US3715421A - Process for the preparation of polyethylene terephthalate filaments - Google Patents

Process for the preparation of polyethylene terephthalate filaments Download PDF

Info

Publication number
US3715421A
US3715421A US00028821A US3715421DA US3715421A US 3715421 A US3715421 A US 3715421A US 00028821 A US00028821 A US 00028821A US 3715421D A US3715421D A US 3715421DA US 3715421 A US3715421 A US 3715421A
Authority
US
United States
Prior art keywords
filaments
rolls
draw
feed
roll
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00028821A
Other languages
English (en)
Inventor
H Martin
B Glutz
H Linz
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.)
Viscosuisse SA
Original Assignee
Societe de la Viscose Suisse SA
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 Societe de la Viscose Suisse SA filed Critical Societe de la Viscose Suisse SA
Application granted granted Critical
Publication of US3715421A publication Critical patent/US3715421A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • 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
    • D02J1/224—Selection or control of the temperature during stretching
    • 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
    • D02J1/225—Mechanical characteristics of stretching apparatus
    • D02J1/226—Surface characteristics of guiding or stretching organs
    • 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

  • ABSTRACT A continuous spin-draw process is disclosed for preparing highly drawn polyethylene terephthalate filaments drawn at speeds greater than 1,800 meters per minute using only one heated draw roll system without the use of any other heating device.
  • Feed and draw rolls are provided with a surface roughness which allows a slipping of the filaments along a number of turns before they leave the feed rolls and after they arrive at the draw rolls.
  • the filaments are partially drawn at the lower temperature of the feed rolls, drawing continues between the feed and draw rolls, and is completed at the higher temperature of the draw rolls with a total draw ratio between 5 and8.
  • This invention relates to a continuous process for the preparation of highly drawn polyethylene terephthalate filaments by melt-spinning of the polymer followed imand winding up the quenched filaments. It is further known that, to obtain their optimal properties, the filaments must be drawn to several times their original length to produce orientation along the fiber axis. This is usually done by winding off the spun filaments and by passing them over sets of rolls driven at different speeds and eventually heating the filaments by various means to facilitate drawing.
  • U.S. Pat. No. 3,216,187 describes, inter alia, a continuous onestep process for the preparation of high-strength polyethylene terephthalate filaments, in which the filaments are heated by passing through a steam jet while moving from the feed rolls to the draw rolls.
  • the temperature of the steam must be very high to transfer sufficient heat to the filaments.
  • Temperatures of 350-450 C. are used, i.e., temperatures which are l00-200 C. above the melting point of the polymer.
  • Another well-known method is to pass the filaments to be drawn over heated pins or plates.
  • the period of contact between the filaments and such heating devices is very short, as the size of the pins and plates is limited by the overall dimensions of the machine.
  • These methods therefore also require the use of rather high temperatures in order to transfer the necessary amount of heat during the short period of contact.
  • the temperature gradient along the diameter of the filaments during drawing is therefore rather high.
  • a much better way to heat the filaments is the use of heated feed and draw rolls. As the filaments can pass over such rolls several times, they may have a considerably longer period of contact with the heating device than when using hot plates or steam jets.
  • the temperature of the heated rolls can therefore be kept considerably lower than that of the other practicable heating devices described above.
  • the temperature of the rolls will always remain below the melting point of the filaments, and the temperature gradient along the diameter of the filaments will be quite moderate.
  • the use of heated rolls is therefore a very safe and effective way of heating the filaments for the purpose of drawing.
  • the amount of heat transferred depends on the size and temperature of the rolls, the number of filament turns around the rolls, and the speed of the filaments.
  • lf freshly spun polyethylene terephthalate filaments which are practically non-crystalline, are for the purpose of being highly drawn, rapidly heated to temperatures of about 180 C., they suddenly start to crystallize and become sticky during a short period of time. It has also been observed that the temperature at which the v filaments become sticky depends, inter alia, on the speed with which the filaments are heated. lf therefore filaments pass from a conventional polished feed roll to a polished draw roll, such filaments having a temperature of at least 180 C., which was found by the inventors to be the minimum temperature to obtain high draw ratios at speeds of 1,800 meters per minute or more, a sticky mass of filaments is wrapped around the draw roll, and the filaments cannot be wound up.
  • British Pat. No. 1,176,164 describes such a process of drawing polyethylene terephthalate filaments by using only one draw roll system heated to 220 C, said draw roll system having a modified surface showing tiny protuberances of equal height which are regularly or irregularly distributed, preferably forming a series of microridges parallel to proceed and cannot the roll axis. It is the aim of this device to allow a steady decrease of the tension of the filaments during their last turns around the draw roll. It is also stated that a roll surface having unequal protuberances is not suitable for this purpose.
  • British Pat. No. 1,176,164 requires the use of an additional hot plate between feed and draw roll, and the wind-up speed is only 152 meters per minute. The process is therefore not suitable to obtain high draw ratios at the high wind-up speeds required for spin-drawing polyethylene terephthalate filaments.
  • the process according to the present invention comprises extruding molten polyethylene terephthalate through a spinnerette to form filaments, quenching the filaments, applying to the filaments a lubricating finish, passing the filaments successively over a feed roll system and a draw roll system, each system comprising at least two cylindrical rolls, each roll having a surface roughness of a roughness height, as defined by ASA B 46.1 1962, of 0.5-2.2 microns, allowing a slipping of the filaments around the feed roll system and the draw roll system of one to five turns, at least one feed roll and one draw roll being motor-driven.
  • the axis of the feed roll from which the filaments leave the feed roll system and the axis of the draw roll at which the filaments arrive at the draw roll system are parallel, while the axes of the feed rolls and the draw rolls, respectively, are skewed.
  • the process includes gradually drawing the filaments in a manner so that starting the drawing occurs while the filaments pass around the last one to five turns before leaving the feed rolls which have a surface temperature of 75l30 C, and completing the drawing while the filaments pass around the first one to five turns after arrival on the draw rolls which have a surface temperature of 180-240 C, drawing the filaments at a total draw ratio of not less than 5,0, and finally winding up the drawn filaments at a speed of not less than 1,800 meters per minute.
  • Both the feed roll system and the draw roll system shall consist of at least two rolls of equal or different size, and at least one feed roll and one draw roll shall be driven by a motor.
  • the use of a motor for the additional rolls depends on whether or not they can be moved without difficulty by the drawing force of the passing filaments.
  • At least one of the feed rolls shall be heated to 75-l 30 C, and preferably to 8090 C, and at least one of the draw rolls shall be heated to 180-240 C, and preferably to 2l0230 C. How many rolls are to be heated is determined by the aim that the filaments assume the same temperature as the heated rolls of the system over which they pass. No other heating device for the purpose of drawing the filaments is provided.
  • the examples describe the use of two heated motordriven feed rolls and two heated motor-driven draw rolls, all rolls having the same size with a diameter of 180 millimeters.
  • the filaments pass several times both over the feed rolls and the draw rolls, before they are finally wound up.
  • the high draw ratios used according to the invention correspond to very high tensions of the filaments during drawing, and, at the temperatures employed, these tensions may be as high as one-third of the breaking strength of the filaments.
  • the high tensions require a special position of the feed and draw rolls, such a position being used in all the examples. All feed and draw rolls should be cylindrical, and as shown in FIG. 4 the axis of the feed roll from which the filaments leave the feed roll system and the axis of the draw roll at which the filaments arrive at the draw roll system shall be parallel.
  • the filaments passing from the feed roll to the draw roll system will form an angle of to the axis of the feed roll from which they leave and to the axis of the draw roll at which they arrive (see FIG. 4), if the use of filament guides is to be avoided. If these conditions are not implemented, the filaments coming from the feed rolls will run off from the draw rolls and will go astray.
  • the axes of the two feed rolls and the axes of the two draw rolls, respectively are skew set (see FIG. 4) to effect a correct separation of the passing filaments.
  • the speed of the feed and draw rolls shall be such as to obtain a draw ratio of not less than 5.0.
  • the draw ratio is defined as the ratio between the surface speed of the draw rolls and the surface speed of the feed rolls.
  • the filaments shall perform at least so many turns around the respective rolls, that the surface speed of the rolls corresponds to the speed of the filaments at a point about half-way between the points of entry to, and exit from, the respective rolls.
  • the draw ratio also depends on the spinning speed of the filaments, higher spinning speeds producing a lower draw ratio.
  • the wind-up speed shall be not less than 1,800 meters per minute.
  • the upper limit of the wind-up speed is given by limitations of performance and equipment and may be as high as 6,000 meters per minute.
  • the optimal draw ratio obtainable also depends on the melt viscosity of the filaments, a lower melt viscosity producing a lower orientation of the spun filaments and therefore permitting a higher draw ratio.
  • the feed and draw rolls have a surface roughness, which will allow a slipping of the filaments along a number of turns before they leave the feed rolls and after they arrive at the draw rolls.
  • polyethyleneterephthalate filaments temporarily become sticky, when, for the purpose of drawing, they are quickly heated to temperatures of about C, so that they wrap up around the draw rolls and cannot properly pass on.
  • the slipping of the filaments allowed by the surface roughness of the rolls makes it possible that the filaments are gradually drawn along their way from the last few turns around the feed rolls up to the first few turns around the draw rolls.
  • filaments are partially drawn and oriented at the lower temperatures of the feed rolls, that the drawing continues between the feed and draw rolls, and that the drawing is completed at the higher temperatures of the draw rolls, finally reaching a high total draw ratio of not less than 5.0.
  • filaments already partially drawnand oriented at lower temperatures on a first draw roll system canproceed to a second draw roll system having substantially higher temperatures without showing any adhesive properties.
  • the process according to the invention applies a gradual drawing of the filaments-on and between one feed roll system and one draw roll system heated to different temperatures, and thereby saves the use of a second heated draw roll system.
  • the roll surface shall consist of a coherent, non-porous coating of tiny, smooth-topped elevations of defined unequal height and defined irregular distribution in all directions of the surface.
  • the description and definition of such a surface can only be made by use of statistical terms introducing averages from a great number of single figures having considerable fluctuations.
  • a surface profile which is the contour of a surface taken, in any direction,in a plane perpendicular to the surface.
  • FIG. 3 shows such a profile of a roll surface according to the invention.
  • the profile was measured with a Talysurf" instrument made by Taylor-Hobson Co., England. One centimeter of the vertical scale represents 0.45 microns, and 1 centimeter of the horizontal scale represents 19.8 microns.
  • the evaluation of the profile is made about the center line which is the line parallel to the general direction of the profile, such that the sums of the areas contained between the center line and those parts of the profile which lie on either side of it are equal (ASA B 46.1 1962).
  • the evaluation was carried out by use of a digital computer permitting an accuracy corresponding to distances of the measured profile of: 0.01 microns in vertical direction and ofi 1.0 microns in horizontal direction.
  • Roughness range which is the distance between the highest and the lowest point of the surface texture measured normal to the center line (Rauhtiefe according to DIN 4762).
  • the roughness range of the surface according to the invention shall be 4.5 8.0 microns.
  • Average Roughness Range which is the distance between the average height of the peaks and the average depth of the bottoms of the surface texture measured normal to the center line.
  • the average roughness range of the the surfaces according to the invention shall be 1.6 3.0 microns.
  • Peak Distance which is the distance between successive peaks.
  • the peak distance of the surfaces according to the invention shall not exceed microns,
  • Average Peak Distance which is the average distance between two successive peaks.
  • the average peak distance of the surfaces according to the invention shall be 40 60 microns.
  • Profile Curvature which is the reciprocal radius of curvature at any point of the profile.
  • the profile curvature of surfaces according to the invention shall not exceed 0.030 microns to exclude any sharp peaks or bends of the profile.
  • the terms adopted to describe and define the surface roughness according to the invention do not include the term roughness width" which is the distance between successive peaks which constitute the predominant pattern of the roughness (ASAB 46.1 1962). This term, which is somewhat similar to that of a wavelength is only applicable to patterns of a predominantly periodic lateral surface texture, different from the surfaces according to the invention with their great fluctuations of peak distance values.
  • a roll surface according to the invention can be produced by several methods, for example by sandblasting under controlled conditions followed by galvanic metal coating, by depositing metals in crystallized form from a gaseous phase, or by affixing small metallic globules of different size. It should be noted that sandblasting alone without a subsequent metal coating would produce elevations having too sharp peaks. It is emphasized that the elevations shall form a nonporous, coherent coating which is abrasion-resistant and impermeable.
  • a composition which does not contain more than 10 per cent by weight of water. As shown in the examples, such a finish facilitates producing filaments of considerably higher draw ratios and higher tenacities than a finish having a high water content or an emulsiontype finish.
  • One of the reasons for the advantage of the finish according to the invention is probably that it does not consume any substantial amount of heat from the heated rolls for the purpose of evaporation of water.
  • a possible modification of the inventive process is characterized by the use of an additional pre-tension roll system comprising at least one unheated motordriven roll and a separator roll, over which the filaments pass on their way from the spinnerette to the feed rolls.
  • the motor-driven pre-tension roll and the separator roll have, of course, the same surface speed, and this speed shall be slightly lower than the surface speed of the feed rolls, the speed difference not to exceed 2 percent. This speed difference will produce some tension of the filaments, which is well within the range of reversible elastic elongation of the undrawn filaments.
  • the advantage of such a pre-tension roll system is that the filaments run very quietly over the feed rolls and do not show any undesired sideway movements. Further advantages are described in detail in Example IV.
  • FIG. 1 is a diagrammatic illustration of apparatus in accordance with one embodiment of the invention.
  • FIG. 2 is a diagrammatic illustration of apparatus in accordance with another embodiment of the invention.
  • FIG. 3 is a profile of a roll surface in accordance with the invention.
  • FIG. 4 is a simplified perspective view of the apparatus illustrated in FIG. 1, and specifically indicating the surface roughness of the feed and draw rolls, as well as the skew sets within the feed roll system and the draw roll system, respectively.
  • FIGS. 1 and 4 show schematically one embodiment of an arrangement suitable for preparing spin-drawn filaments according to the invention.
  • the filaments 2 extruded for spinnerette l are exposed to transversely directed stream of air 3, and are passed over a guiding device 4 and roll 5 applying a lubricating finish. Thereafter, the filaments pass around heated feed rolls 6 and heated draw rolls 7.
  • the drawn filaments are wound-up as usual on bobbin 8.
  • Such an arrangement is used in Examples l, II, and III.
  • FIG. 2 shows schematically another possible embodiment of an arrangement which comprises the same elements as shown in FIG. 1, but, in addition, contains a pre-tension roll 9 with separator roll 10 arranged before the feed rolls.
  • Two relaxation rolls 11 are arranged between draw rolls 7 and windup bobbin 8.
  • Such an arrangement is used in Examples IV, V and VI.
  • the following examples will show details as to the performance of the process and the properties of the filaments obtained.
  • the tenacities of the filaments were determined by the use of an INSTRON Tester and refer to the filament denier at zero elongation.
  • the tension of the filaments passing around the various rolls were measured by a ROTHSCHILD ELECTRONIC TEN- SIOMETER.
  • the intrinsic viscosity [4:] is defined by the following equation:
  • tIISpeC means the specific viscosity at 25 C of a solution of 0.5000 grams of polyethylene terephthalate in 100 milliliters of a mixture of equal parts by weight of phenol and tetrachloroethane.
  • EXAMPLE I This example shows the dependence of filament tenacity, elongation, and shrinkage upon the draw ratio. It further shows, at a fixed draw ratio, the filament tensions existing at various positions in relation to the feed and draw rolls.
  • the polyethylene terephthalate filaments leaving the spinnerette were quenched by transverse air, passed over a convergence guide, and were treated with a lubricating finish.
  • a suitable temperature for the lubricating finish treatment is C.
  • lubricating finishes may be used in the subject invention, and such lubricating finishes and their operative temperatures, per se, form no part of the present invention. Examples of suitable lubricating finishes are set forth hereinafter in Example VI.
  • the filaments passed over two motor-driven rolls, acting simultaneously as withdrawal rolls for the spun filaments and as feed rolls for the drawing process, and then over two motor-driven draw rolls, whereafter the drawn filaments were wound up. All rolls had a diameter of I80 millimeters, and their axes were in a position as prescribed by the specification. The rolls had a surface roughness as roll surface type E of Example V.
  • the two feed rolls were heated to C, and the filaments passed around the feed rolls in 12 turns.
  • Different draw ratios were obtained by variation of the surface speed of the feed rolls between 327 and 372 m/min.
  • the two draw rolls were heated to 210 C, the surface speed of the draw rolls was 2,180 meters per minute, and the filaments also passed around the draw rolls in 12 turns.
  • the filaments were wound up at a speed of 2,000 meters per minute, i.e., at a speed slightly less than the speed of the draw rolls.
  • the spun, undrawn filaments had an intrinsic viscosity of 0.75 and, at a withdrawal speed of 372 meters per minute, a birefringence of 0.6 0.7 X 10*.
  • the drawn filaments had a total denier of 1,000/192 and a finish content of 0.5 0.6 percent. Table I gives the figures for tenacity and break elongation of the drawn filaments at different draw-ratios:
  • the filaments obtained according to the inventive process have been drawn at a high drawratio and possess a high tenacity and a medium break elongation.
  • the filament tension on the feed rolls decreases over the first eight turns.
  • the reason is that the length of the filaments increases when they are heated above their glass transition temperature which is about 70 C.
  • the strong increase of the filament tension during the last four turns around the feed rolls indicates that the pull from the draw rolls has become effective, andthatthe gradual drawing of the filaments has begun.
  • this gradual drawing is made possible by the slipping effect due to the special rough surface of the rolls.
  • the slipping effect is also the cause of the decrease of the filament tension while passing around the first four turns around the draw rolls.
  • Table 1a also shows that at a position about four turns after arrival on, and before departure from, both the feed and draw rolls, the respective filament tensions remain constant within a rather small range. It was also found that, at these positions, the filament speeds coincided with the respective surface speeds of the rolls.
  • the low filament tension at the central turns around the feed rolls may cause undesirable sideway movements of the filaments. This can be prevented by the insertion of an additional unheated pre-tension roll between the spinnerette and the feed rolls, as described in Example IV.
  • the feed rolls had a surface speed of374 meters per minute, and were passed by the filaments in nine turns.
  • the filaments were wound up at a speed of 2,002 meters per minute, i.e., at a speed slightly less than the speed of the draw rolls.
  • the drawn filaments had a total denier of 250/48.
  • Table 2 shows the filament properties at different temperatures of the draw rolls:
  • EXAMPLE III The filaments were spun and drawn as described in Example I, with the following differences: A polymer of higher viscosity was used, so that the spun undrawn filaments had an intrinsic viscosity of0.95. At a surface speed of the feed rolls of 365 meters per minute, the birefringence of the spun filaments was 1.0 X 10*. By variation of the speed of the feed rolls, various draw ratios were obtained, while the surface speed of the draw rolls was kept constant at 2,160 meters per minute. To effect some relaxation, the filaments were wound up at a speed of 2,000 meters per minute, i.e., at a speed slightly less than the speed of the draw rolls. The total denier of the drawn filaments was 1,000/192.
  • Table 3. shows the filament properties at various draw ratios:
  • the filaments were spun and drawn as described in Example I with the following differences: A polymer of higher viscosity was used, so that the spun undrawn filaments had an intrinsic viscosity of about 0.92.
  • the filaments were withdrawn from a spinnerette of 192 holes by means of an unheated motor-driven roll and separator roll, serving as pre-tension rolls and placed between spinnerette and feed rolls. From the draw rolls the filaments passed over another two motor-driven rolls heated to a higher temperature than the draw rolls and serving for the purpose of relaxation and stabilization. The axes of the two pre-tension rolls and the two relaxation rolls are skew set.
  • the feed and draw rolls had a surface roughness as roll surface type E of Example V.
  • the diameter of the motor-driven pre-tension roll was such that its surface speed was about l.5 percent lower than the surface speed of the feed rolls. As explained above, this speed difference produces some tension of the filaments which is well within their range of reversible elastic elongation and prevents undesired sideway movements of the filaments on the feed rolls as described in Example I.
  • Table 4a compares the withdrawal speed and birefringence of the spun filaments with the draw-ratio, tenacity, and break elongation of the drawn filaments:
  • Table 4a shows that the birefringence of the spun, undrawn filaments depends on their withdrawal speed. The filaments spun at a higher speed have a higher orientation and therefore a higher birefringence. Table 4a also shows that the higher spin-oriented filaments withdrawn at higher speed and drawn at a draw-ratio of 5.3 and lower spin-oriented filaments withdrawn at a lower speed and drawn at a draw-ratio of 6.0 produce drawn filaments of about the same tenacity of about 9 grams per denier and the same elongation at break of about 15 percent.
  • Table 4b compares filaments spun and drawn according to A in Table 4a, but with and without the use ofa pre-tension roll:
  • the pre-tensioned filaments are heated more rapidly and therefore require fewer turns than the un-tensioned filaments.
  • Table 4b shows, the tensioned filaments needed only five turns around the feed rolls, while the un-tensioned filaments required eight turns to obtain a satisfactory run.
  • EXAMPLE V This example describes how the nature of the surface of the feed and draw rolls affects the performance of the process and the qualities of the filaments obtained.
  • Filaments were spun and drawn as described in Example IV, selecting the following roll surface speeds: Draw rolls 2,160 m/min., relaxation rolls 2,000 m/min., and wind-up roll 2,002 m/min. The draw ratio was varied by variation of the surface speed of the feed rolls.
  • the surface speed of the pre-tension rolls was about 1.5 percent lower than the surface speed of the feed rolls.
  • the temperature of the heated rolls and the number of filament turns around the rolls were the same as described in Example IV, Table 4.
  • the drawn filaments had a total denier of 1,000/192.
  • Roughness Terms Prescribed Limits (1) Roughness height (2) Roughness range (3) Average roughness range (4) Peak distance (5) Average peak distance (6) Profile curvature 0.5 2.2 microns 4.5 8.0 microns l.6 3.0 microns Max. microns 40 60 microns Max. 0.030 microns roughness terms, and Table b shows the qualities of the corresponding drawn filaments obtained;
  • EXAMPLE Vl This example describes the-effects of the composition of the lubricating finish. Filaments were spun as described in Example V with roll surface (F), but varying the draw ratio of the filaments by variation of the speed of the feed rolls. The following lubricating finishes were used:
  • Lubricating finish based on isooctyl stearate, containing 5 7 percent by weight of water.
  • Table 6 shows the results of the tests. The temperature indicated is the temperature of the finish as applied to the filaments. The content of finish in the filaments was determined by extraction and refers to water-free finish.
  • the draw ratio indicated for finishes (a), (b), and (c), containing more than 10 percent of water, is the maximum draw ratio at which filaments could still be spun and drawn. As Table 5 shows, this draw ratio is substantially lower than the draw ratio obtainable with finishes (d), (e), (f), and (g) the water content of which did not exceed 10 percent as prescribed.
  • Process as set forth in claim 1 including providing said rolls with a surface roughness range. as defined by DIN 4762, of 4.5 8.0 microns, a peak distance of not more than 140 microns, an average peak distance of 40 60 microns, and a profile curvature of not more than 0.030 microns.
  • Process as set forth in claim 4 including providing said rolls with an average roughness range of 1.6 3.0 mlCI'Ol'lS.
  • Process as set forth in claim 1 including providing said rolls with a peak distance of not more than 140 microns.
  • Process in accordance with claim 6 including providing said rolls with an average peak distance of 40 -60 microns.
  • Continuous process for the preparation of highlydrawn polyethylene terephthalate filaments which comprises extruding molten polyethylene terephthalate through a spinnerette to form filaments, quenching the filaments, applying to the filaments a lubricating finish, passing the filaments over feed rolls and draw rolls which have a surface roughness which allows slipping of from one to five turns before the filaments leave the feed rolls and after the filaments arrive at the draw rolls, the feed rolls having a surface temperature of 130 C, and the draw rolls having a surface temperature of 180 240 C and a surface speed at least five times that of the feed rolls, partially drawing the filaments at the lower temperature of the feed rolls, continuing to draw the filaments between the feed rolls and the draw rolls, and completing the drawing of the filaments at the higher temperature of the draw rolls to attain a total draw ratio of 5 to 8, and winding up the drawn filaments at a speed of 1,800 to 6,000 meters per minute.
  • Process as set forth in claim 9 including using a lubricating finish which contains not more than 10 percent by weight of water.
  • said surface roughness consists of a coherent, non-porous, abrasion-resistant, impermeable coating of tiny, smooth-topped elevations of unequal height and irregu- Iardistribution in all directions on the surface of said rolls.

Landscapes

  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Mechanical Engineering (AREA)
  • Artificial Filaments (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
US00028821A 1970-04-15 1970-04-15 Process for the preparation of polyethylene terephthalate filaments Expired - Lifetime US3715421A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US2882170A 1970-04-15 1970-04-15

Publications (1)

Publication Number Publication Date
US3715421A true US3715421A (en) 1973-02-06

Family

ID=21845636

Family Applications (1)

Application Number Title Priority Date Filing Date
US00028821A Expired - Lifetime US3715421A (en) 1970-04-15 1970-04-15 Process for the preparation of polyethylene terephthalate filaments

Country Status (8)

Country Link
US (1) US3715421A (de)
BE (1) BE763271A (de)
CH (1) CH522048A (de)
DE (1) DE2118316C3 (de)
FR (1) FR2089958A5 (de)
GB (1) GB1302650A (de)
LU (1) LU62895A1 (de)
NL (1) NL148958B (de)

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3914835A (en) * 1974-01-14 1975-10-28 Dow Badische Co Apparatus for drawing and crimping synthetic yarn
US3963678A (en) * 1974-06-17 1976-06-15 E. I. Du Pont De Nemours And Company Large denier polyethylene terephthalate monofilaments having good transverse properties
US3975488A (en) * 1972-10-24 1976-08-17 Fiber Industries, Inc. Process for preparing poly(tetramethylene terephthalate) yarn
US3987136A (en) * 1972-11-10 1976-10-19 Barmag Barmer Maschinenfabrik Aktiengesellschaft Process for the production of a synthetic fiber cord
US4003974A (en) * 1975-04-04 1977-01-18 E. I. Du Pont De Nemours And Company Continuous spin-drawing process for preparing polyethylene terephthalate yarns
US4045534A (en) * 1974-05-24 1977-08-30 Allied Chemical Corporation Process for melt-spinning synthetic fibers
US4070432A (en) * 1975-02-13 1978-01-24 Allied Chemical Corporation Production of low shrink polyester fiber
US4101525A (en) * 1976-10-26 1978-07-18 Celanese Corporation Polyester yarn of high strength possessing an unusually stable internal structure
US4113821A (en) * 1971-09-23 1978-09-12 Allied Chemical Corporation Process for preparing high strength polyamide and polyester filamentary yarn
US4123492A (en) * 1975-05-22 1978-10-31 Monsanto Company Nylon 66 spinning process
US4195052A (en) * 1976-10-26 1980-03-25 Celanese Corporation Production of improved polyester filaments of high strength possessing an unusually stable internal structure
US4195161A (en) * 1973-09-26 1980-03-25 Celanese Corporation Polyester fiber
US4247505A (en) * 1978-05-05 1981-01-27 Phillips Petroleum Company Melt spinning of polymers
DE3026520A1 (de) * 1980-07-12 1982-02-11 Davy International Ag, 6000 Frankfurt Verfahren und vorrichtung zur herstellung hochfester technischer garne durch spinnstrecken
US4374797A (en) * 1980-07-12 1983-02-22 Davy Mckee Aktiengesellschaft Process for the production of high strength yarns by spin-stretching and yarns produced by the process, especially from polyamide-6 and polyester filaments
US4486483A (en) * 1983-07-11 1984-12-04 American Hoechst Corporation Polyester film primed with organic acid salts
US4554200A (en) * 1983-07-11 1985-11-19 American Hoechst Corporation Polyester film primed with organic acid salts
US4851172A (en) * 1984-08-21 1989-07-25 Allied-Signal Inc. Process for high speed, multi-end polyester high performance tire and industrial yarn
US5266254A (en) * 1990-02-05 1993-11-30 Rhone-Poulenc Viscosuisse Sa Process for the high-speed spinning of monofilaments
US6115893A (en) * 1996-12-20 2000-09-12 Rhodia Filtec Ag Process and device for producing industrial polyester yarn
EP3327180A1 (de) * 2016-11-25 2018-05-30 Dako Ag Verwendung einer präparationsflüssigkeit mit niedriger viskosität und geringem wassergehalt zur behandlung von fäden

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0224306B1 (de) * 1985-11-25 1990-10-31 Rhône-Poulenc Viscosuisse SA Verfahren und Vorrichtung zum Spinnstrecken von Polyesterfäden
JP5575238B2 (ja) 2009-07-24 2014-08-20 エーリコン テクスティル ゲゼルシャフト ミット ベシュレンクテル ハフツング ウント コンパニー コマンディートゲゼルシャフト マルチフィラメントヤーンを溶融紡糸し延伸し巻き取る方法ならびにマルチフィラメントヤーンを溶融紡糸し延伸し巻き取る方法を実施する装置
DE102009037125A1 (de) 2009-08-11 2011-02-17 Oerlikon Textile Gmbh & Co. Kg Verfahren zum Schmelzspinnen, Verstrecken und Aufwickeln eines multifilen Fadens sowie eine Vorrichtung zur Durchführung des Verfahrens

Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2851732A (en) * 1953-07-14 1958-09-16 Du Pont Split filament bundle at finish roll
US2859472A (en) * 1955-10-05 1958-11-11 Allied Chem Apparatus for reducing shrinkage and creep of thermoplastic yarns
CA611444A (en) * 1960-12-27 G. Evans Cyril Methods and apparatus for preparing elasticized thermoplastic yarns
US2990603A (en) * 1958-04-23 1961-07-04 Leesona Corp Apparatus for draw-stretching and winding yarn
CA628863A (en) * 1961-10-10 B. Macleod Roderick Drawing process
US3009231A (en) * 1957-04-10 1961-11-21 Glanzstoff Ag Apparatus for heat-stretching of synthetic polymer threads
US3091805A (en) * 1960-11-02 1963-06-04 Du Pont Apparatus and process for drawing yarn
US3101990A (en) * 1960-10-13 1963-08-27 Du Pont Process of drawing filamentary structures
US3123891A (en) * 1961-04-10 1964-03-10 Apparatus for drawing textile filaments
US3164650A (en) * 1961-12-18 1965-01-05 American Cyanamid Co Art of dehydrating fibers with lubricating and antistatic coatings
GB1006348A (en) * 1960-10-21 1965-09-29 Inventa Ag Process and apparatus for stretching textile threads of synthetic linear polyamides
GB1011645A (en) * 1963-10-09 1965-12-01 Giuseppe Azimonti & Figli S R Process for stretching filaments of synthetic polymers particularly polyethylene terephthalate
US3329758A (en) * 1963-06-17 1967-07-04 Monsanto Co Treating polyester filament with a surface active compound to permit lagging before drawing
US3366721A (en) * 1966-07-21 1968-01-30 Monsanto Co Process for treating filaments
US3400194A (en) * 1963-11-04 1968-09-03 Du Pont Process for making high-tenacity, low elongation industrial yarn
US3422491A (en) * 1964-09-09 1969-01-21 Asahi Chemical Ind Apparatus for stretching synthetic fibers
US3433008A (en) * 1965-11-19 1969-03-18 Du Pont Bulked yarn
US3481136A (en) * 1967-12-11 1969-12-02 Celanese Corp Process for producing polyester yarn
US3485913A (en) * 1965-10-20 1969-12-23 Toho Beslon Co New method of manufacturing acrylic fibers and the related products
GB1176164A (en) * 1966-05-11 1970-01-01 Ici Ltd Process and apparatus for Drawing Thermoplastic Filamentary Yarns
US3500519A (en) * 1968-04-01 1970-03-17 Techniservice Corp Strand treatment
US3561045A (en) * 1968-07-05 1971-02-09 Courtaulds Ltd Apparatus for manufacture of filaments of varying denier

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH309881A (de) * 1951-12-21 1955-09-30 Phrix Werke Ag Vorrichtung zum Verstrecken von Fäden aus organischen Hochpolymeren.
US3020621A (en) * 1959-12-03 1962-02-13 Du Pont Draw roll
US3216187A (en) * 1962-01-02 1965-11-09 Du Pont High strength polyethylene terephthalate yarn
GB1037629A (en) * 1963-10-30 1966-07-27 British Nylon Spinners Ltd Apparatus for handling and guiding a moving continuous elongated structure
NL164909C (nl) * 1968-10-08 1981-02-16 Algemene Kunstzijde Unie Nv Werkwijze en inrichting voor het in ten minste twee trappen strekken van een thermoplastisch produkt en het volgens de werkwijze vervaardigde produkt.

Patent Citations (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA611444A (en) * 1960-12-27 G. Evans Cyril Methods and apparatus for preparing elasticized thermoplastic yarns
CA628863A (en) * 1961-10-10 B. Macleod Roderick Drawing process
US2851732A (en) * 1953-07-14 1958-09-16 Du Pont Split filament bundle at finish roll
US2859472A (en) * 1955-10-05 1958-11-11 Allied Chem Apparatus for reducing shrinkage and creep of thermoplastic yarns
US3009231A (en) * 1957-04-10 1961-11-21 Glanzstoff Ag Apparatus for heat-stretching of synthetic polymer threads
US2990603A (en) * 1958-04-23 1961-07-04 Leesona Corp Apparatus for draw-stretching and winding yarn
US3101990A (en) * 1960-10-13 1963-08-27 Du Pont Process of drawing filamentary structures
GB1006348A (en) * 1960-10-21 1965-09-29 Inventa Ag Process and apparatus for stretching textile threads of synthetic linear polyamides
US3091805A (en) * 1960-11-02 1963-06-04 Du Pont Apparatus and process for drawing yarn
US3123891A (en) * 1961-04-10 1964-03-10 Apparatus for drawing textile filaments
US3164650A (en) * 1961-12-18 1965-01-05 American Cyanamid Co Art of dehydrating fibers with lubricating and antistatic coatings
US3329758A (en) * 1963-06-17 1967-07-04 Monsanto Co Treating polyester filament with a surface active compound to permit lagging before drawing
GB1011645A (en) * 1963-10-09 1965-12-01 Giuseppe Azimonti & Figli S R Process for stretching filaments of synthetic polymers particularly polyethylene terephthalate
US3400194A (en) * 1963-11-04 1968-09-03 Du Pont Process for making high-tenacity, low elongation industrial yarn
US3422491A (en) * 1964-09-09 1969-01-21 Asahi Chemical Ind Apparatus for stretching synthetic fibers
US3485913A (en) * 1965-10-20 1969-12-23 Toho Beslon Co New method of manufacturing acrylic fibers and the related products
US3433008A (en) * 1965-11-19 1969-03-18 Du Pont Bulked yarn
GB1176164A (en) * 1966-05-11 1970-01-01 Ici Ltd Process and apparatus for Drawing Thermoplastic Filamentary Yarns
US3495295A (en) * 1966-05-11 1970-02-17 Ici Ltd Apparatus for drawing thermoplastic filamentary yarns
US3366721A (en) * 1966-07-21 1968-01-30 Monsanto Co Process for treating filaments
US3481136A (en) * 1967-12-11 1969-12-02 Celanese Corp Process for producing polyester yarn
US3500519A (en) * 1968-04-01 1970-03-17 Techniservice Corp Strand treatment
US3561045A (en) * 1968-07-05 1971-02-09 Courtaulds Ltd Apparatus for manufacture of filaments of varying denier

Cited By (25)

* 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
US3975488A (en) * 1972-10-24 1976-08-17 Fiber Industries, Inc. Process for preparing poly(tetramethylene terephthalate) yarn
US3987136A (en) * 1972-11-10 1976-10-19 Barmag Barmer Maschinenfabrik Aktiengesellschaft Process for the production of a synthetic fiber cord
US4195161A (en) * 1973-09-26 1980-03-25 Celanese Corporation Polyester fiber
US3914835A (en) * 1974-01-14 1975-10-28 Dow Badische Co Apparatus for drawing and crimping synthetic yarn
US4045534A (en) * 1974-05-24 1977-08-30 Allied Chemical Corporation Process for melt-spinning synthetic fibers
US3963678A (en) * 1974-06-17 1976-06-15 E. I. Du Pont De Nemours And Company Large denier polyethylene terephthalate monofilaments having good transverse properties
US4070432A (en) * 1975-02-13 1978-01-24 Allied Chemical Corporation Production of low shrink polyester fiber
US4003974A (en) * 1975-04-04 1977-01-18 E. I. Du Pont De Nemours And Company Continuous spin-drawing process for preparing polyethylene terephthalate yarns
US4123492A (en) * 1975-05-22 1978-10-31 Monsanto Company Nylon 66 spinning process
US4101525A (en) * 1976-10-26 1978-07-18 Celanese Corporation Polyester yarn of high strength possessing an unusually stable internal structure
US4195052A (en) * 1976-10-26 1980-03-25 Celanese Corporation Production of improved polyester filaments of high strength possessing an unusually stable internal structure
US4247505A (en) * 1978-05-05 1981-01-27 Phillips Petroleum Company Melt spinning of polymers
DE3026520A1 (de) * 1980-07-12 1982-02-11 Davy International Ag, 6000 Frankfurt Verfahren und vorrichtung zur herstellung hochfester technischer garne durch spinnstrecken
US4374797A (en) * 1980-07-12 1983-02-22 Davy Mckee Aktiengesellschaft Process for the production of high strength yarns by spin-stretching and yarns produced by the process, especially from polyamide-6 and polyester filaments
US4461740A (en) * 1980-07-12 1984-07-24 Davy Mckee A.G. Process for spin-stretching of high strength technical yarns
US4486483A (en) * 1983-07-11 1984-12-04 American Hoechst Corporation Polyester film primed with organic acid salts
US4554200A (en) * 1983-07-11 1985-11-19 American Hoechst Corporation Polyester film primed with organic acid salts
US4851172A (en) * 1984-08-21 1989-07-25 Allied-Signal Inc. Process for high speed, multi-end polyester high performance tire and industrial yarn
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
US6115893A (en) * 1996-12-20 2000-09-12 Rhodia Filtec Ag Process and device for producing industrial polyester yarn
EP3327180A1 (de) * 2016-11-25 2018-05-30 Dako Ag Verwendung einer präparationsflüssigkeit mit niedriger viskosität und geringem wassergehalt zur behandlung von fäden
WO2018095560A1 (de) * 2016-11-25 2018-05-31 Dako Aktiengesellschaft, Chemische Verwendung einer präparationsflüssigkeit mit niedriger viskosität und geringem wassergehalt zur behandlung von fäden
CN110114521A (zh) * 2016-11-25 2019-08-09 达科化工有限责任公司 低粘度且低水含量的配制液用于处理线的用途

Also Published As

Publication number Publication date
LU62895A1 (de) 1971-08-24
FR2089958A5 (de) 1972-01-07
DE2118316C3 (de) 1984-03-01
CH522048A (de) 1972-04-30
BE763271A (fr) 1971-07-16
DE2118316B2 (de) 1978-01-12
DE2118316A1 (de) 1971-11-04
NL7101765A (de) 1971-10-19
GB1302650A (de) 1973-01-10
NL148958B (nl) 1976-03-15

Similar Documents

Publication Publication Date Title
US3715421A (en) Process for the preparation of polyethylene terephthalate filaments
US4301102A (en) Self-crimping polyamide fibers
US4049763A (en) Process for producing a highly oriented polyester undrawn yarn
US4093147A (en) Flat nylon 66 yarn having a soft hand, and process for making same
US3423809A (en) Process for forming differential shrinkage bulked yarn
US5750215A (en) High speed process for making fully-oriented nylon yarns and yarns made thereby
EP0034880B1 (de) Verfahren zur Herstellung eines Endlosgarnes durch Schmelzspinnen von Polyäthylenterephthalat und nach dem Verfahren hergestellte Polyestergarne
US4390685A (en) Polyester fiber and process for producing same
JP3043414B2 (ja) ポリエステルの細いフィラメントの製造法
US5171504A (en) Process for producing high strength, high modulus thermoplastic fibers
US3790995A (en) Apparatus for the preparation of polyethylene terephthalate filaments
US4113821A (en) Process for preparing high strength polyamide and polyester filamentary yarn
US5137670A (en) Polyester fiber and process for manufacture
US3101990A (en) Process of drawing filamentary structures
EP0528992B2 (de) Schmelzspinnen von ultraorientierten kristallinpolymeren
US3949041A (en) Method for texturing synthetic filament yarn
EP0282660B1 (de) Polyesterfaser und Verfahren zur Herstellung derselben
US4228120A (en) Process for nylon 66 yarn having a soft hand
US4562029A (en) Self-crimping polyester yarn
US4622187A (en) Continuous process for making interlaced polyester yarns
EP0912778B1 (de) Ultra-orientierte kristalline filamente und verfahren eu ihrer herstellung
US5405696A (en) Ultra-oriented crystalline filaments
USRE35972E (en) Ultra-oriented crystalline filaments
US4418032A (en) Process for drawing tows of filaments in water
US3495295A (en) Apparatus for drawing thermoplastic filamentary yarns