US3511905A - Process for the preparation of synthetic polymer filaments - Google Patents

Process for the preparation of synthetic polymer filaments Download PDF

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US3511905A
US3511905A US662527A US3511905DA US3511905A US 3511905 A US3511905 A US 3511905A US 662527 A US662527 A US 662527A US 3511905D A US3511905D A US 3511905DA US 3511905 A US3511905 A US 3511905A
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filaments
drag
temperature
pins
pin
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Horst G Martin
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Viscosuisse SA
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Societe de la Viscose Suisse SA
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    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
    • D01D5/00—Formation of filaments, threads, or the like
    • D01D5/08—Melt spinning methods
    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
    • D01D5/00—Formation of filaments, threads, or the like
    • D01D5/12—Stretch-spinning methods
    • D01D5/16—Stretch-spinning methods using rollers, or like mechanical devices, e.g. snubbing pins

Definitions

  • melt-spun oriented synthetic polymer filaments and yarns are prepared from cooled filaments by passing said filaments over a guiding device and around at least one non-drive roll and subjecting the filaments to a predetermined drag imparted by an aggregate of drag pins disposed in predetermined relationship to the filaments.
  • This invention relates to an improved process for the preparation of oriented synthetic polymer filaments by melt-spinning.
  • filaments useful as textile materials can be prepared by extruding molten synthetic polymers, such as, for example, polyamides, polyesters, copolyamides and polyolefins, through a spinneret, whereafter the filaments are quenched and wound-up as a yarn.
  • molten synthetic polymers such as, for example, polyamides, polyesters, copolyamides and polyolefins
  • the filaments should be drawn to several times their original length, whereby the molecules of the filaments are oriented along the fiber axis and the filaments gain considerably in strength.
  • Such drawing requires complex machinery including sets of rolls driven at different speeds and, eventually, arrangements for heating the filaments.
  • the drawing machinery is either combined with the spinning apparatus or is set up separately, but in any case drawing requires additional equipment, additional space, and additional labor, and the various motor-driven rolls and heating devices consume a considerable energy.
  • French Pat. 976,505 proposes to produce oriented polyamide fibers by withdrawing melt-spun fibers from the spinneret at a speed exceeding 4,500 metres per minute.
  • United States Pat. 2,604,667 describes a similar process for polyethylene terephthalate fibers using speeds exceeding 4,700 metres per minute. These processes always require very high withdrawal speeds.
  • British Pat. 903,427 observes, the quality of filaments manufactured in this manner, leaves much to be desired.
  • British Pat. 903,427 describes a process, wherein the filaments emerging from the spinneret are passed through a spinning tube having a length of about 4 metres.
  • the upper zone of the tube is heated, while the lower zone is kept at room temperature or cooled by blowing air, and the filaments which are said 3,511,905 Patented May 12, 1970 to be drawn while passing through the heated zone, are wound-up at a speed between 1,300 and 2,600 metres per minute.
  • the process according to this invention comprises extruding a molten synthetic polymer through a spinneret to form filaments, cooling said filaments and passing said filaments over a guiding device and around at least one non-driven roll, subjecting said filaments to a drag by passing them over at least one drag pin, said guiding device and said drag pin or pins being at such distance from the spinneret that the filaments, when passing said guiding device and said drag pin or pins, are cooled to a temperature above their glass transition temperature and at least 50 C. below their melting point, while said guiding device and said drag pin or pins are kept at a constant temperature at least 10 C. below the temperature of the filaments and above the dew point of the surrounding air, and orienting said filaments by withdrawing them from said drag pin or pins at a tension of less than 1.0 gram per denier.
  • the required adjustment of tempreature is not only important for orientation of the filaments, but also for their smooth run in the spinning apparatus. If the temperature of the filaments when passing the drag pins is too high, the filaments may become sticky and may adhere to each other, while at too low a temperature, electrostatic forces may cause a mutual repulsion of the filaments. As the filaments leave the spinneret at a temperature above their melting point, they must therefore be cooled, and this cooling is generally effected by the downward movement of the filaments through quiescent or transversely directed air of room temperature. As thin filaments cool down more rapidly than thick ones, the distance from the spinneret, at which the filaments are in the prescribed temperature range, differs considerably for single filaments of different deniers.
  • a polycaprolactam single filament of 7.5 denier was in the prescribed temperature range at a distance of about 70 cm. from the spinneret, while a polycaprolactam single filament of 55 denier needed a respective distance of about 390 cm. Adjustment of the distance between spinneret and drag pins is therefore an important means to regulate the temperature of the filaments at the stage of orientation.
  • the cooling of the filaments in their downward movement from the spinneret does however not progress uniformly and uninterruptedly, but, temporarily, the tem perature of the filaments rises again when they pass the drag pins.
  • This temperature rise is due to heat generated by friction of the filaments at the drag pins and by changes in the molecular arrangement of the filaments. Such changes comprise, for example, molecular orientation, and in case of crystallizing polymers, also crystallization which is triggered by orientation of the filaments.
  • the drag pins are therefore kept at a constant temperature at least 10 C. below the temperature of the filaments but above the dew point of the surrounding air in order to avoid condensation of water vapor on the drag pins. Because there is also some heat transfer from the filaments to the guiding device, this instrument is also kept at a constant temperature which is usually the same as that of the drag pins.
  • the speed at which the oriented filaments are withdrawn from the drag pins can be varied within wide limits.
  • the speeds described in the examples are between 400 and 1000 meters per minute, but higher speeds have been found to be equally suitable.
  • the withdrawal tension is less than 1.0 gram per denier, which is surprisingly low when compared with the tensions required by conventional drawing processes.
  • the denier of the filaments obtained is the same, whether or not the filaments pass over the drag pins, i.e. the oriented filaments have the same denier as the unoriented, asspun filaments.
  • This has certain advantages and permits, for example, preparation of oriented filaments of considerably higher deniers than can be obtained from air-spun filaments by conventional drawing processes.
  • the inventive process provides oriented synthetic polymer filaments of good uniformity and is applicable to all polymers which can be melt-spun.
  • the process permits to prepare single filaments of about 1-90 denier having a tenacity of about 2-5 grams per denier and a corresponding elongation at break varying between 130 and 10 percent.
  • Filaments, yarns, and staple fibers of such properties are suitable for many end uses, and, if desired, the tenacity of the filaments can, in most cases, be further increased, by subjecting them to additional drawing by both direct and separate drawing processes.
  • Preparation of the filaments can also be followed up by other treatments, such as, for example, by relaxation.
  • FIG. 1 shows schematically a possible embodiment of an apparatus suitable for preparing singleand multifilaments according to the invention.
  • the filaments 2 extruded from spinneret 1 are exposed to transversely directed air 3, and are passed over a guiding device 4 consisting of a pin with several U-shaped grooves, one each for a filament or bundle of filaments.
  • the filaments then pass around two non-driven rolls 5 which act like a flywheel and serve to stabilize the run of the filaments. From rolls 5 the filaments pass over two drag pins 6 which are mounted on a turnable socket, so that by turning the socket, the arcs of contact between the filaments and the pins and thereby the drag on the filaments can easily be varied.
  • Guiding device 4 and drag pins 6 preferably consist of hollow tubes which are connected with a circulation system in which a liquid is kept at a constant t mperature
  • the properties of the filaments of a given denier, especially their tenacity and elongation depend on many factors, such as temperature of the extruded polymer, temperature of guiding device and drag pins, temperature of the filaments when passing the drag pins, drag of the filaments at the pins, distance between spinneret and drag pin aggregate, Withdrawal speed and withdrawal tension of the filaments. Many of these process conditions are interdependent, and, in practical operation, adjustments can be confined to regulation of the filament temperature, of the drag to which the filaments are subjected, and of the temperature of guiding device and drag pins. As will be shown in the examples, both an increase of the filament temperature, of the filament drag, and of the drag pin temperature effect an increase of the orientation of the filaments.
  • This tension depends on the drag and the temperature of the filaments, and it has been surprisingly found that a graph plotting the filament tension against the distance between spinneret and drag pin aggregate, passes through a distinct minimum, and that, when the aggregate is at a distance corresponding to, or near said minimum, the filaments are in the prescribed temperature range, i.e. between 50 C. below their melting point and above their glass transition temperature.
  • the filament tension rises, whether the distance between spinneret and aggregate is increased or decreased.
  • the filaments obtained have a high uniformity as regards their diameter and their birefringence, and a good tenacity and a low elongation, while if the aggregate is in an area where rising tension coincides with increasing distance from the spinneret, the uniformity of the filaments is poor, their tenacity low, and their elongation high.
  • the tenacity of the filaments rises, and their elongation drops With rising tension, while in the area where rising tension corresponds with rising distance, relations are reversed.
  • filaments of high uniformity, good tenacity, and low to medium elongation are desired, the filaments of poor uniformity and high elongation may also be interesting for special processes and end uses.
  • a finer regulation of the filament tension can be made by adjusting the drag on the filaments at the pins and the temperature of guiding device and drag pins. Both an increase of the filament drag and of the drag pin temperature raises the filament tension, and because of the described relations between filament tension, tenacity, and elongation, the adjustments mentioned easily permit to prepare filaments ofthe properties desired. While the procedure described is the preferred method, there are,
  • the melting points of the polymers were determined by differential thermal analysis. Values reported by scientists for the glass transition temperatures differ slightly; the approximate figures given in the examples are based on information by R. G. Beaman, Journal of Polymer Science, IX, 470 (1952).
  • the relative viscosity of polyethylene terephthalate was determined at 25 C. in 100 ml. of a solution containing 0.4 g. of polymer in a mixture of equal parts by weight of phenol and tetrachloroethane, the relative viscosity of polyamides was determined at 20 C. in 100 ml. of a solution of 0.2 g. of polymer in 94% sulfuric acid, and the relative viscosity of polypropylene was determined at 135 C. in 100 ml. of a solution of 0.1 g. of polymer in tetrahydronaphthalene.
  • the temperature of the filaments was measured with a Hastings Match Temperature Pyrometer, Model TM- 2A, made by Hastings Raydist Inc., Hampton, Va., USA.
  • the filament tension was determined with a strain gauge, the filament diameter was measured microscopically, and the filament birefringence was determined as usual with a calcite compensator. Variations of diameter and birefringence were determined by measuring the average variation of 25 different tests on a single filament in percent from their mean value.
  • Shrinkage at boiling was determined by measuring the percent change in length of a single filament kept tension-free during five minutes in boiling water. Crystallinity of the filaments was determined by X-ray examination with a Philips-Norelco diffraction apparatus using a nickel-filtered copper radiation and is indicated on an arbitrary scale from zero to one.
  • EXAMPLE I Variation of distance between spinneret and drag pin aggregate
  • An apparatus is used substantially as shown in FIG. 1, but with a total of four drag pins, two pins each mounted on a turnable socket.
  • the diameter of each pin on the first socket was 19 mm, and the diameter of each pin on the second socket was 12 mm.
  • Guiding device and drag pins were made of hollow metal tubes and were connected with a circulation system in which glycol Was kept at a constant temperature of 80 C.
  • the filaments leaving the spinneret were cooled by transverse air having a temperature of 21 C., a moisture content of 65%, and an average speed of 30 m. per minute.
  • the filaments passed over a guiding device, around two non-driven stabilizing rolls, and over the four drag pins.
  • the respective arcs of contact between the filaments and the four pins were successively 84, 65, 51, and 36, and the oriented filaments were withdrawn at a speed of 950 m. per minute.
  • the yarn obtained had a total denier of 300 and was composed of 20 filaments of 15 denier each.
  • the properties of the filaments at varying distances between spinneret and the aggregate comprising guiding device, stabilizing rolls, and drag pins are given in Table l.
  • the distance measured was always the distance between spinneret and the nearest point of the aggregate, i.e. the guiding device.
  • the filament tension was measured between the last drag pin and the wind-up roll, and a graph showing the relation between said tension and the distance between spinneret and aggregate is given in FIG. 2.
  • the minimum filament tension of 0.17 gram per denier corresponds to a distance between spinneret and drag pin aggregate of 55 cm. From this point the tension rises, whether the distance between spinneret and aggregate is increased or decreased. But, in the area where rising tension coincides with rising distance (branch B in FIG. 2), the uniformity of the filaments as indicated by the high variation of diameter and birefringence is bad, their tenacity is low, and their elongation high, while in the area where rising tension corresponds to decreasing distance between spinneret and aggregate (branch A in FIG.
  • the filaments have a good uniformity, with variations of diameter and birefringence below 1 percent, a good tenacity up to 4.7 grams per denier, and a medium to low elongation with a minimum of 13 percent.
  • the higher birefringence and crystallinity of the good tenacity filaments also shows that they possess a higher degree of orientation than the filaments of low tenacity.
  • the shrinkage at boiling of the filaments is seen to be in proportion to their elongation at break.
  • Table 1 further shows that, when other process conditions remain unchanged, a decrease of the distance between spinneret and drag pin aggregate increases the temperature of the filaments and produces higher oriented filaments of higher tenacities and lower break elonga tions.
  • the yarn obtained had a tenacity of 7.6 grams per denier, an elongation at break of 6.7 percent, and a birefringence of 244. Contrary to the usual procedure when drawing polyethylene terephthalate yarns, the feed roll needed no heating.
  • the apparatus had two drag pins of hollow metal tubes mounted on a turnable socket, the diameter of each pin being 12 mm. Drag pins and guiding device were kept at a constant temperature of 40 C.
  • the polycaprolactam was molten at 267 C. and was extruded through a spinneret of 40 holes, each hole having a diameter of 0.23 mm., at a rate of 32v g. per minute.
  • the extruded filaments were cooled by transverse air of 21 C. having a moisture content of 65 percent and an average speed of 30 in. per minute.
  • the arcs ofcontact between the filaments and the two drag pins were 78 and 66, respectively, and. the oriented filaments were withdrawn at a speed of 950 in. per minute.
  • the yarn obtained had a total denier of 300 comprising 40 filaments of 7.5 denier each.
  • the properties of the filaments obtained are given in Table 5:
  • Example II The tests correspond to those reported in Example I for polyethylene terephthalate filaments and show the results of changing the distance between spinneret and drag pin aggregate.
  • the distances suitable for polycaprolactam filaments are considerably larger than those for polyethylene terephthalate filaments of the same denier, the distance corresponding to the minimum tension being 75 cm. for polycaprolactam and 35 cm. for polyethylene terephthalate (cf. Examples II, III, and IV).
  • the crystallinity values also indicate that the filaments of higher tenacities have a higher degree of orientation. All filaments obtained showed a purely hexagonal crystal structure, different from polycaprolactam filaments spun and subsequently drawn on conventional drawing machines the crystal structure of which is monoclinic.
  • Yarn sample V-B having a tenacity of 3.6 g. per denier and an elongation at break of 96% was subjected to additional drawing on a conventional drawing machine comprising feed roll, hot plate, drawing pin, and draw roll.
  • the drawing ratio was 2.1 to 1, and the yarn obtained had a tenacity of 9.2 g. per denier and an elongation at break of 12 percent.
  • EXAMPLE VI Polycaprolactam of the properties described in Example V was molten at 267"v C. and was extruded at a rate of 125 g. per minute using a spinneret of 20 holes, each hole having a diameter of 0.33 mm.
  • the extruded filaments were processed in an apparatus substantially as shown in FIG. 1, but having only one drag pin consisting of a hollow metal tube of 19 mm. diameter.
  • the temperature of drag pin and guiding device was kept constant at 65 C.
  • the filaments were cooled by transverse air as described in Example V along a distance of 1.8 m., and thereafter by quiescent air of room temperature.
  • the total distance between spinneret and drag pin aggregate was 3.9 m.
  • the temperature of the filaments before the drag pin was about 125 C., and the arc of contact between the filaments and the drag pin was 150.
  • the oriented filaments were withdrawn from the drag pin at a speed of 950 m. per minute and at a tension of 0.31 g. per denier.
  • the yarn obtained had a total denier of 1100 comprising 20 single filaments of 55 denier each, a tenacity of 3.5 g. per denier and an elongation at break of 48 percent.
  • an Uster Eveness Tester Model C, made by Zellweger AG, Uster, Switzerland, which measures denier variations by means of a capacity gauge electronically, an average variation of 1.25% on an arbitrary scale was indicated which is very satisfactory.
  • EXAMPLE VII Polycaprolactam of the properties described in Example V was molten at 261 C. and was extruded at a rate of 76 g. per minute using a spinneret of 20 holes, each hole having a diameter of 0.33 mm.
  • the extruded filaments Were processed in an apparatus substantially as shown in FIG. 1, the two drag pins consisting of hollow metal tubes, the diameter of each being 19 mm.
  • the temperature of drag pins and guiding device was kept constant at 60 C.
  • the filaments were cooled by transverse air as described in Example V along a distance of 1.8 m., and thereafter by'quiescent air of room temperature.
  • the total distance between spinneret and drag pin aggregate was 3.9 m.
  • the temperature of the filaments before the first drag pin ' was about 120 C., and the arcs of contact between the filaments and the drag pins were 85 and 60, respectively.
  • the oriented filaments were withdrawn from the drag pins at a speed of 400 m. per minute and at a tension of 0.38 g. per denier.
  • the yarn obtained had a total denier of 1700 comprising 20 single filaments of 85 denier each, a tenacity of 2.7 g. per denier, and an elongation at break of 80 percent.
  • the distance between spinneret and drag pin aggregate was the same as that employed in Example VI for filaments of 55 denier, the increased cooling required by the 85 denier filaments was provided by reducing the withdrawal speed from 950 to 400 in. per minute.
  • the polymer was molten at 285 C. and was extruded through a spinneret of 40 holes, each hole having a diameter of 0.23 mm., at a rate of 32 g. per minute.
  • the extruded filaments were cooled by transverse air as described in Example V, and had before the first drag pin a temperature of about 110 C.
  • the arcs of contact between the filaments and the two drag pins were 110 and 100, respectively, and the oriented filaments were withdrawn at a speed of 950 m. per minute and at a tension of 0.55 g. per denier.
  • the yarn obtained had a total denier of 300 comprising 40 filaments of 7.5 denier each, a tenacity of 4.0 g. per denier, an elongation at break of 63 percent, and a shrinkage at boiling of 7 percent.
  • the copolyamide was molten at 278 C. and was extruded through a spinneret of 40 holes each hole having a diameter of 0.23 mm., at a rate of 32. g. per minute.
  • the extruded filaments were cooled by transverse air as described in Example V, and had before the first drag pin a temperature of about 125 C.
  • the arch of contact between the filaments and the two drag pins were 72 and 67, respectively, and the oriented filaments were withdrawn at a speed of 950 ml. per minute and at a tension of 0.37 g. per denier.
  • the yarn obtained had a total denier of 300 comprising 40 filaments of 7.5 denier each, a tenacity of 4.3 g. per denier, an elongation at break of 64 percent, and a shrinkage at boiling of 7.8 percent.
  • Process for the preparation of orientated synthetic polymer filaments of a synthetic polymer whose utility for textile and technical purposes is improved by drawing with resultant orientation which comprises extruding molten polymer selected from the group consisting of polyamides, polyesters, polyolefins and copolyamides from hexamethylene diamine adipate and caprolactam through a spinnerette to form filaments, cooling said filaments, passing said filaments over a guiding device and at least one non-driven roll, subjecting said filaments to a drag bypassing them over at least one drag pin before contacting the filaments with a driven roll, locating said guiding device and said drag pin at such distance from the spinnerette that the filaments when passing over said guiding device and said drag pin are cooled to a temperature above their glass transition temperature and at least 50 C.
  • said guiding device and said drag pin at a substantially constant temperature at least 10 C. below the temperature of the filaments in contact therewith and above. the dew point of the surrounding air, and orientating said filaments by withdrawing them from said drag pin at a tension less than one gram per denier.
  • Process for the preparation of orientated synthetic polymer filaments of a synthetic polymer whose utility for textile and technical purposes is improved by drawing with resultant orientation, and which filaments have an elongation at break which does not exceed 70% which comprises extruding a molten polymer selected from the group consisting of polyamides, polyesters, polyolefins and copolyamides from hexamethylene diamine adipate and caprolactam through a spinnerette to form filaments, cooling said filaments, passing said filaments over a guiding device and at least one non-driven roll, subjecting said filaments to a drag by passing them over at least one drag pin, locating said drag pin at a distance from the spinnerette so that a decrease of said distance results in an increase of the filament tension and the filaments when passing over the drag pin are cooled to a temperature above their glass transition temperature and at least 50 C.
  • a molten polymer selected from the group consisting of polyamides, polyesters, polyolefins and copoly
  • a process in accordance with claim 8 including withdrawing the filaments from said drag pin at a tension of less than one gram per denier.
  • a process in accordance with claim 8 including maintaining the temperature of the drag pin between 25 C. and 85 C.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)
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BE (1) BE719663A (ref)
BR (1) BR6801093D0 (ref)
CH (1) CH475375A (ref)
DE (1) DE1760938C3 (ref)
ES (1) ES355813A1 (ref)
FR (1) FR1577074A (ref)
GB (1) GB1168767A (ref)
LU (1) LU56739A1 (ref)
NL (1) NL139363B (ref)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3752457A (en) * 1969-12-04 1973-08-14 Snia Viscosa Method and equipment for continuously spinning and stretching synthetic filaments
US3832435A (en) * 1970-07-03 1974-08-27 Hoechst Ag Process for the manufacture of crimped fibers and filaments of linear high molecular weight polymers
US4038357A (en) * 1972-06-28 1977-07-26 Imperial Chemical Industries Inc. Manufacture of synthetic filaments
US4071502A (en) * 1972-11-14 1978-01-31 Toyo Boseki Kabushiki Kaisha Polyester fiber having anti-pilling property and its production
US4093147A (en) * 1974-06-25 1978-06-06 Monsanto Company Flat nylon 66 yarn having a soft hand, and process for making same
US4123492A (en) * 1975-05-22 1978-10-31 Monsanto Company Nylon 66 spinning process
US4195161A (en) * 1973-09-26 1980-03-25 Celanese Corporation Polyester fiber
US5091130A (en) * 1987-07-10 1992-02-25 Courtaulds Plc Process for the production of highly filled yarns
US5266254A (en) * 1990-02-05 1993-11-30 Rhone-Poulenc Viscosuisse Sa Process for the high-speed spinning of monofilaments
US5609888A (en) * 1992-01-09 1997-03-11 Showa Denko Kabushiki Kaisha Apparatus for producing multifilaments
WO2009141424A3 (de) * 2008-05-23 2010-01-14 Oerlikon Textile Gmbh & Co. Kg Verfahren zum schmelzspinnen, verstrecken und aufwickeln eines multifilen fadens sowie eine vorrichtung zur durchführung des verfahrens

Families Citing this family (3)

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Publication number Priority date Publication date Assignee Title
GB1574305A (en) * 1976-03-23 1980-09-03 Ici Ltd Polymeric filaments and processes and apparatus for forming such materials
DE2813012C2 (de) * 1978-03-28 1985-04-18 Institut vysokomolekuljarnych soedinenij Akademii Nauk SSSR, Leningrad Verfahren zur Herstellung von Erzeugnissen aus Schmelzen kristallisierbarer Polymere
ES2019285B3 (es) * 1985-11-25 1991-06-16 Schweizerische Viscose Metodo y dispositivo para trenzado de hilos de poliester

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US3380135A (en) * 1965-06-01 1968-04-30 Monsanto Co Tow tie-in method
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CA700248A (en) * 1964-12-22 Kinzinger Emil Manufacture of artificial filaments of polypropylene
US2591242A (en) * 1949-02-01 1952-04-01 Textile & Chem Res Co Ltd Process for the manufacture of yarns from hydroxylated polyvinyl compounds
US2851732A (en) * 1953-07-14 1958-09-16 Du Pont Split filament bundle at finish roll
US2990236A (en) * 1957-03-25 1961-06-27 Ici Ltd Spinning process
US2991147A (en) * 1957-07-16 1961-07-04 British Nylon Spinners Ltd Process for the manufacture of sintered multifilamentary structures
US2957747A (en) * 1958-07-22 1960-10-25 Du Pont Process for producing crimpable polyamide filaments
GB960500A (en) * 1961-03-09 1964-06-10 Bayer Ag Process for stretching yarns
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US3364294A (en) * 1965-09-20 1968-01-16 Monsanto Co Filament orientation process
US3341394A (en) * 1966-12-21 1967-09-12 Du Pont Sheets of randomly distributed continuous filaments

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3752457A (en) * 1969-12-04 1973-08-14 Snia Viscosa Method and equipment for continuously spinning and stretching synthetic filaments
US3832435A (en) * 1970-07-03 1974-08-27 Hoechst Ag Process for the manufacture of crimped fibers and filaments of linear high molecular weight polymers
US4038357A (en) * 1972-06-28 1977-07-26 Imperial Chemical Industries Inc. Manufacture of synthetic filaments
US4071502A (en) * 1972-11-14 1978-01-31 Toyo Boseki Kabushiki Kaisha Polyester fiber having anti-pilling property and its production
US4195161A (en) * 1973-09-26 1980-03-25 Celanese Corporation Polyester fiber
US4093147A (en) * 1974-06-25 1978-06-06 Monsanto Company Flat nylon 66 yarn having a soft hand, and process for making same
US4123492A (en) * 1975-05-22 1978-10-31 Monsanto Company Nylon 66 spinning process
US5091130A (en) * 1987-07-10 1992-02-25 Courtaulds Plc Process for the production of highly filled yarns
US5266254A (en) * 1990-02-05 1993-11-30 Rhone-Poulenc Viscosuisse Sa Process for the high-speed spinning of monofilaments
US5431999A (en) * 1990-02-05 1995-07-11 Rhone-Poulenc Viscosuisse S.A. Polyester monofilaments
US5609888A (en) * 1992-01-09 1997-03-11 Showa Denko Kabushiki Kaisha Apparatus for producing multifilaments
WO2009141424A3 (de) * 2008-05-23 2010-01-14 Oerlikon Textile Gmbh & Co. Kg Verfahren zum schmelzspinnen, verstrecken und aufwickeln eines multifilen fadens sowie eine vorrichtung zur durchführung des verfahrens
US20110121480A1 (en) * 2008-05-23 2011-05-26 Oerlikon Textile Gmbh & Co. Kg Method for melt spinning, stretching, and winding a multifilament thread as well as a device for performing the method
CN102016138B (zh) * 2008-05-23 2012-01-25 欧瑞康纺织有限及两合公司 用于熔融纺丝、拉伸和卷绕复丝纱线的方法以及实施这种方法的设备
US9428848B2 (en) 2008-05-23 2016-08-30 Oerlikon Textile Gmbh & Co. Kg Method for melt spinning, stretching, and winding a multifilament thread as well as a device for performing the method

Also Published As

Publication number Publication date
NL139363B (nl) 1973-07-16
DE1760938B2 (de) 1974-08-15
BE719663A (ref) 1969-02-03
BR6801093D0 (pt) 1973-03-29
FR1577074A (ref) 1969-08-01
CH475375A (de) 1969-07-15
DE1760938C3 (de) 1980-11-06
GB1168767A (en) 1969-10-29
DE1760938A1 (de) 1972-01-05
ES355813A1 (es) 1969-12-16
NL6809832A (ref) 1969-02-25
LU56739A1 (ref) 1968-11-21

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