EP1185728A1 - Procede de production de fils synthetiques ultrafins - Google Patents

Procede de production de fils synthetiques ultrafins

Info

Publication number
EP1185728A1
EP1185728A1 EP00927131A EP00927131A EP1185728A1 EP 1185728 A1 EP1185728 A1 EP 1185728A1 EP 00927131 A EP00927131 A EP 00927131A EP 00927131 A EP00927131 A EP 00927131A EP 1185728 A1 EP1185728 A1 EP 1185728A1
Authority
EP
European Patent Office
Prior art keywords
melt
yarn
nozzle plate
temperature
filaments
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.)
Granted
Application number
EP00927131A
Other languages
German (de)
English (en)
Other versions
EP1185728B1 (fr
Inventor
Andreas Mueller
Reinhard Wagner
Dietmar Wandel
Heinz Schuettrichkeit
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Roehm GmbH Darmstadt
LL Plant Engineering AG
Original Assignee
ZiAG Plant Engineering GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by ZiAG Plant Engineering GmbH filed Critical ZiAG Plant Engineering GmbH
Publication of EP1185728A1 publication Critical patent/EP1185728A1/fr
Application granted granted Critical
Publication of EP1185728B1 publication Critical patent/EP1185728B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • D01F6/58—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
    • 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
    • D01F6/60—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyamides
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T428/00—Stock material or miscellaneous articles
    • Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
    • Y10T428/2913—Rod, strand, filament or fiber
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
    • Y10T428/00—Stock material or miscellaneous articles
    • Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
    • Y10T428/2913—Rod, strand, filament or fiber
    • Y10T428/2933—Coated or with bond, impregnation or core
    • Y10T428/2964—Artificial fiber or filament
    • Y10T428/2967—Synthetic resin or polymer
    • Y10T428/2969—Polyamide, polyimide or polyester

Definitions

  • the present invention relates to a method for producing a synthetic ultra-fine continuous yarn based on polyester or polyamide in the range 0.25 to 0.9 denier per POY filament by melt spinning at take-off speeds between 2000 and 6000 m / min.
  • a second immiscible amorphous polymer may be added to the polyester or polyamide in an amount of 0.05 to 5 percent by weight.
  • Nakajima describes a process for spinning ultra-fine fibers, the filaments being blown with a radially directed cold air stream in addition to the normal crossflow blowing immediately after the spinning.
  • Tekaat publication at the international man-made fiber conference in Dornbirn 1992, p. 8 describes investigations in the manufacture of microfilament yarns. It was found that the blown air has difficulty penetrating the bundle of threads at high numbers of filaments and that the filaments cool in the middle significantly later than the filaments near the edges.
  • US Pat. No. 5,310,514 (Corovin) claims a process for the production of microfilaments, in which a hot air stream for protection of the freshly spun filaments flows out parallel to them from an annular slot in the nozzle package.
  • the temperature of the hot air is ⁇ 10 K of the melt temperature.
  • the technical implementation is complex and the constancy of the air flow necessary in this critical area is difficult to guarantee.
  • EP0455897 A (Karl Fischer) describes a method for heating the individual filaments via a channel system within the nozzle plate through which hot air is passed. The aim is to improve the warping of the filaments. Compensation for the heat losses of the filaments close to the edge is therefore not possible.
  • the hot gas flows individually around the filaments. The thread distortion is to be supported in this way.
  • the temperatures can be in the range of the melt temperature or above.
  • GB patent 1391471 (Hoechst) describes a heater for technical yarns. This means that a low pre-oriented yarn can be produced with increased throughput.
  • the device consists of two conical half-shells, the lower one is heated and the upper polished shell reflects a large part of the heat radiation onto the filaments. It is expressly pointed out that only a little radiation should hit the nozzle plate.
  • the temperature curve along the heating section is highly parabolic with a maximum of approximately half the length (approx. 120 K above the melt temperature).
  • US Patent 5661880 claims radiant heating of the filaments emerging from the spinneret. A process for spinning with a conical heating section is described. The temperatures on the heating surface are preferably 450 - 700 ° C, well above the melt temperature. In addition, heating of the nozzle plate is claimed by heating tapes running in or on it. The contact time available for heat transfer to the melt is thus reduced to a few seconds. There is no differentiation between different heating of the internal and external melt flows. This is to prevent the melt from being oriented too early in the nozzle capillaries. Moreover deposits on the nozzle are to be reduced and the throughput can be increased.
  • US Patent 5182068 (ICI) describes a process which is said to reduce necking on draws above 5000 m / min. It is said that a heated return with a temperature profile that is constant over the run length (300 °) only causes the neck point to shift, while a return with progressively decreasing temperature profile (300 -> 200 ° C) brings about a clear defusing of the neck point.
  • the thread speed before the necking is increased and the neck-draw ratio before / after the necking is reduced. Speeds above 7000 m / min are required.
  • GB patent 903427 (Inventa) claims a spinning tube with a length of at least. In the upper region there is a temperature of 10 - 80 K below the melt temperature. The temperature in the lower pipe section is less than 100 ° C. The heating can take place either directly or via a heat transfer medium.
  • US Patent 5250245 (DuPont) describes a spin orientation process for the production of fine polyester filaments with improved mechanical properties and titre uniformity. This is achieved by choosing a suitable polymer viscosity and appropriately adapted spinning conditions.
  • the different cooling behavior between inner and outer filaments is decisive for the running stability.
  • the temperature profile of the emerging filaments must therefore be able to be adjusted depending on the polymer throughput.
  • the temperature profile of the filaments that have already emerged so too influence that this cooling behavior is countered has not been considered by the prior art.
  • the aim of the invention is to achieve uniformity in ultra-fine yarns (approx. 0.25-0.89 dpf), as is the case with the current process principle in the production of high-count yarns (approx. 1.0-1.2 dpf) can be reached.
  • blowing systems in practice are based on single-sided blowing to facilitate access. It should be possible to use this principle of one-sided blowing.
  • a polyester such as polyethylene terephthalate (PET), polypropylene or polybutylene terephthalate or polyamide, such as PA 6 or PA 6.6, or copolymers thereof, is used as the raw material.
  • PET polyethylene terephthalate
  • PET polypropylene or polybutylene terephthalate or polyamide, such as PA 6 or PA 6.6, or copolymers thereof
  • PET with an intrinsic viscosity between 0.59 and 0.66 dl / g is preferred. Adequate structural homogeneity and sufficient thermal homogeneity of the melt before reaching the spin pack must be ensured.
  • a second immiscible amorphous polymer can be added to the base polymer in an amount of 0.05 to 5 percent by weight.
  • the polymer added is preferably a copolymer which is composed of at least two of the following monomer units:
  • PET single titer of 0.25-0.9 denier corresponding to a single end titer of the drawn yarn of 0.15 to 0.52 denier
  • the elongation at break in the PET-POY is in a range from 100 to 145% and the specific tensile strength is between 18 and 33 cN / tex. Take-off speeds between 2000 and 6000 m / min are used.
  • Some process parameters for polyester (PET) which are characteristic according to the invention are listed in Table 1.
  • a round packet according to US Pat. No. 5,304,052 or US Pat. No. 5,755,595 is used as the nozzle packet.
  • the dwell time of the melt within the package is adjusted by means of internals so that it does not exceed 12 minutes and does not fall below 5 minutes.
  • a sequence of different fabric layers with the finest mesh sizes of 5 to 15 ⁇ m in combination with or without fine steel sand in the grain size 88 to 250 ⁇ m was used as the filtration medium.
  • sufficient shearing or fragmentation of the higher molecular gels present in the melt is necessary, which can be done either by fine steel sand or by appropriate built-in components in the spin pack with the finest pore openings of 50 to 1000 ⁇ m.
  • the total package pressure was set so that at least 130 bar was reached with filter surface loads of 0.25 to 0.80 g / min / cm 2 .
  • the hole density of the nozzle plates used can be set between 1.5 and 6.0 holes / cm 2 .
  • the diameter d of the capillary bores in the nozzle plate is selected so that the apparent wall shear rate of the melt within the capillaries is between 5,000 and 25,000 s "1 (for PET see Tab. 2). This ensures additional heating of the melt.
  • the capillary diameter is chosen between 0.08 mm and 0.12 mm.
  • the diameter of the individual capillary bores in the nozzle plate does not have to be constant over the cross section of the nozzle plate, but can be adapted in inverse proportion to the temperature gradient measured on the surface of the nozzle plate.
  • the deviation between central and near-edge holes is a maximum of 0.2 d, preferably 0.1 d.
  • the exit speeds are limited by two effects: First, a sufficiently high spraying speed of at least 7 m / min is necessary to avoid the risk of cohesive breaks. On the other hand, an upper limit of 20 m / min must not be exceeded, since otherwise flow anomalies can occur, which are noticeable in an irregular melt leakage from the capillary bore (corkscrew effect).
  • the length L of the capillaries is chosen so that a sufficiently high melt pressure is achieved with the inevitably low filter surface load in front of the nozzle plate. This means that there are sufficient pressure reserves for an even radial distribution of the melt.
  • the pressure in front of the nozzle plate should be between 50 and 100 bar, preferably between 70 and 100 bar.
  • an L / d ratio between 2 and 5 can be selected (see Table 2).
  • T Ra nd - T M _tte measured as the surface temperature difference on the nozzle plate between the center and edge of the nozzle plate in the claimed titer range according to the following relationship about the temperature difference between the spinning beam heating and the polymer
  • the direct supply of the required heat via the walls of the nozzle package was surprisingly effective.
  • additional heat was introduced into the spin pack to heat the melt near the wall. This requires a correspondingly long dwell time in the nozzle package, which, however, could be set with appropriately shaped package internals due to the low package throughput in the claimed titer range.
  • the heat required to set the desired temperature profile is transferred to the melt partial flow near the wall via metallic heat conduction in the nozzle package.
  • This partial melt stream near the wall can either be heated to the required excess temperature over the entire length H of the inner wall of the spin pack in contact with the melt or only on a partial section 1 of the inner wall in contact with the melt, in which case the required one
  • Overtemperature ⁇ Tscmeize pickling is increased according to the area ratio H / 1. This extra heated
  • the surface should then preferably be provided in the lower part of the spin pack at the level of the nozzle plate and finally with the lower edge of the nozzle plate in the form of a heating frame with through openings for the spin packs and with a heating which can be controlled independently of the spinning beam. Separate heating of the spinning beam and the product line is a prerequisite for setting the required temperature difference.
  • the actual draft zone speed range from 200 - approx. 2500 m / min, with an unbalanced profile, slow (not yet drawn) and fast (already drawn) filaments are present in this (fictitious) cross-section. Filaments near the edge without a temperature increase reach their final speed much earlier than filaments in the center of the Bundle of threads. The result is a restless thread run mainly caused by the suction effect of the faster filaments, which suck the slower filaments. In extreme cases, individual filaments stick together and thread breaks occur. The restless thread run has a clear impact on the yarn uniformity. Existing inequalities are increasing here (see Fig. 2).
  • the draft zone extends to the solidification point h 9 s% of the melt, which is defined in such a way that 98% of the thread take-off speed is reached here.
  • the flow field was displayed using a laser light section system from ILA. With this method, the examination area is illuminated in different cutting planes with a powerful, double-pulsed NdYAG laser. An aerosol is applied to the blown air, which reflects the laser pulses in the area of the cutting plane. The visualization is carried out with a high-resolution CCD video camera. The speed and the direction of flow are represented by a vector field.
  • the direction of the vector arrows results from the spatial displacement of the droplets and the velocity of the droplets from the spatial displacement of the droplets and the time interval between two pulses. It has been found that one-sided blowing creates strong inhomogeneities in the thread bundle. These are mainly caused by the Stowage zone in front of the thread bundle and through the swirl area in the lee of the thread bundle (see Fig. 1). These disadvantages are eliminated with the method according to the invention.
  • the distance h to the nozzle plate, on which a balanced temperature profile already exists due to cooling of the filaments near the edge, must be smaller than the distance of the solidification point from the nozzle plate (see Fig. 3).
  • the setting is made by increasing the temperature of the melt heating, for example using laser Doppler anemometry.
  • the thread speeds of near-center and central filaments are measured simultaneously, while the temperature of the melt heating is adjusted so that the speed difference between near-center and central filaments is less than 40% of the pull-off speed of the yarn and preferably less than 15%.
  • the measuring position is located immediately upstream of the drafting zone, which can be represented in the claimed titer range depending on the Filament carefullysatz m F n [g / min], the withdrawal speed from ug z [m / min] and the draft ratio W as:
  • the still molten thread is therefore not directly exposed to the blowing air according to the invention, but is first cooled in a so-called recess.
  • the solidification point of the yarn must not lie within the recess, because otherwise the strong suction effect of the filaments, which starts early in this titer range, causes large amounts of air to be sucked into the recess, causing turbulence in this region.
  • the solidification point must not be too far outside the recess, otherwise the still soft thread is exposed to the surrounding air for too long without protection.
  • the freezing point is therefore chosen so that it is just outside the protected recess.
  • the solidification point can be set specifically by the temperature of the polymer.
  • the absolute level of the necessary process temperature can be found at
  • T melt 30S - 25 ' f
  • a general problem in the manufacture of ultrafine microfilaments is the strong reaction of spinning stability to temperature inhomogeneities. Additional radiation heating in the area of the recess has proven to be annoying (poor thread uniformity), presumably by reducing the thread tension, in particular the outer filaments, which are thus more sensitive to disturbances from the environment (air movement due to the suction effect of the filaments starting).
  • the outer filaments are heated on one side, since the side of the filaments which faces the radiating surface is heated more intensely. Recordings with the laser cutting process showed rapid air changes in the recess area caused by the high speed of the filaments in this area. The build-up of a resting, warm air cushion is hindered. An active supply of heat from the outside to the filaments is therefore predominantly by radiation and not by convection.
  • a passive (non-heated) return only prevents the outer filaments from cooling too quickly.
  • a high level of spinning security is achieved through careful temperature control of the melt by coordinating the size of the heat-transfer surface, the heating temperature and the residence time of the melt in the area of the heating.
  • the size of the heat-transferring surface and the contact time of the partial melt flow running outside for the heat transfer with the inner wall of the package determine the amount of heat that can be transferred.
  • a simple key figure for the Heat transfer can be defined from the ratio of contact length 1 and contact time t to:
  • ⁇ stands for the portion occupied by the melt in a specific cross-section of the spin pack and can be constant in sections or a function of the height.
  • the overtemperature ⁇ T melt heating set was 21 K. Good spinning results were achieved in both cases.
  • the partial melt flow near the wall is either heated to the required excess temperature over the entire length H of the melt-contacting inner wall of the spin pack or only on part of the melt-contacting inner wall with an increased excess temperature ⁇ Ts ch meize-Behe_zung x H / 1 corresponding to the area ratio H / 1.
  • This extra heated surface is then preferably to be provided in the lower part of the spin pack at the level of the nozzle plate in the form of a heating frame with heating to be regulated independently of the spinning beam.
  • the deflection of the individual filaments transversely to the longitudinal axis of the spinning beam is less than 20 mm. According to Fourne (p. 195), vibrations in the blow shaft of 30 - 100 mm are otherwise common.
  • the strong and early suction effect of the filament coulter means that the thread curtain is also blown through in no longer take place in the upper area of the blow duct. Therefore, pressure equalization and laminarization of the air sucked in from the environment is required in this area.
  • the amount of air sucked in in this area can be controlled directly via the targeted setting of a pressure loss, for example by a different number of fine fabric layers or perforated sheets.
  • the sucked-in air is passed through a device for pressure equalization before reaching the filaments and, if necessary, laminated by guide elements (e.g. honeycomb straightener).
  • guide elements e.g. honeycomb straightener
  • the pressure loss caused by the thread take-off depends on the take-off speed ⁇ zu, single filament titer (in denier) and number of filaments n according to the following relationship:
  • the additional pressure loss to be applied via a pressure equalization device must not be greater than (2 to 3) • ⁇ p.
  • the individual bundles of threads are separated by dividers so that a symmetrical air profile is created transverse to the longitudinal axis of the spinning beam.
  • a preferred embodiment of the separating plates is the arrangement of a separating plate common to two adjacent bundles of threads on the division axis (Fig. 4, left).
  • two separating sheets per thread bundle are arranged following the thread run and inclined in the direction of the thread axis, symmetrically to this (Fig. 4 right). Sealing systems at points A prevent the intake of incorrect air.
  • the chambers formed in this way are open towards the bottom, towards the rear and towards the front.
  • the passage surface itself can be largely closed up to the thread bundle or can be porous (e.g. perforated plate) in order to counter the compensating flow with a targeted resistance.
  • PET polymer with an IV of 0.635 dl / g was melted in a conventional extruder and fed to the spinning beam at a product temperature of 300 ° C. via static mixers and the product line.
  • the spinning beam with 6-gang spinning pump, melt distributor and 6 nozzle packs was set to 311 ° C.
  • the throughput per partial pump flow was 19.1 g / min.
  • the melt was in the nozzle package first through two layers of metal sand with increasingly finer grain, then through a multi-layer metal mesh filter, the finest layer of which consisted of a twill weave with 5 ⁇ m, and then through a distributor plate and a second multi-layer metal mesh filter, the finest layer consisted of a twill braid with 15 ⁇ m, an unmounted filter disk made of metal mesh filter with 17000 mesh / cm 2 lying flat on the nozzle plate and subsequently through the nozzle plate with a diameter of 96 mm, the fine bores of which had a capillary diameter of 0.12 mm and a capillary length of 0.48 mm, pressed.
  • the distance between the fine bores on the nozzle plate was 5.8 mm.
  • the filaments emerging from the nozzle passed through an unheated zone largely shielded from the direct blowing directly after the nozzle of 55 mm in length.
  • the thread in the upper area by means of controlled self-suction of the filaments, was supplied with ambient air of approximately the same order of magnitude as on the blower side of the transverse blowing. 485 mm after emerging from the spinneret, the filaments were loaded with preparation in a double oiler system, using oiling stones with special ceramic surfaces. An emulsion with a water content of ⁇ 10% was applied, with 2/3 of the amount applied to the thread in the first oiler being fed to the thread bundle and the remaining third in the second oiler. The thread tension measured after the oiler was 26 cN. The thread was bundled through the rest of the blowing and drop chute over a distance of 2 m before being subjected to an air pressure of 0.6 bar in an interlacer.
  • Any conventional titers in the usual fineness ranges for normal and high count titers can be run on the spinning system designed according to this process without major modifications.

Landscapes

  • 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)

Abstract

L'invention concerne un procédé de production d'un fil continu synthétique ultrafin à base de polyester ou de polyamide, dans la plage de 0,25 à 0,9 deniers par filament préorienté, par filage par fusion pour des vitesses de tirage comprises entre 2000 et 6000 m/min avec une grande sécurité de filature. On peut ajouter au polyester ou au polyamide, un deuxième polymère amorphe non miscible dans une quantité de 0,05 à 5 % en poids. L'invention est caractérisée par le réglage d'un profil de température équilibré dans la section transversale du fil continu avant d'atteindre la zone d'étirage, ainsi que par l'adaptation appropriée entre la longueur de retour et le point d'étirage des filaments dans le puits à soufflerie.
EP00927131A 1999-05-14 2000-05-02 Procede de production de fils synthetiques ultrafins Expired - Lifetime EP1185728B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19922240A DE19922240A1 (de) 1999-05-14 1999-05-14 Verfahren zur Herstellung von ultrafeinen synthetischen Garnen
DE19922240 1999-05-14
PCT/EP2000/003975 WO2000070132A1 (fr) 1999-05-14 2000-05-02 Procede de production de fils synthetiques ultrafins

Publications (2)

Publication Number Publication Date
EP1185728A1 true EP1185728A1 (fr) 2002-03-13
EP1185728B1 EP1185728B1 (fr) 2003-12-10

Family

ID=7908066

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00927131A Expired - Lifetime EP1185728B1 (fr) 1999-05-14 2000-05-02 Procede de production de fils synthetiques ultrafins

Country Status (5)

Country Link
US (1) US6420025B1 (fr)
EP (1) EP1185728B1 (fr)
AT (1) ATE256206T1 (fr)
DE (2) DE19922240A1 (fr)
WO (1) WO2000070132A1 (fr)

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2647746B1 (fr) * 2010-11-29 2016-08-10 Toray Industries, Inc. Fil de polyamide contenant des filaments ultrafines et procédé et dispositif de filage à l'état fondu pour la production de ce fil
CN102864506B (zh) * 2012-09-26 2016-05-11 江苏纺科新复合材料有限公司 无定形、高取向聚乙烯长丝的制备方法
CN105369375A (zh) * 2015-12-04 2016-03-02 浙江古纤道新材料股份有限公司 一种中强丝及其加工方法
CN106435784B (zh) * 2016-11-15 2018-07-17 东华大学 一种聚合物纤维负压熔融纺丝成形方法
FI3692188T3 (fi) * 2017-10-06 2023-12-05 Chemiefaser Lenzing Ag Laite filamenttien pursottamiseksi ja sulakehrättyjen kuitukankaiden valmistamiseksi
CN113969452A (zh) * 2021-10-11 2022-01-25 江苏嘉通能源有限公司 一种高光泽度拉伸变形丝的生产加工设备及方法

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Publication number Priority date Publication date Assignee Title
US4181697A (en) * 1975-04-05 1980-01-01 Zimmer Aktiengessellschaft Process for high-speed spinning of polyamides
JPS5825762B2 (ja) * 1979-04-05 1983-05-30 東洋紡績株式会社 細繊度糸の溶融紡糸方法
DE3026451C2 (de) * 1980-07-12 1985-03-14 Davy McKee AG, 6000 Frankfurt Verfahren zur Herstellung hochfester technischer Garne durch Spinnstrecken und Verwendung von durch das Verfahren hergestellten Garnen
DE3036683C2 (de) * 1980-09-29 1985-01-24 Davy McKee AG, 6000 Frankfurt Verfahren zum Schmelzspinnen von synthetischen Polymeren
US4514350A (en) * 1982-09-23 1985-04-30 Celanese Corporation Method for melt spinning polyester filaments
US5250245A (en) * 1991-01-29 1993-10-05 E. I. Du Pont De Nemours And Company Process for preparing polyester fine filaments
JP2653668B2 (ja) * 1988-04-22 1997-09-17 東レ株式会社 溶融紡糸装置および溶融複合紡糸装置
CA2101788C (fr) * 1991-01-29 2002-05-28 Robert J. Collins Preparation de filaments fins de polyester
JP2842243B2 (ja) * 1994-09-13 1998-12-24 東レ株式会社 溶融紡糸装置
DE19707447A1 (de) * 1997-02-25 1998-08-27 Zimmer Ag Verfahren zur Verarbeitung von Polymermischungen zu Filamenten

Non-Patent Citations (1)

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Title
See references of WO0070132A1 *

Also Published As

Publication number Publication date
US6420025B1 (en) 2002-07-16
WO2000070132A1 (fr) 2000-11-23
EP1185728B1 (fr) 2003-12-10
ATE256206T1 (de) 2003-12-15
DE19922240A1 (de) 2000-11-16
DE50004736D1 (de) 2004-01-22

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