US2943350A - Polyamide melt spinning process and apparatus - Google Patents

Polyamide melt spinning process and apparatus Download PDF

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Publication number
US2943350A
US2943350A US717161A US71716158A US2943350A US 2943350 A US2943350 A US 2943350A US 717161 A US717161 A US 717161A US 71716158 A US71716158 A US 71716158A US 2943350 A US2943350 A US 2943350A
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Prior art keywords
chamber
melt
temperature
spinning
air
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Expired - Lifetime
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US717161A
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English (en)
Inventor
Rodenacker Wolf
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Bayer AG
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Bayer AG
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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
    • D01D1/00—Treatment of filament-forming or like material
    • D01D1/04—Melting filament-forming substances
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G69/00—Macromolecular compounds obtained by reactions forming a carboxylic amide link in the main chain of the macromolecule
    • C08G69/02—Polyamides derived from amino-carboxylic acids or from polyamines and polycarboxylic acids
    • C08G69/04—Preparatory processes
    • 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
    • D01F6/60—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyamides

Definitions

  • This invention relates to the spinning of synthetic linear condensation polyamides, especially those of the type generally referred to as nylon 6,'nylon 66 and nylon .68.
  • Nylon 6 is commercially obtained by polymerisation of caprolactam, While nylon 66 and nylon 68 are obtained from hexamethylene diammonium adipate and hexamethylene diammonium sebacate respectively.
  • the vessel 7 is kept at the melting temperature by,a heating jacket 7a.
  • the two internal chambers 8 and 1 0 which are connected to one another are therefore only" difierent as regards their temperature.
  • the partialsteam pressure 'of the steam in the chamber 8, the other'com stituent in which is nitrogen, is thus defined by the temperature difference between the chamber 8 and theiadditional chamber 10.
  • the shreds come from a shred conta iner1 9 by way of a controlled feed device 20, which is moved by a lever control device 21 and regulator 22.
  • the melt is'thoroughly stirred by a roller 23 which is movedbe tween two wedge-shaped spaces 24 (Fig. 2a). Due to the pressure in the space 24, the melt is supplied by. a
  • the melt is improved, this uniformity being important for the spinning operation and for the textile properties of the filaments which are manufactured.
  • it has the disadvantage that the degree of polymerisation obtained is too low to yield the optimum strength values of the yarn, in spite of its improved uniformity.
  • a further object is the provision of means for controlling the equilibrium between polymerisation and deploymerisation in such a manner that the resultant degree of polymerisation is as high as possible.
  • the objects are accomplished by the invention which consists in conducting the spinning of the melted polyamide in contact with steam, while a constant atmosphere of water vapor, unsaturated at the temperature of the melt, is maintained in the melting chamber.
  • FIG. 1 a diagrammatic side elevational view of a melt spinning apparatus and in Figures 2 and 2a a diagrammatic view of a different type of a melt spinning apparatus.
  • the melt is introduced through a pipe 1 into an annular channel 2.
  • the melt runs down on the wall of a vessel 3 and collects in a sump 4. It is fed by a discharge worm 5 through an outlet opening 6 to the spinning nozzle.
  • a vessel 7 contains .a steam chamber 8 which is connected by a pipe 9 of very large diameter to an additional chamber 10.
  • the additional chamber 10 contains a spray nozzle 11 by means of which there is sprayed water which is withdrawn and circulated by .a pump 13 from the sump having the level 12.
  • a space 28 above the level of the melt is connected by a large-diameter pipe 29 to a yessel 30.
  • the vessel-30 contains a central tube 31 in which is disposed an axial fan 32 serving to circulate a gas, fo'r example nitrogen, in the vessel 30.
  • a space 33 in the .vessel is filled with Raschig rings, which are sprayed with liquid from above through a pipe 34. The sprayed liquid accumulates in a sump 35, from which it is extracted by way of a pump 36 and used again for sprinkling purposes. The washing liquid can be replenished.
  • the partial pressure of .the steam in the melting chamber is kept constant throughout themelting and processing operations.
  • this is effected by attaching to .a conventional melting chamber by way of a largediameter opening an air-conditioning chamber in which the circulated protective gas, which is generally pure nitrogen, is saturated with steam at a substantially lower temperature than the temperature of the melt chamber, but at the same pressure as that obtaining in the melt chamber. Care must be taken that all parts of the melt chamber have a temperature which is above the dew possible to maintain the melt chamber conditions which differ only in temperature, and thereby to produce any desired Water content and thus a constant degree of polymerisation of the melt.
  • Example 1 Shreds of the polyamide of caprolactam, with a water J '7 content of 0.1%, are introduced into the spinning device described with reference to Figures 2 and 2a.
  • the pipe 29 is initially closed, so that the additional chamber 30 is not connected to the melting chamber 28.
  • a temperature of 270 C. at normalpressure is maintained in-the melting chamber.
  • the filaments which are obtained have an elongation-out 23% and a strength of 5.3 grams/denier.
  • the air conditioning chamber is then set to give a temperature of 30 C. and a superatmospheric pressure of 7 pounds per square inch gauge, the operation in the melting chamber being continued at 'a temperature of270 C.
  • a constant steam partial pressure is then obtained in l Using'the same apparatus as in Example 1, monofilamerits of 2 0 denier are spun at a spinning temperature oi Z70, Q. and at normal pressure with a withdrawal speed of 630 metres per minute.
  • the crystallisation velocity is increased from 3 to 18 after adjustment to give a constant steam partial pressure in the melting chambe R n h s sta li at a vg q it m an an mprov ent th so id ficat on.
  • n ds y et hi h g mP i maintaining the partial pressure of the steam in the melt chamber constant throughout the melting and spinning operations by maintaining said melt chamber in open eornrnunication with an air-conditioning chamber, circulating through the latter chamber an inert gas which is saturated with steam at a lower temperature'than the temperature of the melt chamber, but at the same pressure as that in the melt chamber, so that the atmosphere at the melt chamber differs only. in temperature from that of said air-conditioning. chamber whereby the ratio of the partial pressures of the water vapor and the said inert gas are maintained constant at the temperature of the melt, and producing from said spinning process polyamide filaments having improved physical properties.
  • melt chamber is mai ta ned at a emperature bove the dew point of th saturated inert gas, so. that no. condensation ofsteam occurs within said chamber.
  • a spinneret for the extru-- sion of molten polyamide and a melt chamber which supplies molten pblyamide to said spinneret, in combination; an air-conditioning chamber" positioned adjacent saidmelt chamber, a conduit connecting said chambers, means for saturating nitrogen with water vapor. within said air-conditioning chamber, the latter being maintained at a tem e a ure rh t? at in Said me m and means for circulating said saturated nitrogen through said, s nduit i id.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Textile Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Artificial Filaments (AREA)
US717161A 1957-03-08 1958-02-24 Polyamide melt spinning process and apparatus Expired - Lifetime US2943350A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE875019X 1957-03-08

Publications (1)

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US2943350A true US2943350A (en) 1960-07-05

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US717161A Expired - Lifetime US2943350A (en) 1957-03-08 1958-02-24 Polyamide melt spinning process and apparatus

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US (1) US2943350A (en])
BE (1) BE565488A (en])
FR (1) FR1199568A (en])
GB (1) GB875019A (en])
NL (2) NL97740C (en])

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3090773A (en) * 1958-01-28 1963-05-21 Allied Chem Caprolactam polymerization
US4591468A (en) * 1982-03-28 1986-05-27 Imperial Chemical Industries Plc Process for remelting polyamides
EP0201189A2 (en) 1985-04-22 1986-11-12 BASF Corporation Improved high speed process of making polyamide filaments
US4642211A (en) * 1983-10-21 1987-02-10 Basf Aktiengesellschaft Preparation of dry polycaprolactam granules
US4952345A (en) * 1989-02-10 1990-08-28 E. I. Du Pont De Nemours And Company Method for controlling polymer viscosity

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2702605C3 (de) * 1977-01-22 1979-12-13 Basf Ag, 6700 Ludwigshafen Verfahren zur Herstellung von höhermolekularen Polyamiden
AU517825B2 (en) * 1977-04-12 1981-08-27 Union Carbide Corporation Gear pump

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2571975A (en) * 1947-05-10 1951-10-16 Du Pont Melt spinning process

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2571975A (en) * 1947-05-10 1951-10-16 Du Pont Melt spinning process

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3090773A (en) * 1958-01-28 1963-05-21 Allied Chem Caprolactam polymerization
US4591468A (en) * 1982-03-28 1986-05-27 Imperial Chemical Industries Plc Process for remelting polyamides
US4642211A (en) * 1983-10-21 1987-02-10 Basf Aktiengesellschaft Preparation of dry polycaprolactam granules
EP0201189A2 (en) 1985-04-22 1986-11-12 BASF Corporation Improved high speed process of making polyamide filaments
EP0201189B2 (en) † 1985-04-22 1995-02-15 BASF Corporation Improved high speed process of making polyamide filaments
US4952345A (en) * 1989-02-10 1990-08-28 E. I. Du Pont De Nemours And Company Method for controlling polymer viscosity
EP0382569A3 (en) * 1989-02-10 1991-11-06 E.I. Du Pont De Nemours And Company Method for controlling polymer viscosity

Also Published As

Publication number Publication date
NL97740C (en])
GB875019A (en) 1961-08-16
FR1199568A (fr) 1959-12-15
NL225522A (en])
BE565488A (en])

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