US3787265A - Process and apparatus for producing fibrous structures - Google Patents
Process and apparatus for producing fibrous structures Download PDFInfo
- Publication number
- US3787265A US3787265A US00237832A US3787265DA US3787265A US 3787265 A US3787265 A US 3787265A US 00237832 A US00237832 A US 00237832A US 3787265D A US3787265D A US 3787265DA US 3787265 A US3787265 A US 3787265A
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- stream
- gas streams
- extrudate
- polymer
- gas
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- Expired - Lifetime
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- D—TEXTILES; PAPER
- D04—BRAIDING; LACE-MAKING; KNITTING; TRIMMINGS; NON-WOVEN FABRICS
- D04H—MAKING TEXTILE FABRICS, e.g. FROM FIBRES OR FILAMENTARY MATERIAL; FABRICS MADE BY SUCH PROCESSES OR APPARATUS, e.g. FELTS, NON-WOVEN FABRICS; COTTON-WOOL; WADDING ; NON-WOVEN FABRICS FROM STAPLE FIBRES, FILAMENTS OR YARNS, BONDED WITH AT LEAST ONE WEB-LIKE MATERIAL DURING THEIR CONSOLIDATION
- D04H3/00—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length
- D04H3/08—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length characterised by the method of strengthening or consolidating
- D04H3/16—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length characterised by the method of strengthening or consolidating with bonds between thermoplastic filaments produced in association with filament formation, e.g. immediately following extrusion
-
- 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
- D01D5/098—Melt spinning methods with simultaneous stretching
- D01D5/0985—Melt spinning methods with simultaneous stretching by means of a flowing gas (e.g. melt-blowing)
-
- D—TEXTILES; PAPER
- D04—BRAIDING; LACE-MAKING; KNITTING; TRIMMINGS; NON-WOVEN FABRICS
- D04H—MAKING TEXTILE FABRICS, e.g. FROM FIBRES OR FILAMENTARY MATERIAL; FABRICS MADE BY SUCH PROCESSES OR APPARATUS, e.g. FELTS, NON-WOVEN FABRICS; COTTON-WOOL; WADDING ; NON-WOVEN FABRICS FROM STAPLE FIBRES, FILAMENTS OR YARNS, BONDED WITH AT LEAST ONE WEB-LIKE MATERIAL DURING THEIR CONSOLIDATION
- D04H3/00—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length
- D04H3/02—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length characterised by the method of forming fleeces or layers, e.g. reorientation of yarns or filaments
- D04H3/07—Non-woven fabrics formed wholly or mainly of yarns or like filamentary material of substantial length characterised by the method of forming fleeces or layers, e.g. reorientation of yarns or filaments otherwise than in a plane, e.g. in a tubular way
Definitions
- ABSTRACT Apparatus and method for producing filamentary material by extruding substantially axially through an orifice comprising contacting the extruded filament stream downstream of the orifice and prior to hardening with a plurality of converging, substantially planar, high velocity gas streams, each moving substantially in the direction of the filament stream such that they converge upon thetfilament stream at an angle of from about 45 to 5 from the axis of the polymer extrusion nozzle.
- the planes of the gas streams intersect at a point which is at a distance measured perpendicularly from the axis of the extrudate stream at least'equal to the diameter of the extrudate stream.
- This invention relates to the production of filamentary material. It is particularly concerned with novel apparatus and process for spray spinning molten fiberforming polymers to form nonwoven structures.
- the present invention is concerned with an improved method and apparatus for the direct production of filamentary materials. It is an object of the present invention to provide improved method and apparatus for spray spinning molten fiber-forming materials at production rates much higher than the prior artprocesses. At the same time, it is a further object of the invention to produce a substantially uniform spray-spun fibrous structure while minimizing the formation of shot or objectionally short fibers which detract from the desirability of the collected fibrous assembly.
- spinning nozzle means are provided with an extrusion orifice with a fiber-forming material and with a plurality of substantially rectangular gas outlet passages spaced apart from the extrusion orifice to supply jets of high velocity gas for attenuating the extruded filament stream prior to hardening of the filaments.
- the molten polymer and attenuating gas do not flow through the same nozzle or any other part of the spray-spinning equipment.
- the gas passages are separated from the extrusion orifice by an insulating means such as an air space. As a consequence, the gas flow, if it is not heated, would not cause heat transfer from the polymer to the gas.
- Such an arrangement eliminates the need for either heating the attenuating gas or heating the polymer to a sufficiently high degree above the required extrusion temperature such that the heat transfer would only lower the polymer temperature to the required extrusion temperature.
- the direction of the gas jets are such that substantial drag forces are applied to the extruded filament stream in the direction of extrusion for attenuating or drawing the material leaving the extrusion orifice.
- the gas passages are positioned such that the planar gas streams are directed substantially in the direction of flow of the extrudate stream in such a manner that the gas streams converge upon the extrudate stream.
- the planes of the gas streams and the planar projections of the gas outlet passages intersect at a point which is at a distance measured perpendicularly from the axis of the extrudate stream at least equal to the diameter of the extrudate stream.
- the planes of the attenuating gas streams contact the polymer extrudate stream at an angle of from about to 5 from the axis of the polymer extrusion nozzle to project it away from the extrusion orifice.
- a relatively heavy monofil is extruded and a plurality of streams of gas, e.g., steam or air, are directed at a shallow angle in the direction of flow of the freshly extruded monofil.
- gas e.g., steam or air
- the filamentary material will be one or more substantially continuous structures, or relatively long staple fibers, or conventional length fibers, possibly mixed with varying amounts of solid debris or shot.
- the severity of the gas streams varies the attenuation and determines the denier of the resulting fibrous material which may range from about 0.1 up to about 50, although for maximum surface and strength the fiber denier is preferably mostly below about 25 denier. Actually each product will include a range of deniers which will add to its strength and performance.
- the extrudate is discharged onto a suitable collection surface such as a rotating collector drum.
- a suitable collection surface such as a rotating collector drum.
- the height or length of the resulting structure can be set by traverse or by use of multiple side-by-side extruders whose spray patterns overlap. The duration of spray obviously controls the thickness of the resulting structures.
- the conditions of extrusion and collection are such that each new layer when deposited is sufficiently tacky so as to adhere to the preceding layer so that the total structure will be shape-retaining without further treatment.
- the filament-forming material may comprise any known suitable polymeric material which is plasticizable, soluble or fusible. If soluble materials are used in conjunction with a solvent, the problem of solvent removal is encountered which, of course, is avoided where fusible materials are employed.
- fusible materials include polyolefins such as homopolymers and copolymers of olefins, e.g.
- ethylene and propylene especially stereospecific or crystalline polyethylene and polypropylene
- polyamides such as nylon 66, nylon 6, and the like
- polyesters such as polyethyleneterephthalate
- cellulose esters such as cellulose acetate, and especially the secondary triacetate
- polyurethanes polystyrene
- polymers of vinylidene monomers such as vinyl chloride, vinyl acetate, vinylidene chloride, and especially acrylonitrile; and mixtures thereof.
- FIG. 2 is a schematic plan view of the extrusion apparatus and process in accordance with the present invent1on;
- FIG. 3 is a graph illustrating vectorially the forces resulting from two converging planar gas streams
- FIG. 4 is a schematic illustration showing how the vector force component illustrated in FIG. 3 both defleet and accelerate the filament stream.
- FIG. 5 is a front elevation of one embodiment of an extrusion nozzle and planar attenuating gas jets useful in the apparatus and process illustrated in FIG. 2;
- FIG. 6 is a schematic perspective illustration of an extrusion nozzle having a pair of planar attenuating gas jets positioned on each side of the extrusion nozzle;
- FIG. 7 is a perspective view of a planar attenuating gas jet shown in FIG. 6.
- FIG. 8 is a schematic front elevation of the preferred arrangement for utilizing four extrusion nozzles.
- a fiber-forming, thermoplastic polymer preferably a polyolefin
- an extruder 10 provided with an adapter section 12 to which a gas, such as steam or air, is supplied.
- a gas such as steam or air
- extrusion temperatures may be anywhere above the melting point of the polymer, it has been found that best results are obtained by heating the polymer to at least 150C., and preferably from about 250 to about 350C. above the softening point of the polymer being extruded.
- polypropylene having hereinafter defined characteristics will generally be heated to temperatures of from about 325 to about 400C.
- Polyethylene on the other hand, will be heated to from about 350 to about 450C.
- a hot, molten stream of polymer 16 is discharged through a nozzle 14.
- nozzles having one or more polymer orifices may be used. Also, a plurality of nozzles per collector may be employed. However, there must be at least two planar gas streams per polymer orifice.
- the attenuating gas orifices 18 are of an elongated rectangular cross section, as shown in FIGS. 5 and 6, to emit substantially planar gas streams 17.
- the gas streams 17 act on the polymer stream 16 in convergence region 20 to form an attenuated filament 22 wherein it cools and partially solidifies while moving toward collection surface 24 on which it is collected as a cylindrical structure 26.
- the collection surface 24 is ordinarily rotated at a speed sufficient to provide a moving surface of from about 25 to about 125 feet per minute by a motor drive.
- Collection surface 24 is in surface contact with roller 28, which acts as an idler roll and whose bias against the mandrel can be adjusted; the extent of the bias will effect how tightly the tacky filament packs against previous layers on the cartridge 26.
- Both the collection surface 24 and the roller 28 are reciprocated laterally by a traversing mechanism 30 whose throw determines the shape of the cylinder; the throw may be of constant length or may change in the course of package build-up to produce a particular shape as may be needed for acceptance in a receptacle of predetermined corresponding shape.
- the force of the attenuating gas on the polymer stream causes the polymer to attenuate greatly, e.g., from 10 to 500 times, based on diameter ratios, and possibly fibrillate to a slight degree to produce a substantially continuous fiber.
- Some turbulence and resultant whipping about of the polymer stream occurs. Consequently, a generally random, stereo reticulate structure of fiber results as the material impinges on the collector. Since the polymer is still in a somewhat molten or tacky state when it strikes the collector, some sticking together occurs at the points where fiber intersects. For brevity, this sticking will be referred to as interfiber bonding, although it is to be understood that this bonding will ordinarily result from an individual fiber looping about and sticking or bonding to itself.
- the collection surface 24 should be from about 6 to about 48 inches, preferably IO to 30 inches, from polymer exit nozzle 14. With greater distances the spray pattern is difficult to control and the resultant web tends to be nonuniform. Shorter distances result in a web which contains too great a quantity of shot, i.e., beads of non-attenuated polymer, which undesirably affects subsequent processing, web uniformity and surface area.
- FIG. 2 there is schematically shown a top view of the apparatus of this invention.
- a plurality of converging substantially planar gas streams 18 (corresponding substantially to planar projections of gas outlet passages 17) issue from substantially rectangular gas outlet passages 17.
- the axis 19 of the nozzle 14 corresponds to the direction in which the polymer stream is extruded.
- the gas jets 17 are positioned along side the extrusion nozzle 14 in such a manner that the gas streams 18 are directed substantially in the direction of flow of the polymer extrudate along the nozzle axis 19.
- the planes of the gas streams and planar projections of the gas outlet passages intersect at a point 21 which is at a distance B measured perpendicularly from intersection point 21 to the nozzle axis 19.
- the distance B is at least equal to the diameter of the extrudate stream at a point 23 along the nozzle axis in juxtaposition to the point of intersection 21.
- B is at least 0.06 inch, most preferably from about 0.2 to 2.0 inches.
- the point 23, which defines the perpendicular distance from the nozzle 14 to the intersection point 21 is a distance A of at least 2.0 inches from the point of extrusion nozzle 14, preferably from about 2.5 to 7.0 inches.
- the attenuating gas jets 17 are positioned along side the extrusion nozzle such that the planes of the attenuating gas streams 18 intersect the nozzle axis 19 (also the axis of the extrudate stream) at an angle (a, and 04 less than 45 to more than about 5 degrees, preferably from about 10 to 40 degrees, to project the extrudate stream away from the extrusion nozzle.
- the force of the gas streams 18 are shown vectorially.
- the Y force component is in the direction of the extrusion nozzle axis and polymer extrudate stream, and serves to accelerate and attenuate the extrudate stream.
- Angles a, and 01 shown in FIG. 2 are not the same so that the intersection point of the planes of the gas streams is off the nozzle axis and extrudate stream.
- FIG. 4 shows that the effect of this is to deflect the extrudate stream 16, first to one side and then to the other, in addition to attenuating the extrudate. If a, and
- planar filament streams 18 would intersect on the nozzle axis and substantially on the extrudate stream. As can be seen from the examples, this leads to much lower surface area when compared to the method of this invention illustrated in FIG. 2. It is probable that the effect of the gas streams intersecting on the extrudate stream is to cut the stream and produce a less open, lower surface area product.
- the illustrated extrusion nozzle 14 has a center polymer exit orifice 115, as shown in FIG. 5, which ordinarily has a diameter of from about 0.01 to about 0.10 inch, and preferably from about 0.015 to about 0.030 inch.
- polymer is generally of about 30 and respectively.
- the polypropylene extrudate is collected on a metal drum having a diameter of 1 inch to produce annular cylindrical structures.
- the total through put of polypropylene is about 6 lb./hr.
- EXAMPLE 2 Polypropylene. as in Example 1, is spra spun through one or more circular orifices, utilizing planar attenuating gas jets, as shown in FIG. 6, spaced at a distance of 2 inches from the axis of each extrusion orifice. The spray spun structure was collected on a cylindrical drum. The prociss eafiaiuifi for lz runs are summarized in Table 1 below:
- FIGS. 6 and 7 show, in perspective, a preferred embodiment of a gas jet for emitting a substantially planar gas stream.
- the gas enters through gas inlet passage 25 and is emitted through rectangular elongated gas orifree 18.
- EXAMPLE 1 Isotactic polypropylene having an intrinsic viscosity of 1.5 and a melt flow rating of 30 is spray-spun at a melt temperature of 390C. through four extrusion orifices arranged as shown in FIG. 8. Each orifice is of a substantially circular cross-section having a diameter of about 0.016 inch. Referring to FIG. 8, two planar attenuating gas jets, as shown in FIG. 6, were spaced at a distance of 2 inches from the axis of each extrusion nozzle, in approximately parallel relationship to each other along side each extrusion orifice.
- the elongated rectangular air jets had an orifice width of 0.010 inch and a length of about 1.88 inches and each emitted ambient air flowing at a rate of about 56 cubic feet per minute at a pressure of about 65 p.s.i.g.
- the gas jets 17 are positioned so that the planes of gas streams l8 intersect at a point 21 which is at a distance B of five-sixteenths inch from the axisof the extrudate streamwhich corresponds to nozzle axis 19.
- the distance A which defines the distance from the orifice 14 to the intersection point 21, is 4 inches.
- the attraction may be either physical or chemical, depending on the system i volved and the temperature employed.
- Physical adsorption (frequently referred to as van der Waals adsorption) is the result of a relatively weak interaction between a solid and a gas. This type of adsorption has one primary characteristic. Essentially all of a gas adsorbed can be removed by evacuation at the same temperature at which it was adsorbed.
- Equation 1 The expression describes the great majority of low temperature adsorption data. Physical measurements of the volume of gas adsorbed as a function of pressure at a fixed temperature, therefore, permit calculation of V,,,, the volume of gas required to form a layer one molecule thick. Equation 1 can be rearranged to the linear form Then a plot of data for P/V (P, P) versus P/P, gives a straight line, the intercept and slope of which are l/V,,,C and (C 1)V,,,C, respectively. The value of V is thus readily extracted from a series of measurements. From this information and knowledge of the physical dimensions of single molecules, the surface area of the adsorbing solid is computed.
- the preferred fiber-forming polymers employed in the present invention are the polyolefins, such as polyethylene or polypropylene.
- the melt index of the polyolefin prior to extrusion will ordinarily be from about 5 to 60 and preferably from about to 40.
- the intrinsic viscosity will be from about 1.0 to about 2.5 and preferably from about 1.0 to about 2.0.
- thermoplastic, melt-extrudable, fiber-forming polymers such as polyamides, polyesters, phenol-formaldehyde resins, polyacetals, and cellulose esters, e.g., cellulose acetate.
- spray spinning is aided by mixing the polymer with a melt depressant to facilitate melting without decomposition.
- Air will normally be employed as the attenuating gas for reasons of economy.
- gases e.g., steam, nitrogen, helium, etc.
- the attenuating gas will be at ambient temperature. Heated gas,
- a temperature of 250 to 500C may also be advantageously used, however.
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- Engineering & Computer Science (AREA)
- Textile Engineering (AREA)
- Mechanical Engineering (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
- Nonwoven Fabrics (AREA)
- Filtering Materials (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US23783272A | 1972-03-24 | 1972-03-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3787265A true US3787265A (en) | 1974-01-22 |
Family
ID=22895391
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US00237832A Expired - Lifetime US3787265A (en) | 1972-03-24 | 1972-03-24 | Process and apparatus for producing fibrous structures |
Country Status (14)
Country | Link |
---|---|
US (1) | US3787265A (pt) |
JP (1) | JPS5620383B2 (pt) |
BE (1) | BE797236A (pt) |
BR (1) | BR7302109D0 (pt) |
CA (1) | CA1038571A (pt) |
DE (1) | DE2314264C2 (pt) |
ES (2) | ES412969A1 (pt) |
FR (1) | FR2177924B1 (pt) |
GB (1) | GB1392408A (pt) |
IT (1) | IT983605B (pt) |
NL (1) | NL7304095A (pt) |
SE (2) | SE399573B (pt) |
SU (1) | SU608484A3 (pt) |
ZA (1) | ZA731735B (pt) |
Cited By (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3019154A1 (de) * | 1979-05-25 | 1980-12-04 | Celanese Corp | Auffangvorrichtung fuer ein spritzgesponnenes, ein schlauchvlies bildendes fadenmaterial |
US4475972A (en) * | 1981-10-01 | 1984-10-09 | Ontario Research Foundation | Implantable material |
US4812184A (en) * | 1986-02-04 | 1989-03-14 | Albany International Corp. | Method of manufacturing a hollow filament separatory module with constricted bundle end |
US4815660A (en) * | 1987-06-16 | 1989-03-28 | Nordson Corporation | Method and apparatus for spraying hot melt adhesive elongated fibers in spiral patterns by two or more side-by-side spray devices |
US5026450A (en) * | 1989-10-13 | 1991-06-25 | Nordson Corporation | Method of applying adhesive to the waist elastic material of disposable garments |
US5582907A (en) * | 1994-07-28 | 1996-12-10 | Pall Corporation | Melt-blown fibrous web |
US5591335A (en) * | 1995-05-02 | 1997-01-07 | Memtec America Corporation | Filter cartridges having nonwoven melt blown filtration media with integral co-located support and filtration |
US6074869A (en) * | 1994-07-28 | 2000-06-13 | Pall Corporation | Fibrous web for processing a fluid |
US6197141B1 (en) * | 1997-12-11 | 2001-03-06 | Kent M. Madsen | Process of applying filament netting for pest control of vegetation |
US6736274B2 (en) | 2001-08-17 | 2004-05-18 | Total Filter Technology, Inc. | Nonwoven tubular filter extracting |
EP2399451A1 (en) * | 2010-06-25 | 2011-12-28 | L.C. Maan engineering B.V. | Combination of a cup, an envelope and a substrate |
CN102787374A (zh) * | 2012-07-20 | 2012-11-21 | 东华大学 | 一种制备超细纤维的熔喷模头 |
WO2016168505A1 (en) * | 2015-04-16 | 2016-10-20 | Stryker Corporation | System and method for manufacturing variable stiffness catheters |
JP2020196960A (ja) * | 2019-05-31 | 2020-12-10 | ヤマシンフィルタ株式会社 | メルトブロー装置及びナノファイバ製造方法 |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4726901A (en) * | 1984-01-06 | 1988-02-23 | Pall Corporation | Cylindrical fibrous structures with graded pore size |
JPS61146862A (ja) * | 1984-12-15 | 1986-07-04 | 三井化学株式会社 | 綿状物の製造方法 |
JPH038855A (ja) * | 1990-05-14 | 1991-01-16 | Toray Ind Inc | 柔軟で高い伸縮性を有する弾性不織布の製造方法 |
DE102009041401A1 (de) * | 2009-09-12 | 2011-03-24 | Hydac Filtertechnik Gmbh | Filterelement mit einem Filtermedium sowie Verfahren zum Herstellen desselben |
DE102015210735A1 (de) * | 2015-06-11 | 2016-12-15 | M & A - Dieterle GmbH Maschinen- und Apparatebau | Verfahren zur Herstellung eines Faser-Kunststoff-Verbunds, Verfahren zur Herstellung eines Laminats, Faser-Kunststoff-Verbund sowie Enderzeugnis |
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US2315735A (en) * | 1940-05-15 | 1943-04-06 | Nat Gypsum Co | Method of and apparatus for blowing mineral wool |
US3543332A (en) * | 1966-09-21 | 1970-12-01 | Celanese Corp | Apparatus for producing fibrous structures |
US3565729A (en) * | 1962-02-03 | 1971-02-23 | Freudenberg Carl | Non-woven fabric |
US3684415A (en) * | 1968-08-14 | 1972-08-15 | Exxon Research Engineering Co | Melt blown roving die |
US3704198A (en) * | 1969-10-09 | 1972-11-28 | Exxon Research Engineering Co | Nonwoven polypropylene mats of increased strip tensile strength |
Family Cites Families (5)
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GB848231A (en) * | 1957-08-21 | 1960-09-14 | Owens Corning Fiberglass Corp | A method and apparatus for finely dividing heat softenable materials |
DE1560800A1 (de) * | 1966-02-10 | 1971-01-07 | Lutravil Spinnvlies | Verfahren und Vorrichtung zur Herstellung von Mischvliesen durch Schmelzspinnen |
CA995430A (en) * | 1968-12-23 | 1976-08-24 | Robert R. Buntin | Non-woven polypropylene mats by melt blowing |
US3650866A (en) * | 1969-10-09 | 1972-03-21 | Exxon Research Engineering Co | Increasing strip tensile strength of melt blown nonwoven polypropylene mats of high tear resistance |
US3795571A (en) * | 1969-10-09 | 1974-03-05 | Exxon Research Engineering Co | Laminated non-woven sheet |
-
1972
- 1972-03-24 US US00237832A patent/US3787265A/en not_active Expired - Lifetime
-
1973
- 1973-03-13 ZA ZA731735A patent/ZA731735B/xx unknown
- 1973-03-19 GB GB1314673A patent/GB1392408A/en not_active Expired
- 1973-03-22 DE DE2314264A patent/DE2314264C2/de not_active Expired
- 1973-03-22 CA CA166,722A patent/CA1038571A/en not_active Expired
- 1973-03-23 NL NL7304095A patent/NL7304095A/xx not_active Application Discontinuation
- 1973-03-23 SU SU731900554A patent/SU608484A3/ru active
- 1973-03-23 JP JP3277773A patent/JPS5620383B2/ja not_active Expired
- 1973-03-23 BR BR732109A patent/BR7302109D0/pt unknown
- 1973-03-23 FR FR7310569A patent/FR2177924B1/fr not_active Expired
- 1973-03-23 IT IT22076/73A patent/IT983605B/it active
- 1973-03-23 SE SE7304167A patent/SE399573B/xx unknown
- 1973-03-23 BE BE129179A patent/BE797236A/xx not_active IP Right Cessation
- 1973-03-23 ES ES412969A patent/ES412969A1/es not_active Expired
-
1975
- 1975-08-01 ES ES439943A patent/ES439943A1/es not_active Expired
-
1976
- 1976-01-16 SE SE7600443A patent/SE7600443L/xx unknown
Patent Citations (5)
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US2315735A (en) * | 1940-05-15 | 1943-04-06 | Nat Gypsum Co | Method of and apparatus for blowing mineral wool |
US3565729A (en) * | 1962-02-03 | 1971-02-23 | Freudenberg Carl | Non-woven fabric |
US3543332A (en) * | 1966-09-21 | 1970-12-01 | Celanese Corp | Apparatus for producing fibrous structures |
US3684415A (en) * | 1968-08-14 | 1972-08-15 | Exxon Research Engineering Co | Melt blown roving die |
US3704198A (en) * | 1969-10-09 | 1972-11-28 | Exxon Research Engineering Co | Nonwoven polypropylene mats of increased strip tensile strength |
Cited By (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3019154A1 (de) * | 1979-05-25 | 1980-12-04 | Celanese Corp | Auffangvorrichtung fuer ein spritzgesponnenes, ein schlauchvlies bildendes fadenmaterial |
US4475972A (en) * | 1981-10-01 | 1984-10-09 | Ontario Research Foundation | Implantable material |
US4812184A (en) * | 1986-02-04 | 1989-03-14 | Albany International Corp. | Method of manufacturing a hollow filament separatory module with constricted bundle end |
US4815660A (en) * | 1987-06-16 | 1989-03-28 | Nordson Corporation | Method and apparatus for spraying hot melt adhesive elongated fibers in spiral patterns by two or more side-by-side spray devices |
US5026450A (en) * | 1989-10-13 | 1991-06-25 | Nordson Corporation | Method of applying adhesive to the waist elastic material of disposable garments |
US5582907A (en) * | 1994-07-28 | 1996-12-10 | Pall Corporation | Melt-blown fibrous web |
US5586997A (en) * | 1994-07-28 | 1996-12-24 | Pall Corporation | Bag filter |
US6074869A (en) * | 1994-07-28 | 2000-06-13 | Pall Corporation | Fibrous web for processing a fluid |
US5652050A (en) * | 1994-07-28 | 1997-07-29 | Pall Corporation | Fibrous web for processing a fluid |
US5846438A (en) * | 1994-07-28 | 1998-12-08 | Pall Corporation | Fibrous web for processing a fluid |
US5733581A (en) * | 1995-05-02 | 1998-03-31 | Memtec America Corporation | Apparatus for making melt-blown filtration media having integrally co-located support and filtration fibers |
US5681469A (en) * | 1995-05-02 | 1997-10-28 | Memtec America Corporation | Melt-blown filtration media having integrally co-located support and filtration fibers |
US5591335A (en) * | 1995-05-02 | 1997-01-07 | Memtec America Corporation | Filter cartridges having nonwoven melt blown filtration media with integral co-located support and filtration |
US6197141B1 (en) * | 1997-12-11 | 2001-03-06 | Kent M. Madsen | Process of applying filament netting for pest control of vegetation |
US6736274B2 (en) | 2001-08-17 | 2004-05-18 | Total Filter Technology, Inc. | Nonwoven tubular filter extracting |
EP2399451A1 (en) * | 2010-06-25 | 2011-12-28 | L.C. Maan engineering B.V. | Combination of a cup, an envelope and a substrate |
CN102787374A (zh) * | 2012-07-20 | 2012-11-21 | 东华大学 | 一种制备超细纤维的熔喷模头 |
WO2016168505A1 (en) * | 2015-04-16 | 2016-10-20 | Stryker Corporation | System and method for manufacturing variable stiffness catheters |
US10426917B2 (en) | 2015-04-16 | 2019-10-01 | Stryker Corporation | System and method for manufacturing variable stiffness catheters |
JP2020196960A (ja) * | 2019-05-31 | 2020-12-10 | ヤマシンフィルタ株式会社 | メルトブロー装置及びナノファイバ製造方法 |
Also Published As
Publication number | Publication date |
---|---|
GB1392408A (en) | 1975-04-30 |
BR7302109D0 (pt) | 1974-07-25 |
FR2177924A1 (pt) | 1973-11-09 |
AU5353573A (en) | 1974-09-26 |
CA1038571A (en) | 1978-09-19 |
JPS5620383B2 (pt) | 1981-05-13 |
IT983605B (it) | 1974-11-11 |
DE2314264A1 (de) | 1973-10-04 |
ES439943A1 (es) | 1977-03-01 |
JPS496265A (pt) | 1974-01-19 |
SU608484A3 (ru) | 1978-05-25 |
DE2314264C2 (de) | 1985-08-08 |
ES412969A1 (es) | 1976-06-16 |
ZA731735B (en) | 1974-10-30 |
BE797236A (fr) | 1973-09-24 |
NL7304095A (pt) | 1973-09-26 |
SE7600443L (sv) | 1976-01-16 |
SE399573B (sv) | 1978-02-20 |
FR2177924B1 (pt) | 1978-05-12 |
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Owner name: OSMONICS, INC., 5951 CLEARWATER DR., MINNETONKA, M Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:CELANESE CORPORATION;REEL/FRAME:004179/0896 Effective date: 19830808 |