US2295942A - Manufacture of filaments - Google Patents

Manufacture of filaments Download PDF

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Publication number
US2295942A
US2295942A US349840A US34984040A US2295942A US 2295942 A US2295942 A US 2295942A US 349840 A US349840 A US 349840A US 34984040 A US34984040 A US 34984040A US 2295942 A US2295942 A US 2295942A
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United States
Prior art keywords
screw
flute
polymer
chamber
spinneret
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
US349840A
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English (en)
Inventor
Reuben T Flelds
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.)
EIDP Inc
Original Assignee
EI Du Pont de Nemours and Co
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
Priority to BE461923D priority Critical patent/BE461923A/xx
Application filed by EI Du Pont de Nemours and Co filed Critical EI Du Pont de Nemours and Co
Priority to US349840A priority patent/US2295942A/en
Priority to GB9804/41A priority patent/GB550991A/en
Application granted granted Critical
Publication of US2295942A publication Critical patent/US2295942A/en
Priority to FR940947D priority patent/FR940947A/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • A—HUMAN NECESSITIES
    • A01—AGRICULTURE; FORESTRY; ANIMAL HUSBANDRY; HUNTING; TRAPPING; FISHING
    • A01K—ANIMAL HUSBANDRY; AVICULTURE; APICULTURE; PISCICULTURE; FISHING; REARING OR BREEDING ANIMALS, NOT OTHERWISE PROVIDED FOR; NEW BREEDS OF ANIMALS
    • A01K47/00—Beehives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/275—Recovery or reuse of energy or materials
    • B29C48/277—Recovery or reuse of energy or materials of materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/285—Feeding the extrusion material to the extruder
    • B29C48/286—Raw material dosing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/285—Feeding the extrusion material to the extruder
    • B29C48/29—Feeding the extrusion material to the extruder in liquid form
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
    • B29C48/793—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling upstream of the plasticising zone, e.g. heating in the hopper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/25—Component parts, details or accessories; Auxiliary operations
    • B29C48/78—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling
    • B29C48/80—Thermal treatment of the extrusion moulding material or of preformed parts or layers, e.g. by heating or cooling at the plasticising zone, e.g. by heating cylinders
    • B29C48/83—Heating or cooling the cylinders
    • B29C48/832—Heating
    • 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
    • D01D1/00—Treatment of filament-forming or like material
    • D01D1/04—Melting filament-forming substances
    • 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
    • D01D1/00—Treatment of filament-forming or like material
    • D01D1/06—Feeding liquid to the spinning head
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
    • B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
    • B29C48/05—Filamentary, e.g. strands
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • This invention relates to the manufacture of filaments and, more particularly, to the manuiacture of relatively coarse filaments of synthetic linear condensation polymers by melting and spinning the polymers.
  • synthetic linear condensation polymers new polymeric materials such as described in United States Patents 2,071,250 and- 2,071,253, and in United States application Serial No. 136,031, filed April 9, 1937, now Patent No. 2,130,948, all of W. H. Carothers.
  • More specific objects are to provide equipment and procedure to eiTect melting of the polymers without access of oxygen, to minimize the duration of exposure of the molten material to temperatures capable of causing its decomposition, to deliver molten material bubble-free to the spinneret under uniform pressure, and to conduct the process as a whole, from melting to spinning, under minimum pressure, in order to minimize the content of releasable gases within the molten material.
  • a further object of the invention is to provide equipment which is adapted to handle molten polymer over a wide range of consistency and over a wide range of initial admixture with gas, and to provide so effectively for the escape of water vapor that it is adapted to handle initially wet polymer.
  • a process which comprises melting a synthetic linear condensation polymer while blanketed with carbon dioxide to the exclusion of oxygen and at no greater than atmospheric pressure, introducing the melted polymer into a screw pump having a capacity at its intake end several times greater than its capacity at its discharge .end, and delivering said molten polymer under pressure to a spinneret to cause the molten polymer to pass through the orifice of the spinneret and emerge as a filament, the polymer being kept out of contact with oxygen from the time it is melted until its emergence from the spinneret as a filament.
  • the melted polymer may be forced through the spinneret either by the pressure developed in the screw pump or by auxiliary pumping means interposed between the screw pump and the spinneret.
  • the fllame t should be rapidly cooled as it is extruded a this is preferably accomplished by bringing it into contact with water.
  • capacity of the screw pump is meant the volume of material forwarded per turn of the screw, assuming geometrically perfect delivery with no compression or slippage.
  • capacity of the screw pump must be several times as great at its intake end as at its delivery end, preferably in a ratio of not less than 4 to 1.
  • the screw pump may be constructed so that its change in capacity from end to end is gradual, it is usually more convenient to construct the screw pump so that the capacity is changed abruptly at some point alongdvhe Rrew and this type of screw pump is preferred.
  • the screw pump is used to deliver the molten polymer directly to the spinneret without any interposed auxiliary pumping means.
  • a chamber I I which is desirably of cylindrical shape with a truncated conical bottom and is provided with a cover I2 containing a port I3 through which the polymer may be fed into the chamber.
  • a cover I2 containing a port I3 through which the polymer may be fed into the chamber.
  • a cover I2 In the lower part of the chamber II are banks of tubes I, I4 running at right angles to each other and adapted to carry a heating fluid for melting the polymer.
  • the cylindrical sides and coni- 1 cal lower portion of the chamber are enclosed in a Jacket l-5 similarly adapted to carry a heating fluid in circulation, and the tubes I4, I4 preferably communicate with this jacket so that a single source of heating fluid will provide the circulation thereof in .both Jacket and tubes.
  • the heating chamber II is provided also with means for the entry and escape of the blanketing gas.
  • these take the form of pipes passing through the cover I2 and, preferably, the intake pipe I6 extends downward within the chamber nearly to the level of the uppermost of the banks of tubes while the outlet pipe I1 is located near or in communication with the port I3.
  • the blanketing gas, carbon dioxide is fed into the chamber II through the pipe I6 and flows out of the chamber either through the pipe I! or, if the port I3 is open, then also through this port.
  • This y depthoithe flute is meant the distance, measured radially, from the floor of the flute in the screw to the inner surface of the casing of the screw pump. Practically, the depth of this flute should bebetween .050" and .150". If an un-' usually viscous melt were to be pumped, the depth of the flute might be slightly greater.
  • the present invention resides in the discovery that proceeding as described above coarse filaments of .010" diameter and greater, especially those filaments of- .020? diameter and greater, undrawn, may be readily extruded without flaws whereas applicant has been unable to find any other practical way of manufacturing such coarse,
  • the procedure of the present invention is carefully designed to reduce the gases absorbed by the molten polymer to such a minimum that they are not released from the extruded filament.
  • the feeding port I3 be provided with a cover I8 and that this be kept in place whenever the port is not being used for feeding.
  • An opening at the bottom of the truncated conical portion of the chamber II communicates with an opening into the casing I9 of a screw pump of special design.
  • This casing I9 is provided with a jacket 20 for the circulation of a heating fluid, this jacket 20 and the jacket I5 of the heating chamber intercommunicating through a duct 2
  • This closed circulating system is provided with an inlet 22 in the jacket t5 and with an outlet 23 in the jacket 20 for return of the heating fluid to the source of heat.
  • the interior wall of the casing I 9 of the screw .pump is accurately cylindrical. Within it, with clearance as hereinafter described, rotates the screw member 24 which, at the intake end of the screw pump, is extended through the casing I9 to constitute a shaft 25 by which the screw member 24 may be rotated through a chain drive actuating a pulley or sprocket 26 keyed to this shaft 25.
  • the screw member 24 carries a double-lead flute 21 which terminates in a circumferential groove 28.
  • the screw member 24 carries a single-lead flute having a capacity substantial- 1y less than that of the double-lead flute'Z'I.
  • the dimensions of the screw pump may suitably be as follows:
  • the important influences on the diameter are the linear rate at which the filament produced is carried away from the spinneret and the rate of rotation of the pump screw.
  • - polymer which is a viscous liquid, may be likened to rolling a pencil between the palms of the hands with one palm held stationary. That is,
  • the molten polymer is, in effect, rolled between generated, as hereinafter described, by the screw member 24 within the casing 19, the molten polymer is extruded to form filaments and the like.
  • the channel communicating with the spinneret is contained within a block 3! attached to the casing I! of the screw pump at the discharge end.
  • a second hole cut in the block 3 I conveniently at right angles with the channel 32 and not extending through the block, constitutes a channel 34 which serves to connect the channel 32 with the spinneret 30.
  • Molten polymer enters the casing IQ of the screw pump from theheating chamber II and is carried along in the direction of the spinneret by the rotation of the screw member 24.
  • the side walls of the flute offer resistance to the desired motion of the molten polymer and, for this reason, the flute must not be too narrow; it has been found that the width of the flute should not be less than about 0.125 inch, and preferablynot less than about 0.25 inch.
  • the width of the flute should not be too great, since on a screw of reasonable length the path of the flute would be shortened thereby too much to prevent back eter of the screw, and it has been found to be a desirable rule that the width of the flute shall not exceed one third of the diameter, regardless At a fixed ratio of width of flute to diameter of screw, a change in the latter does not appreciably change the length of path of the flute upon a screw member of given length, nor does it'change the angle of the flute with respect to a longitudinal element of the screw member. The limiting ratio of one to three provides for an adequately long path upon a screw member of reasonable length, and also avoids the loss of efliciency which results when this angle is too small.
  • the diameter of the screw member will, for practical reasons, be ordinarily between about one inch and three inches. For reasons of rigidity and torsional strength it must not be too small, whereas on the other hand there is no point in making it too large, since the corresponding increase in peripheral speed, at a given rotational speed, tends to increase the intensity of friction upon and within the molten polymer and thus to cause objectionable overheating.
  • a combination of the narrowest feasible flute (stated above to be about 0.125 inch). upon a screw member of the smallest feasible diameter (stated above to be one inch), represents a ratio, of width of flute to diameter of screw, of one to eight. But in general, particularly on screws of larger diameters, the ratio may permissibly be as low as one to ten.
  • the width of the flute is conveniently expressed in terms of the diameter of the screw member, as being between one tenth and one third of that diameter. member of diameter 1.625 inches, such as that described above, the preferred range of width of flute, i. e., 0.25 to 0.50 inch, lies within this somewhat broader range.
  • the pitch'of the screw ordinarily, will be automatically determined by the width of the flute employed because'the width of the land'. between successive convolutions of the flute will be made as narrow as efllciency in sealing between convolutions of the flute and acceptable resistance to wear will permit; increasing the In the case of a screw width of the land beyond this point would be simply uneconomical as it would serve no good purpose. It has been found that a width of .050 for the land" is, sufllcient both to give adequate resistance to wear and to seal the flute eflectively.
  • auxiliary pumping means such as a gear pump is to be interposed between the screw pump and the spinneret, a feasible but not preferred embodiment of the invention, for the purpose of furnishing the desired pressure for extruding the molten polymer through the spinneret, more leeway is permitted-in the design of the screw pump because the screw pump is then only required to compress the,molten polymer and dissolve the entrapped gases, not to deliver the polymer at a pressure high enough to extrude it through the spinneret. Also,'-at the intake end of the screw pump, the dimensions of the flute in the screw need not be within the limits discussed above although it is preferred that they should be.
  • the heat-- ing chamber ll maybe widely varied in design providing only that it is adapted to effect the melting of the polymer at atmospheric pressure while the polymer is completely blanketed with carbon dioxide gas. Connecting the heating jackets l5 and 20 is obviously a matter of con- .venience since independent heating jackets would function just as, well.
  • spinneret 30 forms no part of the present invention.
  • the construction of these spinnerets is well known in the art and the selection of a suitable one will be based on considerations not involving the present invention.
  • the present invention has been described in connection with the melting and spinning of synthetic linear condensation polymers of which.
  • the synthetic linear condensation polymers include synthetic linear polyamides, that is, synthetic linear polymers containing -CONH,- units in the linear'chain, synthetic linear polymers such as polyesters, polyethers, polyacetals, and mixed polyester-polyamides, such as may be prepared by condensation reactions as described in-United States Patent 2,071,250.
  • the filament-forming material used in accordance withthe present invention may contain modifying agents, e. g., luster-modifying agents, plasticizers, pigments, dyes, antioxidants, resins. et cetera.
  • modifying agents e. g., luster-modifying agents, plasticizers, pigments, dyes, antioxidants, resins. et cetera.
  • the present invention may be used to advantage in the handling of compositions in which the formation of bubbles may be caused by the presence of a modifying agent.
  • the invention provides a method and an apparatus whereby organic filament-forming compounds, and compositions comprising them, can be spun into coarse filaments of uniform diameter, free from bubbles and discoloration.
  • the appartus is simple, and the relatively low pressures involved make for economy of construction and safety in operation.
  • the invention makes feasible the use of polymer of high content of moisture.
  • Process of preparing coarse filaments of at least .020" diameter from a synthetic linear condensation polymer which comprises melting said polymer while blanketed with carbon dioxide gas under a pressure not exceeding atmospheric pressure, introducing the molten polymer into a screw pump having a capacity at its intake end several times greater than its capacity at its discharge end, and delivering said molten polymer under pressure to a spinneret to cause said molten polymer to be extruded therethrough in the form of a filament.
  • Process of preparing coarse filaments of at least .020" diameter from a synthetic linear condensation polymer which comprises melting said polymer while blanketed with carbon dioxide gas under a pressure not exceeding atmospheric pressure, introducing the molten polymer into a screw pump having a capacity at its intake end at least four times as great as its capacity at its discharge end, and delivering said molten polymer under a pressure of about 75 pounds per square inch to a spinneret to cause said molten polymer, to be extruded therethrough in the form of a filament.
  • Apparatus for preparing coarse filaments from a synthetic linear which comprises a chamber for melting said polymer, means for heating said chamber, means for introducing an inert gas heavier than air into I ket at least the lower portion thereof, a screw pump disposed below said chamber and having its intake end communicating with the bottom of said chamber, and a spinneret in communication with the discharge end of said screw pump, said screw pump having a capacity at its intake end at least four times as great as its capacity at its discharge end and comprising a screw provided at the discharge end with a flute between .050" and .150" in depth and .25" and .50" in width.
  • Apparatus for preparing coarse filaments from a synthetic linear condensation polymer which comprises a chamber open to the atmosphere for melting said polymer, means for heating said chamber, means for introducing an inert gas heavier than air into said chamber to blanket at least the lower portion thereof, a screw pump disposed below said chamber and having its intake end communicating with the bottom of said chamber, and a spinneret in communication with the discharge end of said screw pump, said screw condensation polymer,
  • Apparatus for preparing coarse filaments from a synthetic linear condensation polymer which comprises a chamber open to the atmosphere for melting said polymer, means for heating said chamber, means for introducing an inert gas heavier than air into said chamber to blanket at least the lower portion thereof, a screw pump disposed below said chamber and having its intake end communicating with the bottom of said chamber, and a spinneret in communication with the discharge end of said screw pump, said screw pump having a capacity at its intake end at least four times as great as its capacity at its discharge end and comprising a screw between 1.0" and 2.0" in diameter and provided at the discharge end with a flute between .050" and .150" in depth and between one-tenth and one-third of the diameter of the screw in width.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Environmental Sciences (AREA)
  • Textile Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Animal Husbandry (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Multicomponent Fibers (AREA)
  • Nozzles For Electric Vacuum Cleaners (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
US349840A 1940-08-02 1940-08-02 Manufacture of filaments Expired - Lifetime US2295942A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BE461923D BE461923A (xx) 1940-08-02
US349840A US2295942A (en) 1940-08-02 1940-08-02 Manufacture of filaments
GB9804/41A GB550991A (en) 1940-08-02 1941-08-01 Improvements in and relating to the manufacture of coarse filaments
FR940947D FR940947A (fr) 1940-08-02 1945-11-08 Procédé de fabrication de filaments à partir de substances polymérisées et appareil pour son application

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US349840A US2295942A (en) 1940-08-02 1940-08-02 Manufacture of filaments

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US2295942A true US2295942A (en) 1942-09-15

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US349840A Expired - Lifetime US2295942A (en) 1940-08-02 1940-08-02 Manufacture of filaments

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US (1) US2295942A (xx)
BE (1) BE461923A (xx)
FR (1) FR940947A (xx)
GB (1) GB550991A (xx)

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2479727A (en) * 1947-07-23 1949-08-23 Daniels Farrington Elimination of fissures with carbon dioxide
US2480615A (en) * 1946-08-28 1949-08-30 Du Pont Working of polyethylene
US2515136A (en) * 1947-07-18 1950-07-11 Wingfoot Corp Method of melting polymers
US2517711A (en) * 1945-07-13 1950-08-08 Celanese Corp Production of artificial materials
US2571975A (en) * 1947-05-10 1951-10-16 Du Pont Melt spinning process
US2596272A (en) * 1947-03-27 1952-05-13 Bata Narodni Podnik Method and device for an automatic supply of low molecular raw material for continuous production and spinning of polyamides
US2605502A (en) * 1949-10-05 1952-08-05 Celanese Corp Preparation of filamentary material
DE875559C (de) * 1943-11-24 1953-05-04 Camille Dreyfus Vorrichtung zum Zufuehren fester Stoffe in einen erhitzten Behaelter
US2638631A (en) * 1949-08-09 1953-05-19 Polymer Corp Production of strip stock from polyhexamethylene adipamide
US2641799A (en) * 1950-05-15 1953-06-16 Baldwin Rubber Co Apparatus for extruding pellets
US2683073A (en) * 1951-08-22 1954-07-06 Du Pont Process for preventing nylon gel formation
US2696023A (en) * 1949-07-11 1954-12-07 Polymer Corp Method for molding articles from plastic materials
US2698459A (en) * 1951-06-21 1955-01-04 American Viscose Corp Spinning or extruding apparatus
DE926682C (de) * 1943-05-14 1955-04-21 Hoechst Ag Verfahren und Vorrichtung zum Schmelzspinnen
US2707306A (en) * 1952-08-22 1955-05-03 Celanese Corp Melt spinning apparatus
US2725596A (en) * 1953-01-29 1955-12-06 Celanese Corp Extruder
US2740986A (en) * 1951-04-24 1956-04-10 Ici Ltd Melt spinning apparatus
US2747222A (en) * 1951-06-11 1956-05-29 Polymer Corp Production of nylon rod
US2889577A (en) * 1956-06-27 1959-06-09 Nat Plastics Products Company Spooling
US2923970A (en) * 1960-02-09 genovese
US3035303A (en) * 1958-11-14 1962-05-22 Ici Ltd Extrusion of organic thermoplastic polymeric materials
US3072957A (en) * 1960-04-21 1963-01-15 Monsanto Chemicals Mixers
DE1167482B (de) * 1950-05-31 1964-04-09 Toyo Rayon Co Ltd Schmelzspinnvorrichtung fuer organische Stoffe
US3285592A (en) * 1963-05-27 1966-11-15 Kanegafuchi Spinning Co Ltd Method and apparatus for dehydrating and melting thermoplastic polymers for spinning or molding
US3345445A (en) * 1963-03-15 1967-10-03 Snia Viscosa Melt spinning process of polyamides
US3360822A (en) * 1964-11-09 1968-01-02 Barmer Maschinenfabrik Ag Wupp Hot melt extruder
US3554449A (en) * 1968-12-23 1971-01-12 Prismo Universal Corp Portable plastic melter
US4161391A (en) * 1978-03-14 1979-07-17 Allied Chemical Corporation Melting apparatus
US5061170A (en) * 1989-12-08 1991-10-29 Exxon Chemical Patents Inc. Apparatus for delivering molten polymer to an extrusion
US5458838A (en) * 1992-03-11 1995-10-17 Kabushiki Kaisha Kobe Seiko Sho Heating and extruding method for bulk preform
US5814278A (en) * 1996-04-26 1998-09-29 Minnesota Mining And Manufacturing Company Shrouded reaction vessel
US20150016211A1 (en) * 2013-07-09 2015-01-15 Wenger Manufacturing, Inc. Steam/water static mixer injector for extrusion equipment

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE528734A (xx) * 1953-06-25
BE550654A (xx) * 1955-10-10 1900-01-01
DE1118394B (de) * 1956-09-20 1961-11-30 Bayer Ag Verfahren zum Schmelzen von Polyamidschnitzeln bei der Herstellung synthetischer Faeden

Cited By (39)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2923970A (en) * 1960-02-09 genovese
DE926682C (de) * 1943-05-14 1955-04-21 Hoechst Ag Verfahren und Vorrichtung zum Schmelzspinnen
DE875559C (de) * 1943-11-24 1953-05-04 Camille Dreyfus Vorrichtung zum Zufuehren fester Stoffe in einen erhitzten Behaelter
US2517711A (en) * 1945-07-13 1950-08-08 Celanese Corp Production of artificial materials
US2480615A (en) * 1946-08-28 1949-08-30 Du Pont Working of polyethylene
US2596272A (en) * 1947-03-27 1952-05-13 Bata Narodni Podnik Method and device for an automatic supply of low molecular raw material for continuous production and spinning of polyamides
US2571975A (en) * 1947-05-10 1951-10-16 Du Pont Melt spinning process
US2515136A (en) * 1947-07-18 1950-07-11 Wingfoot Corp Method of melting polymers
US2479727A (en) * 1947-07-23 1949-08-23 Daniels Farrington Elimination of fissures with carbon dioxide
US2696023A (en) * 1949-07-11 1954-12-07 Polymer Corp Method for molding articles from plastic materials
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Also Published As

Publication number Publication date
FR940947A (fr) 1948-12-28
GB550991A (en) 1943-02-03
BE461923A (xx) 1900-01-01

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