CN1234839A - Process for making high tenacity aramid fibers - Google Patents
Process for making high tenacity aramid fibers Download PDFInfo
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- CN1234839A CN1234839A CN97199148A CN97199148A CN1234839A CN 1234839 A CN1234839 A CN 1234839A CN 97199148 A CN97199148 A CN 97199148A CN 97199148 A CN97199148 A CN 97199148A CN 1234839 A CN1234839 A CN 1234839A
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- tow
- solidification liquid
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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
- D01D5/06—Wet spinning methods
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
- D01F6/60—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyamides
- D01F6/605—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyamides from aromatic polyamides
-
- 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
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- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
- Artificial Filaments (AREA)
Abstract
A process is disclosed for making para-aramid filaments of especially high strength by extruding a solution of para-aramid through fine capillaries and drying the resulting filaments under high tension.
Description
Background of invention
Invention field
The present invention relates to make the method for the extra high aramid fibre of intensity, the included technology point of this method is: special spinning head spinning aperture, special curing condition and special dry tension force.
Prior art is described
United States Patent (USP) 4,965,033 is authorized at the 1990-10-23 that applies for of Chiou, and discloses a kind of method of the solidification liquid stream spinning aramid fibre that utilizes high-quality (mass density), sprays.
United States Patent (USP) 3,767,756, the 1973-10-23 that applies at Blades authorizes, and 5,173,236, the 1992-12-22 that applies at Yang authorizes, and disclosing and having adopted the spinneret orifice diameter respectively is 0.025～0.25mm (1～10 mil) and less than the spinning head of 0.064mm (2.5 mil) spinning aramid fibre, and under the tension force at about 0.3 gram/dawn (gpd) method of this fiber of drying.
United States Patent (USP) 4,726,922 is authorized at the 1988-02-23 that applies for of Cochran and Yang, the spinning aramid fibre is disclosed and under the tension force of 3～7gpd dry this fiber to improve the method for fibre strength.
Summary of the invention
A kind of poly-(terephthalic acid (TPA) is to the benzene diester) (poly (p-phenylene terephthalate)) method of yarn that intensity is 28gpd at least of making is provided, may further comprise the steps: (a) extrude the tow that logarithmic viscosity number is 4 acid solution at least from spinning head, wherein comprise poly-(terephthalate p-phenylenediamine (PPD)) (poly (p-phenyleneterephthalamide)) of 30g/100mL acid at least, pass the non-freezing action fluid layer of inertia then, enter into coagulating bath, then in company with the coagulation bath of the constantly overflow spin duct of flowing through together; (b) enter in 2 milliseconds of times that spin duct begins from tow, be symmetry and hand over into 0 °～85 ° angle around tow with tow, inject additional solidification liquid down, (ⅰ) mass flowrate of keeping overflow and injecting the solidification liquid summation to the ratio between the tow mass flowrate greater than about 250, (ⅱ) keep the average linear velocity injected in the spin duct with overflow solidification liquid summation in the level that is lower than the tow line speed of leaving spin duct, (ⅲ) keep inject and the two flow rate of overflow solidification liquid at constant numerical value; And (c) with the tow drying,
Its improvements comprise, adopt spinning head and the tow of the highest 0.051mm of spinneret orifice diameter (2 mil) to carry out drying under at least 3.0 gram/dawn (gpd) tension force.
The accompanying drawing summary
Fig. 1 can be used for implementing this method is used for fiber of the present invention with manufacturing equipment sectional drawing.
Detailed Description Of The Invention
People have just poured into increasing effort and have developed high-intensity yarn and fabric.Each improvement is all hard-earned and significant, because even small improvement all will bring huge benefit.
Yarn of the present invention has the intensity of 28gpd at least, can adopt device depicted in figure 1 to make.Generally speaking, this yarn can be according to United States Patent (USP) 3,767,756 disclosure, adopt logarithmic viscosity number be at least 4.0 poly-(poly P phenylene diamine terephthalamide) (PPD-T), be dissolved in concentration and be at least in 98% the sulfuric acid and produce.PPD-T solution is extruded from spinning head, passes air-gap, and enters into coagulating bath.Spinning head has the spinneret orifice that diameter is equal to or less than 0.051mm (2.0 mil).It is found that the fibre bundle greater than the spinneret orifice of 0.051mm (2 mil) is produced it is believed that to have lower degree of molecular orientation, thereby causes the reduction of intensity, therefore, not as the tow made from the less spinneret orifice of diameter solid like that.From the angle of implementing, be difficult to use less than the spinneret orifice of about 0.025mm (1 mil), and may can not produce the acceptable fiber of quality.
Fig. 1 is the view profile of preferred coagulating bath 1.Bathing 1 is a kind of circular structure of being made up of the embedding disk 2 in the supporting construction 3 of packing into.Supporting construction 3 is included under the pressure quench liquid 5 is incorporated into the import 4 of going in the distribution loop 6, and distribution loop comprises filler 7, and it is fit to be used for promoting quench liquid along the coagulating bath even supply in 1 a peripheral week.
Solidification liquid can be incorporated in the bath via the grading ring (manifold) (being distribution loop) of periphery, and grading ring comprises baffle plate or filler, with provide solidification liquid along spinneret orifice uniform distribution and towards the no turbulent flow of spinneret orifice.Under the situation that circle is bathed, grading ring can surround this bath.Under the situation that the rectangle that has bar hole is bathed, grading ring still can surround bath, and still, solidification liquid is only introduced from solidification liquid one side that is parallel to the bar shaped seam.Only require flow to spinneret orifice solidification liquid stream near spinneret orifice for no turbulent flow.Therefore, filler 7 can be bead, a series of screen cloth, honeycomb, sintered metal plates or other similar elements.
Pass after the filler 7, quench liquid passes porous plate or screen cloth 8, and equably, no remarkable turbulent flow or back-mixing ground along continuous straight runs flow to 1 the center of bathing, at this, rapid lime set 5 contacts with the tow of extruding from spinning head 10 9, and quench liquid 5 and tow 9 flow in the spin duct 14 downwards by perforate 11 together then.
Certain profile can be made in the bottom of this bath, be denoted as A and B the zone, it can promote towards perforate 11 evenly, no turbulent flow.The convergent shape towards this hole also can be made in the peripheral region in this hole.Preferably, in no turbulent flow zone, the degree of depth of solidification liquid be no more than bathe wide by 20%.
For the small-scale spinning, 20 monofilament for example, suitable bath is wide to be to comprise the perforate of diameter 3.1mm in the bath by about 6.35cm (2.5 inches), take the convergent runner, the initial diameter of taper is about 12mm.For fairly large spinning, 1,000 monofilament for example, suitable bath is wide to be comprising the perforate of diameter 9mm, to take the convergent runner by about 23cm, and the initial diameter of taper is about 28mm.
Embed disk 2, comprise nozzle ring device 12, its operation principle is similar to United States Patent (USP) 4,298, disclosed spray nozzle device in 565.Hole 11 preferably has lip 13, and in other words, the diameter in hole 11 is slightly littler than the diameter of spin duct 14, so that help to gather tow 9 to prevent the wall adhesion mutually with hole 11 and spin duct 14.Quench liquid 5 enters into path 16 via opening 15, enter into one or more nozzle perforates 17 again, so quench liquid 5 just goes downstream together in company with tow 9 and other quench liquids 5 and flows through spin duct, until coming out to march on towards the wire device (not shown) from exporting 18.According to known operation sequence, tow is wound into the yarn that this method is produced at last through washing and/or neutralization and dry.
Preferably, form 0～85 ° angle (θ) between the liquid flow path direction that caused of spray-hole 17 and the tow.Though equaling 90 °, θ also can obtain satisfied result,, select the θ angle can make the control of process become very responsive like this, be worthless in industrial operation therefore.30 ° is specially suitable angle in the industrial production.The position of spray-hole 17 is near perforate 11 and the condensable fluid of ejection is entered point within 2 milliseconds of spin duct tow to spray at tow and flow downward.
When the prolongation of spinning head, spinneret orifice, nozzle and any spin duct all comes into line carefully along identical axis, and work as nozzle member through well-designed and aligning, thereby can provide around strand just during the jet of symmetry, this method will provide maximum improvement.The deviation of the alignment of any nozzle member or any solid particle are at the resident of nozzle opening so that cause symmetrical destruction, all can reduce or obliterate improved effect.This kind symmetry can realize by providing with respect to two or more spray-holes or the slit of strand symmetric arrangement.
According to this method, control overflow solidification liquid (Q
1) and inject solidification liquid (Q
2) the two flow rate and maintain constant level so that realize according to improvement of the present invention.The mass flowrate of tow mass flowrate should be controlled at greater than about 250 than (R).Preferably, mass flowrate (R) is greater than about 300.
In enforcement of the present invention, overflow condensable fluid (Q
1) flow rate control by the degree of depth (size h) of regulating perforate 11 top body lotions, the adjusting of this degree of depth is to realize by the amount of being metered into that enters in the bath, yet also depends on the diameter of spin duct 14.Size h is generally less than 1 inch (2.5cm), preferred about 0.5 inch (1.3cm).If h is too small, then owing to the proal swabbing action of tow, air will be inhaled in the spin duct 14, and this tensile property and mechanical quality for the finished product yarn all is disadvantageous.Therefore, h must be even as big as guaranteeing the numerical value do not have bubble to carry secretly.According to above Consideration, can calculate the diameter of suitable spin duct 14.Because quench liquid (Q
1) overflow flow rate by outlet opening is subjected to the influence of the strand that moves through same hole to a great extent, this effect also must be taken into account in the lump.For example, the overflow flow rate by 9.5mm (0.375 inch) diametric hole under the hydrostatic head effect of 15.9mm (0.625 inch) is about 1.5L/min (0.4 gpm) under the situation of mobile strand not; Under the situation of the tow of forming by 1000 monofilament of filament denier 1.5, be about 8.7L/min (2.3 gpm) with the 686m/min motion.This is normally owing to pass due to the swabbing action that the moving tow of this liquid layer causes by boundary layer effect.In order to offset this effect, the size in hole, promptly cross section diameter should be done suitable selection.
Inject solidification liquid (Q
2) flow rate preferably be pressed into a kind of size and control through the spray-hole of selecting by metering.The minimum cross section size of nozzle (as, aperture or flow width) generally in 0.05～2.5mm (2～100 mil).Wish that flow rate and spray-hole satisfy--the axial velocity of injecting solidification liquid surpass processed tow speed at least about 50%, preferably should surpass at least about 80%--and pull effect to prevent the strand that can cause intensity to reduce.Yet the axial velocity of injecting solidification liquid should not substantially exceed 200% of processed tow, preferably is no more than the about 150% of yarn speed, to prevent the excessive turbulence to strand, causes the measured value of yarn strength to reduce.Therefore, must adopt appropriate liquid flow rate and spray-hole or the slit injected, they should be able to provide greater than about 250, be preferably greater than about 300 merging solidification liquid quality-flow rate ratio to the tow quality, inject and should also provide the solidification liquid speed of appropriately injecting simultaneously greater than about 6.0 with respect to yarn speed to the ratio of momentum of overflow solidification liquid.
In the method for the invention, the average linear velocity of merging solidification liquid should maintain the speed of leaving spin duct less than strand in the spin duct.Like this, will prevent because " creep " in the tow causes the loss of yarn strength, and because of before the feeding roller, lacking the production continuity problem that enough tension force may cause.
The present invention is applicable to the various spinning speeds in the wide region, is particularly useful for the spinning speed of 300m/min at least, preferably at least about 350m/min, although higher spinning speed can cause really, with the reduction of comparing than low spinning speed on intensity.Though along with of the raising of quality-flow rate than (R) and ratio of momentum (Φ), the strength advantage that the inventive method obtained will continue to strengthen, and thereby can offset because of the continuation of spinning speed improves the tendency that causes intensity to reduce, still, it is believed that, when mass flowrate surpasses 5000 than (R), and ratio of momentum (Φ) surpasses after 50, and the effect of improvement will be no longer obvious, therefore, considering technically will be no longer economical, especially for the heavy dawn spinning such as 1500 dawn.
Fiber has just been finished manufacture process through washing and drying after spinning and having passed through coagulating bath.Fiber must fully wash to remove the acid of whole traces, so that eliminate the possibility of the fiber degradation relevant with acid.Can use the combination of independent water or water and alkaline solution to come washing the fibre.A kind of washing methods easily is (as saturated NaHCO with aqueous base
3Or 0.05N NaOH) spray leaves coagulating bath and around the strand to roller, so that its acid content is reduced to about 0.01% (by fiber butt).
Fiber can warm-up mill (as, 160 ℃) on realize easily dry.The preferred washing methods of the present invention is to adopt the spray washing fiber and make it continuously by maintaining about 150 ℃ drying roller.
A key element of this method relates to carries out drying with fiber under the high-tension of about 3.0～7.0gpd.If dry tension force is less than 3.0gpd, and the degree of molecular orientation of then making fiber will reduce, and cause intensity decreases, and if dry tension force then can cause too much strand broken end greater than 7.0gpd, and relevant operation just is difficult to carry out.Especially the dry tension force of preferred about 3.0～5.0gpd.
Method of testing
Tensile property
Intensity provides divided by line density by fracture strength.Modulus is by the initial slope of stress/strain curves and is scaled with the intensity same units and draws.Length when elongation is fracture increases percentage.Intensity and modulus all are to be that unit calculates by gpd earlier, and the result who obtains is multiplied by 0.8826 again, is to be the numerical value of unit with dN/tex.Each measured value that provides is the mean value of breaking 10 times.
The dawn number is that 9000 meters yarns or monofilament are the weight of unit with the gram, and the dtex number then is 10,000 meters long, is the weight of unit with the gram.
The tensile property of yarn is through balance under condition determination at least after the 14h, measures under the condition of 24 ℃ and 55% relative humidity.Before the mensuration, every one thread by add be twisted to 1.1 twist multiplier (for example, the yarn at nominal 1500 dawn be coupled with about 0.8 turn/centimetre the twist).The sample of every twisting adopts the stress/strain device of typical tape recording, and testing length is set at 25.4cm, and by 50%/min stretch (is benchmark with original unstretched length).
The twist multiplier of yarn (TM) is defined as follows:
TM=(tpi) (dawn number)
1/2/ 73=(tpc) (dtex number)
1/2/ 30.3
Tpi=number of twists/inch wherein;
The tpc=number of twists/centimetre.
The tensile property of yarn is different from and is lower than the tensile property of monofilament, and therefore, these numerical value of yarn can't be successfully and estimated by the numerical value of monofilament exactly.
Ratio of momentum (Φ)
The definition of ratio of momentum is to inject the momentum (M of solidification liquid along the strand direction
2) with the momentum (M of overflow solidification liquid
1) ratio, i.e. Φ=M
2/ M
1The definition of momentum is the product of mass flowrate and flowing velocity.The computational methods of ratio of momentum are described in the United States Patent (USP) 4,298,565 above-mentioned, in example, calculate according to following formula,
Φ=Q
2 2×d
1 2cosθ/(4Q
1 2×d
2(d
1+d
2cosθ))
Wherein
Q
1It is the overflowing liquid flow rate
Q
2Be to inject the liquid flow rate
d
1It is the spin duct internal diameter
d
2It is the minimum dimension of spray-hole
θ injects acute angle folded between liquid and the strand.
As long as d
1And d
2, and Q
1And Q
2All adopt same unit, then ratio Φ is just irrelevant with selected unit.
Quality-flow rate is than (R)
This numerical value is the solidification liquid mass flowrate of merging and the ratio of tow (butt) mass flowrate.The base unit of liquid flow rate Q is a gpm.
Q * 3899=mass flowrate g/min
With regard to tow, base unit is: speed (Y), unitary code/minute (being ypm); And dawn number (D), g/9000m.
YD * (0.9144/9000)=mass flowrate g/min.
So mass flowrate just becomes Q/YD * 3.8376 * 107.
In this formula, suppose that the density of solidification liquid is about 1.03g/ml.
Example
In the example below, poly-(poly P phenylene diamine terephthalamide) that the preceding about 6.3dL/g of logarithmic viscosity number of dissolving forms a back about 5.5dL/g (PPD-T) arrived as United States Patent (USP) 4,340 by spinning, in 559 the equipment, wherein adopts plate G.The spin duct diameter is 0.76cm (0.3 inch), adopts 0.21 and the nozzle of 0.42mm (8 and 16 mil), is that 30 ° direction is injected by injecting stream and strand angle.The preparation solvent that spinning solution adopted is about 100.1% sulfuric acid, and the concentration of polymer in spinning solution is about 19.4wt%.
As show shown in I and the II spinning head of employing 0.051 and 0.064mm (2.0 and 2.5 mil).The spinneret orifice number of used spinning head comprises 133,266,400,500,560 and 666 holes.Air-gap, promptly tow plays and just contacts the distance of being passed by till the solidification liquid from leaving the spinning head surface, is about 0.635cm (0.25 inch).Solidification liquid maintains about 3 ℃.Yarn tension is about 1.0gpd during the washing, then all samples is neutralized by the described method in back.
Example of the present invention adopts 325～1680 mass flowrate (R), and the spinning head that has the 0.051mm spinneret orifice.Yarn carries out drying under greater than the tension force of 2gpd, the line density of yarn was 160～1500 dawn.
Comparative Examples adopts same polymer and same spinning equipment, spinning under essentially identical condition, and different is that dry tension force is different with spinning head spinneret orifice size, specifically as shown in the table I.
The table I
1 2 A B C D E F 2.0 2.0 2.5 2.0 2.5 2.5 2.5 2.5 ( mil ) 266 400 133 133 266 500 560 666 ( gpd ) 3.5 3.5 0.7 0.3 2.0 2.1 2.1 2.1 ( mil ) 16 16 8 16 8 8 8 8Q1 ( gal/min ) 1.32 1.32 1.6 1.3 1.4 1.7 1.7 1.7Q2 ( gal/min ) 1.65 1.65 1.1 2.0 0.9 0.9 0.9 0.9 ( ypm ) 400 400 750 500 400 400 400 400φ ( ) 6.1 6.1 3.8 9.2 3.3 2.2 2.2 2.2R ( ) 712 475 690 1266 552 332 297 249 400 600 200 200 400 750 840 1000 ( gpd ) 28.5 28.2 23 27 27 26.5 27 26.5 ( ％ ) 3.2 3.2 3.0 3.5 3.3 3.3 3.4 3.4 ( gpd ) 830 800 750 700 760 740 760 740
In following example, quality is as top employed PPD-T, adopts and is spun into silk with top identical equipment and spinning condition, and different is, used different spinning heads, and some other condition also changes, specifically as showing as shown in the II.The table II gives the yarn property of these examples.
The table II
1 2 3 4 5 6 7 A B 2.0 2.0 2.0 2.0 2.0 2.0 2.0 2.5 2.5 ( mil ) 270 270 270 270 270 1000 1000 1000 1000 ( gpd )--3.0 to 3.5--2.3 0.8 ( mil ) 16 16 16 16 16 16 16 8 8Q1 ( gal/min ) Q2 ( gal/min ) ( ypm ) 350 350 350 350 350 350 350 350 775φ ( ) R ( ) 1075 1075 1275 1680 785 370 325 199 140 270 270 216 162 400 1000 1200 1500 1500 1.0 1.0 0.8 0.6 1.5 1.0 1.2 1.5 1.5 ( gpd ) 31.3 30.9 31.0 30.2 29.5 28.7 28.6 26.5 23.5 ( ％ ) 3.4 3.4 3.4 3.3 3.5 3.6 3.6 3.0 3.6 ( gpd ) 934 887 862 819 850 820 810 760 570
Claims (4)
1. make poly-(poly P phenylene diamine terephthalamide) method of yarn that intensity is 28gpd at least for one kind, may further comprise the steps: (a) extrude the tow that logarithmic viscosity number is 4 acid solution at least from spinning head, wherein comprise poly-(terephthalate the p-phenylenediamine (PPD))/100mL acid of 30g at least, pass the non-freezing action fluid layer of inertia then, enter into coagulating bath, then in company with the coagulation bath of the constantly overflow spin duct of flowing through together; (b) enter in 2 milliseconds of times that spin duct begins from tow, be symmetry and hand over into 0 °～85 ° angle around tow with tow, inject additional solidification liquid down, (ⅰ) mass flowrate of keeping overflow and injecting the solidification liquid summation to the ratio between the tow mass flowrate greater than 250, (ⅱ) keep the average linear velocity injected in the spin duct with overflow solidification liquid summation in the level that is lower than the tow line speed of leaving spin duct, (ⅲ) keep inject and the two flow rate of overflow solidification liquid at constant numerical value; And (c) with the tow drying,
Its improvements comprise, adopt spinning head and the tow of the highest 0.051mm of spinneret orifice diameter (2 mil) to carry out drying under the tension force of at least 3.0 gram/dawn (gpd).
2. the process of claim 1 wherein that overflow and the ratio of injecting the mass flowrate of solidification liquid summation and tow mass flowrate are greater than 300.
3. the process of claim 1 wherein that spinning head spinneret orifice diameter is 0.025mm (1 mil)～0.051mm (2 mil).
4. the process of claim 1 wherein that tow carries out drying under the tension force of 3.0gpd～7.0gpd.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US2945296P | 1996-10-25 | 1996-10-25 | |
| US60/029,452 | 1996-10-25 | ||
| US08/950,250 | 1997-10-14 | ||
| US08/950,250 US5853640A (en) | 1997-10-14 | 1997-10-14 | Process for making high tenacity aramid fibers |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1234839A true CN1234839A (en) | 1999-11-10 |
| CN1076405C CN1076405C (en) | 2001-12-19 |
Family
ID=26704957
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97199148A Expired - Fee Related CN1076405C (en) | 1996-10-25 | 1997-10-22 | Process for making high tenacity aramid fibers |
Country Status (7)
| Country | Link |
|---|---|
| EP (1) | EP0934434B1 (en) |
| JP (1) | JP3888645B2 (en) |
| KR (1) | KR100431679B1 (en) |
| CN (1) | CN1076405C (en) |
| DE (1) | DE69719351T2 (en) |
| EA (1) | EA001176B1 (en) |
| WO (1) | WO1998018984A1 (en) |
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| CN1973065B (en) * | 2004-06-25 | 2012-03-28 | 东丽株式会社 | Spinning pack for dry-wet spinning, and apparatus and method for producing fiber bundle |
| CN101983264B (en) * | 2008-03-31 | 2012-07-04 | 可隆工业株式会社 | Para-aramid fiber and method of preparing the same |
| CN101821438B (en) * | 2007-10-09 | 2013-03-27 | 纳幕尔杜邦公司 | High linear density, high modulus, high tenacity yarns and methods for making the yarns |
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| KR100930204B1 (en) * | 2008-06-27 | 2009-12-07 | 주식회사 코오롱 | Aramide fiber and method for manufacturing the same |
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| JP6105203B2 (en) | 2009-02-17 | 2017-03-29 | テイジン・アラミド・ビー．ブイ． | Process for producing filament yarns from aromatic polyamides |
| KR101192918B1 (en) | 2010-12-27 | 2012-10-18 | 코오롱인더스트리 주식회사 | Method for manufacturing Aramid fiber |
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| US4340559A (en) * | 1980-10-31 | 1982-07-20 | E. I. Du Pont De Nemours And Company | Spinning process |
| US4898704A (en) * | 1988-08-30 | 1990-02-06 | E. I. Du Pont De Nemours & Co. | Coagulating process for filaments |
| US5173236A (en) * | 1991-03-08 | 1992-12-22 | E. I. Du Pont De Nemours And Company | Method for spinning para-aramid fibers of high tenacity and high elongation at break |
| US5330698A (en) * | 1993-04-19 | 1994-07-19 | E. I. Du Pont De Nemours And Company | Process for making high elongation PPD-T fibers |
-
1997
- 1997-10-22 JP JP52057798A patent/JP3888645B2/en not_active Expired - Fee Related
- 1997-10-22 CN CN97199148A patent/CN1076405C/en not_active Expired - Fee Related
- 1997-10-22 EP EP97913738A patent/EP0934434B1/en not_active Expired - Lifetime
- 1997-10-22 WO PCT/US1997/019148 patent/WO1998018984A1/en active IP Right Grant
- 1997-10-22 KR KR19997003607A patent/KR100431679B1/en not_active IP Right Cessation
- 1997-10-22 DE DE69719351T patent/DE69719351T2/en not_active Expired - Lifetime
- 1997-10-22 EA EA199900408A patent/EA001176B1/en not_active IP Right Cessation
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1325704C (en) * | 2001-08-11 | 2007-07-11 | 莱恩真纤维有限公司 | Precipitating bath |
| CN1973065B (en) * | 2004-06-25 | 2012-03-28 | 东丽株式会社 | Spinning pack for dry-wet spinning, and apparatus and method for producing fiber bundle |
| CN101821438B (en) * | 2007-10-09 | 2013-03-27 | 纳幕尔杜邦公司 | High linear density, high modulus, high tenacity yarns and methods for making the yarns |
| CN101983264B (en) * | 2008-03-31 | 2012-07-04 | 可隆工业株式会社 | Para-aramid fiber and method of preparing the same |
| CN103328698B (en) * | 2011-01-13 | 2016-04-06 | 纳幕尔杜邦公司 | Copolymer fibre and yarn and preparation method thereof |
| CN103328698A (en) * | 2011-01-13 | 2013-09-25 | 纳幕尔杜邦公司 | Copolymer fibers and yarns and processes for making same |
| CN103498207A (en) * | 2013-10-21 | 2014-01-08 | 中蓝晨光化工研究设计院有限公司 | Solidification forming device suitable for manufacturing aramid III fibers through dry jetting and wet spinning method |
| CN103498207B (en) * | 2013-10-21 | 2016-05-18 | 中蓝晨光化工研究设计院有限公司 | A kind of solidification forming device that is applicable to dry spray-wet spinning manufacture aramid IIII fiber |
| WO2017173887A1 (en) * | 2016-04-08 | 2017-10-12 | 山东万圣博科技股份有限公司 | Device for accelerating coagulation bath process used in high-speed spinning of para-aramid fibers |
| CN108486678A (en) * | 2018-04-28 | 2018-09-04 | 义乌华鼎锦纶股份有限公司 | A kind of preparation method of graphene/polyamide 6 composite fibre |
| CN109537074A (en) * | 2018-12-28 | 2019-03-29 | 中国纺织科学研究院有限公司 | Coagulation forming device for cellulose spinning |
| CN110747524A (en) * | 2019-11-26 | 2020-02-04 | 中芳特纤股份有限公司 | Coagulating bath device for para-aramid dry-jet wet spinning and spinning method thereof |
| CN110747524B (en) * | 2019-11-26 | 2022-04-15 | 中芳特纤股份有限公司 | Coagulating bath device for para-aramid dry-jet wet spinning and spinning method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| KR100431679B1 (en) | 2004-05-17 |
| CN1076405C (en) | 2001-12-19 |
| EP0934434B1 (en) | 2003-02-26 |
| EA001176B1 (en) | 2000-10-30 |
| EA199900408A1 (en) | 1999-10-28 |
| KR20000052793A (en) | 2000-08-25 |
| DE69719351D1 (en) | 2003-04-03 |
| EP0934434A1 (en) | 1999-08-11 |
| JP3888645B2 (en) | 2007-03-07 |
| JP2002515949A (en) | 2002-05-28 |
| WO1998018984A1 (en) | 1998-05-07 |
| DE69719351T2 (en) | 2003-10-30 |
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