US3492691A - Spinning of fibres - Google Patents

Spinning of fibres Download PDF

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Publication number
US3492691A
US3492691A US573532A US3492691DA US3492691A US 3492691 A US3492691 A US 3492691A US 573532 A US573532 A US 573532A US 3492691D A US3492691D A US 3492691DA US 3492691 A US3492691 A US 3492691A
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polymer
stream
air
flow
spinneret
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US573532A
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English (en)
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Paul Lambton Inwood Carr
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Imperial Chemical Industries Ltd
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Imperial Chemical Industries Ltd
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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
    • D01D5/088—Cooling filaments, threads or the like, leaving the spinnerettes
    • D01D5/092—Cooling filaments, threads or the like, leaving the spinnerettes in shafts or chimneys

Definitions

  • the present invention relates to the melt-spinning of fibre-forming polymers.
  • the present invention we provide a process for the spinning of a fibre-forming polymer wherein the said polymer in the liquid state is forced through one or a plurality of holes in a spinneret plate, the stream or streams of polymer formed thereby travelling substantially vertically downwards from the spinneret plate and solidifying as it, or they, pass through the ambient fluid, a flow of ambient fluid being induced by the movement of the stream or streams of polymer initially towards the stream or group of streams of polymer and then following the path of the, or of each, polymer stream, deflecting means being disposed at intervals along the length of the path of the stream or streams of polymer whereby the flow of the ambient fluid towards the stream or each stream, of polymer and thereafter following the path of the, or of each, stream of polymer, is a stable laminar flow, the said conditions of stable laminar flow persisting until the temperature of the, or of each, stream of polymer falls to the solidification point.
  • ambient fluid we mean gases and vapours which are chemically inert towards the polymer; the most convenient gas to use is air.
  • a polymer at a temperature above its melting point is forced through a hole to form a narrow stream of molten polymer.
  • This stream of polymer normally travels vertically downwards and is acted upon by a force in a downwards direction along the length of the stream in such a manner as to attenuate the stream as it cools and eventually solidifies.
  • the speed of movement of the polymer stream along its length increases with distance from the spinneret and becomes quite high at a moderate distance from the exit of the spinneret hole.
  • the uses to which filaments are put demand a high degree of uniformity in the filaments; this in turn demands a high degree of uniformity of the thermal history of all parts of the filament. That is any particular point in the final filament must have been subice jected to substantially the same profile of temperature change as any other point at the same distance from the long axis of the filament.
  • a spinneret plate is used in which are bored a series of holes in some regular geometrical pattern, for example a circle or oval.
  • the flow of air induced towards the polymer streams must come from essentially one side of each polymer stream, that is the side away from the volume which is substantially enclosed by the polymer streams. It is therefore the inflow of air from this side which must be controlled.
  • Convection currents may, for example, be induced by the heated air leaving the vicinity of the polymer stream at points more distant from the exit from the spinneret hole and where the polymer stream has solidified.
  • the members may suitably form a series of control surfaces, of which there should be at least two.
  • the control surfaces may be in the form of complete collars surrounding the group of polymer streams or of more than one member substantially delineating a collar.
  • the collars may, for example, be in the form of annular discs, but are preferably of such shape that the parts further away from the polymer streams are at progressively higher levels with a smooth graduation in order to minimize the entry of rising currents of air between successive control surfaces.
  • Such a formation of the control surfaces also minimizes the breaking away of the zone of air adjacent to the polymer streams and moving with them.
  • the collars may advantageously be in the form of the surface of a conical frustum with the wider part uppermost, or of the surface generated by the rotation of a portion of an exponential curve about the abscissa.
  • the plurality of control surfaces may comprise a single member; such member may, for example be a suitably offset Archimedean screw with a least two complete turns.
  • a greater number than two control surfaces produces an improvement, albeit with diminishing magnitude of improvement with number. Below a separation of about 5 mm., the effect of air drag impairs the necessary free flow of air. At separation greater than about mm., the requisite effect in producing a stable laminar flow is not observed, and the results produced are inferior to those for a lesser separation.
  • Such an arrangement has the effect of smoothing out turbulence in the air stream as it starts to flow between the adjacent control surfaces, and thus facilitates the establishment of laminar flow.
  • the mmeber or members comprising each control surface may be of continuous laminar form or may be pierced by a number of apertures.
  • the number and disposition of such apertures should not be such as to permit the passage freely through them of the ambient fluid in more than a minor amount compared to the total flow.
  • control surfaces should be such that the edge of each control surface nearer to the polymer stream is distant by a predetermined amount.
  • the predetermined amount is controlled mainly by the nature of the ambient fluid and to only a minor extent by the linear speed of the polymer stream and should be such that no part of the member is appreciably nearer to the polymer stream than the point at which the induced air-flow in the direction of motion of the polymer stream is from about 1% to about of the value of the linear rate of motion of the polymer stream. This value may be calculated on the basis of normal physical principles.
  • a suitable distance between a control surface and the polymer stream may be as small as about 4 mm. but should not exceed about 30 mm.
  • a control surface should extend radially for a distance of at least about mm.
  • the inner edge of the control surface may advantageously be conformed so that the distance from it of each of the outermost of the polymer streams is approximately equal.
  • the disposition ,of the control surfaces along the length of the polymer streams should be such as will ensure the closest approximation to laminar flow in the fluid flow induced towards the polymer streams.
  • the effectiveness of the disposition can be checked by the observation of the movement of smoke trails introduced into the vicinity of the control surfaces.
  • melt-spinning is carried out according to the process of our invention, that is with laminar flow of the ambient fluid towards the polymer streams and thereafter along with the polymer streams, the conditions are such that the rate of heat transfer from the polymer streams to the ambient fluid is minimized.
  • the use of the process of our invention results in the minimum degree of orientation, other things being equal. This is manifested in the spun fibre by its possessing a relatively low birefringence. In normal use of melt-spin fibres a predetermined degree of orientation has to be arrived at in order that the fibre shall have the desired useful properties.
  • cold drawing is resorted to, that is drawing of a temperature below the melting point of the polymer of which the fibre is composed.
  • this cold drawing step it is found that fibres as spun having a low degree of orientation can successfully be drawn to a higher draw ratio than fibres having a high degree of orientation as spun.
  • a fibre of low degree of orientation as spun may be of higher denier than when the as-pun orientation is higher.
  • the process of our invention permits the spinning of a higher denier fibre.
  • our invention permits an increase in the windup speed and increase in the throughput per spinneret hole for the same degree of orientation.
  • FIGURE 1 shows a cross-section in a vertical plane through the centre of a spinneret plate, of a series of deflecting members. A multiplicity of polymer streams is shown for clarity, although such a section would not show more than two;
  • FIGURE 2 shows a plan view 0 fthe uppermost deflecting member
  • FIGURE 3 is a representation of a threadline being formed under the conditions of our invention.
  • FIGURE 4 is one representation of a threadline being formed under conditions outside our invention.
  • the members are held in their relative positions (1 /2 inches separation between adjacent annular parts) by means of nuts 10 screwed on to the threaded rods 7, 8 and 9.
  • the assembly of members is disposed with the rods 7, 8 and 9 vertical and the bases of the conical frustal portions 6 uppermost.
  • the uppermost member has its annular part at 2.5 cm. from the spinneret plate.
  • the assembly hereinbefore described was for use with a spinneret plate in which were bored 15 spinning holes of .009 inch diameter with centres on a circle of 1 cm. diameter. The assembly was so positioned with respect to the streams of polymer issuing from the spinning holes that each polymer stream was approximately 4 mm. from the nearest point of each of the conical frustal portions 6.
  • EXAMPLE 1 (A) Using the described apparatus, poly(ethylene terephthalate) of viscosity ratio 1.7 as measured in orthochlorophenol solution at 1% concentration at 25 C., and containing 0.5% of titanium dioxide delustrant, was melt-spun at a temperature of 290 C. at a throughput per hole of 0.4 g. per minute through 15 circular holes of 0.009 inch diameter on a circle of radius 0.25 inch (0.635 cm.). The fibre was wound up at 1,500 cm. per second. The coefiicient of variation of the resultant yarn was determined by weighing 25 lengths of yarn of 10 metres length and calculating the coeflicient in the usual manner. The coeflicient of variation was found to be 0.66%.
  • Example 1A was repeated exactly with the single distinction that a cylinder of gauze was fitted around the assembly of members.
  • the gauze was of 32 meshes per inch and made of 30 gauge wire (British Standard Wire Gauge).
  • the gauze cylinder was in contact with the outer edge of each member of the assembly of members and extended from the spinneret plate to the lowest of the members. Thus the induced flow of ambient air had to flow through the meshes of the gauze.
  • the yarn produced had a coeflicient of variation, measured as described in Example 1A, of 0.4%.
  • EXAMPLE 3 Poly(ethylene terephthalate) of viscosity ratio the same as that used in Example 1, was spun through a single circular hole of 0.009 inch diameter at a throughput per hole of 1.6 g. per minute. The stream of molten polymer was led through the centre points of 1 cm. holes in the centre of a series of 7 cm. discs each disposed horizontally in similar relation to that described for the members for Example 1. The resultant monofil was wound up at 1,500 cm. per second. The monofil was of 16 denier. This is product I.
  • EXAMPLE 4 (A) Using the apparatus of Example 1A, isotactic polypropylene of viscosity ratio 2.8, as measured on a 1% solution in deccehydro-naphthalene at 135 (3., at a temperature of 285 C., at a throughput of 0.25 gm./min./hole through circular holes of diameter 0.015 in. diameter (0.0381 cm.) with centres on a circle of radius 0.635 cm. The yarn was wound up at 10 metres/sec. Using the assembly of members as described in Example 1, the coeificient of variation of the spun yarn was 2.6%.
  • Example 4A was repeated exactly with the only distinction that the assembly of members was omitted.
  • the coefiicient of variation of the spun yarn was 4.3%.
  • the number of members was 8 and all were of identical shape and dimensions similarly oriented and similarly disposed with relation to each other and to the spinneret plate as shown in FIGURE 1.
  • Each member was of the form described in connection with Example 1 with conical angle 100, and base of conical frustum 12 cm. diameter. The top of the conical frustum being of 5.8 cm. diameter for the uppermost member reducing by uniform stages to 5.2 cm. for the lowermost member. This variation was in conformity with the convergence of the filaments to a guide 1.5 metres below the spinneret.
  • the various members were spaced from adjacent members by 2.5 cm.
  • a gauze cylinder was fitted round the device as described in Example 2. The uppermost member was 2.5 cm. from the spinneret plate.
  • the device was fitted below a spinneret plate in which were bored spinneret holes of 0.009 inch diameter in a scatter pattern such that the overall diameter of the set of filaments was initially 5 cm. and the hole spacing was approximately 1 cm.
  • the assembly was positioned so that the clearance between the filaments and the inner edge of each member was approximately 4 mms.
  • Poly(ethylene terephthalate) of viscosity ratio as measured as described in Example 1, 1.7 and containing 0.5% by weight of titanium dioxide was spun under the following conditions:
  • a further improvement in the stability of the air can be effected by incorporating vertical fins in the space between adjacent control surfaces. This is because disturbances in the flow are three dimensional disturbances.
  • EXAMPLE 6 The apparatus was as used in Example 5 with the single exception that vertically and radially disposed laminar members were placed symmetrically between, and forming a bridge between, each adjacent pair of members (5 of FIGURE 1) and between the uppermost member 5 and the spinneret plate.
  • the coefficient of variation of the spun yarn using the stabilization device with this modification was 1.1% measured as before in Example 5.
  • Our invention is applicable not only to an array of spinneret holes with radial symmetry but also to other configurations, for example, a rectangular configuration.
  • EXAMPLE 7 (A) The apparatus used was as described in Example 6 with the distinctions that the spinneret holes were 24 in number and that the spinneret holes were arranged in 6 straight rows of 4 forming a rectangular pattern of overall dimensions 5 cm. x 2.2 cms. The coefficient of variation of the yarn spun using this apparatus was 1.75%.
  • FIG- URES 1 and 2 By way of further explanation of the conditions pertaining in the use of our invention, reference is made to FIG- URES 1 and 2.
  • the threadline 1 moving away from the spinneret 2 under the conditions of our invention induces a flow of air inward as shown by the streamlines and thence in stable laminar flow in the direction of motion of the threadline.
  • the velocity profile of the induced air flow is shown at 4.
  • the transition to turbulence, shown at 5 occurs beyond the point where the threadline has solidified. Under these conditions the heat transfer at a point at a particular distance from the spinneret is constant with time.
  • FIGURE 2 under conditions outside of our invention there is an unstable laminar region 6 which exhibits large lowfrequency fluctuations.
  • Apparatus for melt spinning a fibre-forming polymer comprising: a spinneret for forming at least one stream of polymer travelling substantially vertically downwardly from said spinneret through the ambient fluid in the vicinity of the stream; and ambient fluid control means for inducing the ambient fluid to flow laminarly toward the polymer stream and thereafter laminarly along the path of the polymer stream until the temperature of the stream falls to the solidification point, said means including ambient fluid deflecting elements disposed at spaced-apart intervals along the length of the path of the stream, said deflecting elements being out of contact with and at least partially surrounding the polymer stream, said deflecting elements being collar-shaped annular discs having a central portion shaped as a depending converging conical frustum so as to define at least two annular control surfaces each of which is shaped such that a point moving radially along the surface from the iner to the outer edge has at no time any downward component of motion, the inner edge of each control surface being spaced from the polymer stream not less than about

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
US573532A 1965-08-20 1966-08-19 Spinning of fibres Expired - Lifetime US3492691A (en)

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GB35785/65A GB1088240A (en) 1965-08-20 1965-08-20 Melt spinning of fibre-forming polymers

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3679786A (en) * 1970-05-21 1972-07-25 Phillips Fibers Corp Method and apparatus for melt spinning of synthetic filaments
EP0217097A3 (de) * 1985-08-31 1988-02-17 b a r m a g Barmer Maschinenfabrik Aktiengesellschaft Spinnschacht mit perforierter Teillänge in Düsennähe
US5433591A (en) * 1991-07-23 1995-07-18 Barmag Ag Apparatus for making a synthetic filament yarn
US5688458A (en) * 1992-03-18 1997-11-18 Maschinenfabrik Rieter Ag Method and device to manufacture synthetic endless filaments
US5700490A (en) * 1994-09-30 1997-12-23 Barmag Ag Apparatus and method for the thermal treatment of fibers
WO2002004719A1 (en) * 2000-07-10 2002-01-17 E. I. Du Pont De Nemours And Company Method of producing polymeric filaments

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SG67284A1 (en) * 1991-09-06 1999-09-21 Akzo Nobel Nv Apparatus for high speed spinning multifilament yarns and use thereof
DE4208568A1 (de) * 1992-03-18 1993-09-23 Zimmer Ag Verfahren und vorrichtung zur herstellung synthetischer endlosfilamente
DE9306510U1 (de) * 1992-06-13 1993-06-09 Barmag AG, 5630 Remscheid Spinnvorrichtung zum Spinnen synthetischer Fäden
BR9400682A (pt) * 1993-03-05 1994-10-18 Akzo Nv Aparelho para a fiação em fusão de fios multifilamentares e sua aplicação

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3274644A (en) * 1964-04-27 1966-09-27 Du Pont Adjustable profile chimney
US3313001A (en) * 1965-09-24 1967-04-11 Midland Ross Corp Melt spinning apparatus
US3358326A (en) * 1964-12-03 1967-12-19 Stamicarbon Device for the production of artificial filaments by the melt spinning method

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3274644A (en) * 1964-04-27 1966-09-27 Du Pont Adjustable profile chimney
US3358326A (en) * 1964-12-03 1967-12-19 Stamicarbon Device for the production of artificial filaments by the melt spinning method
US3313001A (en) * 1965-09-24 1967-04-11 Midland Ross Corp Melt spinning apparatus

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3679786A (en) * 1970-05-21 1972-07-25 Phillips Fibers Corp Method and apparatus for melt spinning of synthetic filaments
EP0217097A3 (de) * 1985-08-31 1988-02-17 b a r m a g Barmer Maschinenfabrik Aktiengesellschaft Spinnschacht mit perforierter Teillänge in Düsennähe
US5433591A (en) * 1991-07-23 1995-07-18 Barmag Ag Apparatus for making a synthetic filament yarn
US5688458A (en) * 1992-03-18 1997-11-18 Maschinenfabrik Rieter Ag Method and device to manufacture synthetic endless filaments
US5700490A (en) * 1994-09-30 1997-12-23 Barmag Ag Apparatus and method for the thermal treatment of fibers
WO2002004719A1 (en) * 2000-07-10 2002-01-17 E. I. Du Pont De Nemours And Company Method of producing polymeric filaments
US20020037411A1 (en) * 2000-07-10 2002-03-28 Frankfort Hans R. Method of producing polymeric filaments
US20040140582A1 (en) * 2000-07-10 2004-07-22 Frankfort Hans R. E. Method of producing polymeric filaments

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GB1088240A (en) 1967-10-25
NL6611719A (en, 2012) 1967-02-21

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