CN1400342A - Production method of high strength polyethylene fibre and fibre - Google Patents
Production method of high strength polyethylene fibre and fibre Download PDFInfo
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- CN1400342A CN1400342A CN 01123737 CN01123737A CN1400342A CN 1400342 A CN1400342 A CN 1400342A CN 01123737 CN01123737 CN 01123737 CN 01123737 A CN01123737 A CN 01123737A CN 1400342 A CN1400342 A CN 1400342A
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Abstract
The present invention relates to a method for producing high-strength polyethylene fibre, and is characterized by that it utilizes semi-closed temp. control zone and matched parameters of molecular weight, dope concentration, spinneret, orifice diameter, length-diameter ratio and extrusion rate, and utilizes the regulation of longitudinal extensional rheological behavirous of spinning dope or extruded spinning melt to eliminate partial macromolecualr entanglement points so as to obtain the grey yarn with suitable hypermolecular structure, then said grey yarn is undergone the process of after-stretching treatment, and the high-strength polyethylene fibre can be obtained. It is low in production cost, can meet the different titre and performance/cost ration requirements, and can produce high-strength polyethylene fibre whose lowest titre is 0.5 d and strength is 15-51 g/d.
Description
What the present invention relates to is a kind of manufacture method of high-tenacity polyethylene fibre, and specifically, what the present invention relates to is that a kind of utilization is spun the elongational flow distortion before solidifying of fiber axis in the journey and removed the method for the big molecular entanglement point of part with the manufacturing high-tenacity polyethylene fibre.
High-tenacity polyethylene fibre is the composite fibre materials with superhigh intensity and modulus that adopts ultra-high molecular weight polyethylene (molecular weight is more than 1,000,000) to manufacture, and is one of three big high performance fibre material (ultra-high molecular weight polyethylene, carbon fiber, aramid fiber) in the world at present.Because of its specific strength, specific modulus height, in the advanced lightweight composite, demonstrate great advantage, having brought into play very important effect aspect modernized war and defend equipment, aerospace and the Aero-Space, also obtained application more and more widely in civilian and industry purposes field.
1979, Holland DSM N. V. has applied for adopting the gel spinning technology to make the patent of superhigh molecular weight polyethylene fibers (NL7900990, NL7904990 and corresponding US4344908, special public clear 64-8732, US4422993), has drawn back the prelude of the research and the industrialization development of superhigh molecular weight polyethylene fibers.Its principle is to adopt the decahydronaphthalene solvent to prepare spinning solution, make flexible macromolecular chain under the dilution of solvent, remove excessive entanglement, stoste is extruded after air (dry-spinning) or water (wet spinning) cooling generation are separated through spinneret orifice, obtain having the nascent gel fiber of chain-folded lamellae and tie molecule network structure thereof, obtain having the high-tenacity polyethylene fibre of extended-chain configuration through desolventizing and super times hot-stretch, intensity reaches as high as 35g/d (3GPa).
After United States Union Signal Co. has bought the patent of Dutch DSM N. V., having developed kerosene or white oil with independent intellectual property right again voluntarily is solvent, Freon 113 (trichorotrifluoroethane) is the wet method gel spinning technology (US430577, special fair 1-16924, EP0064167, EP0205960) of extractant, and the intensity of gained fiber can reach 35g/d.Because kerosene or white oil are not volatile, this patent extraction ability excellence, the second reagent Freon 113 of high volatility extracts and replaces the first solvent kerosene or the white oil in the nascent gel fiber, make the second reagent volatile dry obtain the dry state gel fiber then, obtain having the high-tenacity polyethylene fibre of extended-chain configuration through super times hot-stretch.This process route is owing to need to reclaim a large amount of water of separation kerosene one by one---Freon 113 mixture (one ton of fiber of every production need separate tens of tons of mixtures of recovery), thereby production cost height.In addition, the U.S. will ban use of the freon that atmosphere is had destruction in 2002, so the said firm faces the problem (substituting the chlorine Leon with the carbitol analog derivative) of changing second extraction agent.
Japan Japan spins company and has bought Dutch DSM N. V. patent and reached the industrialization development cooperation agreement with DSM N. V., having developed decahydronaphthalene jointly is the dry method gel spinning industrialization technology (spy opens flat 4-209817, the spy opens flat 7-166414) of solvent, and fibre strength can reach 45g/d.Because decahydronaphthalene is easy to volatilization, can directly recycling without second reagent extraction, production cost is low.
1982-1985, domestic have how tame research unit to carry out kerosene in succession, white oil, paraffin or paraffin oil, the research and the industrialization development work of decahydronaphthalene equal solvent system superhigh molecular weight polyethylene fibers, the enterprise that existing several families go into operation has on a small scale all adopted second reagent of similar United States Union Signal Co. first reagent to be carried out the wet method gel spinning process route of extraction and displacement, wherein successful is that China Textile University is first reagent with kerosene or white oil, with gasoline is the wet method gel spinning technology (CN1056544A) of second extraction agent, the intensity of its " in too the strong PE-IV of superelevation " reaches 35g/d, filament number 4d; But because the effect of extracting of gasoline make the residual composition in the fiber wayward, and residual composition often brings adverse effect to the serviceabilities such as anti-creep of fiber not as good as freon.Exist wet method frozen glue spinning process route need separate a large amount of mix reagents of recovery in addition equally and cause the high problem of production cost.
Spinning company with Dutch DSM and Japanese Japan is that the intensity of the resulting fiber of decahydronaphthalene solvent dry method gel spinning of representative can reach 45g/d, and filament number can reach 2.1d;
With the United States Union Signal Co. is that the kerosene of representative or the intensity of the resulting fiber of white oil solvent wet method gel spinning technology can reach 35g/d, and filament number can reach 3.4d.
Since the patent of first part of superhigh molecular weight polyethylene fibers gel spinning of Dutch DSM N. V.'s application in 1979, the patent documentation of relevant this technology does not descend more than 100 piece, do not describe in detail one by one at this, only just representative and analyze with the closely-related production technology of the present invention.
Adopting paraffin or paraffin oil is solvent when carrying out the super high molecular weight polyethylene gel spinning, because that paraffin or paraffin oil are difficult to extraction is clean, residual composition makes the creep resistance variation of gained fiber, so this technology path is eliminated substantially.
United States Union Signal Co. be representative be solvent with kerosene or white oil, with second reagent is the wet method gel spinning production technology of extractant, owing to need to separate reclaim a large amount of reagent mixtures, thereby the production cost height, and gained fiber thick (filament number is minimum to be 3.4d).
(the decahydronaphthalene solvent is volatilization and recycling directly to spin the decahydronaphthalene solvent dry method gel spinning production technology that company is representative with Dutch DSM and Japanese Japan, need not consume the second a large amount of reagent extracts solvent), because the few and fiber good combination property of residual impurity, and production cost low (the spinning solution concentration that the spy opens among the flat 7-166414 can be up to 15%).But the filament number of its high-performance trade mark (as SK-75) is more than the 2d, still can not satisfy the application scenario that thinner requirement is arranged for fiber.
Main purpose of the present invention is to provide a kind of production cost low and be suitable for the industrialization steady production, and can be fit to the manufacture method of the high-tenacity polyethylene fibre that different fiber numbers require.
Another object of the present invention is to provide a kind of lowest Denier that adopts the preceding method manufacturing can reach the high-tenacity polyethylene fibre of 0.5d, intensity 15-51g/d.
Purpose of the present invention can be achieved in the following manner: in the spinning technique process of preparation superhigh molecular weight polyethylene fibers, employing is provided with the semi-enclosed temperature-controlled area of certain-length below spinnerets, and be complementary with aperture, draw ratio and the rate of extrusion of raw molecule amount, spinning solution concentration or spinning melt, spinneret orifice, by regulating the longitudinal stretching rheology after spinning solution or spinning melt are extruded, the precursor of removing the big molecular entanglement point of part and obtaining having suitable supramolecular structure, through after the road stretching obtain high-tenacity polyethylene fibre.
Below be detailed description of the present invention, by following description also in conjunction with the embodiments, can be expressly understood the present invention more.
As everyone knows, adopting super high molecular weight (1 * 10
6More than) when polyvinyl resin prepares polyethylene fiber, because the very long big molecular flexibility chain of polyethylene very easily causes chain entanglement, make the macromolecular chain of excessive entanglement be orientated the high-strength polyethylene fiber that obtains having extended-chain configuration by drawn.
The technical conceive of the disclosed gel spinning technology of prior art is: remove macromolecular chain by the technology of preparing of spinning solution and tangle, promptly the diluting effect by solvent draws back the distance between the big molecule, stoste obtains having the appropriateness frozen glue precursor of molecular entanglement point greatly after being extruded into fibre, through surpassing the high-tenacity polyethylene fibre that times hot-stretch and macromolecular orientation obtain having extended-chain configuration.
In the present invention, described " the big molecular entanglement point of appropriateness " is meant that should there be an amount of big molecular entanglement point in resulting precursor, this be because, just can't transmit tensile stress when point is very few if tangle in the precursor, thereby big molecular folding chain can not obtain stretching and orientation is stretched by the tie molecule between chain-folded lamellae; And the development that can limit macromolecular orientation and extended-chain configuration when too much is put in the entanglement in the precursor.
In general,, can obtain " the big molecular entanglement point of appropriateness " by regulating different original liquid concentrations corresponding to different molecular weight, higher molecular weight is corresponding to lower original liquid concentration; Lower molecular weight is corresponding to higher original liquid concentration.
But, in the preparation process of fiber, must consider the pressure before the spinnerets of spinning solution when spinneret orifice is extruded, if hypotony before the spinnerets, the horizontal plucked of the fiber that can cause different spinneret orifices to extrude, or same spinneret orifice extrudes vertical plucked of fiber, so must make spinning solution have the necessary enough former fluid viscosity of pressure before the spinnerets of setting up.
In the prior art, adopt " the big molecular entanglement point of appropriateness " pairing spinning solution viscosity of adjusting original liquid concentration realization precursor often well below setting up " the preceding pressure of enough spinneretss " required spinning solution viscosity, spinning Cheng Zhangli in addition also has certain requirement and restriction for the concentration and the viscosity of spinning solution, and above-mentioned various factors must be considered in comprehensive balance.
Major technique of the present invention is contemplated that: utilize and spin the elongational flow distortion releasing part big molecular entanglement point of fiber axis before solidifying in the journey, the big molecular entanglement point of part is removed in longitudinal stretching rheology after promptly extruding by spinning solution or melt, thereby had " appropriateness big molecular entanglement point " extend simultaneously and refinement the shish-kebab structure precursor, and then obtain the high-strength polyethylene fiber of different fiber numbers requirements through the stretching of road, back.
Researcher of the present invention adopts described scheme to solve only to rely on the stoste technology of preparing to remove the defective of big molecular entanglement in the prior art, solve " the big molecular entanglement point of appropriateness " pairing spinning solution low viscosity and " pressure before enough spinneretss " or " spinning Cheng Zhangli " pairing spinning solution high viscosity problem of contradiction each other simultaneously, when obtaining high fibre strength, be met the fiber that different fiber numbers require.
" the semi-enclosed temperature-controlled area of spinnerets below " of the present invention is meant and is positioned at the spinnerets below, outer likeness in form " lower ending opening chimney " or " upper and lower end opening chimney " shape, length is at 10-40cm, the upper end is for advancing the silk mouth, the lower end is a filament mouth, and (circular or other shape) is the temperature-controlled area territory of heating and temperature controlling device on every side.
In fact, the setting that improves spinning solution or spinning melt rheological property in the semi-enclosed temperature-controlled area below spinnerets of the present invention is not rarely seen for the synthetic fiber spinning equipment, even also existing report for the spinning of ultra-high molecular weight polyethylene, as US5068073 (1977) and Polymer Bulletin 23, all having reported among the 353-359 (1990) and adopted this kind " heat pipe " or " hot stove (hot jacket) ", is content and the process that solvent carries out the ultra-high molecular weight polyethylene high speed spinning with kerosene.
But, above-mentioned technology is not introduced " spin journey and remove the big molecular entanglement point of part " this notion, or because of spinning solution concentration low excessively (1.5%), big molecular entanglement point is excessively reduced with the raising of longitudinal stretching rheology, thereby fibre strength decreases (even fiber plucked longitudinally also can appear in the single hole spinning under this low concentration, be difficult to obtain first break draft performance uniformity precursor, thereby the industrialization of being unrealized so far); Or, influenced macromolecular " spin journey separate twine " effect because of rate of extrusion too high (5-150 rice/minute), make the gained precursor lose the first break draft performance and can not get high-intensity fiber.
Researcher of the present invention finds, though having mentioned, prior art utilize the semi-enclosed temperature-controlled area of spinnerets below to improve spinning solution or spinning melt rheological property, but, only mate mutually when proper, just can reach the effect of big molecule " spin journey separate twine " according to the parameters that makes of the present invention.
Aperture, draw ratio and the rate of extrusion of the spinnerets semi-enclosed temperature-controlled area in below of the present invention and raw molecule amount, spinning solution concentration or spinning melt, spinneret orifice are complementary, and the temperature that is meant the semi-enclosed temperature-controlled area in spinnerets below is at 120-320 ℃; Raw molecule amount 1 * 10
6-6 * 10
6Spinning solution concentration 4-15% or spinning melt; The aperture 0.6-1.0 millimeter of spinneret orifice; Draw ratio 6/1-30/1; Rate of extrusion 0.5-5 rice/minute.
When adopting decahydronaphthalene to be solvent dry method gel spinning, the temperature of the semi-enclosed temperature-controlled area in spinnerets below is controlled to be 120-180 ℃; When adopting 1 * 10
6Be controlled to be 250-320 ℃ during the molecular weight melt spinning.
When adopting lower molecular weight (1 * 10
6-3.5 * 10
6) polyethylene, during decahydronaphthalene solvent dry method gel spinning, spinning solution concentration is controlled to be 7-15%; When adopting higher molecular weight (3.5 * 10
6-6 * 10
6) polyethylene, during decahydronaphthalene solvent dry method gel spinning, spinning solution concentration is controlled to be 4-7%.When the aperture of adopting spinneret orifice was 0.6 millimeter, draw ratio was 6/1; When 1.0 millimeters in the aperture of adopting spinneret orifice, draw ratio 30/1.
When adopting higher molecular weight polyethylene dry method gel spinning, should adopt bigger spinneret orifice diameter and lower rate of extrusion; When adopting lower molecular weight polyethylene dry method gel spinning, should adopt less spinneret orifice diameter and higher rate of extrusion.
Of the present invention by regulating the longitudinal stretching rheology after spinning solution or spinning melt are extruded, the precursor of removing the big molecular entanglement point of part and obtaining having suitable supramolecular structure is meant molecular weight, spinning solution concentration or the spinning melt corresponding to material polyethylene, aperture, draw ratio and the rate of extrusion of spinneret orifice, and the longitudinal stretching rheology has an optimum value.
Higher when the molecular weight of material polyethylene, spinning solution concentration is higher, aperture spinneret orifice is less, this optimum value was on the low side when rate of extrusion was higher; Lower when the molecular weight of material polyethylene, spinning solution concentration is lower, the aperture of spinneret orifice is big, this optimum value was higher when rate of extrusion was low.
Longitudinal stretching rheology degree described in the present invention all can not be had the precursor structure of " the big molecular entanglement point of appropriateness " when being too high or too low, need be determined by experiment, generally is controlled at V/V
0=5-100 scope (V
0Be the spinneret orifice rate of extrusion, V is for spinning the journey pulling speed).
Below be embodiments of the invention, the embodiment that the present invention provides is in order to further specify the specific embodiments of the invention scheme, rather than is used for limiting protection scope of the present invention, and protection scope of the present invention can be seen claim; Any variation of being done in the present invention's design all should be among scope of the present invention.
Embodiment 1
In the present embodiment, with polyvinyl resin with super-high molecular weight powder (M
W=3.5 * 10
6) 77 gram and decahydronaphthalene (technical grades, B.P185-195 ℃) 923 grams, antioxidant, lubricant is placed in the stainless steel cauldron earlier, the antioxidant that is used for the present invention, lubricant is that prior art often adopts, do not give unnecessary details one by one at this, open then and stir, heating, be warming up to 97 ℃ of swellings 1 hour, be warming up to 160 ℃ of fully dissolvings then, and under this temperature, be incubated 1 hour, carry out vacuum defoamation thereafter, taken off the feed liquid of bubble and extruded with 1.5 meters/minute speed from spinneret orifice (1 millimeter in aperture, draw ratio 30/1) through measuring pump, hot jacket (155 ℃ of the hot jacket inside center regional temperatures) back that through a length is 30 centimetres is with 52.5 meters/minute hauling speed derivation.
The gained gel fiber is through 11.2 times of drawing-offs in hot path (105-135 ℃) behind the decahydronaphthalene volatile dry.The fiber number 0.5d of gained fiber, fracture strength 51g/d, modulus 1530g/d, extension at break 3.1%.
Embodiment 2
With polyvinyl resin with super-high molecular weight powder (M
W=5 * 10
6) 56 gram and decahydronaphthalene (technical grades, B.P185-195 ℃) 944 grams, antioxidant, lubricant are placed in the stainless steel cauldron earlier, open and stir, heat, be warming up to 100 ℃ of swellings 1 hour, be warming up to 165 ℃ of fully dissolvings then, and under this temperature, be incubated 1 hour, carry out vacuum defoamation thereafter, taken off the bubble feed liquid through measuring pump from spinneret orifice (1 millimeter in aperture, draw ratio 30/1) extruding with 1.35 meters/minute speed, is that the hauling speed with 19 meters/minute derives behind 30 centimetres the hot jacket (160 ℃ of hot jacket inside center regional temperatures) through a length.
The gained gel fiber is through 13.5 times of drawing-offs in hot path (105-135 ℃) behind the decahydronaphthalene volatile dry.The fiber number 1.6d of gained fiber, fracture strength 46g/d, modulus 1450g/d, extension at break 3.4%.
Embodiment 3
With polyvinyl resin with super-high molecular weight powder (M
W=5 * 10
6) 65 gram and decahydronaphthalene (technical grades, B.P185-195 ℃) 935 grams, antioxidant, lubricant is placed in the stainless steel cauldron earlier, open and stir, heating, be warming up to 100 ℃ of swellings 1 hour, be warming up to 165 ℃ of fully dissolvings then, and under this temperature, be incubated 1 hour, carry out vacuum defoamation thereafter, taken off the bubble feed liquid through measuring pump from spinneret orifice (1 millimeter in aperture, draw ratio 30/1) extrudes with 1 meter/minute speed, through a length is that derive with 5 meters/minute hauling speed 30 centimetres hot jacket (135 ℃ of hot jacket inside center regional temperatures advance silk mouth and are positioned at 10 centimetres of spinnerets belows) back.
The gained gel fiber is through 17.2 times of drawing-offs in hot path (105-135 ℃) behind the decahydronaphthalene volatile dry.The fiber number 4.2d of gained fiber, fracture strength 41g/d, modulus 1292g/d, extension at break 3.8%.
Embodiment 4
With polyvinyl resin with super-high molecular weight powder (M
W=5 * 10
6) melt extrude screw tip pressure 8MPa, 295 ℃ of temperature through charging hopper feeding single screw extrusion machine.
Melt extrusion is extruded with 1 meter/minute speed from spinneret orifice (0.6 millimeter in aperture, draw ratio 6/1) through measuring pump, and through a length being derives with 100 meters/minute hauling speed behind 30 centimetres the hot jacket (290 ℃ of hot jacket inside center regional temperatures) and reel.7.2 times of the drawing-offs in hot path (125-145 ℃) of gained precursor.The fiber number 1.9d of gained fiber, fracture strength 15g/d, modulus 407g/d, extension at break 7%.
Embodiment 5
Other are identical with embodiment 4, and the speed of different is 1.2 meters/minute of melts is extruded, and derive and reel with 115 meters/minute hauling speed, 7.4 times of the drawing-offs in hot path (125-135 ℃) of gained precursor.The fiber number 1.85d of gained fiber, fracture strength 16g/d, extension at break 6.5%.
Embodiment 6
Other is identical with embodiment 4, and different is 1 millimeter of spinneret orifice diameter, draw ratio 30/1,8.3 times of the drawing-offs in hot path (125-145 ℃) of gained precursor, the fiber number 4.9d of gained fiber, fracture strength 15.2g/d, modulus 402g/d, extension at break 7.4%.
Adopt parameter matching of the present invention, and utilize described draft flowing deformation, removed the mode of the big molecular entanglement point of part, overcome existing method and mainly removed the technological deficiency that big molecular entanglement brings by the stoste preparation process, a kind of cost is low, suitability for industrialized production stable thereby provide, can satisfy different fiber number requirements, the high-tenacity polyethylene fibre of intensity 15-51g/d.
Claims (13)
1, a kind of manufacture method of high-tenacity polyethylene fibre, be included in the spinning technique process of preparation superhigh molecular weight polyethylene fibers, one semi-enclosed temperature-controlled area is set below spinnerets, and aperture, draw ratio and the rate of extrusion of raw molecule amount, spinning solution concentration or spinning melt, spinneret orifice are complementary, it is characterized in that by regulating the longitudinal stretching rheology after spinning solution or spinning melt are extruded, so that the big molecular entanglement point of part is removed, obtain having the precursor of suitable supramolecular structure, through after the road stretch and to obtain high-tenacity polyethylene fibre.
2, method according to claim 1 is characterized in that the length of the semi-enclosed temperature-controlled area of described spinnerets below is 10-40cm, and its upper end is for advancing the silk mouth, and the lower end is a filament mouth, is heating and temperature controlling device on every side.
3, method according to claim 2, the profile that it is characterized in that described semi-enclosed temperature-controlled area is " lower ending opening chimney " or " the upper and lower end opening chimney " shape that adapts with the spinning head profile.
4, method according to claim 1, the temperature that it is characterized in that described semi-enclosed temperature-controlled area is at 120-320 ℃; Raw molecule amount 1 * 10
6-6 * 10
6Spinning solution concentration 4-15%, or spinning melt; The aperture 0.6-1.0 millimeter of spinneret orifice; Draw ratio 6/1-30/1; Rate of extrusion 0.5-5 rice/minute.
5, according to claim 1 or 4 described methods, it is characterized in that when adopting decahydronaphthalene be solvent when carrying out the dry method gel spinning, the temperature of the semi-enclosed temperature-controlled area in spinnerets below is controlled to be 120-180 ℃; Poly molecular weight preferred 1 * 10
6-3.5 * 10
6, spinning solution concentration is controlled to be 7-15%.
6, according to claim 1 or 4 described methods, it is characterized in that when adopting decahydronaphthalene be solvent when carrying out the dry method gel spinning, the temperature of the semi-enclosed temperature-controlled area in spinnerets below is controlled to be 120-180 ℃; Poly molecular weight preferred 3.5 * 10
6-6 * 10
6, spinning solution concentration is controlled to be 4-7%.
7, method according to claim 1 is characterized in that should adopting bigger spinneret orifice diameter and lower rate of extrusion when adopting higher molecular weight polyethylene dry method gel spinning; When adopting lower molecular weight polyethylene dry method gel spinning, should adopt less spinneret orifice diameter and higher rate of extrusion.
8, according to claim 1 or 4 described methods, it is characterized in that molecular weight 3.5 * 10 with 5.6-7.7%
6-5 * 10
6Polyethylene resin powder and 92.3-94.4% decahydronaphthalene in stainless steel cauldron, be configured to mixed liquor, add an amount of antioxidant, lubricant, open then and stir, heating, be warming up to 97-100 ℃ of swelling 1 hour, be warming up to 160-165 ℃ of fully dissolving again, and under this temperature, be incubated 1 hour, carry out vacuum defoamation thereafter, taken off the bubble feed liquid through measuring pump from spinneret orifice (1 millimeter in aperture, draw ratio 30/1) with 1.0-1.5 rice/minute speed extrude, through a length be behind 30 centimetres the hot jacket (135-160 ℃ of hot jacket inside center regional temperature) with 5-52.5 rice/minute hauling speed derive.
The gained gel fiber through behind the decahydronaphthalene volatile dry in hot path (105-135 ℃) drawing-off 11.2-17.2 doubly, the fiber number 0.5-4.2d of gained fiber, fracture strength 41-51g/d, modulus 1292-1530g/d, extension at break 3.1-3.8%.
9,, it is characterized in that when adopting 1 * 10 according to claim 1 or 4 described methods
6When molecular weight carried out melt spinning, the temperature of semi-enclosed temperature-controlled area was controlled to be 250-320 ℃.
10, according to any one described method of claim 1 or 4 or 9, it is characterized in that polyvinyl resin with super-high molecular weight powder (M
W=1 * 10
6) melt extrude screw tip pressure 8MPa, 295 ℃ of temperature through charging hopper feeding single screw extrusion machine;
Melt extrusion through measuring pump from spinneret orifice (aperture 0.6-1.0 millimeter, draw ratio 6/1-30/1) extrudes with 1 meter/minute speed, through a length be behind 30 centimetres the hot jacket (290 ℃ of hot jacket inside center regional temperatures) with 100-115 rice/minute hauling speed derive and reel, the gained precursor in hot path (125-145 ℃) drawing-off 7.2-8.3 doubly, the fiber number 1.85-4.9d of gained fiber, fracture strength 15-16g/d, modulus 407g/d, extension at break 6.5-7.4%.
11,, it is characterized in that described longitudinal stretching rheology extent control is at V/V according to claim 1 or 4 described methods
0Between=the 5-100.
12, a kind of high-tenacity polyethylene fibre that adopts the described method of claim 1 to make, the fiber number of described fiber is 0.5-4.9d, intensity 15-51g/d.
13, fiber according to claim 12 is characterized in that fiber number 0.5-4.2d, fracture strength 41-51g/d, modulus 1292-1530g/d, the extension at break 3.1-3.8% of described fiber.
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2001
- 2001-07-30 CN CN 01123737 patent/CN1221690C/en not_active Expired - Lifetime
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