EP0046815B1 - Procédé pour le filage-étirage en continu de polyester - Google Patents

Procédé pour le filage-étirage en continu de polyester Download PDF

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Publication number
EP0046815B1
EP0046815B1 EP80105143A EP80105143A EP0046815B1 EP 0046815 B1 EP0046815 B1 EP 0046815B1 EP 80105143 A EP80105143 A EP 80105143A EP 80105143 A EP80105143 A EP 80105143A EP 0046815 B1 EP0046815 B1 EP 0046815B1
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EP
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Prior art keywords
temperature
filaments
process according
draw
steam
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Expired
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EP80105143A
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German (de)
English (en)
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EP0046815A1 (fr
Inventor
Maxwell Charles Hamlyn
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Allied Corp
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Allied Corp
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Application filed by Allied Corp filed Critical Allied Corp
Priority to DE8080105143T priority Critical patent/DE3071388D1/de
Priority to EP80105143A priority patent/EP0046815B1/fr
Publication of EP0046815A1 publication Critical patent/EP0046815A1/fr
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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
    • D—TEXTILES; PAPER
    • D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
    • D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
    • D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
    • D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
    • D01F6/62—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyesters

Definitions

  • This invention relates to the simultaneous (coupled) spin-drawing of continuous filament synthetic fibers from industrial polyester polymer. More particularly, it relates to an improved process for the production of low shrinkage, continuous polyester fibers which are particularly useful in the preparation of industrial products, including industrial belts, conveyor belts, and reinforced elastomeric structures. Still more particularly, it relates to a continuous process for the production of low shrinkage continuous polyester fibers by melt-spinning the polymer followed immediately by drawing the spun fibers wherein the spun fibers are heated substantially immediately above their second order transition temperature by being passed through a steam impinging draw point localizing jet at a steam temperature of 460°C to 580°C. Yarn thermal shrinkage is reduced and yarn dimensional stability improved with no adverse yarn property changes such as lower strength or higher elongation at break.
  • the present invention relates to an improved process for the simultaneous spin-drawing of one or more ends of multifilament, continuous filament, synthetic polyester industrial fiber wherein the improvement comprises localizing the draw point of the fiber through use of a noncondensing steam jet at a stream temperature of about 460°C to 580°C so that a reduced shrinkage industrial fiber is produced.
  • the present invention also relates to an improved process for the simultaneous spin-drawing of one or more ends of synthetic fibers from an industrial polyester polymer whereby a reduced shrinkage industrial fiber is produced.
  • the process which includes the steps of supplying a melt of the polymer to a spinning unit, extruding the molten polymer through a spinnerette having a plurality of extrusion orifices into a gaseous medium, cooling the extruded polymer filaments, lubricating the filaments, heating the filaments substantially immediately above their second order transition temperature, drawing and then winding up the filaments, is improved by passing the filaments through a steam impinging draw point localizing jet at a temperature of about 482°C to 580°C to thereby heat the filaments substantially immediately above their second order transition temperature.
  • the percent thermal shrink is reduced without significant effect on other yarn properties.
  • the present invention further relates to a process for the simultaneous spin-drawing of one or more ends of multifilament, continuous filament, synthetic polyester industrial fiber.
  • This process in addition to reducing percent thermal shrink, produces a dimensionally stable polyester industrial fiber.
  • the process comprises the steps of:
  • the melt have an intrinsic viscosity of about 0.68 to 0.96, most preferably of about 0.68 to 0.78 and that it be supplied at a temperature of about 272°C. to 310°C. It is also preferred that the steam temperature for localizing the draw point of the fiber be about 510°C. to 580°C.
  • the intrinsic viscosity of the polyester melt is given as a measure for the mean molecular weight, which is determined by standard procedures wherein the concentration of the measuring solution amounts to 0.5 g./100 mL, the solvent is a 60 percent phenol/40 percent tetrachloroethane mixture, and the measuring temperature is 25°C.
  • the tenacity or breaking strength in grams per denier is defined by ASTM Standards, Part 24, American Society for Testing and Materials, 1916 Race Street, Philadelphia, Pennsylvania, page 33 (1965), as "the maximum resultant internal force that resists rupture in a tension test," or "breaking load or force, expressed in units of weight required to break or rupture a specimen in a tensile test made according to specified standard procedures.”
  • % U.E is meant elongation at break in percent.
  • shrinkage is defined as "percent decrease in length of a material when exposed to elevated temperatures for a specified period of time and under 0.05 g.p.d. tension.” In the present invention the percent thermal shrinkage (% T.S.) is measured between two metal plates maintained at 177°C. for a time period of 60 seconds.
  • modulus in grams per denier, also known as tensile modulus (Young's Modulus), is expressed as the ratio of change in stress to change in strain in the initial straight-line portion of the stress-strain curve extrapolated to 100 percent elongation.
  • toughness also known as toughness index
  • the term "toughness”, also known as toughness index, is defined (above reference) as "the actual work per unit volume (or per unit mass) of material which is required to rupture the material. It is proportional to the area under the load-elongation curve from the origin to the breaking point.”
  • the toughness index is routinely measured in grams centimeter per denier centimeter.
  • the mechanical quality rating is made by visual examination of a stationary package wherein a rating of 1 to 3 to assigned with 1 being excellent and 3 being substandard.
  • a strobe examination is made by flashing a strobe on a rotating package wherein the strobe frequency is identical to the RPMs of the package and wherein a visual rating of 1 to 4 is assigned with 1 being excellent and 4 being unacceptable.
  • the preferred polyesters are the linear terephthalate polyesters, i.e., polyesters of a glycol containing from 2 to 20 carbon atoms and a dicarboxylic acid component containing at least about 75 percent terephthalic acid.
  • the remainder, if any, of the dicarboxylic acid component may be any suitable dicarboxylic acid such as sebacic acid, adipic acid, isophthalic acid, sulfonyl-4,4'-dibenzoic acid, or 2,8-di-benzofuran-dicarboxylic acid.
  • the glycols may contain more than two carbons atoms in the chain, e.g., diethylene glycol, butylene glycol, decamethylene glycol, and bis - (1,4 - (hydroxymethyl) - cyclohexane.
  • linear terephthalate polyesters which may be employed include (poly(ethylene terephthalate), poly(ethylene terephthalate/5 - chloroisophthalate) (85/15), poly(ethylene terephthalate/5 - [sodium sulfo] - isophthalate) (97/3), poly(cyclohexane - 1,4 - dimethylene terephthalate), and poly(cyclohexane - 1,4 - dimethylene terephthalate/hexahydroterephthalate) (75/25).
  • Figure is a schematic front view of the apparatus used for the method of this invention
  • Figure 2 is a schematic of the draw panel designated by the numeral 21 in Figure 1.
  • Ends 14 and 15 are extruded from the spinnerette at a rate of 15 to 34 kg (35 to 75 pounds) per hour per end, and are passed downwardly from the spinnerette into a substantially stationary column of air contained in a heated sleeve 16 of conventional height, most preferably about 38.1 cm (15 inches).
  • the extrusion rate will differ depending on the denier and number of ends of yarn being extruded.
  • a single continuous end of 1000 denier would be extruded from the spinnerette at a rate of about 15 to 23 kg (35 to 50 pounds) per hour, most preferably 18 kg (40 pounds) per hour, while three continuous ends would be extruded from the spinnerette at a rate of about 40 to 68 kg (90 to 150 pounds) per hour, most preferably at a rate of 55 kg (120 pounds) per hour.
  • Yarn leaving heated sleeve 16 is passed directly into the top of the quench chamber of conventional quenching apparatus 17.
  • the quench chamber is an elongated chimney of conventional length, preferably from 1.5 to 2.0 m (60 to 80 inches).
  • Ends 14 and 15 of yarn are lubricated by finish applicator 18 and then the ends are separated and the filaments in each end converged by guides 19.
  • a conventional spinning finish composition is used to lubricate the filaments.
  • Finish applicator 18 is depicted as a lube roll which may be rotated either with or against the direction of the yarn movement; it is preferred that the lube roll rotate with the direction of yarn movement. Rotation of the lube roll is at a rate of about 1.5 to 5 revolutions per minute, typically 3.1 revolutions per minute, for a lube roll having a diameter of about 7.62 to 20.3 cm (3 to 8 inches), typically 15.2 cm (6 inches).
  • the filaments be coated with from about 0.2 to about 1.0 weight percent based on the weight of the yarn of the finish, most preferably 0.5 percent.
  • Ends 14 and 15 are then transported via interfloor tube and aspirator 20 to spin draw panel 21 (see Figure 2) where they are fed to wrap around pretension roll 23 and accompanying separator roll 23a and then feed roll 24 and accompanying separator roll 24a.
  • feed roll 24 the ends are then passed through conventional steam impinging draw point localizing jet 25, supplying steam at a temperature of about 460°C. to 580°C., and at a pressure of about 600 to 960 kPa absolute (75 to 125 psig), and then to a pair of draw rolls 26 and 26a.
  • the ends pass from draw rolls 26 and 26a to relax roll 27 and accompanying separator roll 27a.
  • the yarn ends then pass through a conventional air operated interlacing jet 28 and are taken up by winder 22.
  • the ultimate objective is to obtain a yarn temperature of about 190°C. to 220°C. for a given yarn residence time of about 0.25 to 0.5 second, most preferably about 0.4 second. It is believed that the best mode of achieving this objective is by maintaining both of draw rolls 26 and 26a at a temperature of 225°C to 230°C. This, however, should not be construed as discounting other acceptable draw roll temperatures such as dual rolls at a temperature of 190°C to 215°C or a single roll, preferably roll 26a, at 225°C to 230°C. In any event, it has been found that at draw roll temperatures of greater than 237°C the yarn starts sticking to the rolls, and at draw roll temperatures of less than 190°C, there is an undesirable increase in % U.E.+% T.S.
  • Relax roll 27 is maintained at the minimum temperature necessary to maintain temperature equilibrium during processing, preferably 60°C to 120°C.
  • Examples 1 to 5 and 10 are controls provided to demonstrate the effect upon yarn properties of varying the steam temperature in the localising jet 25, while Examples 6 to 9, 11 and 12 illustrate the invention. In the Examples parts and percentages are by weight unless otherwise indicated.
  • a melt of polyethylene terephthalate having an intrinsic viscosity of 0.87 to 0.96 was supplied at a rate of 17 kg (37.5 pounds) per hour per end and at a temperature of about 300°C to the apparatus shown in Figures 1 and 2.
  • the molten polymer was fed by extruder 11 to spin pump 12 which fed spin block 13 containing a conventional spin pot as shown in Figure 1 of U.S. Patent US-A-4,072,457 to Cooksey et al.
  • the pressure drop through the filter assembly of the spin pot averaged 200 to 400 atmospheres (20,000 to 40,000 kPa absolute).
  • a split spinnerette designed for the simultaneous extrusion of two multi-filament ends of 192 filaments each was utilized, the spinnerette orifices having a diameter of about 0.05 cm (0.021 inch) and being spaced so that the distance between the filaments formed per end was about 0.71 to 1.0 cm (0.28 to 0.40 inch) immediately below the spinnerette.
  • the two ends 14 and 15 of multifilament, continuous filament yarn passed downwardly from the spinnerette into a substantially stationary column of air contained in a heated sleeve 16, about 38.1 cm (15 inches) (38.1 cm) in height, the temperature of the sleeve itself being maintained at about 400°C.
  • Yarn leaving heated sleeve 16 was passed directly into the top of the quench chamber of quenching apparatus 17.
  • Quenching apparatus 17 was as shown in Figure 1C of U.S. Patent US ⁇ A ⁇ 3,999,910 to Pendlebury et al., hereby incorporated by reference. Quenching air at about 18.33 C. (about 65°F). and 60 percent relative humidity was supplied at about 1.9 M'/sec.
  • the spin finish applied consisted of 15 parts of a stearic acid ester of a mixture of secondary alcohols having the general structure where n is 5 to 6, 15 parts refined coconut oil, 13 parts of ethoxylated lauryl alcohol, 2 parts of dinonylsodium-sulfosuccinate, 5 parts ethoxylated tallow amine, 10 parts of sodium salt of alkylarylsulfonate, and 40 parts mineral oil having a boiling range between about 266°C.
  • Yarn was produced in accordance with the process of Example 1, varying only the temperature of steam in the draw point localizing jet 25 for each of Examples 2-8. Physical properties and quality of the yarn so produced are set forth in Table I.
  • Example 1 the 290°C. temperature of Example 1 was set as the lower limit for evaluation as the yarn kept breaking out and could not be strung up at draw point localizing steam temperatures below 290°C. It can be seen that % U.E.+% T.S. dropped at every draw point localizing steam temperature increase; there appears to be approximately an inverse straight line relationship such that each 10°C. rise in draw point localizing steam temperature results in about an 0.18 to 0.20 percent reduction in % U.E.+% T.S. The % T.S. is clearly reduced at each increase in draw point localizing steam temperature and shows an inverse straight line relationship with draw point localizing steam temperature between 360°C. and 520°C. where each 10°C. rise in draw point localizing steam temperature causes a 0.23 percent reduction in % T.S.
  • Yarn was produced in accordance with the process of Example 1 with the following variations.
  • the melt was supplied at a temperature of about 282°C.
  • Heated sleeve 16 was maintained at a temperature of about 300°C.
  • Draw point localizing jet 25 was supplied with steam at a temperature of about 550°C. and at a pressure of 860 kPa absolute (110 psig).
  • Draw roll 26a was maintained at a temperature of about 230°C.
  • relax roll 27 was maintained at a temperature of about 120°C.
  • the tension between pretension 23 and feed 24 rolls was increased to 500 grams (0.08 gram per denier).
  • Yarn tension was increased to about 1.0 gram per denier as the ends passed to relax roll 27, and winder 22 tension was increased to about 0.2 gram per denier.
  • the draw ratio was approximately 5.9. Table II below sets forth the physical properties and quality of the yarn so produced.
  • Yarn was produced in accordance with the process of Example 1 with the following variations.
  • the melt had an intrinsic viscosity of about 0.68 to 0.78 and was supplied at a temperature of about 283°C.
  • Draw point localizing jet 25 supplied steam at a temperature of about 425°C. to 430°C.
  • Table III below sets forth the physical properties of yarn so produced.
  • Yarn was produced in accordance with the process of Example 1 with the following variations.
  • the melt had an intrinsic viscosity of about 0.68 to 0.78 and was supplied at a temperature of about 275°C.
  • Heated sleeve 16 was maintained at a temperature of about 250°C.
  • Draw point localizing jet 25 was supplied with steam at a temperature of about 550°C. and at a pressure of 860 kPa, absolute (110 psig). The draw ratio was 6.2 to 1.
  • Draw roll 26a was maintained at a temperature of about 225°C. to 230°C.
  • Relax roll 27 was maintained at a temperature of about 115°C. while yarn tension to relax roll 27 was maintained at about 0.9 to 1.0 gram per denier.
  • Yarn ends were taken up by winder 22 at a tension of from about 0.06 to 0.6 gram per denier, typically 0.2 gram per denier. Table III below sets forth the physical properties of the yarn so produced.
  • Yarn was produced in accordance with the process of Example 11, except that the temperature of steam in the draw point localizing jet 25 was 580°C. Physical properties of the yarn so produced are set forth in Table III below.
  • a high strength dimensionally stable product is produced according to Example 11.
  • a major advantage of this process is the ability to produce such a product from lower intrinsic viscosity polymer which is cheaper to produce as it requires less energy than high intrinsic viscosity polymer, gives increased capacity from the same equipment, and results in lower COOH, desirable for improved thermal stability.

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

Claims (10)

1. Procédé pour réaliser simultanément le filage-étirage d'une ou plusieurs extrémités de fibre industrielle de polyester synthétique multifilament ou à filament continu comprenant les étapes suivantes:
(a) fournir à l'état fondu un polymère de polyester à un groupe de filage;
(b) extruder le polyester fondu à travers un dispositif de filage comportant plusieurs orifices d'extrusion pour former des filaments;
(c) faire avancer les filaments à travers une zone de refroidissement brusque;
(d) lubrifier les filaments;
(e) faire passer les filaments lubrifiés sur un système d'avancement à rouleaux maintenu à une température inférieure à 50°C;
(f) faire passer ensuite les filaments à travers un jet de vapeur de localisation frappant ces derniers au point d'étirage pour chauffer les filaments sensiblement immédiatement au-dessus de leur température de transition du second ordre;
(g) faire passer les filaments sur une paire de rouleaux d'étirage;
(h) faire passer les filaments sur un système de rouleaux de détente; et
(i) embobiner les filaments, caractérisés par les étapes prises en combinaison, consistant à:
(1) faire avancer les filaments extrudés résultant de l'étape (b) à travers une colonne d'air sensiblement stationnaire contenue dans un fourreau chauffé ayant une température supérieure à 200° à 450°C avant de faire avancer les filaments à travers la zone de refroidissement brusque de l'étape (c);
(2) utiliser de la vapeur à une température de 482° à 580°C pour le jet de localisation de l'étape (f);
(3) maintenir au moins un des rouleaux d'étirage à une température comprise entre 190° et 237°C dans l'étape (g);
(4) maintenir le système de rouleaux de détente à une température de 60° à 135°C et la tension de fil à 0,4 à 2,0 grammes par denier dans l'étape (h) et
(5) embobiner les filaments à une tension de 0,06 à 0,6 grammes par denier dans l'étape (i).
2. Procédé selon la revendication 1 dans lequel le polymère de polyester à l'état fondu est fourni à un taux de 15 à 34 kg (35 à 75 Ibs) per heure par extrémité et à une température de 272° à 310°C.
3. Procédé selon l'une des revendications 1 ou 2 dans lequel le polymère de polyester à l'état fondu a une viscosité intrinséque de 0,68 à 0,96.
4. Procédé selon l'une des revendications 1, 2 ou 3 dans lequel pendant l'étape (1) consistant à avancer les filaments extrudés à travers une colonne d'air sensiblement stationnaire, le fourreau chauffé a une température d'environ 250°C.
5. Procédé selon l'une quelconque des revendications précédentes dans lequel, au cours de l'étape (f), la vapeur est à une température de 510° à 580°C.
6. Procédé selon la revendication 5 dans lequel la vapeur est à une température d'environ 550°C.
7. Procédé selon l'une quelconque des revendications précédentes dans lequel le polyester est du (poly) téréphtalate d'éthylène.
8. Procédé selon l'une quelconque des revendications précédentes dans lequel, au cours de l'étape (g) les deux rouleaux d'étirage sont maintenus à une température de 190° à 237°C.
9. Procédé selon la revendication 8 dans lequel les deux rouleaux d'étirage sont maintenus à une température de 190° à 230°C.
10. Procédé selon l'une quelconque des revendications 1 à 7 dans lequel lors de l'étape (g) un des rouleaux d'étirage est maintenu à une température de 225° à 230°C et l'autre rouleau d'étirage n'est pas chauffé.
EP80105143A 1980-08-29 1980-08-29 Procédé pour le filage-étirage en continu de polyester Expired EP0046815B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DE8080105143T DE3071388D1 (en) 1980-08-29 1980-08-29 Continuous spin-draw polyester process
EP80105143A EP0046815B1 (fr) 1980-08-29 1980-08-29 Procédé pour le filage-étirage en continu de polyester

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP80105143A EP0046815B1 (fr) 1980-08-29 1980-08-29 Procédé pour le filage-étirage en continu de polyester

Publications (2)

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EP0046815A1 EP0046815A1 (fr) 1982-03-10
EP0046815B1 true EP0046815B1 (fr) 1986-01-29

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EP80105143A Expired EP0046815B1 (fr) 1980-08-29 1980-08-29 Procédé pour le filage-étirage en continu de polyester

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Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH692704A5 (de) * 1997-10-08 2002-09-30 Rieter Ag Maschf Spinnstreckspul-Maschine.

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1395810A (en) * 1971-09-23 1975-05-29 Allied Chem Process for producing drawn filaments
GB1407111A (en) * 1972-01-12 1975-09-24 Allied Chem Multiple-end spin-draw and take-up for multifilament synthetic polymers
US4070432A (en) * 1975-02-13 1978-01-24 Allied Chemical Corporation Production of low shrink polyester fiber

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4113821A (en) * 1971-09-23 1978-09-12 Allied Chemical Corporation Process for preparing high strength polyamide and polyester filamentary yarn

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1395810A (en) * 1971-09-23 1975-05-29 Allied Chem Process for producing drawn filaments
GB1407111A (en) * 1972-01-12 1975-09-24 Allied Chem Multiple-end spin-draw and take-up for multifilament synthetic polymers
US4070432A (en) * 1975-02-13 1978-01-24 Allied Chemical Corporation Production of low shrink polyester fiber

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DE3071388D1 (en) 1986-03-13
EP0046815A1 (fr) 1982-03-10

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