US2273188A - Method and apparatus for producing artificial structures - Google Patents

Method and apparatus for producing artificial structures Download PDF

Info

Publication number
US2273188A
US2273188A US267386A US26738639A US2273188A US 2273188 A US2273188 A US 2273188A US 267386 A US267386 A US 267386A US 26738639 A US26738639 A US 26738639A US 2273188 A US2273188 A US 2273188A
Authority
US
United States
Prior art keywords
pressure
chamber
molten
extrusion
autoclave
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
US267386A
Other languages
English (en)
Inventor
Graves George De Witt
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 BE464699D priority Critical patent/BE464699A/xx
Application filed by EI Du Pont de Nemours and Co filed Critical EI Du Pont de Nemours and Co
Priority to US267386A priority patent/US2273188A/en
Priority to DEP80627D priority patent/DE740273C/de
Application granted granted Critical
Publication of US2273188A publication Critical patent/US2273188A/en
Priority to FR925323D priority patent/FR925323A/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • 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
    • D01D1/10—Filtering or de-aerating the spinning solution or melt
    • D01D1/103—De-aerating
    • 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
    • D01D4/00—Spinnerette packs; Cleaning thereof

Definitions

  • This invention relates to the extrusion of molten organic filamentand film-forming compositions in the form of filaments, yarns, ribbons,
  • the synthetic linear polymers with which this invention is particularly concerned may, for example, be prepared by the condensation reactions described in U. S. Patents Nos. 2,071,250, 2,071,252 and 2,071,253.
  • the most valuable of these superpolymers for filaments, yarns and films are the These polyamides are of two types: those obtainable from monoaminomonocarboxylic acids or their amide-forming derivatives, including caprolactam, and those obtainable from the reaction of suitable diamines and dibasic carboxylic acids. This latter type of polyamide is more fully described in U. S. Patent No. 2,130,948.
  • These superpolymers are capable of being extruded in the molten state directly into the form of filaments, yarns, bristles, ribbons and the like.
  • melt spinning This process is hereinafter referred to as melt spinning
  • melt spinning These polymers are best prepared in a large autoclave without a solvent and under conditions so that at the end of the polymer-making cycle there is produced a large volume of the material in the form of a very viscous liquid, 10-20 above its melting point.
  • .It is a further object of this invention to provide an improved method and apparatus for the melt spinning of suchpolymers directly from the reaction vessel in which the polymer is synthesized;
  • molten fiber-forming polymer in general, by transferring portions of the molten fiber-forming polymer from the vessel in which it is synthesized through a lock or valve into an auxiliary chamber, where it may be subjected to pressure and/or vacuum and from whence it is led by suitable valves, conduits, etc., to an extrusion device such as a spinneret and spun in the form of filaments, yarns, ribbons and the like.
  • Figure 1 is a diagrammatic cross-sectional view of one modification of this invention.
  • Figure 2 is a diagrammatic cross-sectional view of another modification of the invention.
  • FIG. 1 is'shown a closed polymerizing autoclave 8 with a conduit ID, provided with a three-way valve l2 for removing or introducing gases.
  • the autoclave is shown partially filled with the molten composition I4.
  • ! has a conduit 2
  • the autoclave 8 and auxiliary chamber 20 may also be joined by the conduit 24 to permit transfer of the gas which is displaced during a transfer of the composition I4 from 8 to 20.
  • the conduit 25 is provided with a valve 26.
  • the pump 32 is adapted to meter the molten material from chamber 20 to the spinneret assembly 34.
  • the molten composition is forced through the spinneret assembly 34, and as a consequence is spun in the form of filaments or the like which are drawn off and collected in an orderly manner.
  • valve I8 When a sufficient quantity of the material M has been admitted to chamber 20, the valve I8 is closed and vacuum is applied to the chamber 20, through the conduit 2
  • the vacuum in chamber 20 removes gaseous decomposition products from the molten material M.
  • the valve 22 i then reversed and gas admitted to the system. This increase in pressure tends to dissolve any remaining bubbles and to keep in solution any additional decomposition products formed. Since the solution of bubbles can be increased and further bubble formation inhibited by applying superatmospheric pressures through the valve 22', this is usually preferred.
  • valve 30 is then opened.
  • the molten material led through the passage 28 to the pump 32 which meters it to the spinneret assembly 34 from which it is forced in the form of a plurality of continuous filaments 36 which are collected in an orderly manner in the form of a yarn.
  • vacuum is applied to the autoclave 8 through .the valve l2 and conduit II] to remove bubbles, after which the valve I2 is reversed and gas is admitted to autoclave 8 until a pressure equal to or slightly in excess of that in chamber 20 is reached.
  • the valves I8 and 26 are opened and the supply of material M in the chamber 20 is replenished without interrupting the spinning.
  • valves I8 and 26 are then closed and the pressure in the autoclave 8 released through the valve l2 and the steps of applying a vacuum and pressure to autoclave 8 repeated.
  • the suppl of material in the chamber 28 again approaches exhaustion, the transfer of an additional quantity of polymer from 8 to 2D is repeated.
  • auxiliary feeding chambers connected between the pump and autoclave so that one chamber may be filled with the molten composition from the autoclave and subjected to pressure and/or vacuum while the other is feeding the composition to the pump and spinneret assembly.
  • conduit I6 is split into conduits IBa and I6b, each provided with a valve IM and lb.
  • 6a is connected to an auxiliary feeding chamber 20a having an outlet conduit 28a and a valve 30a.
  • 6b is connected to an auxiliary feeding chamber 202) having an outlet conduit 2% and a valve 302).
  • Conduits 28a and 28b lead to a single conduit 3i which is connected to pump 32.
  • Each of the auxiliary feeding chambers 20a and 20b may be connected to the autoclave B by means of'a return pipe 24 and valve 26 as shown in Figure 1.
  • the chambers 20a and 20b are provided with conduits 2
  • the two auxiliary feeding chambers 20a and 20b together with their respective conduits and valves, ofier parallel lines of flow between the autoclave 8 and pump 32.
  • the molten composition may be fed to pump 32 from one feeding chamber, for example chamber 20a, during the same period that the other feeding chamber, chamber 28b, is being charged and subjected to pressure and/or vacuum from the autoclave 8.
  • the procedure may then be reversed to feed pump 32 from chamber 20b during the same period as chamber 20a is being charged from the autoclave.
  • the actual steps of charging, and subjecting to pressure and/or vacuum, the feeding chambers and feeding of the composition to the pump will be the same as those above described with reference to Figure 1.
  • three feeding chambers may be used to serve two spinning positions.
  • an autoclave of substantially any type or size may be used for the synthesizing of the molten organic filament-forming composition, from a standpoint of economy in commercial operations the autoclave should have a capacity of at least pounds and preferably at least 250 pounds, and be of such a type as will quickly and uniformly heat the reactants to the desired temperature, and maintain the molten composition at a substantially constant temperature.
  • the size of the auxiliary chambers and the quantity of material admitted will depend on several factors. It will depend, on the one hand,
  • the auxiliary chamber should have a capacity of at least one gallon and preferably at least five gallons. On the other hand, to eliminate bubbles from the products it is preferred that the auxiliary chamber does not greatly exceed a capacity of gallons, or at the most gallons.
  • the molten polymer it is preferred, in general, to subject the molten polymer to alternate vacuum and pressure whereby to eliminate bubbles therefrom.
  • the subjecting of the molten material to a vacuum may be eliminated, and bubble solution maybe secured by solely subjecting the molten material to pressure.
  • This can conveniently be accomplished by alternately subjecting the molten polymer to atmospheric pressure and superatmospheric pressure.
  • the composition comes to equilibrium with the gaseous decomposition products at atmospheric pressure, and any excess passes off into the atmosphere. Then, upon subjecting the composition to superatmospheric pressure the gaseous decom-, position products remaining are dissolved in the molten metal.
  • valves l2 and 22 willusually be connected to the source of such a gas.
  • the single pump illustrated in the figures may be replaced by two pumps mounted in series, the first having a greater capacity than the second as disclosed in Graves application Serial No. 232,314, filed September 29, 1938.
  • the molten material is thus subjected to a high pressure between the two pumps and bubbles dissolved thereby, insuring the supply of bubblefree polymer to the second or metering pump.
  • Such a combination may result in yarns of even more uniform denier and permits wider latitude in the quantity of molten material admitted to the auxiliary chamber and the gas pressures and vacuums employed.
  • filament-forming composition in which decomposition and/or bubble formation during extrusion may be present.
  • synthetic linear polymers such as polyesters, polyethers, polyacetals and mixed polyester-polyamides such as may be prepared by condensation reactions as described in U. S. Patent No. 2,071,250.
  • Other types of ments, yarns, ribbons and synthetic polymers such as ethylene polymers, vinyl polymers, polystyrene and polyacrylic acid derivatives may also be spun with advantage in accordance with the present invention.
  • the filament-forming material used in accordance with the present invention may contain modifying agents; e. g., luster-modifying agents, plasticizers, pigments and dyes, anti-oxidants, resins, etc.
  • the modifying agents may be added either to the composition in the autoclave or in the auxiliary feeding chamber.
  • the present invention can be used to advantage in extruding filmor filament-forming compositions in which the bubble formation is caused by the presence of a modifying agent.
  • this invention has been illustrated by the spinning of yarn from a single position, this invention is not so limited. Similarly, as indicated previously, this invention may be used in the production of film, ribbons, bristles and the like, or may be used for the coating of wire, fabrics, etc.
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions, during the extrusion thereof, at a pressure sufliciently high to bles therefrom, and during said extrusion of one of said successive portions subjecting at least a portion of the remainder of said given quantity 1 of said superpolymer to a pressure substantially below said extrusion pressure, and then to a pressure at least equal to said extrusion pressure, and then passing, under pressure, another of said successive portions from said remainder of said given quantity of superpolymer, for said continuous extrusion through said structureforming device.
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions,
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer, not to exceed one-fifth of said given quantity, and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions, during the extrusion thereof, at a superatmospheric pressure sufliciently high to eliminate bubbles therefrom, and during said extrusion of one of said successive portions subjecting at least a portion of the remainder of said given quantity of said superpolymer to a pressure substantially below said extrusion pressure, and then to a pressure at least equal to said extrusion pressure, and then passing, under pressure, another of said successive portions from said remainder of said given quantity of superpolymer, for said continuous extrusion through said structure-forming device.
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions, during the extrusion thereof, at a superatmospheric pressure sufiiciently highto eliminate bubbles therefrom, and during said extrusion of one of said successive portions subjecting the remainder of said given quantity of superpolymer to a pressure substantially below said extrusion pressure, and then to a pressure at least equal to said extrusion pressure, and then passing, under pressure, another of said successive portions from said remainder of said given quantity of said superpolymer, for said continuous extrusion through said structure-forming device.
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions, during the extrusion thereof, at a pressure sufficiently high to eliminate bubbles therefrom, and during said extrusion of one of said successive portions subjecting another of said successive portions of said given quantity of superpolymer to a pressure substantially below said extrusion pressure, and then to a pressure at least equal to said extrusion pressure, and then passing, under pressure, said other of said successive portions of said given quantity of superpolymer, for said continuous extrusion through said structureforming device.
  • the steps comprising withdrawing, in a closed system from a given quantity, successive fractional portions of molten superpolymer and extruding said successive portions in a continuous extrusion operation through a structure-forming device, continuously maintaining said withdrawn portions, during the extrusion thereof, at a pressure sufficiently high to eliminate bubbles therefrom, and during said extrusion of one of said successive portions subjecting another of said successive portions of said given quantity of said superpolymer to a vacuum substantially below said extrusion pressure, and thenv to a pressure at least equal to said extrusion pressure, and then passing, under pressure, said other of said successive portions of said given quantity of said superpolymer, for said continuous extrusion through said structure-forming device.
  • a reaction vessel for synthesizing a linear superpolymer at a temperature above the melting point thereof, a closed auxiliary feeding chamber connected to said reaction vessel, whereby a portion of said superpolymer from said vessel may be passed to said chamber, means for passing gas from the chamber to said vessel, means for closing the connection between said vessel and chamber, means for evacuating said vessel, means for passing a gas into said chamber, means for passing said polymer from said chamber into a pump, a spinneret assembly, and means for passing said polymer from said pump to said spinneret assambly.
  • a closed system comprising a reaction vessel for synthesizing a linear superpolymer at a temperature above the melting point thereof, an auxiliary feeding chamber, conduit means connecting said chamber to said vessel, means for closing said conduit means, conduit means for passing a gas from said chamber to said vessel, means for evacuating said vessel, means for evacuating said chamber, means for passing a gas into said vessel, means for passing a gas into said chamber, a pump, conduit means connecting said pump to said chamber, a spinneret assembly, and conduit means connecting said spinneret assembly to said pump.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
US267386A 1939-04-12 1939-04-12 Method and apparatus for producing artificial structures Expired - Lifetime US2273188A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
BE464699D BE464699A (US07860544-20101228-C00003.png) 1939-04-12
US267386A US2273188A (en) 1939-04-12 1939-04-12 Method and apparatus for producing artificial structures
DEP80627D DE740273C (de) 1939-04-12 1940-04-13 Verfahren zur kontinuierlichen Verformung hitzeempfindlicher schmelzbarer linearer Superpolymeren
FR925323D FR925323A (fr) 1939-04-12 1946-04-08 Procédé et installation pour la fabrication de produits synthétiques façonnés

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US267386A US2273188A (en) 1939-04-12 1939-04-12 Method and apparatus for producing artificial structures

Publications (1)

Publication Number Publication Date
US2273188A true US2273188A (en) 1942-02-17

Family

ID=23018552

Family Applications (1)

Application Number Title Priority Date Filing Date
US267386A Expired - Lifetime US2273188A (en) 1939-04-12 1939-04-12 Method and apparatus for producing artificial structures

Country Status (4)

Country Link
US (1) US2273188A (US07860544-20101228-C00003.png)
BE (1) BE464699A (US07860544-20101228-C00003.png)
DE (1) DE740273C (US07860544-20101228-C00003.png)
FR (1) FR925323A (US07860544-20101228-C00003.png)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2437704A (en) * 1943-11-24 1948-03-16 Celanese Corp Method and apparatus for the melt extrusion of artificial materials
US2437686A (en) * 1943-11-24 1948-03-16 Celanese Corp Process for the extrusion of fused artificial materials
US2462149A (en) * 1944-12-22 1949-02-22 Int Standard Electric Corp Process for treatment of cable insulated with thermoplastic material
US2503251A (en) * 1945-02-16 1950-04-11 Ici Ltd Production of filaments, fibers, and the like
US2515250A (en) * 1947-11-07 1950-07-18 Dow Chemical Co Method of making and storing compositions comprising thermoplastic resins and normally gaseous solvents
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
DE914668C (de) * 1943-05-31 1954-07-08 Phrix Werke Ag Verfahren zum kontinuierlichen Verspinnen von linearen Superpolymeren, insbesondere Superpolyamiden
US2707306A (en) * 1952-08-22 1955-05-03 Celanese Corp Melt spinning apparatus
US2720463A (en) * 1950-11-17 1955-10-11 American Cyanamid Co Gelatin capsule casting composition preparation
US2757416A (en) * 1950-09-12 1956-08-07 Polymer Corp Method for handling and melting nylon to be used in molding articles
US2810630A (en) * 1953-11-02 1957-10-22 Hoechst Ag Device for the continuous polymerization and extrusion of organic synthetic substances, especially polyamides
US2888711A (en) * 1950-09-01 1959-06-02 British Celanese Production of filamentary materials
US2911678A (en) * 1957-04-12 1959-11-10 Phillips Petroleum Co Molding of void-free olefin polymers using pressure, vacuum and directional cooling
US2918701A (en) * 1956-02-23 1959-12-29 Eastman Kodak Co Method for pelleting organic thermoplastic materials
WO2014151735A1 (en) * 2013-03-15 2014-09-25 Ascend Performance Materials Operations Llc Polymerization coupled compounding process
US20200200224A1 (en) * 2018-12-25 2020-06-25 Jtekt Corporation Method of manufacturing constituent member of constant-velocity joint

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE887691C (de) * 1949-12-05 1953-08-27 Phrix Werke Ag Verfahren und Vorrichtung zum kontinuierlichen Verformen, ins-besondere Verspinnen organischer Hochpolymere aus dem Schmelzfluss
DE1118394B (de) * 1956-09-20 1961-11-30 Bayer Ag Verfahren zum Schmelzen von Polyamidschnitzeln bei der Herstellung synthetischer Faeden
BE529624A (US07860544-20101228-C00003.png) * 1958-08-05
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

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH139146A (de) * 1928-03-12 1930-04-15 Ig Farbenindustrie Ag Verfahren um kolloidale Lösungen, aus denen durch Koagulierung Fasern, Bändchen, Filme und dergleichen gewonnen werden sollen, zu fördern und zu filtrieren.
NL30471C (US07860544-20101228-C00003.png) * 1929-03-27
FR700710A (fr) * 1930-08-18 1931-03-06 Procédé et appareil de fabrication continue et automatique de viscose pour fabrication de soie artificielle

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE914668C (de) * 1943-05-31 1954-07-08 Phrix Werke Ag Verfahren zum kontinuierlichen Verspinnen von linearen Superpolymeren, insbesondere Superpolyamiden
US2437686A (en) * 1943-11-24 1948-03-16 Celanese Corp Process for the extrusion of fused artificial materials
US2437704A (en) * 1943-11-24 1948-03-16 Celanese Corp Method and apparatus for the melt extrusion of artificial materials
US2462149A (en) * 1944-12-22 1949-02-22 Int Standard Electric Corp Process for treatment of cable insulated with thermoplastic material
US2503251A (en) * 1945-02-16 1950-04-11 Ici Ltd Production of filaments, fibers, and the like
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
US2515250A (en) * 1947-11-07 1950-07-18 Dow Chemical Co Method of making and storing compositions comprising thermoplastic resins and normally gaseous solvents
US2888711A (en) * 1950-09-01 1959-06-02 British Celanese Production of filamentary materials
US2757416A (en) * 1950-09-12 1956-08-07 Polymer Corp Method for handling and melting nylon to be used in molding articles
US2720463A (en) * 1950-11-17 1955-10-11 American Cyanamid Co Gelatin capsule casting composition preparation
US2707306A (en) * 1952-08-22 1955-05-03 Celanese Corp Melt spinning apparatus
US2810630A (en) * 1953-11-02 1957-10-22 Hoechst Ag Device for the continuous polymerization and extrusion of organic synthetic substances, especially polyamides
US2918701A (en) * 1956-02-23 1959-12-29 Eastman Kodak Co Method for pelleting organic thermoplastic materials
US2911678A (en) * 1957-04-12 1959-11-10 Phillips Petroleum Co Molding of void-free olefin polymers using pressure, vacuum and directional cooling
WO2014151735A1 (en) * 2013-03-15 2014-09-25 Ascend Performance Materials Operations Llc Polymerization coupled compounding process
US10077341B2 (en) 2013-03-15 2018-09-18 Ascend Performance Materials Operations Llc Polymerization coupled compounding process
US10081712B2 (en) 2013-03-15 2018-09-25 Ascend Performance Materials Operations Llc Polymerization coupled compounding process
US10590245B2 (en) 2013-03-15 2020-03-17 Ascend Performance Materials Operations Llc Polymerization coupled compounding process
US11447609B2 (en) 2013-03-15 2022-09-20 Ascend Performance Materials Operations Llc Polymerization coupled compounded nylon
US20200200224A1 (en) * 2018-12-25 2020-06-25 Jtekt Corporation Method of manufacturing constituent member of constant-velocity joint
US11859676B2 (en) * 2018-12-25 2024-01-02 Jtekt Corporation Method of manufacturing constituent member of constant-velocity joint

Also Published As

Publication number Publication date
BE464699A (US07860544-20101228-C00003.png)
DE740273C (de) 1943-10-16
FR925323A (fr) 1947-09-01

Similar Documents

Publication Publication Date Title
US2273188A (en) Method and apparatus for producing artificial structures
US2361717A (en) Process for making polyamides
US2731081A (en) Method for the removal of monomers, etc. from molten polymers
US2289774A (en) Process and apparatus for shaping polymeric materials
US3113843A (en) Apparatus for separating a vapor from a viscous material such as molten polymer
US2212770A (en) Process for forming films from synthetic linear polymers
US2289860A (en) Process and apparatus for the production of artificial fibers and the like
US3461193A (en) Novel procedure for starting the flash-extrusion of expandable resin compositions
EP0244217B2 (en) Process and apparatus
US2369506A (en) Producing filaments from molten organic compositions
US2217743A (en) Apparatus
US2278875A (en) Method and apparatus for the production of artificial structures
US2683073A (en) Process for preventing nylon gel formation
US2571975A (en) Melt spinning process
US2323383A (en) Production of artificial materials
US2888711A (en) Production of filamentary materials
US3357955A (en) Continuous preparation of polyamides wherein relative viscosity and amineend value of final product are maintained constant
US2303340A (en) Production of artificial materials
US2573949A (en) Dissolving of polymers
US2318679A (en) Production of artificial filaments, films, and like materials
US2611929A (en) Method of producing shaped articles from artificial or synthetic fiberor film-forming materials
US3753661A (en) Apparatus for the preparation of filamentary material
US3466357A (en) Method and apparatus for spinning organic high polymers
US2364387A (en) Production of polymer
US3557544A (en) Compositions and yarn made therefrom