US3619452A - Filament quenching apparatus and process - Google Patents

Filament quenching apparatus and process Download PDF

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US3619452A
US3619452A US805261A US3619452DA US3619452A US 3619452 A US3619452 A US 3619452A US 805261 A US805261 A US 805261A US 3619452D A US3619452D A US 3619452DA US 3619452 A US3619452 A US 3619452A
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foam
gas
diffuser
quenching
porous
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David M Harrison
Thomas E Miles
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Honeywell International Inc
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Allied Chemical Corp
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F05—INDEXING SCHEMES RELATING TO ENGINES OR PUMPS IN VARIOUS SUBCLASSES OF CLASSES F01-F04
    • F05C—INDEXING SCHEME RELATING TO MATERIALS, MATERIAL PROPERTIES OR MATERIAL CHARACTERISTICS FOR MACHINES, ENGINES OR PUMPS OTHER THAN NON-POSITIVE-DISPLACEMENT MACHINES OR ENGINES
    • F05C2201/00—Metals
    • F05C2201/02—Light metals
    • F05C2201/021—Aluminium

Definitions

  • Massengill ABSTRACT An apparatus and process for producing a substantially nonturbulent stream of cooling gas for quenching a melt extruded filament which comprises a quenching chamber, wherein a melt extruded filament is passed therethrough, and a gas entry chamber, the gas entry chamber being provided with means for introducing a cooling gas.
  • the quenching chamber and the gas entry chamber are separated from each other by a porous, multicellular, polymeric foam diffuser which is capable of diffusing gas entering from the gas entry chamber and permitting the diffused gas to pass therethrough into the quenching chamber as a substantially nonturbulent stream of gas thereby quenching the melt extruded filament and producing greater cross-sectional uniformity in the filament.
  • This invention relates to an apparatus and process for the production of a substantially nonturbulent stream of quenching gas for quenching one or more synthetic filaments produced by a melt spinning process.
  • one or more filaments extrudes from one or more spinnerettes and passes into a quenching chamber.
  • the quenching chamber comprises one or more walls which can be a perforated plate, screen or both which separates the quenching chamber from an adjoining gas entry chamber which is in communication with a cooling gas supply system.
  • the synthetic polymer extruding from the spinnerette is a viscous liquid at an elevated temperature. Cooling of this liquid takes place in the quenching chamber where a cooling gas, which is usually air, is contacted with the filaments.
  • the cooling gas enters the quenching chamber from the gas entry chamber through the perforated plate or plates in a direction substantially perpendicular to the filaments.
  • the filaments pass through the quenching chamber in a direction substantially parallel to the perforated plate or plates separating the gas entry chamber from the quenching chamber.
  • the use of the perforated plate or plates is necessary to reduce cooling gas turbulence because the filaments are highly vulnerable to cooling gas turbulence since they are in the liquid phase at entry into the quenching chamber. Turbulence in the cooling gas stream detracts from the uniformity, the orientation capacity, and the strength of the filaments.
  • the volume between the inner and outer perforated plates serves as a plenum chamber to further disperse the cooling gas and reduce its turbulence.
  • the perforated plates therefore serve the purpose of further dispersing and reducing the turbulence of the cooling gas supplied to the quenching chamber so that the extruded filaments have more uniform properties throughout their whole length.
  • the prior art also teaches that the turbulence of the gas stream in the quenching chamber can be reduced by using a number of screen layers of the same or different mesh lying against each other in place of or in addition to the perforated plate or plates.
  • the mesh in the direction of gas flow can be the same of successively larger or smaller.
  • the apparatus and process described above is adequate for low filament extrusion rates; however, in keeping with the competitive demands of the modern textile industry, higher filament extrusion rates are now required and effective quenching of the filaments is a problem using the conventional apparatus and process described above.
  • the above-described apparatus is used with a high filament extrusion rate and a relatively low cooling gas rate which will produce filaments having an acceptable Percent Uster and drawing performance
  • the filaments are wound on the takeup package at a relatively high temperature and excessive package growth may occur with certain polymers which produces a loose, sloughing and unacceptable fiber package.
  • the cooling gas rate is increased to a point where an acceptable fiber package can be produced, the resulting filaments have an unacceptably high Percent Uster with accompanying high wraps and breaks upon drawing or subsequent processing.
  • a typical perforated plate which has been used in the prior art has under 50 percent open area which consists of small diameter holes spaced at regular centers.
  • a check of the cooling gas velocity through the perforations has shown that the gas turbulence in the quenching chamber is caused by a jetting action of the gas through the perforations. This jetting action causes turbulence in the quenching chamber and produces filaments having nonuniform cross section.
  • a substantially nonturbulent stream of cooling gas can be produced for quenching a melt extruded filament by separating the gas entry chamber and the quenching chamber with a porous, multicellular, polymeric foam diffuser which is capable of diffusing the cooling gas entering from the gas entry chamber.
  • the porous, multicellular polymeric foam diffuser diffuses the cooling gas and permits it to pass therethrough into the quenching chamber as a substantially nonturbulent stream of gas thereby quenching the melt extruded filament and producing a, filament having a more uniform cross section, a significantly improved Percent Uster and a significantly improved drawing performance at high filament extrusion rates.
  • an apparatus for producing a substantially nonturbulent stream of cooling gas for quenching a melt extruded filament which comprises a quenching chamber wherein a melt extruded filament is passed therethrough and a gas entry chamber, said gas entry chamber being provided with means for introducing a cooling gas.
  • the quenching chamber and the gas entry chamber are separated from each other by a porous, multicellular, polymeric foam diffuser which is capable of diffusing within said diffuser gas entering from the gas entry chamber and permitting said difi'used gas to pass therethrough said diffuser into said quenching chamber as a substantially nonturbulent stream of gas thereby quenching the melt extruded filament and producing greater cross-sectional uniformity in said filament at a high filament extrusion rate.
  • the greater cross-sectional uniformity in the filament results in a filament having a more uniform cross section, a significantly improved Percent Uster and a significantly improved drawing performance.
  • porous, multicellular polymeric foam difiuser used to define the present invention is to be understood to mean that a sufficient number of the foam cells are interconnecting to an extent that the foam is considered to be opencelled and is capable of diffusing gas in accordance with the present invention.
  • a process for quenching a melt extruded filament which comprises introducing a cooling gas into a gas entry zone and passing the gas from the gas entry zone into a porous, multicellular, polymeric foam diffusion zone.
  • the gas is diffused within the porous, multicellular, polymeric foam difi'usion zone and the diffused gas is permitted to pass therethrough the diffusion zone into a quenching zone as a substantially nonturbulent stream of gas.
  • a melt extruded filament is passed through the quenching zone and is quenched in the quenching zone by the substantially nonturbulent stream of cooling gas thereby producing greater cross-sectional uniformity in the filament.
  • the porous, multicellular, polymeric foam diffuser used in the present invention can have a foam thickness, generally perpendicular to the axis of the quenching chamber or apparatus, of about A to 4, preferably about A to 2, inches and can have a length, generally parallel to the axis of the quenching chamber or apparatus, of about 6 to 72, preferably about 6 to 24, inches.
  • the width of the porous, multicellular, polymeric foam diffuser is determined by the configuration of the filaments in the quenching chamber.
  • the porous, multicellular, polymeric foam can have about 50 to 200, preferably about 75 to 150, cells per lineal inch and a'cellular void volume of about 50 to 97, preferably about 75 to 97, percent of the total volume of the porous, multicellular polymeric foam.
  • the polymer volume of the porous, multicellular, polymeric foam can be about 3 to 50, preferably about 3 to 25, percent of the total volume of the porous, multicellular, polymeric foam.
  • the bulk density of the porous, multicellular, polymeric foam can range from about I to l0, preferably about L4 to 6, lb. per cu. ft.
  • the porous, multicellular, polymeric foam diffuser can be made from flexible or rigid foam.
  • the range of gas velocity flow through the porous, multicellular, polymeric foam diffuser can be about 30 to 120, preferably about 40 to 90, SCFM per sq. ft. at a pressure differential across the porous, multicellular, polymeric foam of about 0.15 to 4, preferably about 0.2 to 2, inches of water.
  • the humidity of the entering gas can be established at any given desired humidity level and a suitable humidity range can be from about 40 to 95 percent relative humidity at 20 C.
  • the porous, multicellular, polymeric foam diffuser can be a foamed synthetic polymer such as a polyurethane foam, a vinyl foam, which can be produced from a vinyl such as polyvinyl chloride or polyvinyl acetate, and the like.
  • the porous, multicellular, polymeric foam diffuser can be a natural or synthetic foam rubber such as acrylic, neoprene, polybutadiene, nitrile, butadiene-acrylonitrile, butadiene-styrene, polyisobutylene, polyisoprene, vinyl pyridine, silicone, and the like.
  • a particularly advantageous aspect of the porous, multicellular, polymeric foam diffuser used in the present invention is its ability to diffuse cooling gas in three dimensions thereby producingthe substantially non turbulent stream of cooling gas.
  • the porous, multicellular, polymeric foam diffuser is a porous, multicellular polyurethane foam.
  • Polyurethane foams suitable for use in the present invention can be produced by reacting an organic compound having reactive hydrogen atoms and a stoichiometric excess of an organic polyfunctional isocyanate with water in the presence of a suitable catalyst and foam stabilizing agent. When water reacts with the excess isocyanate groups not previously reacted, carbon dioxide is formed which is entrapped in the reaction mixture and thereby causes it to foam.
  • An auxiliary blowing agent such as a volatile fluorocarbon, may also be employed.
  • the polyurethane foam can be produced by the prepolymer method wherein the organic compound having reactive hydrogen atoms is first reacted with the organic polyfunctional isocyanate or by the one-shot method wherein the reactants are simultaneously mixed together and reacted.
  • the preparation of suitable polyurethane foams is typically described in US. Pat. Nos. 3,171,820 at columns 1 through 20 and 3,198,757 at columns l' through 6.
  • Suitable polyurethane foams useful in this invention include those of the polyester and polyether type.
  • a particularly useful type of polyurethane foam is reticulated polyester foam or reticulated polyether foam.
  • an additional pressure drop across the porous, multicellular polymeric foam diffuser can be provided by covering the gas intake surface of the porous, multicellular, polymeric foam diffuser with a cooling gas distribution means such as a woven or nonwoven felt material which can be produced from a natural or synthetic fiber.
  • a cooling gas distribution means such as a woven or nonwoven felt material which can be produced from a natural or synthetic fiber.
  • Suitable fibers include cotton, wool, polyamides, polyesters and the like.
  • Suitable felt materials can have a total weight of between about to 40, preferably about to 30, oz. per sq. yard. When such a felt material is used, the pressure drop across it is usually about 0.5 to 2 inches of water.
  • the scope of the present invention includes the use of the porous, multicellular, polymeric foam diffuser to diffuse cooling gas in cross current quenching wherein the cooling gas is passed across the extruded filament in a direction substantially perpendicular to the filament and is then exhausted; cocurrent quenching wherein the cooling gas is passed into the quenching chamber and travels in a direction substantially parallel to the filament downward through the quenching chamber into and through a cooling stack; inflow quenching wherein the cooling gas is passed into the quenching chamber and travels in a direction substantially parallel to the filament downward through the quenching chamber and is then exhausted after passing therethrough the quenching chamber; and the like.
  • the apparatus and process of the present invention can be used to quench synthetic filaments such as a polyamide,
  • polyester polyolefin, polysulfone, polyphenyloxide, polycarbonate, polyacrylonitrile and the like or polymer. blends thereof.
  • Suitable polyamides include, for example, those prepared by condensation of hexamethylene diamine and adipic acid, condensation of hexamethylene diamine and sebacic acid known as nylon 6,6 and nylon 6,10, respectively condensation of bis(para-aminocyclohexyl)methane and dodacanedioic acid, or by polymerization of -caprolactam, 7-aminoheptanoic acid, B-caprylactam, 9-aminopelargonic acid. 1 l-aminoundecanoic acid, and l2-dodecalactam, known as nylon 6, nylon 7, nylon 8, nylon 9, nylon l l, and nylon 12, respectively.
  • Suitable polyesters can be prepared in general by condensation reactions between dicarboxylic acids or their derivatives and comounds containing two hydroxyl groups, or materials possessing both an alcohol group and a carboxylic acid group or derivative thereof; or by polymerization of lactones.
  • the preferred polyester is polyethylene terephthalate.
  • FIG. 1 is cross sectional view showing a fiber melt extrusion apparatus and process illustrating the present invention which uses a porous, multicellular, polymeric foam diffuser to diffuse filament quenching gas.
  • FIG. 2 is an illustration showing one embodiment of a porous, multicellular, polymeric foam diffuser and a method of fabrication.
  • a cooling gas which is preferably air, which is introduced into gas entry chamber 1 by appropriate gas transfer means.
  • Gas entry chamber 1 is formed by outer cylindrical neoprene rubber bellows 2 which surrounds inner cylindrical neoprene rubber bellows 3 in a concentric manner thereby forming an annular gas entry chamber.
  • Cooling gas entering gas entry chamber 1 is passed through filter felt 4 and then through perforated metal cylinder 5 into porous, multicellular, polymeric foam difluser 6.
  • Perforated metal cylinder 5 distributes the cooling gas entering diffuser 6 into smaller streams.
  • the cooling gas is diffused in diffuser 6 nd enters quench chamber 7 as a substantially nonturbulent stream thereby quenching filaments 8 emerging from Spinnerette assembly 9.
  • the cooling gas is ,then passed downward through quench chamber 7 into and through cooling stack 10 and is exited through suitable exit means (not shown).
  • the filaments extruded through spinnerette assembly 9 and quenched in quench chamber 7 are collected on takeup means 11 and then are drawn into yarn.
  • Spinnerette 9 is surrounded by cylindrical wall 12 which surrounds and encloses the filaments extruding from Spinnerette 9.
  • Cylindrical neoprene rubber bellows 2 is connected to inner flange 13 which is positioned near the bottom of cylindrical wall 12 thereby creating the outer extremity of gas entry chamber 1.
  • Perforated metal cylinder 5 is connected to inner flange 14 which is positioned at the bottom of cylindrical wall 12 thereby forming the inner extremity of the upper part of gas entry chamber 1.
  • the bottom of perforated cylinder 5 is connected to outer flange 15 which is positioned at the top of cooling stack 10 Cooling stack 10 serves as a further cooling chamber for the quenched filaments and additional cooling of the filaments takes place within this cylindrical stack.
  • Inner cylindrical neoprene rubber bellows 3 is connected to the upper part of cooling stack 10 thereby completing the lower inner extremity of gas entry chamber 1.
  • Filter felt 4 which can be a woven or nonwoven felt material, is wrapped around perforated metal cylinder 5 and serves to provide a means for producing an additional pressure drop across diffuser 6 and to filter dust and other undesirable contaminants from the cooling gas prior to its entry into quench chamber 7.
  • Diffuser 6 is inserted against perforated cylinder 5 and is held in place by flange 17 positioned at the bottom of cylindrical wall 12 and flange 18 positioned at the top of cooling stack 10 thereby completing the filament quenching apparatus of the present invention.
  • porous, multicellular, polymeric foam diffuser 6 can be cut from porous bulk material or can be fabricated from slab stoclt.
  • a suitable adhesive can be used to join the ends to form diffuser 6.
  • a suitable adhesive for polyurethane foam is a fast-drying nitrile adhesive marketed as Cycleweld K-l86 by the Chemical Division of Chrysler Corporation.
  • polycaproamide was melt extruded at a temperature of 275 C., under a pressure of 2,500 p.s.i.g. through 204-orifice spinnerette assembly 9, each of the orifices having a-diameter of 0.022 inch, to produce a 5,500 denier undrawn fiber.
  • the polycaproamide was melt extruded through spinnerette 9 at a rate of 45 lbs. per hour.
  • the filaments travelled vertically downward through quench chamber 7 and cooling stack 10. In this manner, the filaments were quenched by means of cocurrent quenching.
  • the polyurethane foam diffuser separating gas entry chamber 1 and quench chamber 7 was cylindrical in shape with an inner diameter of 8%inches, an outer diameter of l0- inches, a foam thickness of I inch and a length of 8'/4 inches.
  • the polyurethane foam diffuser was of the polyester type and had 100 cells per lineal inch, a cellular volume of 96 percent of the total volume of the foam and a polymer volume of 4 percent of the total volume of the foam.
  • the rate of gas fiow through polyurethane foam diffuser 6 was 0.55 SCFM/sq. in. with a pressure differential across the foam of 0 25 inches of water.
  • the extruded fiber was collected at about 1,800 feet per minute on takeup means 11 and was then drawn about 4.6 times its extruded length to produce a 1,260 denier yarn.
  • the yarn had a relative viscosity of 55, as determined at a concentration of l I grams of polymer in 100 ml. of 90 percent formic acid at 25 C. (ASTM-D-789-62T), and a tenacity of about 9.0 grams per denier.
  • the undrawn filaments produced above were tested for cross-sectional uniformity by measuring the Percent Uster in accordance with ASTM-Dl,425-60T and were found to have an average Percent Uster of 5.5.
  • Polycaproamide was melt extruded and a 5,550 denier undrawn fiber was produced in the same manner as described above except that polyurethane foam diffuser 6 was replaced by a perforated metal cylinder of the prior art which was inserted between perforated metal cylinder 5 and quench chamber 7 to disperse the cooling air stream in quench chamber 7.
  • the undrawn filaments produced were tested for crosssectional uniformity in the same manner as above and were found to have an have an average Percent Uster of 15.
  • a comparison of the average undrawn filament Percent Uster of 5.5 obtained using the apparatus and process of the present invention with the average undrawn filament Percent Uster of 15 obtained using a conventional apparatus and process illustrates the very great improvement in undrawn filament cross-sectional uniformity of the fiber produced in accordance with the apparatus and process of the present invention.
  • EXAMPLE 2 In the operation of the apparatus in FIG. I, polycaproamide was melt extruded at a temperature of 275 C., under a pressure of 2,000 p.s.i.g. through a 204-orifice spinnerette assembly 9, each of the orifices having a diameter of 0.022 inch, to produce a 5,500 denier undrawn fiber.
  • the polycaproamide was melt extruded through spinnerette 9 at a rate of lbs. per hour.
  • the air 6 passed through filter felt 4 (two layers of 10.5 oz. per sq. yd. cotton felt) and perforated metal cylinder 5 into polyurethane foam diffuser 6.
  • the air was diffused in polyurethane foam diffuser 6 and entered quench chamber 7 as a substantially nonturbulent stream thereby cooling the filaments emerging from spinnerette 9.
  • the cooling air passed downward through quench chamber 7 into cooling stack 10 and was exited through a suitable exit means (not shown).
  • the filaments travelled vertically downward through quench chamber 7 and cooling stack 10. In this manner, the filaments were quenched by means of cocurrent quenching.
  • the polyurethane foam diffuser separating gas entry chamber I and quench chamber 7 was cylindrical in shape with an inner diameter of 8-% inches, an outer diameter of lO-k inches, a foam thickness of 1 inch and a length of 8'/4 inches.
  • the polyurethane foam diffuser was of the polyester type and had 100 cells per lineal inch, a cellular volume of 96 percent of the total volume of the foam and a polymer volume of 4 percent of the total volume of the foam.
  • the rate of gas flow through polyurethane foam diffuser 6 was 0.48 SCFM/sq. in. with a pressure differential across the foam of 0.22 inches of water.
  • the fiber was collected at about 1600 feet per minute on takeup means 11 and then was drawn about 4.8 times its extruded length to produce a 1260 denier yarn.
  • the yarn had a relative viscosity of 55, as determined at a concentration of l l 5 grams of polymer in I00 ml. of 90 percent formic acid at 25 C. (ASTM-D-789-62T), and a tenacity of about 8.9 grams per denier.
  • the undrawn filaments produced above were tested for cross-sectional uniformity by measuring the Percent Uster in accordance with ASTM-D-l425-60T and were found to have an average Percent Uster of 5.3.
  • Polycaproamide was melt extruded and a I260 denier yarn was produced in the same manner as described above except that polycaproamide was melt extruded through spinnerette 9 at a rate of only 32 lbs. per hour, the cooling air rate was reduced from I05 SCFM to 75 SCFM, and polyurethane foam diffuser 6 was replaced by a perforated metal cylinder of the prior art which was inserted between perforated metal cylinder 5 and quench chamber 7 to disperse the cooling air stream in quench chamber 7.
  • the undrawn filaments produced were tested for cross-sectional uniformity in the same manner as above and were found to have an average Percent Uster of 8.5.
  • a comparison of the average undrawn filament Percent Uster of 5.3 obtained using the apparatus and process of the present invention with the average undrawn filament Percent Uster of 8.5 obtained using a conventional apparatus and process also illustrates the very great improvement in undrawn filament cross-sectional uniformity of the fiber produced in accordance with the apparatus and process of the present invention.
  • this example illustrates that the apparatus and process of the present invention produces a 25 percent greater undrawn filament extrusion rate without any sacrifice in undrawn filament cross-sectional uniformity and permits higher cooling air rates to be used.
  • EXAMPLE 3 In the operation of the apparatus in FIG. 1, polycaproamide was melt extruded at a temperature of 275 C. through a 204- orifice spinnerette assembly 9, each of the orifices having a diameter of 0.022 inch, to produce a 5500 denier undrawn fiber.
  • the polycaproamide was melt extruded through spinnerette 9 at various pressures and rates as contained in table I nication with the lower portion of said wall and extending toward said takeup means;
  • b lo 5 means to supply a pressurized cooling gas to said diffuser.
  • the combination of claim 2 including a cooling stack in F. and at various rates as contained in table I below and was Communication with the lower P r i of Said diffuser and passed through the filament quenching apparatu i tending toward said takeup means; means integrating said cordance with the present invention in the same manner as in Wall, Said diffuse! and Said cooling Stack y examples 1 and 2. l0 dimensionally stable quenching apparatus.
  • Polycaproamide was also melt extruded in the same manner The combination of Claim 2 wherein Said P T as above except that polyurethane diffuser 6 was ticellular, polymeric foam diffuser has about 10 200 C6llS replaced by a perforated metal cylinder of the prior art which P meal Inch of foam; 3 p ym r ll m f about 3 to 50 was inserted between perforated metal cylinder 5 and quench Pmcent based on the total foam Volume; a f bulk chamber 7 to dispel-Se the cooling air stream in quench of about to 10 lb. per cu.
  • Table I shows that an improvement in undrawn fiber Per- 20
  • the combination of claim 5 wherein said polyurethane and an improvement in drawn yarn properties becomes signififoam is polyether foam.
  • the relative humidity of the air en I The combmatilon of claim 4 p i tering gas chamber 1 was 65 percent at R ticellular, polymeric foam diffuser comprises a natural or
  • ticellular, polymeric foam diffuser is provided with gas dis- TABLE I Polyeaproamlde throughput, lb. per hr.
  • An apparatus for producing a substantially nonturbulent stream of cooling gas for quenching a melt extruded filament which comprises a quenching chamber, wherein a melt extruded filament is passed therethrough, and a gas entry chamber, said gas entry chamber provided with means for introducing a cooling gas; said quenching chamber and said gas entry chamber being separated from each other by a porous, multicellular, polymeric foam diffuser capable of diffusing tribution means to provide an additional pressure drop across said diffuser.
  • a process for quenching a melt extruded filament which comprises introducing a cooling gas into a gas entry zone; passing said gas from said gas entry zone into a porous, multicellular, polymeric foam diffusion zone; diffusing said gas within said diffusion zone and permitting said diffused gas to pass therethrough said diffusion zone into a quenching zone as a substantially nonturbulent stream of gas; passing a melt extruded filament through said quenching zone thereby quenching the melt extruded filament in said quenching zone and producing greater cross-sectional uniformity in said filament.
  • porous, multicellular polymeric foam diffusion zone comprises a porous, multicellular, polymeric foam diffuser which has about 50 to 200 cells per lineal inch of foam; a polymer volume of about 3 to 50 percent based on the total foam volume; and a foam bulk density of about 1 to lb. per cu. ft.
  • porous, multicellular, polymeric foam diffuser comprises a synthetic polymeric foam selected from the group consisting of vinyl foam and polyurethane foam.
  • porous, multicellular, polymeric foam diffuser comprises a natural or synthetic foam rubber.
  • porous, multicellu lar, polymeric foam diffusion zone is provided with gas dispolyester, polyolefin,
  • tribution means to provide an additional pressure drop across said diffusion zone.
  • polysulfone polyphenyloxide, polycarbonate, polyacrylonitrile and polymer blends thereof.
  • the polyester is said filament is

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Textile Engineering (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
US805261A 1969-03-07 1969-03-07 Filament quenching apparatus and process Expired - Lifetime US3619452A (en)

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US (1) US3619452A (de)
BE (1) BE745677A (de)
CA (1) CA1033925A (de)
CH (1) CH510132A (de)
DE (1) DE2000958A1 (de)
ES (1) ES376620A1 (de)
FR (1) FR2037373A5 (de)
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NL (1) NL6917220A (de)

Cited By (12)

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US3834847A (en) * 1970-01-16 1974-09-10 Du Pont Open cell foam device for gas distribution in filament quenching chimneys
US4212606A (en) * 1978-05-25 1980-07-15 Allied Chemical Corporation Quench stack reel assembly and clamping device
US4492557A (en) * 1983-07-19 1985-01-08 Allied Corporation Filament quenching apparatus
US4504085A (en) * 1978-05-25 1985-03-12 Allied Corporation Reel assembly and clamping device
EP0184318A1 (de) * 1984-11-01 1986-06-11 E.I. Du Pont De Nemours And Company Fadenkühlapparat mit Platte, Schaumstoff und Sieb
US5219582A (en) * 1991-12-06 1993-06-15 E. I. Du Pont De Nemours And Company Apparatus for quenching melt spun filaments
US5421843A (en) * 1993-09-30 1995-06-06 Basf Corporation Apparatus for removing emissions
US5650112A (en) * 1993-07-28 1997-07-22 Lenzing Aktiengesellschaft Process of making cellulose fibers
US5698151A (en) * 1993-07-01 1997-12-16 Lenzing Aktiengesellschaft Process of making cellulose fibres
US6350399B1 (en) 1999-09-14 2002-02-26 Kimberly-Clark Worldwide, Inc. Method of forming a treated fiber and a treated fiber formed therefrom
US20040052883A1 (en) * 2002-09-13 2004-03-18 Mcconnell John Stanley Delayed quench apparatus
US20200035381A1 (en) * 2017-01-16 2020-01-30 Tomoegawa Co., Ltd Copper fiber nonwoven fabric for wiring, wiring unit, method for cooling copper fiber nonwoven fabric for wiring, and temperature control method for copper fiber nonwoven fabric for wiring

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CH663222A5 (de) * 1983-02-25 1987-11-30 Barmag Barmer Maschf Spinnanlage fuer chemiefasern.
CN107012518B (zh) * 2017-05-12 2023-02-10 苏州软石智能装备有限公司 环形吹风冷却设备及其风室
DE102020007036A1 (de) * 2020-11-18 2022-05-19 Oerlikon Textile Gmbh & Co. Kg Vorrichtung zum Abkühlen extrudierter Filamente

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US3389429A (en) * 1966-09-13 1968-06-25 Allied Chem Spinning apparatus
US3508296A (en) * 1968-01-02 1970-04-28 Teijin Ltd Melt spinning apparatus

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US3389429A (en) * 1966-09-13 1968-06-25 Allied Chem Spinning apparatus
US3508296A (en) * 1968-01-02 1970-04-28 Teijin Ltd Melt spinning apparatus

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3834847A (en) * 1970-01-16 1974-09-10 Du Pont Open cell foam device for gas distribution in filament quenching chimneys
US4212606A (en) * 1978-05-25 1980-07-15 Allied Chemical Corporation Quench stack reel assembly and clamping device
US4504085A (en) * 1978-05-25 1985-03-12 Allied Corporation Reel assembly and clamping device
EP0131788A3 (en) * 1983-07-19 1986-06-11 Allied Corporation Filament quenching apparatus
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US20200035381A1 (en) * 2017-01-16 2020-01-30 Tomoegawa Co., Ltd Copper fiber nonwoven fabric for wiring, wiring unit, method for cooling copper fiber nonwoven fabric for wiring, and temperature control method for copper fiber nonwoven fabric for wiring

Also Published As

Publication number Publication date
CH510132A (de) 1971-07-15
CA1033925A (en) 1978-07-04
FR2037373A5 (de) 1970-12-31
DE2000958A1 (de) 1970-09-24
NL6917220A (de) 1970-09-09
ES376620A1 (es) 1972-05-01
GB1240099A (en) 1971-07-21
BE745677A (fr) 1970-07-16

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