Classifications

• • 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
  • C08G73/00—Macromolecular compounds obtained by reactions forming a linkage containing nitrogen with or without oxygen or carbon in the main chain of the macromolecule, not provided for in groups C08G12/00 - C08G71/00
  • C08G73/06—Polycondensates having nitrogen-containing heterocyclic rings in the main chain of the macromolecule
  • C08G73/10—Polyimides; Polyester-imides; Polyamide-imides; Polyamide acids or similar polyimide precursors
  • C08G73/14—Polyamide-imides
• • 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
  • C08G18/00—Polymeric products of isocyanates or isothiocyanates
  • C08G18/06—Polymeric products of isocyanates or isothiocyanates with compounds having active hydrogen
  • C08G18/08—Processes
  • C08G18/0804—Manufacture of polymers containing ionic or ionogenic groups
  • C08G18/0819—Manufacture of polymers containing ionic or ionogenic groups containing anionic or anionogenic groups
  • C08G18/0828—Manufacture of polymers containing ionic or ionogenic groups containing anionic or anionogenic groups containing sulfonate groups or groups forming them
• • 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
  • D01F6/74—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polycondensates of cyclic compounds, e.g. polyimides, polybenzimidazoles
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
  • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y10S528/00—Synthetic resins or natural rubbers -- part of the class 520 series
  • Y10S528/906—Fiber or elastomer prepared from an isocyanate reactant

Definitions

• ABSTRACT A process for producing brilliant thermostable polyamideimide fibers and such fibers so produced, such process comprising extruding an N-methylpyrrolidone solution of a polymer having a structure characterized by the following linkagesz' B. amide linkages of the formula:
• Ar represents a bivalent aromatic radical
• Ar represents a trivalent aromatic radical
• R represents a bivalent aromatic, aliphatic, cycloaliphatic or arylaliphatic radical
• M represents an alkali or alkaline earth metal
• linkages B representing at least 3 percent of the total of linkages A, B and C in an aqueous N-methylpryyolidone coagulating bath
• drawing the extruded filaments in air at a rate of at least 1.5 X drying the filaments to eliminate N-methylpyrrolidone; and drying the filaments.
• the filaments obtained are characterized in being brilliant, homogenous, thermostable filaments.
• French Patent 1,223,162 involves the spinning of sulfonated acrylic polymers in order to improve the homogeneity of coagulation of the acrylic fibers having the natural tendency to form voids at the time of their coagulation in wet spinning.
• any sul-' fonic group containing monomer copolymerimble with acrylonitrile can be utilized to improve the homogeneity of coagulation and, accordingly to improve the characteristics of the fibers.
• thermostable polyamide-imide fibers and such fibers so produced, wherein such method eliminates the various deficiencies and disadvantages of conventional wet spinning processes.
• the brilliant thermostable polyamide-imide fibers are prepared by wet spinning an N-methylpyrrolidone solution of a polymer comprising:
• Ar represents a bivalent aromatic nucleus, i.e. either a monocyclic or bicyclic aromatic nucleus
• Ar represents a trivalent aromatic nucleus, preferably a monocyclic aromatic nucleus
• R represents a bivalent aromatic nucleus, aliphatic, cycloaliphatic or arylaliphatic radical
• M represents an alkali or alkaline earth metal.
• Ar represents a bivalent aromatic nucleus as set forth above, the polyamide-imide may contain structural units wherein Ar, represents an aliphatic or cycloaliphatic radical, although such structural units are present only in a minor proportion in the polymer structure, i.e. at least percent of the Ar radicals are the divalent aromatic nucleus.
• the B linkage as described above i.e. the linkage derived from an alkali or alkaline earth metal salt of dicarboxy-3,5 benzene sulfonic acid is present in the polymer structure in an amount of at least 3 mole percent based upon the total number of linkages A, B and C.
• linkages c are optionally present in the polymer structure, the same generally comprising from O to 20 mole percent. The remaining linkages comprise linkage A.
• the polymers of the present invention hereinafter referred to as sulfonated polyamide-imides" can be obtained by a conventional polymerization reaction.
• the sulfonated polyamide-imide can be prepared in substantially stoichiometric proportions by polymerizing at least one aromatic diisocyanate with an acid reagent comprising at least one aromatic acid anhydride and an alkali or alkaline earth salt of dicarboxy-3,5 benzene sulfonic acid in an anhydrous polar organic solvent.
• the system may contain minor amounts of an aromatic, aliphatic, cycloaliphatic or arylaliphatic diacid.
• aromatic diisocyanates which can be used in the production of the sulfonated polyamide-imides can comprise any of the conventional monocyclic and bicyclic diisocyanates, including the symmetrical and unsymmetrical diisocyanates. Accordingly, suitable examples include toluylene diisocyanates, diisocyanatodiphenylmethane, diisocyanatodiphenylpropane, diisocyanatodiphenyl-ether, etc. Of
• bicyclic diisocyanates the symmetrical bicyclic diisocyanates are preferred.
• an aliphatic or cycloaliphatic diisocyanate may be added to the reaction system in a minor proportion, i.e. up to about 20 mole percent based upon the diisocyanate component.
• The. addition of such an aliphatic or cycloaliphatic diisocyanate tends to improve certain properties of the polyamide-imide, such as the solubility of the finished product, flexibility and elasticity of the shaped articles produced therefrom.
• the acid anhydride which is utilized to produce the polyamide-imide generally comprises an anhydride of a benzene tricarboxylic acid.
• the preferred benzene tricarboxylic acid in accordance with the present invention comprises trimellic acid, trimellitic anhydride being preferred.
• substituted derivatives of such benzene tricarboxylic acid anhydrides can be advantageously utilized in accordance with the present invention as long as the substituent does not interfere with the polyamide-imide forming reaction.
• the dicarboxylic acids which are utilized in accordance with the present invention can be aromatic, aliphatic, or cycloaliphatic dicarboxylic acids, although aromatic dicarboxylic acids are preferred.
• Suitable aromatic dicarboxylic acids include for example: isophthalic, terephthalic, 4,4'-diphenyl dicarboxylic 3,3-diphenyl dicarboxylic, 4,4-diphenylether dicarboxylic, 3,3'-diphenylether dicarboxylic, 4,4-diphenylthioether dicarboxylic.
• Aliphatic dicarboxylic acids oxalic, succinic, adipic, azelaic, sebacic, acids.
• Cycloaliphatic dicarboxylic acids l,3-cyclohexane dicarboxylic and 1,4-cyclohexai1e dicarboxylic acids.
• aromatic dicarboxylic acids such as terephthalic acid and isophthalic acid are preferred as are aliphatic dicarboxylic acids such as adipic acid, sebacic acid, and succinic acid.
• the dicarboxylic acid is generally present in the reaction system in an amount of -20 mole percent.
• the B linkages i.e. the linkages derived from an alkali or alkaline earth salt of dicarboxy-3,5 benzene sulfonic acid are present in the final polyamide-imide in an amount of at least 3 mole percent, based upon the total linkages A, B and C, preferably in an amount of 3-l0 mole percent.
• an amount greater than about mole percent is disadvantageous for economic reasons.
• the amount of linkages being present in the polyamide-imide varies somewhat with regard to the count of the filaments that are to be obtained. Thus, for example, good results are obtained with an amount of about 4 mole percent in the case of rather fine filaments, e.g.
• the remainder of the polyamide-imide comprises amideimide linkages A and, optionally, amide linkages C.
• the amide linkages C are present in the final polyamide-imide only in a minor amount, i.e. of from O to about 20 mole percent.
• the remainder of course comprises the amide imide linkages A.
• a solution of the polymer preferably an N-methylpyrrolidone solution is extruded into an aqueous coagulating bath containing 30 to 75 percent by weight of N-methylpyrrolidone and, thereafter the filaments produced are drawn in air at a rate of at least 1.5 X, generally under ambient temperature conditions. The drawn filaments are thereafter washed to eliminate the N-methylpyrrolidone and dryed by any known conventional means.
• sulfonated copolyamides-imides can be obtained by the reaction in a polar organic solvent medium of substantially stoichiometric proportions of a diamine and a reagent comprising an acid chloride function and an anhydride function, an alkali or alkaline earth dicarboxy-3,5 benzene sulfonate dichloride and, optionally, a dichloride of an aromatic, aliphatic, cycloaliphatic or arylaliphatic dicarboxylic acid.
• the polar organic solvent utilized to produce the polyamide-irnide can comprise any of those conventionally utilized in such polymer production.
• the polar organic solvent can comprise such materials as for example, dimethylformamide, dimethylacetamide, hexamethyl phosphoryltriamide, tetramethylene sulfone and preferably, N-methylpyrrolidone.
• N-methylpyrrolidone is employed as the organic solvent in the production of the polyamide-imide it is generally unnecessary to eliminate the solvent prior to utilizing a solution of the polymer in the extrusion step.
• N-methylpyrrolidone utilized as the organic solvent in the polymerization process
• the solution of the sulfonated polyamide-imide directly obtained from polymerization can be utilized in'the extrusion without first separation of the polymer. It is often preferable however to separate the polymer from the solution and then redissolve the polymer in N-methylpyrrolidone for extrusion so as to eliminate any byproducts which may be formed during the polycondensation reaction.
• the sulfonated polyamide-imides which are utilized in accordance with the present invention are those which have an inherent viscosity greater than about 0.5 and, preferably, less than about 1.4.
• the inherent viscosity is measured at 25 C. with a 0.5 percent by weight solution in N-methylpyrrolidone.
• the sulfonated polyamide-imide is one having an inherent viscosity of between 0.8 and 1.2.
• the solution of the sulfonated polyamide-imide is one which has a viscosity of from about 150 to about 3,000 poises at 25C. (measured by a Drage viscosimeter using speed II and a mobile 47.2). It is preferred in accordance with the present invention that the viscosity of the sulfonated polyamide-imide solution not exceed 1,500 poises.
• the spinning solution normally contains the concentration of the sulfonated polyamide-imide polymer of between 10 and 30 percent by weight, preferably between 15 and 25 percent by weight. Additionally, the spinning solution can contain other various conventional adjuvants such as pigments, dulling agents, etc.
• the temperature of the solution at extrusion is not critical to the process of the present invention and, the same can vary within broad limits, depending upon the viscosity of the spinning solution. For example, a spinning solution having a low viscosity can easily be extruded at ordinary ambient temperatures although it is preferred to extrude high viscosity solutions at elevated temperatures, e.g. for example at C. or more so as to avoid utilizing high pressures in the spinneret.
• Such variables however are the conventional variables utilized in spinning and extrusion processes and are not critical or peculiar to the process of the present invention.
• the sulfonated polyamide-imide filaments are extruded into a coagulating bath comprising an aqueous solution containing 30 to 75 percent by weight of N- methylpyrrolidone. It is preferred in accordance. with the present invention that such coagulating bath contain at least 50 percent by weight of N'-methylpyrrolidone since such higher concentrations allow the production of filaments having better drawability and, therefore, filaments having superior final properties.
• the speed of passage of the extruded filaments in the coagulating bath can vary within broad limits and the process of the present invention is not dependent thereon.
• the speed of passage of the filaments depends upon the N-methylpyrrolidone concentration in the coagulating bath and the distance the filaments must travel in the bath.
• Such passage speed in the coagulating bath generally varies between to 60 meters per minute, although higher or lower speeds can be employed where desired for particular purposes. Generally, there is no advantage in spinning at lower speeds because this reduces the economic advantages of the process.
• the passage speed of the filaments in the coagulating bath is too excessive the drawability of the filaments in air is reduced. Accordingly it is generally preferred to operate within the limits set forth above.
• the length of the coagulating bath can vary within broad limits again depending upon the N-methylpyrrolidone concentration in the coagulating bath. For example, a coagulating bath of 10 centimeters is sufficient to obtain good coagulation with a bath containing less than 50 percent N- methylpyrrolidone. Similarly, there is an advantage in using lengths greater than 40 centimeters where the concentration of the N-methylpyrrolidone in the coagulating bath exceeds 65 percent. Also, it is generally preferable to increase the length of the coagulating bath when a high number of strands are spun by the same spinneret.
• the temperature of the coagulating bath is not critical to the process of the present invention and the same can be suitably chosen within wide limits. However, to achieve the best results in accordance with the present invention the coagulating bath is preferably at a temperature of between and 40 C. Here again, however, higher or lower temperatures than the range set forth above can be advantageously utilized when desired for particular purposes.
• the coagulated filaments are drawn, in air, at a rate of at least 1.5 X, for example, between L? and 2 or more, there being no maximum to the amount of drawing except that which the filaments can withstand without breaking.
• the rate of drawing increases the brilliance of the filaments increases.
• the drawing should be conducted as high as possible, the minimum being at least 1.5 X.
• the filaments are washed in order to remove any Nmethylpyrrolidone which may adhere to the filaments.
• the filaments can be washed with water utilizing any known conventional means.
• the washing can be performed in successive vats in which water circulates countercurrent or by utilizing washing rollers or any other similar means.
• the washed filaments are then dried by any known conventional means such as for example in a conventional dryer or on rollers.
• the temperature of this drying is not critical to the process of the present invention and such temperature can vary within broad limits. When the speed of drying is greater, the temperature is usually higher. It is generally advantageous to perform the drying with progressively higher temperatures, temperatures reaching and even exceeding 260 C. being applicable.
• the drawn filaments can be further drawn in a secondary drawing operation through any known conventional means.
• this second drawing can take place in an oven by the use of plates, rollers, rollers and plates, etc., and should be conducted at a temperature of at least 300 C., temperatures up to and exceeding 420 C. being applicable.
• the rate of this second drawing is at least l.5 although the rate can vary within broad limits, depending upon the qualities desired in the finished yarn.
• this secondary drawing is optional in accordance with the present invention and need not be utilized to obtain a brilliant yarn as described previously.
• This secondary drawing when utilized can be performed in one or more stages, continuously or intermittently with the preceding operations.
• this second drawing can be combined with drying and to accomplish this a zone of higher temperature can be utilized at the end of the drying so as to permit the secondary drawing.
• the process of the present invention allows for the production of very brilliant filaments, fibers and yarns not previously obtainable by the wet spinning of polyamide-imides.
• such process is dependent upon the introduction into a polyamide-imide of linkages derived from an alkali or alkaline earth salt of dicarboxy-3,5 benzene sulfonic acid in an amount of at least 3 mole percent, based upon the polyamide-imide; extruding the polymer into a coagulating bath containing 30 to 75 percent by weight of N- methylpyrrolidone; drawing the filaments in air at a rate of at least 1.5 X; washing the drawn filaments to eliminate the N- methylpyrrolidone; drying the washed filaments by any known conventional means; and, optionally, again drawing the filaments at a rate of at least 1.5 X.
• filaments which are produced have excellent physical properties and are very resistant to exposure at high temperatures. Moreover, such filaments have excellent affinity for basic dyes.
• viscosity of the solutions is measured by a Drage viscosimeter using speed II and mobile 47.2 unless otherwise indicated.
• the inherent-viscosity is measured at 25 C. utilizing a 0.5 solution by weight of N-methylpyrrolidone.
• a solution is obtained with a viscosity at 25 C. of 180 poises and the polymer has an inherent viscosity of 1.65.
• the solution is extruded at a speed of 10 m/min through a spinneret having 64 orifices of 0.05 mm in diameter, into a coagulating bath containing 30 percent N-methylpyrrolidone and 70 percent water, the length of 'travel of the yarn in the coagulating bath being 20 cm.
• the yarn in a gel state, is drawn in air at ambient temperature at a rate of 1.5 X. Then the drawn yarn is washed in water to remove the solvent and dried on a roller at 60
• the yarn which is obtained is very brilliant.
• the yarn has a count of 260 dtex/64 filaments, a dry tenacity of 9 g/tex and a dry elongation of 13 percent.
• the yarn is then subjected to a second drawing at 380 C. at a rate of 6.9 X. After thissecond drawing the yarn has a dry tenacity of 33 g/tex and a dry elongation of 14 percent.
• the viscosity at 25 C. of the solution obtained through the foregoing reaction is 458 poises and the inherent viscosity of the polymer 8 is 1.00.
• the solution is extruded at a speed of 10 m/min through a spinneret having 200 orifices of 0.055 mm in diameter into the same coagulating bath as in Example 1.
• the yarn, in the gel state, is drawn at a rate of 2 and thereafter washed in water and finally dried on two rollers at 40 and 150 C., respectively.
• the yarn which is obtained is very brilliant.
• the yarn has a count of 800 dtex/200 filaments, a dry tenacity of 17 g/tex and a dry elongation of 20 percent.
• the yarn After a second drawing at 400 C. at a rate of 3.1 X, the yarn has a count of 278 dtex/200 filaments, a dry tenacity of 33 g/tex and a dry elongation of 9 percent.
• the viscosity at 25 C. of the solution which is obtained is 413 poises and the inherent viscosity of the polymer is 1.20.
• the solution is extruded at a speed of 10 m/min through a spinneret having 15,000 orifices of 0.08 mm in diameter into a coagulating bath containing 65 percent N-methylpyrrolidone and 35 percent water, the travel of the cable in the bath being cm.
• the cable in the gel state, is drawn in air at ambient temperature at a rate of 1.75 X.
• the cable is then washed in water countercurrent is successive washing vats and is placed without tension on a perforated endless belt of a ventilated dryer the temperature of which varies from 70 to C. from one end of the dryer to the other.
• the cable obtained through the above procedure is very brilliant. It has a count of 45,000 dtex/l5,000 filaments, a dry tenacity of 12 g/tex and a dry elongation of 12 percent.
• the cable is thereafter overdrawn in an oven at 400 C. at a rate of 2 X.
• the cable then has a count of 33,600 dtex, a dry tenacity of 29 g/tex, and a dry elongation of 13 percent.
• diisocyanatodiphenylether 35 molar parts trimellitic anhydride 25.55 molar parts terephthalic acid 7 molar parts sodium dicarboxy-3,5 benzene sulfonate 2.45 molar parts in dehydrated N-methylpyrrolidone.
• the viscosity at 25 C. of the solution obtained by the above reaction is 720 poises and the inherent viscosity of the polymer is 1.81.
• the solution is extruded at a speed of 10 m/min through a spinneret having 200 orifices of 0.055 mm in diameter into a coagulating bath containing 50 percent N-methylpyrrolidone and 50 percent water, the travel of the yarn in the bath being cm.
• the yarn, in the gel state is drawn at a rate of 1.8 X in air at ambient temperature, then washed and dried on two rollers, the respective temperatures of which are 40 and 150 cC.
• the yarn obtained by the foregoing procedure is very brilliant.
• the yarn has a count of 800 dtex/200 filaments, a dry tenacity of 19 g/tex and a dry elongation of 12 percent.
• the yarn After overdrawing at 400 C. at a rate of 2.6 X, the yarn has a dry tenacity of 40 g/tex and a dry elongation of 5 percent.
• EXAMPLE 7 200 molar parts 157 molar parts 38 molar parts 10 molar parts diisocyanatodiphenylmethane trimellitic anhydride terephthalic acid sodium dicarboxy-3,5 benzene sulfonate
• the solution which is obtained has a 19.6 percent concentration and a viscosity at C. of 1,500 poises.
• the solution is diluted to bring its concentration to 17 percent and its viscosity falls to 300 poises.
• the inherent viscosity of the polymer is 1.43.
• the solution is extruded at a speed of 10 m/min through a spinneret having 64 orifices of 0.05 mm in diameter into a coagulating bath containing 60 percent N-methylpyrrolidone and 40 percent water, the travel of the yarn in the bath being 20 cm.
• the yarn, in the gel state is drawn at a rate of 2 X in air, washed in water and dried on a roller at 50 C.
• the drawn yarn which is obtained is brilliant and silky, very soft to the touch.
• the yarn has a count of 280 dtex/64 filaments, a dry tenacity of 17 g/tex and a dry elongation of percent.
• the yarn is then overdrawn at a rate of 2.3 X at 340 C. lts count is then 120 dtex, its dry tenacity 39 g/tex and its dry elongation 12 percent.
• the viscosity at 25 C. of the solution which is obtained is 400 poises and the inherent viscosity of the polymer is 1.21.
• the solution is extruded at a speed of m/min through a spinneret having 64 orifices of 0.06 mm in diameter into a coagulating bath containing 52 percent N-methylpyrrolidone and 48 percent water, kept at 20 C., the travel of the yarn in the bath being 40 cm.
• the yarn in the gel state, is drawn in air at a rate of 1.94 X before its passage in several loops over a washing roller, the peripheral speed of which is 68.4 m/min.
• the yarn is washed countercurrent on the washing roller by demineralized water with a delivery of 170 cm min, and then passes in several loops over a drying roller.
• This drying roller has several different temperature levels: 40 C. at the input of the yarn and 420 C. at its output. The hot, dry yarn coming from this drying roller then undergoes a drawing of 2.17 X before being wound at a speed of 149 m/min.
• the yarn which is obtained is very brilliant.
• the yam has a count of 191 dtex, a dry tenacity of 30.9 g/tex and a dry elongation of 8 percent EXAMPLE 9 coagulating bath containing 48 percent water and 52 percent N-methylpyrrolidone at a temperature of 20 C.
• the yarn is drawn in air at a rate of 1.8 X before being sent in several loops over an ensemble of two washing rollers turning at a speed of 81 m/min.
• the yarn is then dried on the same drying roller as in Example 8, but the temperature of which is kept at 250 C. at the exit..
• the yarn then passes over a plate at 300 C. and finally is wound at a speed of 142 m/min, giving it a drawing of 1.75 X. l
• the yarn which is obtained is very brilliant and has a count of 212 dtex, a dry tenacity of 28.1 g/tex, and a dry elongation of 9.4 percent.
• the solution is extruded at a speed of 45 m/rnin through a spinneret having 64 orifices of 0.06 mm in diameter into a coagulating bath containing 48 percent water and 52 percent N-methylpyrrolidone at a temperature of 20 C.
• the cable in the gel state, is drawn in air at ambient temperature at a rate of 1.8 X, before being washed on washing rollers on which it passes in a number of loops.
• the yarn then passes over a drying roller similar to that of Example 8, but the exit temperature of which is 360 C. and then passes over a delivery roller at a speed of 145 mm/min, giving it a drawing of 1.8 X between the drying roller and this delivery roller.
• the yarn then passes over a plate kept at 400C. where it is drawn 1.4 X before being wound at a speed of 210 m/min.
• the yarn which is obtained is very brilliant and presents a count of dtex, a dry tenacity of 31.8 g/tex, and a dry elongation of 10.7 percent.
• the cable in a gel state, is drawn at a rate of 1.8 X. Then the cable is washed with water countercurrently in successive washing vats and is placed without tension on a perforated endless belt of a ventilated dryer, the dry temperature of which varies from 100 to 140 C. from one end of the dryer to the other and the moist temperature of which is 85 C.
• the cable which is obtained is very brilliant and has a count of 176,000 dtex/40,000 filaments, a tenacity per unit filament of 15 g/tex and an elongation of 50 percent.
• the cable is overdrawn in an oven at 400 C. at a rate of 2 X.
• the tenacity per unit strand after overdrawing becomes 40 g/tex and its elongation: 20 percent.

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• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Health & Medical Sciences (AREA)
• Medicinal Chemistry (AREA)
• Polymers & Plastics (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Manufacturing & Machinery (AREA)
• General Chemical & Material Sciences (AREA)
• Textile Engineering (AREA)
• Artificial Filaments (AREA)
• Macromolecular Compounds Obtained By Forming Nitrogen-Containing Linkages In General (AREA)

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Cited By (27)

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Citations (1)

• 1971
  • 1971-01-14 FI FI87/71A patent/FI55686C/fi active
  • 1971-02-02 US US112083A patent/US3673160A/en not_active Expired - Lifetime
  • 1971-02-05 NL NLAANVRAGE7101578,A patent/NL168570C/xx not_active IP Right Cessation
  • 1971-02-11 BE BE762828A patent/BE762828A/xx not_active IP Right Cessation
  • 1971-02-11 LU LU62584D patent/LU62584A1/xx unknown
  • 1971-02-11 IL IL36176A patent/IL36176A/en unknown
  • 1971-02-11 NO NO510/71A patent/NO131608C/no unknown
  • 1971-02-11 SE SE7101727A patent/SE374395B/xx unknown
  • 1971-02-11 DK DK62771AA patent/DK127514B/da not_active IP Right Cessation
  • 1971-02-11 CH CH203871A patent/CH519595A/fr not_active IP Right Cessation
  • 1971-02-12 DE DE2106704A patent/DE2106704C3/de not_active Expired
  • 1971-02-12 JP JP46006120A patent/JPS516770B1/ja active Pending
  • 1971-02-12 AT AT121071A patent/AT316723B/de not_active IP Right Cessation
  • 1971-04-19 GB GB2151571A patent/GB1308582A/en not_active Expired

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