EP0263603A1 - Frisage de fils de polyester - Google Patents

Frisage de fils de polyester Download PDF

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Publication number
EP0263603A1
EP0263603A1 EP87308038A EP87308038A EP0263603A1 EP 0263603 A1 EP0263603 A1 EP 0263603A1 EP 87308038 A EP87308038 A EP 87308038A EP 87308038 A EP87308038 A EP 87308038A EP 0263603 A1 EP0263603 A1 EP 0263603A1
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Prior art keywords
yarn
speed
mpm
texturing
draw
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German (de)
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EP0263603B1 (fr
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Cecil Everett Reese
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EIDP Inc
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EI Du Pont de Nemours and Co
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    • D—TEXTILES; PAPER
    • D02—YARNS; MECHANICAL FINISHING OF YARNS OR ROPES; WARPING OR BEAMING
    • D02J—FINISHING OR DRESSING OF FILAMENTS, YARNS, THREADS, CORDS, ROPES OR THE LIKE
    • D02J1/00—Modifying the structure or properties resulting from a particular structure; Modifying, retaining, or restoring the physical form or cross-sectional shape, e.g. by use of dies or squeeze rollers
    • D02J1/22—Stretching or tensioning, shrinking or relaxing, e.g. by use of overfeed and underfeed apparatus, or preventing stretch
    • 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
    • D01F6/78—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from copolycondensation products
    • D01F6/84—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from copolycondensation products from copolyesters
    • D—TEXTILES; PAPER
    • D02—YARNS; MECHANICAL FINISHING OF YARNS OR ROPES; WARPING OR BEAMING
    • D02G—CRIMPING OR CURLING FIBRES, FILAMENTS, THREADS, OR YARNS; YARNS OR THREADS
    • D02G1/00—Producing crimped or curled fibres, filaments, yarns, or threads, giving them latent characteristics
    • D02G1/02—Producing crimped or curled fibres, filaments, yarns, or threads, giving them latent characteristics by twisting, fixing the twist and backtwisting, i.e. by imparting false twist
    • D02G1/0286—Producing crimped or curled fibres, filaments, yarns, or threads, giving them latent characteristics by twisting, fixing the twist and backtwisting, i.e. by imparting false twist characterised by the use of certain filaments, fibres or yarns

Definitions

  • This invention concerns improvements in and relating to texturing yarns, and is more particularly concerned with improved polyester draw-texturing feed yarns having a capability of being draw-textured at high speeds without excessive broken filaments and with other advantages, to such high speed process of draw-texturing, and to a process for preparing such feed yarns.
  • Any broken filaments are undesirable, since they may cause difficulties, and even yarn breaks, during subsequent processing, and also fabric defects.
  • the number of broken filaments that may be tolerated in practice will depend upon the intended use for the textured yarn and eventual fabric. In practice, in the trade, the ends of the bobbin are examined for broken filaments, and the number of protruding broken filaments is counted so as to give a measure of the probable number of broken filaments in the yarn of that package. The total number of these broken filaments counted is then divided by the number of pounds in the package and expressed as BFC. For certain end uses, the maximum that can be tolerated is between 0.5 and 0.6 BFC, i.e., between 5 and 6 broken filaments for every 10 lbs.
  • DTFY polyester multifilament draw-texturing feed yarn
  • the present invention provides a solution to this problem.
  • a process whereby an improved new polyester feed yarn can be draw-textured at high speeds to give yarns of satisfactory texture without excessive BFC.
  • improved new polyester feed yarns are provided, whereby this problem can be solved.
  • a process for preparing these improved new feed yarns there is provided a process for preparing these improved new feed yarns.
  • use of the feed yarns can provide other advantages, even when increased speed of texturing is not necessary or desirable.
  • a continuous process for preparing polyester draw-texturing feed yarns involving the steps of first forming a molten polyester by reaction (a) of ethylene glycol with terephthalic acid and/or esters thereof, followed by polycondensation (b), these reaction steps being carried out in the presence of appropriate catalysts therefor, and then melt-spinning the resulting molten polyester into filaments and withdrawing them at a speed of about 3,000 to 4,000 mpm, preferably at speeds in the lower portion of this range, such as about 3,000 to 3,200 mpm, to provide partially oriented yarns of low crystallinity, wherein the polyester is modified by introducing into the polymer, as a solution in ethylene glycol, a substance selected from the group consisting of trimesic acid, trimellitic acid or an ester thereof in amount as indicated approximately by the line AB of Figure 1 of the accompanying drawing.
  • a partially oriented polyester multifilament draw-texturing feed yarn of low crystallinity as shown by a boil-off shrinkage of about 45% and an elongation to break of about 155%, consisting essentially of polymerized ethylene terephthalate residues chain-branched with trimellitate or trimesate residues in amount about 6 MEQ, and of relative viscosity about 21 LRV.
  • the boil-off shrinkage may be about 20-25%, the elongation to break about 133%, and the amount of trimesate or trimellitate residues about 4 MEQ.
  • the elongation (to break) is a measure of orientation (as is birefringence), the elongation being reduced as the spin-orientation is increased, while the shrinkage is affected by the crystallinity, as well as the orientation, and is reduced as the crystallinity increases.
  • a multifilament draw-texturing feed yarn that has been prepared by polymerizing ethylene and terephthalate derivatives with trimesate or trimellitate residues acting as chain-brancher and by spin-orienting at a withdrawal speed of at least about 3,000 to 4,000 mpm, preferably a lower speed, such as about 3,000 to 3,200 mpm, and that is capable of being draw-textured at a speed of at least 1,000 mpm to provide a package of textured yarn with not more than about 0.5 BFC and a TYT of over 20.
  • a process for preparing a false-twist textured yarn wherein a multifilament polyester feed yarn is subjected to s imultaneous draw-texturing at a speed of at least 500 mpm, the feed yarn consists essentially of polymerized ethylene terephthalate residues and of trimesate or trimellitate residues acting as a chain-brancher, and the resulting package of textured yarn has not more than about 0.5 BFC and over 20 TYT.
  • the new feed yarns and their process of preparation make possible the provision of textured polyester yarns having increased dye-uptake and/or improved crimp, as compared with prior commercial polyester yarns textured under comparable conditions.
  • the amount of chain-brancher will depend on various considerations, especially the spinning speed, since it will generally be desirable to use as much chain-brancher as possible to obtain increased advantages in certain respects, whereas the amount should not be so much as will cause spinning difficulties, and this will depend on the withdrawal speed in the sense that the desired amount of chain-brancher will be reduced as the withdrawal speed is increased. Furthermore, an advantage in dye uniformity of the textured yarns (and fabrics) has been obtained by withdrawing the filaments of the feed yarns at lower speeds within the speed range indicated.
  • the preparation of the feed yarn is preferably by a continuous process in which the steps of polymerization and spinning are coupled together, because the alternative process that has been carried out in some plants of first making the polyester and then extruding it in the form of ribbons which are cooled with water and cut into pellets or flakes, which are then remelted for a separate process of spinning into filaments, can introduce uncertainties and problems, which can lead to variability in the resulting feed yarn filaments. It will be emphasized that uniformity of the polyester filaments in the feed yarn is of great importance in achieving high draw-texturing speeds without excessive broken filaments.
  • trimellitic acid or trimesic acid, or a derivative thereof in small amounts (e.g. 4-6 MEQ) as a chain-brancher in the process of preparation of the polyester, which is accordingly a copolymer. It is believed that such chain-branching has not previously been used commercially for the objective of producing a feed yarn capable of being draw-textured at high speeds, e.g., of 1,000 mpm, without excessive broken filaments, e.g., not more than about 0.5 BFC, while giving desirably bulky yarns, e.g. of TYT over 20. It is not, however, new to suggest the use of chain-branchers for other purposes.
  • U.S.P. 4,092,299 suggests a high draw ratio polyester feed yarn and its draw-texturing and companion U.S.P. 4,113,704 suggests a polyester filament-forming polymer and its method of production. Since the two disclosures are practically identical, only U.S.P. 4,092,299 will be discussed.
  • MacLean et al., U.S.P. 4,092,299 suggests improving productivity by using a chain-brancher in such amount that the polyester has 1-15 or 2-14 microequivalents of reactive branching sites per gram of polymer (MEQ), and preferably 5-12 MEQ.
  • MEQ reactive branching sites per gram of polymer
  • the increased productivity is obtained by increasing the draw ratio during draw-texturing and/or increasing the withdrawal speed during filament formation, because the orientation (birefringence) of the feed yarn is reduced by using chain-brancher.
  • the optimum level of chain branching is discussed in column 11, and will depend on many factors. Pentaerythritol is sug gested as the preferred chain brancher, but is not desirable according to the present invention, because it volatizes during polymer preparation.
  • a volatile chain-brancher such as pentaerythritol
  • pentaerythritol may be quite adequate for operation at low texturing speeds and for MacLean's objective of increasing productivity, it is not a solution to the problem of providing a draw-texturing feed yarn capable of draw-texturing at a speed of, e.g., 1,000 mpm without excessive broken filaments, e.g., not more than about 0.5 BFC, while giving a desirably bulky yarn, e.g., over 20 TYT.
  • a chain-brancher that is adequately stable (both in monomer form during processing and polymerization and in polymeric form during formation of the polymer and spinning into filaments and subsequent processing), not so volatile as to cause problems and variability during preparation of the polymer, and that is soluble in the catalyzed glycol for ease of addition to the reaction.
  • Trimellitic acid and its ester derivatives fulfill all these functions, and it is believed that trimesic acid and its ester derivatives would have similar functions and advantages.
  • MacLean is not limited to the use of pentaerythritol, but covers other chain-branching agents having a functionality greater than 2, that is containing more than 2 functional groups such as hydroxyl, carboxyl or ester. Accordingly, other polyhydroxy chain branchers are mentioned, and aromatic polyfunctional acids or their esters (column 7). Trimesic acid, trimethyl trimesate and tetramethyl pyromellitate are specifically mentioned in lines 41-42, but are not used in the Examples.
  • trimer acid is used in amounts 11,800 and 23,600 ppm (said to be 6.5 and 12.9 MEQ, but calculated instead as 12.9 and 21.1 MEQ, respectively) and mellitic acid (benzene hexacarboxylic acid) is used in amounts 9.8 and 14.7 MEQ.
  • the only texturing speed mentioned by MacLean is 200 ypm (column 10, line 15).
  • the withdrawal (spinning) speeds vary between 3,400 and 4,400 ypm in Examples 2 and 4, and are 5,500 and 6,000 ypm in Example 6, and are otherwise 3,400 ypm.
  • Productivity MacLean's objective), it was said, "definitely increases with spinning speed over most of the speed range capability of the equipment used" (column 11, lines 58-60), and it was impossible to determine whether the productivity curve continued to increase with spinning speed.
  • the chain-brancher is conveniently dissolved in the catalyzed EG solution that is used in an otherwise conventional ester interchange reaction between DMT and EG using appropriate catalysts to prepare the prepolymer. Further polymerization (sometimes referred to as finishing) is carried out under vacuum with an appropriate material such as phosphorus again in conventional manner to prepare a polymer of the required viscosity (measured as LRV).
  • the resulting polymer is then preferably passed continuously to the spinning unit without intermediate conversion into flake and remelting, and is spun to prepare partially oriented filaments of low crystallinity at withdrawal speeds of 3,000 mpm or more, with particular care in the spinning conditions to provide uniform filaments, to minimize breaks during the spinning or during subsequent draw-texturing operations at high speed.
  • TMTM has three reactive carboxyl groups of which two are reacted in the molecular chain. The other one reacts to form a side chain which is referred to as a chain branch. If and when these chain branches react with another molecule, a crosslink is formed. Obviously there are many more chain branches than crosslinks formed. Also because there are only three of these (carboxyl) reactive sites in TMTM, there is only one for chain branching. Therefore, the equivalent weight and the molecular weight are the same. 0.15% by weight of TMTM (on the weight of the polymer) is the same as 1,500 ppm and is almost 6 MEQ (5.95). Similarly, 0.10% of TMTM (1,000 ppm) is almost 4 MEQ. Trimesic acid has the same molecular weight as trimellitic acid, so the same values apply.
  • chain-brancher has been noted to provide significantly higher spinning tensions, than with unmodified polymer. This is believed to be an important advantage in the process of the invention.
  • an important advantage in the resulting textured yarns, obtained by draw-texturing of the improved modified feed yarns of the present invention, is the low number of broken filaments (BFC) obtained even when the texturing is carried out at the very high speeds indicated.
  • the resulting textured yarns also have other advantages.
  • the dyeability, or dye-uptake is improved. This, in retrospect, may not seem so surprising, since there have been several prior suggestions of using other trifunctional chain-branching agents in polyester polymers in much larger amounts (0.5-0.7 mole percent, i.e. about 10 times as much) in order to obtain better dyeability, oil-stain release or low pilling, as mentioned in column 1 of MacLean.
  • a further improvement in the textured yarns is the improved crimp properties, as shown by the CCA and TYT values in the Examples.
  • This is an important advantage commercially. In practice, it is necessary to operate the draw-texturing process so as to obtain textured yarn having at least equivalent crimp properties to those that are already available commercially.
  • the crimp properties can be adjusted to some extent by varying the draw-texturing conditions, and this can also depend on the skill and knowledge of the texturer, who may be forced to reduce the texturing speed in order to improve the crimp properties of the resulting textured yarn.
  • a desirable objective for the texturer is to achieve or surpass the target crimp properties, while reducing his costs by operating at the maximum possible speed.
  • the invention is further illustrated in the following Examples.
  • the yarn properties are measured as in U.S. Patent 4,134,882 (Frankfort and Knox) except as follows.
  • BFC Broken Filament Count
  • TYT Text Yarn Tester measures the crimp of a textured yarn continuously as follows.
  • the instrument has two zones. In the first zone, the crimp contraction of the textured yarn is measured, while in the second zone residu al shrinkage can be measured. Only the first zone (crimp contraction) is of interest, however, for present purposes.
  • the textured yarn is taken off from its package and passed through a tensioning device which increases the tension to the desired level, 10 grams for 160 denier yarn (0.06 gpd). The yarn is then passed to a first driven roll, and its separator roll, to isolate the incoming tension from the tension after this first roll. This roll is hereafter referred to as the first roll.
  • the yarn is passed through a first tension sensor, and through an insulated hollow tube, which is 64.5 inches ( ⁇ 164 cm) long and 0.5 inches (1.27 cm) in diameter and which is maintained at 160°C, to a second set of rolls, a driven roll and a separator, which isolate the tension in the yarn in the first zone from that in the next zone, and to a third set of rolls, a driven roll and a separator roll, which further isolates the tension in zone one from the tension in zone two.
  • the circumferential speed of roll three is set enough faster than roll two so that roll two imparts 2 grams tension to a 160-denier threadline ( ⁇ 0.013 gpd), and rolls two and three are controlled by the first tension sensor at such speeds as to insure that the tension in zone one is that desired, ( ⁇ 0.001 gpd).
  • the speed of the fourth set of rolls is controlled by the second sensor and that tension is set at 10 grams of a 160-denier yarn or 0.0625 gpd.
  • the total tensions will change with a change in denier of the textured yarn. As indicated, only the relative speeds in and out of the first zone are of interest in this instance.
  • the TYT is calculated as a percentage from the circumferential speed V1 of the first roll and V2 of the second roll: -
  • CCA Cosmetic Coefficient Contraction
  • a looped skein having a denier of 5,000 is prepared by winding the textured yarn on a denier reel. The number of turns required on the reel is equal to 2,500 divided by the denier of the yarn.
  • a 500 gm. weight is suspended from the looped skein to initially straighten the skein. This weight is then replaced by a 25-gram weight to produce a load of 5.0 mg/denier in the skein.
  • the weighted skein is then heated for 5 minutes in an oven supplied with air at 120°C, after which it is removed from the oven and allowed to cool.
  • Copolymer for the new and improved feed yarn for draw texturing is prepared by copolymerizing dimethyl terephthalate (DMT), ethylene glycol (EG) and about 4.3 MEQ trimethyl trimelli tate (TMTM) (about 4.3 microequivalents per gram of DMT).
  • 4.3 MEQ is 0.11% of TMTM per gram of copolymer.
  • the TMTM is dissolved in and added with the catalyzed glycol. At the concentration required, the TMTM is completely soluble in the catalyzed glycol and neither enhances nor inhibits the catalytic properties of the manganese and antimony salts which are used as catalysts. Catalyst contents are identical to those used for standard PET.
  • the required amount of phosphorus is added when the exchange is complete and before proceeding with polymerization to inactivate the manganese catalyst during polymerization.
  • 0.3% of TiO2 based on DMT is added, as a glycol slurry to the material, after the exchange is complete and before the polymerization, to provide opacity in the resulting DTFYs. It is found that the addition, exchange and polymerization process conditions used for standard PET are acceptable. Indeed, the polymerization proceeds faster for the new copolymer. In the preparations used herein, both the copolymer and the standard (linear polymer) PET (used as control) were prepared in a continuous polymerization process.
  • the resulting new copolymer has a LRV slightly higher than that of the control, somewhat more than 21 vs. standard polymer of about 20.5.
  • the new copolymer also had a slightly higher melt viscosity than the control. This increased melt viscosity was not enough to cause problems in polymer making, polymer transport or spinning. The polymer is pumped from the continuous polymerizer to the spinning machines where it is spun into the new and improved feed yard for draw texturing.
  • the new copolymer is pumped through a filter pack and thence through a spinneret which has 34 capillaries, each 15 ⁇ 60 mils (diameter ⁇ length). Spinning temperatures are somewhat higher than those required for standard PET (about 300°C vs. about 293°C for the standard PET).
  • the extruded filaments are quenched by passing room temperature air across the filaments below the spinneret, using the same cross-flow system as for the standard PET filaments. The amount of air flow across the filaments is adjusted to obtain the best operability. Finish is applied after the filaments are quenched. Filaments are then converged into a threadline and handled as a threadline thereafter.
  • This threadline is passed at 4,000 ypm (3,600 mpm) around the first godet, called a feed roll, thence to a second godet, called a let-down roll, through an interlace device and thence to an appropriate wind-up at about 4,000 ypm.
  • the circumferential speed of the let-down godet is adjusted to give the tension between the feed and let-down godets that provides the best spinning continuity.
  • the DTFY has tensile and other physical properties that are acceptable for DTFY. These properties are set out and compared with standard PET control DTFY in Table IA. Because the new DTFY is spun at 4,000 ypm, but has orientation properties (elongation and birefringence) more like standard POY spun at 3,500 ypm, standard POY spun at each speed was prepared and used as control. The crystallinity of the new DTFY is greater than either control (density and C.I.).
  • Each DTFY is textured on a laboratory model, Barmag FK6-900 texturing machine, which is equipped for friction false twist texturing, with as disc stack a Barmag T-6 arrangement, using a 0-9-0 array of "Kyocera" ceramic discs with a spacing of 0.75 mm. Texturing speed comparisons are made over the speed range from 750 to 1,150 mpm, incremented in 100 mpm intervals. The draw ratio to avoid surging for each yarn is determined and used. The temperatures of the first and second heater plates are set at 220°C and 190°C, conditions used by many in the trade for PET yarns. During texturing, practically no br eaks occurred with the new yarn at any of these speeds.
  • Table IIB shows that the performance of the DTFY decreases as the TMTM content is decreased below about 4 MEQ.
  • Example 1 is repeated for items S, X, V and Y, except that the concentration of TMTM is changed as shown in Table IIA.
  • concentration of TMTM is changed as shown in Table IIA.
  • the TMTM concentration is increased slightly further to 6.3 MEQ, spinning continuity is so poor, with individual filaments pulling away from the spinneret, that this either causes the spinning threadline to break or the free end filament is recaptured by the threadline and carried to the wind-up.
  • Each such yarn is textured on a Barmag M-80, but otherwise as in Example 1. Operability was excellent, even at 1,000 mpm. Each textured yarn was evaluated for textured yarn properties, and compared with controls E and B spun at 3,500 ypm and 4,000 ypm without TMTM in Table IIB. Broken filaments are much fewer of the TMTM-containing yarns than for the control, but item X (containing less than 1 MEQ of TMTM) gave some results of borderline acceptability.
  • the TYT crimp properties of these yarns is best understood from the plot of TYT vs. TMTM content (MEQ) shown in Figure 2. The preferred concentration is about 4 MEQ of TMTM at this withdrawal speed (4,000 ypm).
  • This Example shows the spinning of the new yarn at a spinning speed of 3,500 ypm (3,200 mpm), in the preferred range, and the change in properties as the TMTM content is varied at this spinning speed, following essentially Example 1 in other respects.
  • 3500 ypm (3,200 mpm) it is found that the concentration of TMTM can be increased to levels of 6.3 MEQ and still obtain feed yarn acceptable for draw texturing. Polymers can be made without serious problems at concentrations even higher than about 6.3 MEQ, even up to about 8 MEQ.
  • the melt viscosity for the required Relative Viscosity increased sig nificantly.
  • the increase is, however, readily compensated for in polymer making and spinning at 3,500 ypm (3,200 mpm) by moderate and acceptable increases in temperature.
  • TMTM concentration is increased from about 6.3 MEQ to about 8 MEQ melt viscosity increases sharply, for the desired relative viscosity, and I could not compensate for this increase in melt viscosity by using higher temperatures in polymer making, polymer transport and especially in spinning.
  • the higher melt viscosity sharply increases the melt fracture of the spinning filaments with the accompanying defects in the as-spun yarn and a very sharp increase in the number of spinning breaks.
  • the usual corrective actions of adjusting spinning temperature, varying capillary dimensions and adjusting quench did not overcome the problems, especially at a TMTM concentration of about 7.9 MEQ and higher.
  • Table III compares the spinning conditions used and the properties of the DTFY for the two TMTM-chain branched yarns selected for further evaluation and a control without any TMTM.
  • the best spinning temperature found for each polymer summarized in the Table.
  • the denier of each feed yarn was set during yarn preparation to give approximately 150 denier textured yarn.
  • Each yarn was textured at texturing speeds from 750 mpm to 1,050 mpm, incremented in 100 mpm intervals, on the FK6-900 as in Example 1, and the results are summarized in the Table.
  • the BFC is not dramatically better for the TMTM chain branched yarn than for the control.
  • both TMTM chain branched yarns show a much lower BFC level than the control, which is unacceptable.
  • the higher level of TMTM chain branched yarn is much better in BFC than the lower level.
  • both TMTM chain branched yarns have higher dye uptake than the control and again the higher dye uptake than the control and again the higher level of TMTM chain branched yarn has the higher dye uptake.
  • Significantly better dye uniformity is noted at these lower preferred spinning speeds, which are contrary to the preference expressed by MacLean, who had an entirely different objective.

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  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)
  • Artificial Filaments (AREA)
  • Polyesters Or Polycarbonates (AREA)
  • Woven Fabrics (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
EP87308038A 1986-09-12 1987-09-11 Frisage de fils de polyester Expired - Lifetime EP0263603B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US90729986A 1986-09-12 1986-09-12
US907299 1986-09-12

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EP0263603A1 true EP0263603A1 (fr) 1988-04-13
EP0263603B1 EP0263603B1 (fr) 1992-11-25

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EP (1) EP0263603B1 (fr)
JP (2) JPS6375112A (fr)
KR (1) KR900001319B1 (fr)
CN (1) CN1013690B (fr)
BR (1) BR8704682A (fr)
CA (1) CA1295800C (fr)
DE (1) DE3782798T2 (fr)
DK (1) DK475887A (fr)
ES (1) ES2035865T3 (fr)
GR (1) GR3006792T3 (fr)
IL (1) IL83875A (fr)
MX (1) MX159963A (fr)
NO (1) NO873810L (fr)
PL (1) PL267708A1 (fr)
TR (1) TR24290A (fr)
ZA (1) ZA876820B (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0294912A2 (fr) * 1987-02-11 1988-12-14 E.I. Du Pont De Nemours And Company Matériau de remplissage fibreux en polyester et procédé
US4945151A (en) * 1989-03-08 1990-07-31 E. I. Du Pont De Nemours And Company Continuous production of polyester filaments
ES2048610A1 (es) * 1990-04-05 1994-03-16 Rhone Poulenc Fibres Procedimiento para la obtencion de politereftalato de etileno modificado, fibras exentas de bolas obtenidas a partir del polimero asi modificado.
WO1994025651A1 (fr) * 1993-05-04 1994-11-10 Wellman, Inc. Etirage-texturation a alimentation a chaud pour la teinture foncee du polyester
US5756033A (en) * 1996-08-01 1998-05-26 Zimmer Aktiengesellschaft Process of making poy polyester fiber
WO2005108661A2 (fr) * 2004-04-15 2005-11-17 Invista Technologies S.A.R.L. Fils de polyester de tenacite elevee

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04114030A (ja) * 1990-09-03 1992-04-15 Teijin Ltd ポリエステルの製造法
US7892993B2 (en) * 2003-06-19 2011-02-22 Eastman Chemical Company Water-dispersible and multicomponent fibers from sulfopolyesters
JP6071785B2 (ja) 2013-07-12 2017-02-01 株式会社堀場製作所 濃度測定装置
CN104651972A (zh) * 2015-03-17 2015-05-27 江苏江南高纤股份有限公司 直接纺丝低起球聚酯毛型纤维长丝束的制造方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3771307A (en) * 1971-08-24 1973-11-13 Du Pont Drawing and bulking polyester yarns
FR2346472A2 (fr) * 1976-04-03 1977-10-28 Hoechst Ag Utilisation de filaments en polyesters reticules pour l'enlacement de meches de preparation
US4092299A (en) * 1976-06-23 1978-05-30 Monsanto Company High draw ratio polyester feed yarn and its draw texturing
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FR2346472A2 (fr) * 1976-04-03 1977-10-28 Hoechst Ag Utilisation de filaments en polyesters reticules pour l'enlacement de meches de preparation
US4092299A (en) * 1976-06-23 1978-05-30 Monsanto Company High draw ratio polyester feed yarn and its draw texturing
US4415521A (en) * 1982-03-15 1983-11-15 Celanese Corporation Process for achieving higher orientation in partially oriented yarns

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Cited By (9)

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Publication number Priority date Publication date Assignee Title
EP0294912A2 (fr) * 1987-02-11 1988-12-14 E.I. Du Pont De Nemours And Company Matériau de remplissage fibreux en polyester et procédé
EP0294912A3 (fr) * 1987-02-11 1990-03-21 E.I. Du Pont De Nemours And Company Matériau de remplissage fibreux en polyester et procédé
US4945151A (en) * 1989-03-08 1990-07-31 E. I. Du Pont De Nemours And Company Continuous production of polyester filaments
ES2048610A1 (es) * 1990-04-05 1994-03-16 Rhone Poulenc Fibres Procedimiento para la obtencion de politereftalato de etileno modificado, fibras exentas de bolas obtenidas a partir del polimero asi modificado.
WO1994025651A1 (fr) * 1993-05-04 1994-11-10 Wellman, Inc. Etirage-texturation a alimentation a chaud pour la teinture foncee du polyester
US5756033A (en) * 1996-08-01 1998-05-26 Zimmer Aktiengesellschaft Process of making poy polyester fiber
US5965259A (en) * 1996-08-01 1999-10-12 Lurgi Zimmer Aktiengesellschaft Process of making poy polyester fiber
WO2005108661A2 (fr) * 2004-04-15 2005-11-17 Invista Technologies S.A.R.L. Fils de polyester de tenacite elevee
WO2005108661A3 (fr) * 2004-04-15 2006-02-09 Invista Tech Sarl Fils de polyester de tenacite elevee

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NO873810L (no) 1988-03-14
ES2035865T3 (es) 1993-05-01
PL267708A1 (en) 1988-07-21
DK475887A (da) 1988-03-13
KR900001319B1 (ko) 1990-03-08
GR3006792T3 (fr) 1993-06-30
BR8704682A (pt) 1988-04-26
JPH0319914A (ja) 1991-01-29
IL83875A0 (en) 1988-02-29
CA1295800C (fr) 1992-02-18
CN1013690B (zh) 1991-08-28
JPS6375112A (ja) 1988-04-05
DE3782798D1 (de) 1993-01-07
DK475887D0 (da) 1987-09-11
MX159963A (es) 1989-10-17
DE3782798T2 (de) 1993-04-29
ZA876820B (en) 1989-05-30
EP0263603B1 (fr) 1992-11-25
CN87106836A (zh) 1988-05-04
IL83875A (en) 1990-09-17
KR880004151A (ko) 1988-06-02
NO873810D0 (no) 1987-09-11
TR24290A (tr) 1991-07-30

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