EP1356143B1 - Procede de filage et de bobinage de filaments en pet - Google Patents

Procede de filage et de bobinage de filaments en pet Download PDF

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Publication number
EP1356143B1
EP1356143B1 EP01991856A EP01991856A EP1356143B1 EP 1356143 B1 EP1356143 B1 EP 1356143B1 EP 01991856 A EP01991856 A EP 01991856A EP 01991856 A EP01991856 A EP 01991856A EP 1356143 B1 EP1356143 B1 EP 1356143B1
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EP
European Patent Office
Prior art keywords
filaments
dtex
filament
spinning
winding
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP01991856A
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German (de)
English (en)
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EP1356143A1 (fr
Inventor
Alexander Klein
Dietmar Wandel
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LL Plant Engineering AG
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ZiAG Plant Engineering GmbH
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Publication date
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Publication of EP1356143A1 publication Critical patent/EP1356143A1/fr
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Anticipated expiration legal-status Critical
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Classifications

    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65H—HANDLING THIN OR FILAMENTARY MATERIAL, e.g. SHEETS, WEBS, CABLES
    • B65H54/00—Winding, coiling, or depositing filamentary material
    • B65H54/02—Winding and traversing material on to reels, bobbins, tubes, or like package cores or formers
    • B65H54/40—Arrangements for rotating packages
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65H—HANDLING THIN OR FILAMENTARY MATERIAL, e.g. SHEETS, WEBS, CABLES
    • B65H55/00—Wound packages of filamentary material
    • B65H55/04—Wound packages of filamentary material characterised by method of winding
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65H—HANDLING THIN OR FILAMENTARY MATERIAL, e.g. SHEETS, WEBS, CABLES
    • B65H2701/00—Handled material; Storage means
    • B65H2701/30—Handled filamentary material
    • B65H2701/31—Textiles threads or artificial strands of filaments

Definitions

  • the 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.
  • 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.
  • 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.
  • 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
  • PET Polyethylene terephthalate
  • 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.
  • 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 which are amorphous and insoluble in the polyester matrix are preferred.
  • they 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.
  • 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.
  • 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.
  • 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 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.
  • preoriented, non-crystalline Filaments such filaments having an elongation at break between 90 and 165%, exhibit.
  • PET preferably has a intrinsic viscosity (intrinsic viscosity) in the range of 0.55 dl / g to 0.75 dl / g.
  • 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.
  • the homogeneity of the melt has a direct influence on the Material properties of the spun filaments.
  • a spinning pump of the type Promix the company Barmag / D with integrated mixer can be used.
  • 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.
  • 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 latter an increase in the Melting temperature immediately before the extrusion of 4 - 10 ° C corresponds.
  • 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.
  • 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 Disansaugungs monos 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.
  • 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.
  • 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.
  • a special suitable ⁇ lerstatt 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 ⁇ leracheses is designed as a homogenization distance, the preferably has oil reservoirs.
  • 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.
  • 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.
  • the filaments are vortexed before being wound up.
  • 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.
  • they require high winding voltages, which make the coil assembly negative affect and saddle formation, slipping and Fadenabellern on lead the bobbin.
  • 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.
  • 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.
  • 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.
  • the winder with a coperadchangtechnik 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.
  • the touch roller with at least 0.3% higher frequency than the drive of To head for Spuldorns.
  • 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 °
  • the angle between the Thread running direction on the bobbin and the perpendicular to the bobbin as Designation angle called.
  • 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.
  • 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.
  • the POY coils at least 4 Hours at 12 to 28 ° C and a relative humidity between 40 - 90% store the further processing.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Artificial Filaments (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)

Claims (5)

  1. Procédé pour produire et bobiner des filaments non-cristallins et pré-orientés, qui sont composés au moins de 90 % en poids de PET, par rapport au poids total du filament, à une vitesse de filage au démarrage supérieure à 3800 m/mn, caractérisé en ce que :
    a) le taux d'étirage est fixé dans l'intervalle de 50 à 250,
    b) les filaments traversent directement après la sortie de la filière une zone de décélération du refroidissement de 20 mm à 300 mm de long,
    c) les filaments sont refroidis sous la température de solidification,
    d) les filaments sont rassemblés à une distance entre 500 mm et 2500 mm de la face inférieure de la filière,
    e) une préparation de filage est dosée, en utilisant au moins une pointe d'un appareil à ensimer par fil, avec une variation de la quantité de préparation ajoutée d'écart type inférieur à 90,
    f) des pointes d'appareil à ensimer, des éléments de liaison et de guidage de fil munis de surfaces à faible frottement sont utilisées,
    g) la tension de fil devant les godets de filage est fixée entre 0,07 cN/dtex et 0,5 cN/dtex.
    h) le fil est enchevêtré avec une tension filaire entre 0,05 cN/dtex et 0,20 cN/dtex et une pression d'air entre 1,0 bar et 5,5 bars, dans lequel un nombre de noeuds est fixé à au moins 10 n/m avec un coefficient de variation du nombre de noeud au-dessous de 100 %.
    i) le fil est embobiné avec une tension filaire entre 0,03 cN/dtex et 0,20 cN/dtex, dans lequel l'entraínement du rouleau de contact du tambour d'enroulement est effectué avec une fréquence au moins 0,3 % plus élevée que l'entraínement du mandrin de la bobine et l'angle de déplacement du fil varie entre un minimum de 3,5° et un maximum de 7,5° au cours du temps de bobinage.
  2. Procédé selon la revendication 1, caractérisé en ce que la vitesse de filage au démarrage est fixée dans l'intervalle de 4200 à 8000 m/mn, en particulier dans l'intervalle de 4600 à 6000 m/mn.
  3. Procédé selon la revendication 1 ou la revendication 2, caractérisé en ce qu'un PET est utilisé, lequel est mélangé avec un additif polymère jusqu'à 2,5 % en poids par rapport au poids total du filament en tant que matériau améliorant l'allongement.
  4. Procédé selon au moins l'une quelconque des revendications précédentes, caractérisé en ce que le filament est refroidi à l'aide d'un dispositif de refroidissement, qui réduit la cristallisation induite par la contrainte aux vitesses de filage élevées.
  5. Procédé selon au moins l'une quelconque des revendications précédentes, caractérisé en ce qu'un PET est utilisé, lequel est mélangé avec un additif polymère jusqu'à 2,5 % en poids par rapport au poids total du filament en tant que matériau améliorant l'allongement, et le filament est refroidi à l'aide d'un dispositif de refroidissement, qui réduit la cristallisation induite par la contrainte aux vitesses de filage élevées.
EP01991856A 2000-12-19 2001-12-17 Procede de filage et de bobinage de filaments en pet Expired - Lifetime EP1356143B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10063286 2000-12-19
DE10063286A DE10063286A1 (de) 2000-12-19 2000-12-19 Verfahren zum Spinnen und Aufspulen von PET-Filamenten
PCT/EP2001/014876 WO2002050348A1 (fr) 2000-12-19 2001-12-17 Procede de filage et de bobinage de filaments en pet

Publications (2)

Publication Number Publication Date
EP1356143A1 EP1356143A1 (fr) 2003-10-29
EP1356143B1 true EP1356143B1 (fr) 2005-06-22

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EP01991856A Expired - Lifetime EP1356143B1 (fr) 2000-12-19 2001-12-17 Procede de filage et de bobinage de filaments en pet

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US (1) US20040026818A1 (fr)
EP (1) EP1356143B1 (fr)
KR (1) KR100820098B1 (fr)
CN (1) CN1298899C (fr)
AT (1) ATE298376T1 (fr)
AU (1) AU2002231712A1 (fr)
DE (2) DE10063286A1 (fr)
MY (1) MY124905A (fr)
PL (1) PL365326A1 (fr)
TW (1) TW554096B (fr)
WO (1) WO2002050348A1 (fr)

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CN108396402B (zh) * 2018-03-15 2020-12-15 江苏垶恒复合材料有限公司 一种高韧性涤纶短纤维及其制备方法
CA3118074A1 (fr) * 2018-10-29 2020-05-07 Dror Selivansky Couvertures de durcissement de beton et fibres textiles antibacteriennes
US10668664B1 (en) * 2018-11-09 2020-06-02 Thermwood Corporation Systems and methods for printing components using additive manufacturing
EP3884092A1 (fr) 2018-11-22 2021-09-29 BB Engineering GmbH Procédé et dispositif pour le filage à l'état fondu de filaments
CN111060418B (zh) * 2019-12-16 2022-08-02 广东溢达纺织有限公司 纱线干涩判断方法
BR102021025568B1 (pt) * 2021-12-17 2023-01-17 Senai/Cetiqt - Serviço Nacional De Aprendizagem Industrial-Centro De Tecnologia Da Indústria Química E Têxtil Processo de reaproveitamento de resíduos têxteis sintéticos para obtenção de fio contínuo

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CN1060827C (zh) * 1996-03-18 2001-01-17 中国纺织大学 聚酯全伸展丝的高速一步法纺丝工艺、装置及其锡克斯热管
EP1002146B1 (fr) * 1997-08-05 2002-06-12 Röhm GmbH & Co. KG Procede de traitement de melanges polymeres pour former des filaments
DE10022889B4 (de) * 2000-05-25 2007-12-20 Lurgi Zimmer Gmbh Verfahren zum Herstellen von synthetischen Fäden aus einer Polymermischung auf Polyesterbasis
US6667003B2 (en) * 2000-05-25 2003-12-23 Zimmer A.G. Method for the manufacture of synthetic fibers from a melt mixture based on fiber forming polymers

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CN1633528A (zh) 2005-06-29
KR100820098B1 (ko) 2008-04-10
AU2002231712A1 (en) 2002-07-01
US20040026818A1 (en) 2004-02-12
MY124905A (en) 2006-07-31
PL365326A1 (en) 2004-12-27
DE50106599D1 (de) 2005-07-28
KR20030061826A (ko) 2003-07-22
ATE298376T1 (de) 2005-07-15
TW554096B (en) 2003-09-21
DE10063286A1 (de) 2002-06-20
EP1356143A1 (fr) 2003-10-29
WO2002050348A1 (fr) 2002-06-27
CN1298899C (zh) 2007-02-07

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