and with a gear metering pump of the feed device supplied and there by an injection nozzle in the flow direction of the Supplied polyester component.
  • a static mixer from. Sulzer type Both 15-element SMX and 15 mm inner diameter SMX were used Melt homogeneously mixed together and finely dispersed.
  • the melt viscosity of the type Plexiglas 7N was 810 Pa s (2.4 Hz, 255 ° C), whereby the ratio of additive and polyester melt viscosity was 2.5: 1.
  • the transported amount of melt was 63 g / min with a residence time of 6 min, the dose added by the spin pump to the nozzle pack became such adjusted so that the POY titer was about 102 dtex.
  • After the spin pump before entering the Nozzle package was an element static mixer, type HD-CSE with 10 mm Internal diameter of the company Fluitec installed.
  • the trace heating of Product line and spin block containing the pump and nozzle pack, were set at 255 ° C.
  • the nozzle package contained steel sand as filter media the grain size 350-500 microns with a height of 30 mm and a 20 micron Vliesund a 40 ⁇ m mesh filter.
  • the melt was passed through a nozzle plate of 80 mm diameter and 34 holes with a diameter of 0.25 mm and extruded a length of 1.0 mm.
  • the nozzle pressure was about 120-140 bar.
  • the cooling delay zone had a length of 100 mm, with 30 mm heated wall and 70 mm insulation and unheated frame were.
  • the Melt filaments were then subsequently in a blow shaft with Querstromanblasung a blow length of 1500 mm cooled.
  • the cooling air had a speed of 0.35 m / sec, a temperature of 18 ° C and a relative Humidity of 80%.
  • the solidification point of the filaments was at a distance of about 800 mm below the spinneret.
  • the bundled thread was then fed to the winding machine.
  • the distance between oiler and first withdrawal godet was 3.2 m.
  • the conditioning time was between 105 and 140 ms.
  • a pair of godets became S-shaped from the thread entwined.
  • Between the godets was a Temco Entanglingdüse installed, which was operated with an air pressure of 1.5 bar.
  • According to the Speed setting was the winding speed of the winder of the type SW6 of the company Barmag adjusted so that the Aufspilladenschreib 5 cN.
  • the indoor climate was at 24 ° C at 60% Relative humidity adjusted so that in the environment of the Filament winding set a temperature of about 34 ° C.
  • the PTMT filament coils were exposed to normal climate for four weeks according to DIN 53802 and then a draw texturing machine from Barmag, type FK6-S-900, submitted.
  • the experimental parameters of stretch texturing for Production of so-called SET filaments are shown in Table 3, which Material properties of the resulting bulky SET filaments are in Table 4 summarized.
  • Heater 2 [° C] 160 160 160 Texturing error [n / 10 km] 0 0 0 thread tension F 1 , in front of aggregate [cN] 17 18 19 F 2 , according to aggregate [cN] 19 21 21 F 2 -CV [%] 0.78 0.93 0.89 F 2 -CV: coefficient of variation of F 2 Material properties of the stretch-textured filaments material properties example 1 Example 2 Example 3 Titre [dtex] 67 69 79 Tear strength [cN / tex] 26.9 29.6 28.2 Elongation at break [%] 38.6 37.8 38.0 visual staining assessment evenly evenly evenly evenly evenly evenly evenly Crimp resistance [%] 84 85 79 Crimping [%] 25 24 23

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Artificial Filaments (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Treatments For Attaching Organic Compounds To Fibrous Goods (AREA)
  • Shaping By String And By Release Of Stress In Plastics And The Like (AREA)
  • Extrusion Moulding Of Plastics Or The Like (AREA)

Claims (9)

  1. Procédé de fabrication et d'enroulement de filaments de polyester préorientés, constitués d'au moins 90 % en poids par rapport au poids total du filament de polyester, de polybutylène-téréphtalate (PBT) et/ou de polytriméthylène-téraphtalate (PTMT), de préférence de PTMT, caractérisé en ce que
    a) l'étirement est configuré dans une plage de 70 à 500,
    b) les filaments passent directement après la sortie de la filière, dans une zone de retard de refroidissement de 30 mm à 200 mm de longueur,
    c) les filaments sont refroidis à la température de solidification,
    d) les filaments sont liés à intervalle de 500 mm et 2500 mm à partir de la face inférieure de la filière,
    e) la tension du fil avant et entre les galets d'étirement est réglée entre 0,05 cN/dtex et 0,20 cN/dtex,
    f) le fil est enroulé avec une tension comprise entre 0,025 cN/dtex et 0,15 cN/dtex,
    g) la vitesse d'enroulement est réglée entre 2200 m/min. et 6000 m/min.,
    h) et un polyester étant utilisé, mélangé à raison de 0,05 % en poids à 2,5 % en poids par rapport au poids total du filament, à un polymère additif utilisé comme agent d'augmentation de l'allongement.
  2. Procédé selon la revendication 1, caractérisé en ce que l'on utilise du PBT et/ou du PTMT présentant un indice de viscosité limite dans la plage de 0,7 dl/g à 0,95 dl/g.
  3. Procédé selon la revendication 1 et/ou 2, caractérisé en ce que, lors de l'enroulement dans l'environnement de la bobine de fil, la température est de ≤ 45° C.
  4. Procédé selon au moins l'une quelconque des revendications précédentes, caractérisé en ce que l'on stocke les bobines de POY pendant au moins 4 heures à une température de 12 à 35° C et avec une humidité relative de 40 à 85 % avant de procéder à un traitement ultérieur.
  5. Procédé selon au moins l'une quelconque des revendications précédentes, caractérisé en ce que l'on règle la vitesse d'enroulement entre 2500 m/min. et 6000 m/min.
  6. Filaments de polyester préorientés obtenus par un procédé selon au moins l'une quelconque des revendications précédentes, caractérisé en ce qu'ils présentent, après 4 semaines de stockage dans des conditions normales selon la norme DIN 53802,
    a) un allongement à la rupture entre 90 % et 165 %,
    b) un rétrécissement au bouillissage d'au moins 30 %,
    c) un Normal-Uster inférieur à 1,1 %,
    d) une double réfraction entre 0,030 et 0,058,
    e) une densité inférieure à 1,35 g/cm3, de préférence inférieure à 1,33 g/cm3,
    f) un coefficient de variation de la charge de rupture ≤ 4,5 %,
    g) un coefficient de variation de l'allongement à la rupture de ≤ 4,5 %.
  7. Procédé de fabrication de filaments de polyester gonflants, caractérisé en ce que l'on transforme des filaments selon la revendication 6 dans une machine de texturation par étirement, à une vitesse d'au moins 500 m/min. et selon un rapport d'étirement d'au moins 1:1,35, en un fil gonflant.
  8. Filaments de polyester-SET gonflants obtenus par un procédé selon la revendication 7, caractérisé en ce que leur résistance à la rupture est supérieure à 26 cN/tex et l'allongement à la rupture est de 36 %.
  9. Filaments de polyester-HE gonflants obtenus par un procédé selon la revendication 7, caractérisé en ce que leur résistance à la rupture est supérieure à 26 cN/tex et l'allongement à la rupture est de 30 %
EP01992808A 2000-11-03 2001-11-02 Procede pour filer et enrouler des filaments de polyester en utilisant des additifs de filage, filaments de polyester obtenus par ce procede de filage, texturation par etirage des filaments de polyester et filaments de polyester gonflants obtenus par cette texturation par etirage Expired - Lifetime EP1330564B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10054422 2000-11-03
DE10054422 2000-11-03
PCT/EP2001/012684 WO2002036864A1 (fr) 2000-11-03 2001-11-02 Procede pour filer et enrouler des filaments de polyester en utilisant des additifs de filage, filaments de polyester obtenus par ce procede de filage, texturation par etirage des filaments de polyester et filaments de polyester gonflants obtenus par cette texturation par etirage

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EP1330564A1 EP1330564A1 (fr) 2003-07-30
EP1330564B1 true EP1330564B1 (fr) 2005-03-16

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EP01992806A Expired - Lifetime EP1330563B1 (fr) 2000-11-03 2001-11-02 Procede de filage et d'enroulement de filaments polyester, des filaments polyester obtenus par ce procede de filage, etirage-texturation des filaments polyester et filaments polyester textures obtenus par etirage-texturation
EP01992808A Expired - Lifetime EP1330564B1 (fr) 2000-11-03 2001-11-02 Procede pour filer et enrouler des filaments de polyester en utilisant des additifs de filage, filaments de polyester obtenus par ce procede de filage, texturation par etirage des filaments de polyester et filaments de polyester gonflants obtenus par cette texturation par etirage

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EP (2) EP1330563B1 (fr)
JP (2) JP2004513249A (fr)
KR (2) KR20030043790A (fr)
CN (2) CN1210448C (fr)
AT (2) ATE291114T1 (fr)
AU (2) AU2002224824A1 (fr)
BR (2) BR0113515A (fr)
CA (2) CA2405495A1 (fr)
DE (4) DE10151893A1 (fr)
EA (2) EA003882B1 (fr)
EG (2) EG23364A (fr)
ES (2) ES2237616T3 (fr)
HK (1) HK1054577B (fr)
MX (2) MXPA03001318A (fr)
MY (1) MY136398A (fr)
TW (2) TW587108B (fr)
WO (2) WO2002036862A1 (fr)

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JP3910038B2 (ja) * 2001-10-18 2007-04-25 旭化成せんい株式会社 前配向糸パッケージとその製造方法
JP3862996B2 (ja) * 2001-10-31 2006-12-27 帝人ファイバー株式会社 ポリトリメチレンテレフタレートフィラメント糸およびその製造方法
WO2003069034A1 (fr) * 2002-02-12 2003-08-21 Zimmer Ag Procede de production et d'enroulage de fils multifilaments polyester, ainsi que fils multifilaments polyester pouvant etre obtenus a l'aide de ce procede et dispositif d'enroulage d'au moins un fil multifilament
DE10213921B4 (de) * 2002-03-28 2006-10-12 Röhm Gmbh Verfahren zum Spinnen und Aufspulen von Polyester-Multifilament-Garnen unter Verwendung von Spinnadditiven sowie durch das Spinn-Verfahren erhältliche Polyester-Multifilament-Garne
TW200741049A (en) * 2005-12-27 2007-11-01 Shell Int Research Polyester yarn and process for producing
CN115262049A (zh) * 2021-04-30 2022-11-01 上海凯赛生物技术股份有限公司 一种聚酰胺56加弹丝及其制备方法
CN113481624B (zh) * 2021-06-24 2023-04-28 杭州惠丰化纤有限公司 一种涤纶丝及其生产工艺

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US3975488A (en) * 1972-10-24 1976-08-17 Fiber Industries, Inc. Process for preparing poly(tetramethylene terephthalate) yarn
JP2001512793A (ja) * 1997-08-05 2001-08-28 ルルギ ツィマー アクチエンゲゼルシャフト ポリマー混合物をフィラメントに加工する方法
JPH11172526A (ja) * 1997-11-26 1999-06-29 Asahi Chem Ind Co Ltd 低熱応力ポリエステル繊維及びその紡糸方法
JP3249097B2 (ja) * 1999-07-12 2002-01-21 旭化成株式会社 仮撚加工に適したポリエステル繊維及び製造方法
TW522179B (en) * 1999-07-12 2003-03-01 Asahi Chemical Ind Polyester yarn and producing method thereof
US6287688B1 (en) * 2000-03-03 2001-09-11 E. I. Du Pont De Nemours And Company Partially oriented poly(trimethylene terephthalate) yarn

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MY136398A (en) 2008-09-30
BR0113515A (pt) 2003-07-15
MXPA03001319A (es) 2004-07-30
EP1330564A1 (fr) 2003-07-30
JP2004513249A (ja) 2004-04-30
CA2405885A1 (fr) 2002-05-10
EP1330563A1 (fr) 2003-07-30
DE10151893A1 (de) 2002-07-25
AU2002215998A1 (en) 2002-05-15
EA003951B1 (ru) 2003-10-30
CN1432079A (zh) 2003-07-23
EG23028A (en) 2004-01-31
KR20030043790A (ko) 2003-06-02
TW587108B (en) 2004-05-11
WO2002036862A8 (fr) 2003-11-27
EG23364A (en) 2005-02-28
ES2237616T3 (es) 2005-08-01
JP2004532356A (ja) 2004-10-21
HK1054577B (zh) 2005-08-05
ATE291114T1 (de) 2005-04-15
EP1330563B1 (fr) 2005-03-23
EA200201194A1 (ru) 2003-04-24
KR100783124B1 (ko) 2007-12-07
HK1054577A1 (en) 2003-12-05
MXPA03001318A (es) 2003-06-30
CN1210448C (zh) 2005-07-13
AU2002224824A1 (en) 2002-05-15
DE50105726D1 (de) 2005-04-28
DE10151875A1 (de) 2002-08-29
WO2002036862A1 (fr) 2002-05-10
CA2405495A1 (fr) 2002-10-07
CN1210449C (zh) 2005-07-13
BR0113527A (pt) 2003-07-15
ES2236349T3 (es) 2005-07-16
KR20030061305A (ko) 2003-07-18
ATE291651T1 (de) 2005-04-15
CN1432078A (zh) 2003-07-23
DE50105643D1 (de) 2005-04-21
EA200201196A1 (ru) 2003-06-26
WO2002036864A1 (fr) 2002-05-10
TW589420B (en) 2004-06-01
EA003882B1 (ru) 2003-10-30

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