CN115807273A - High-uniformity ultra-high molecular weight polyethylene fiber and preparation method thereof - Google Patents
High-uniformity ultra-high molecular weight polyethylene fiber and preparation method thereof Download PDFInfo
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- 239000004699 Ultra-high molecular weight polyethylene Substances 0.000 title claims abstract description 58
- 229920000785 ultra high molecular weight polyethylene Polymers 0.000 title claims abstract description 58
- 239000000835 fiber Substances 0.000 title claims abstract description 50
- 238000002360 preparation method Methods 0.000 title claims abstract description 10
- 238000000034 method Methods 0.000 claims abstract description 34
- 238000009987 spinning Methods 0.000 claims abstract description 23
- 239000011347 resin Substances 0.000 claims abstract description 19
- 229920005989 resin Polymers 0.000 claims abstract description 19
- 239000000843 powder Substances 0.000 claims abstract description 18
- 230000008961 swelling Effects 0.000 claims abstract description 17
- 239000002904 solvent Substances 0.000 claims abstract description 16
- 239000007863 gel particle Substances 0.000 claims abstract description 13
- 239000012752 auxiliary agent Substances 0.000 claims abstract description 9
- 238000002156 mixing Methods 0.000 claims abstract description 6
- 238000000465 moulding Methods 0.000 claims abstract description 5
- 238000000265 homogenisation Methods 0.000 claims description 13
- 230000008569 process Effects 0.000 claims description 12
- 230000003068 static effect Effects 0.000 claims description 9
- 230000006835 compression Effects 0.000 claims description 8
- 238000007906 compression Methods 0.000 claims description 8
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- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000000155 melt Substances 0.000 claims description 5
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 4
- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 claims description 4
- NNBZCPXTIHJBJL-UHFFFAOYSA-N decalin Chemical compound C1CCCC2CCCCC21 NNBZCPXTIHJBJL-UHFFFAOYSA-N 0.000 claims description 4
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 claims description 4
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 4
- BKIMMITUMNQMOS-UHFFFAOYSA-N nonane Chemical compound CCCCCCCCC BKIMMITUMNQMOS-UHFFFAOYSA-N 0.000 claims description 4
- CXWXQJXEFPUFDZ-UHFFFAOYSA-N tetralin Chemical compound C1=CC=C2CCCCC2=C1 CXWXQJXEFPUFDZ-UHFFFAOYSA-N 0.000 claims description 4
- RSJKGSCJYJTIGS-UHFFFAOYSA-N undecane Chemical compound CCCCCCCCCCC RSJKGSCJYJTIGS-UHFFFAOYSA-N 0.000 claims description 4
- 239000003963 antioxidant agent Substances 0.000 claims description 3
- 230000003078 antioxidant effect Effects 0.000 claims description 3
- 239000002480 mineral oil Substances 0.000 claims description 3
- 235000010446 mineral oil Nutrition 0.000 claims description 3
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 2
- 239000004698 Polyethylene Substances 0.000 claims description 2
- 239000003086 colorant Substances 0.000 claims description 2
- 150000008282 halocarbons Chemical class 0.000 claims description 2
- 239000003208 petroleum Substances 0.000 claims description 2
- -1 polyethylene Polymers 0.000 claims description 2
- 229920000573 polyethylene Polymers 0.000 claims description 2
- PXXNTAGJWPJAGM-UHFFFAOYSA-N vertaline Natural products C1C2C=3C=C(OC)C(OC)=CC=3OC(C=C3)=CC=C3CCC(=O)OC1CC1N2CCCC1 PXXNTAGJWPJAGM-UHFFFAOYSA-N 0.000 claims description 2
- 239000008096 xylene Substances 0.000 claims description 2
- 239000003017 thermal stabilizer Substances 0.000 claims 1
- 229920002521 macromolecule Polymers 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 51
- 238000009826 distribution Methods 0.000 description 8
- 230000000052 comparative effect Effects 0.000 description 5
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- RFFLAFLAYFXFSW-UHFFFAOYSA-N 1,2-dichlorobenzene Chemical compound ClC1=CC=CC=C1Cl RFFLAFLAYFXFSW-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
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- 238000011161 development Methods 0.000 description 2
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- 238000005227 gel permeation chromatography Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000035772 mutation Effects 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000012805 post-processing Methods 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- 239000004793 Polystyrene Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000011088 calibration curve Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010036 direct spinning Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012760 heat stabilizer Substances 0.000 description 1
- 229920006253 high performance fiber Polymers 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 238000000053 physical method Methods 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
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Classifications
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- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
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Abstract
The invention relates to a high-uniformity ultra-high molecular weight polyethylene fiber and a preparation method thereof, wherein the method comprises the steps of fully mixing ultra-high molecular weight polyethylene resin powder, a solvent and an auxiliary agent, swelling and then dissolving in a screw to obtain an ultra-high molecular weight polyethylene solution; homogenizing the obtained ultrahigh molecular weight polyethylene solution for preset time, and then feeding the solution into a spinning manifold; and extruding and molding to obtain gel strands, and then removing the solvent and performing hot stretching to obtain the ultra-high molecular weight polyethylene fiber. Compared with the prior art, the method has the advantages that the formed solution is homogenized, so that the orientation of macromolecules in the solution is improved, the performance of a finished product is improved, the size of gel particles is reduced, or the number of the gel particles is reduced, the uniformity of the solution is improved, and finally obtained fibers are good in mechanical property, low in variation rate and good in thermal stability.
Description
Technical Field
The invention relates to the technical field of preparation of ultra-high molecular weight polyethylene fibers, in particular to a high-uniformity ultra-high molecular weight polyethylene fiber and a preparation method thereof.
Background
With the development of the fiber synthesis and spinning process of the world high and new technology, the ultra-high molecular weight polyethylene fiber is continuously innovated and enters a high-speed development stage at present. Users place further demands on fiber properties, whether for civilian or military use. Therefore, many manufacturers adopt a method for improving the molecular weight of raw materials to obtain high-performance fibers, but the spinning difficulty is increased, and the uniformity of the solution is difficult to ensure.
The invention patent CN109306061A provides a preparation method of a spinning solution, which comprises the steps of firstly pre-swelling an ultra-high molecular weight polyethylene material by adopting a physical method, and then mixing a swelling solution and a solvent for thermal dissolution treatment, so as to obtain a uniform spinning solution. The method improves the uniformity of the spinning solution by increasing the swelling efficiency, but the implementation process is complicated and difficult to control.
The invention patent CN111118615A also provides a method for processing the spinning solution of the ultra-high molecular weight polyethylene fiber, which comprises the steps of pressurizing the spinning solution under the protection of nitrogen, and enabling the spinning solution to enter a double-screw extruder after the spinning solution is subjected to high temperature and high pressure and single-screw homogenization, thereby improving the uniformity of finished fibers. The method has large equipment investment and brings potential safety hazards to production at high temperature and high pressure.
Patent CN106801260A refers to a spinning pack for preparing ultra-high molecular weight polyethylene fibers, which improves the uniformity of the solution and the uniformity of the components by the installation mode, form, internal structure characteristics, etc. of the pack.
As described above, the treatment of the spinning dope and the improvement of the equipment are both aimed at improving the uniformity of the solution and obtaining a fiber product with stable performance. However, the common control method is that before the solution is formed, the solution is dissolved and then is rarely subjected to technical treatment, and the solution is generally formed by direct spinning. The method obviously shows the dependence of solution stability on the stock solution, and the finished product has poor processing performance and unstable product size or weight.
Disclosure of Invention
The invention aims to solve the problems and provide the high-uniformity ultrahigh molecular weight polyethylene fiber and the preparation method thereof, so that the orientation of macromolecules in a solution is improved, the performance of a finished product is improved, the size of gel particles is reduced, or the number of the gel particles is reduced, the uniformity of the solution is improved, and the finally obtained fiber has good mechanical property, low variation rate and good thermal stability.
The purpose of the invention is realized by the following technical scheme:
the invention provides a preparation method of high-uniformity ultra-high molecular weight polyethylene fibers, which comprises the following steps:
s1: fully mixing ultrahigh molecular weight polyethylene resin powder, a solvent and an auxiliary agent, wherein the mass ratio of the ultrahigh molecular weight polyethylene resin powder to the solvent is 1-20 to 1, and the mass ratio of the ultrahigh molecular weight polyethylene resin powder to the auxiliary agent is 1000;
s2: homogenizing the ultra-high molecular weight polyethylene solution obtained in the step S1 for preset time, and then feeding the solution into a spinning manifold;
s3: and (3) extruding and molding the solution obtained in the step (S2) through a spinning manifold to obtain gel strands, and then removing the solvent and performing hot stretching to obtain the ultra-high molecular weight polyethylene fibers.
Further, in S1, the screws are co-rotating twin screws, and the conveying section threads at the screw outlets are subjected to volume compression at least twice, so that the output pressure of the ultra-high molecular weight polyethylene solution is not less than 5MPa.
More preferably, the output pressure is 6MPa or more. Because the swelling solution of the ultra-high molecular weight polyethylene prepared by the method has low viscosity and weak conveying propelling force, the viscosity can be obviously increased only after the dissolution. Therefore, the closer to the screw outlet, the higher the solution viscosity and the more effective the volume compression, to ensure the delivery pressure. If the output pressure is too low, the pressure drop is large after long-time homogenization treatment, which results in insufficient spinning pressure and low quality of the gel precursor.
Further, in S1, the swelling mode is kettle-type swelling, and the swelling temperature is 110 +/-5 ℃.
The kettle type swelling is a process that the ultrahigh molecular weight polyethylene is fully mixed with the solvent in a constant temperature kettle with a jacket by dispersion means such as stirring, and the solvent is absorbed until the volume is expanded.
Further, the swelling temperature of the ultra-high molecular weight polyethylene resin varies depending on the molecular weight, molecular structure, etc., but is also at least more than 120 ℃. If the swelling point is reached, the viscosity of the solution increases, which causes difficulty and unevenness in blanking.
Further, in S1, the viscosity average molecular weight of the ultra-high molecular weight polyethylene resin powder is 400 to 1000 ten thousand,
3-7, and the proportion of the ultra-high molecular weight polyethylene resin powder particles with the particle size of 120-220 mu m is more than or equal to 70 percent.
Further, in S1, the solvent is selected from one or more of halogenated hydrocarbon, mineral oil, decalin, tetrahydronaphthalene, naphthalene, xylene, toluene, dodecane, undecane, decane, nonane, octene, chlorobenzene, petroleum ether, low molecular weight polyethylene wax.
Further, in S1, the auxiliary agent is selected from one or more of an antioxidant, a flow promoter, a heat stabilizer, a colorant, and a functional powder.
Further, in S2, the homogenization treatment is completed in the melt pipeline, and the homogenization time is not less than 10min. The time is too short, the thermal action time is not enough, the gel particles are difficult to be further unwound, and otherwise, the macromolecule is easy to degrade at high temperature.
Further, in S2, the homogenization treatment process is a constant temperature process, and the temperature of the melt pipe is 3-5 ℃ lower than the temperature of the solution in the pipe. Although the dissolution of the high polymer is an endothermic reaction, the high polymer melt is sheared to generate heat because a large number of meshing blocks are designed in the screw, and the actual solution temperature is slightly higher than the set temperature.
Further, in S2, the homogenization treatment process employs one or more sets of static mixers in series, so as to eliminate the difference caused by the flow shear of the solution, and simultaneously, the residence time of the solution in the pipeline is prolonged by the static mixers, so that the size of the gel particles which are not completely dissolved is reduced or the number of the gel particles is reduced under the heating condition.
Furthermore, the static mixer selects SK type, and the length of single group is more than or equal to 500mm. For high viscosity fluids, the pressure drop is small and mixing is adequate.
The invention provides the ultrahigh molecular weight polyethylene fiber prepared by the method, wherein the dry heat shrinkage rate of the ultrahigh molecular weight polyethylene fiber is less than or equal to 2% at 100 ℃ and less than or equal to 3% at 120 ℃. The dry heat shrinkage rate is an index of the thermal stability of the reaction fiber, the size of the index has important influence on the post-processing stability of the fiber, the fluctuation reflects the change of internal stress in the production process, and the uniformity and the stability of the performance are reflected to a certain extent.
The core innovation points of the invention are as follows:
the invention selects the ultra-high molecular weight polyethylene solution to pass through a constant temperature melt pipeline, and then the gel silk is spun after homogenization treatment for a certain time. On one hand, the ultra-high molecular weight polyethylene solution is in a stretching flow field in a pipeline because of the pushing of the pressure of the screw, the stretching flow changes to enable the macromolecule to be more easily oriented, the molecular arrangement also tends to be regular, and the performance is favorably improved. But at the same time, the intermolecular force is also increased, the extensional viscosity is also increased, and the flow shear of the solution in the pipeline and the wall of the pipeline has obvious inconsistency at the moment.
Therefore, the invention adopts one or more groups of static mixers to be combined to eliminate the difference of the solution caused by flow shearing, thereby achieving the purposes of good dispersion and full mixing between the fluids. On the other hand, the static mixer also prolongs the retention time of the solution in the pipeline, so that the size of a part of gel particles which are not completely dissolved can be reduced or the number of the gel particles can be reduced under the heating condition, thereby being more beneficial to improving the performance of the finished fiber.
Compared with the prior art, the invention has the following technical advantages:
1) According to the technical scheme, the obtained ultra-high molecular weight polyethylene solution is homogenized and then spun into the gel silk, so that the fiber performance is improved, and the variation rate of the fiber is reduced.
2) The technical scheme reduces the sensitivity of finished fiber to raw materials, so that the process has wide application range and wider raw material sources.
3) The technical scheme prolongs the homogenization time of the solution, not only does not influence the yield, but also improves the stability of the finished product.
4) The technical scheme has the advantages of small equipment investment, simple process, convenient operation and easy control.
Detailed Description
The method comprises the steps of improving the output pressure through the optimized design of the screw, and reducing or reducing the size or the number of gel particles through solution homogenization treatment, so that a uniform spinning solution is prepared, and the high uniformity and the high stability of finished fibers are ensured. The invention improves the output pressure of the screw and prolongs the homogenization time of the spinning solution so as to achieve the purpose of reducing or reducing the size or the number of gel particles. The fiber prepared by the process has higher breaking strength, smaller mutation rate and better thermal stability.
The present invention will be described in detail by way of examples, which should not be construed as limiting the invention thereto. The characteristic values of the ultrahigh-molecular-weight polyethylene fibers obtained in the present invention were measured and evaluated as follows.
(1) Weight average molecular weight Mw, number average molecular weight Mn and Mw/Mn of raw resin
The weight average molecular weight Mw, the number average molecular weight Mn and Mw/Mn are determined by Gel Permeation Chromatography (GPC). The measurement solvent used was o-dichlorobenzene, and the column temperature was set to 145 ℃. The sample concentration was set to 1.0mg/ml, and 200. Mu.l was injected for measurement. The calibration curve of the molecular weight was prepared by a universal calibration method using a polystyrene sample having a known molecular weight.
(2) Fiber denier, breaking Strength, elongation at Break, and modulus testing
The fineness of the fiber is measured according to GB/T14343-2008 chemical fiber filament linear density test method, and the breaking strength, the breaking elongation and the modulus of the fiber are measured according to GB/T19975-2005 high-strength fiber filament tensile property test method.
(3) Determination of broken bobbin rate and broken filament rate
Calculating according to 8 hours per shift, repeatedly breaking the bobbin or accumulating and superposing the broken filaments, cutting the broken filaments when the filaments are long or continuously appear, knotting after the filaments are tidy, counting the bobbin breaking times, and calculating according to the following formula:
tube breakage = number of fiber breaks/total number of fiber bundles involved in hot drawing × 100%
Broken filament rate = number of times broken filament appears/total number of fiber bundles involved in hot drawing × 100%
(4) Measurement of Dry Heat shrinkage
Measured with a thermal contraction measuring instrument. Firstly, taking a plurality of fiber samples, carrying out humidity adjustment treatment according to GB/T6529, then placing the fiber samples into an instrument for testing, selecting the heat treatment temperature to be 100 ℃/120 ℃ for heating for 30 minutes, then carrying out balance treatment again, and then calculating the dry heat shrinkage rate of the fiber.
The present invention will be described in detail with reference to specific examples. In the technical scheme, characteristics such as preparation means, materials, structures or composition ratios and the like which are not explicitly described are all regarded as common technical characteristics disclosed in the prior art.
It should be noted that in the technical scheme, the mass ratio of the ultrahigh molecular weight polyethylene resin powder to the solvent is 1 to 20-1, the mass ratio of the ultrahigh molecular weight polyethylene resin powder to the auxiliary agent is 1000 to 1000, and the ultrahigh molecular weight polyethylene resin powder and the auxiliary agent enter the screw to be dissolved after swelling, and the above parameters are non-innovative points and adopt numerical values in the above range.
Example 1
The molecular weight is 600 ten thousand, the molecular weight distribution
5.5, and 70 percent of ultrahigh molecular weight polyethylene resin powder with the particle size distribution range of 120-220 mu m, and the ultrahigh molecular weight polyethylene resin powder and an antioxidant are uniformly mixed according to the weight ratio of 1000. And (3) performing volume compression twice on a material conveying section of the screw close to the machine head by adopting an equal-depth unequal-distance principle to obtain the ultra-high molecular weight polyethylene solution, wherein the output pressure of the screw is 6.3MPa. The solution sequentially passes through a constant temperature melt pipe with two groups of static mixers connected in series, the temperature is 5 ℃ lower than the solution temperature (the solution temperature changes along with the change of parameters such as resin types, solvent viscosity, solid content and the like), and the solution enters a spinning box after being homogenized for 10minAnd (3) a body. And then extruding and molding by a metering pump and a component to obtain gel filaments, and then carrying out desolventizing, hot stretching and other steps to obtain the ultra-high molecular weight polyethylene fiber.
Example 2
The difference from example 1 is that: after homogenization treatment for 15min, the mixture enters a spinning beam.
Example 3
The difference from example 1 is that: and performing primary volume compression on a material conveying section of the screw close to the machine head to obtain the ultra-high molecular weight polyethylene solution, wherein the output pressure of the screw is 5.5MPa.
Example 4
The difference from example 1 is that: the solution delivered from the screw was passed through only one set of thermostatic melt channels of the static mixer.
Example 5
The difference from example 1 is that: the modified molecular weight is 400 ten thousand, the molecular weight distribution
3.1, and 84 percent of ultrahigh molecular weight polyethylene resin powder with the particle size distribution range of 120-220 mu m.
Example 6
The difference from example 1 is that: the modified molecular weight is 400 ten thousand, the molecular weight distribution
7.0, and the proportion of the particle size distribution range of 120-220 mu m is 70 percent. The homogenization treatment time was increased to 15min, and the mixture was fed into a spinning beam.
Comparative example 1
The molecular weight is 600 ten thousand, the molecular weight distribution
5.5, and 70 percent of ultra-high molecular weight polyethylene resin powder with the grain size distribution range of 120-220 mu m, is evenly mixed with a proper amount of auxiliary agent, then is injected with mineral oil with the constant temperature of 110 ℃ for swelling, and then is dissolved by a double screw. Normal screw conveyingAnd (4) feeding the solution without a volume compression section to obtain the ultra-high molecular weight polyethylene solution, wherein the output pressure of the screw is 4.6MPa. The solution passes through a constant temperature melt pipeline, the set temperature is 5 ℃ lower than the solution temperature, the total time in the melt pipeline is 4min, and then the solution enters a spinning manifold. And then extruding and molding by a metering pump and a component, and then removing the solvent from the prepared gel strand silk, thermally stretching and the like to obtain the ultra-high molecular weight polyethylene fiber.
Comparative example 2
The difference from comparative example 1 is that: the material conveying section at the screw head adopts one-time volume compression to obtain the ultra-high molecular weight polyethylene solution, and the output pressure is 5.6MPa.
Comparative examples 1 and 2 use one volume compression to ensure the delivery pressure, but neither does the residence time in the overall melt channel. The raw materials and process parameters of the above examples and comparative examples are shown in table 1, and the performance test results of the prepared ultra-high molecular weight polyethylene fibers are shown in table 2.
TABLE 1
TABLE 2
According to the test results, the fiber prepared by the method has the advantages of good performance, low mutation rate, low tube breakage rate, low broken filament rate and stable processing process. The dry heat shrinkage rate is small, and the size or the weight of a post-processing product is stable.
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make modifications and alterations without departing from the scope of the present invention.
Claims (10)
1. A preparation method of high-uniformity ultrahigh molecular weight polyethylene fibers is characterized by comprising the following steps:
s1: fully mixing the ultrahigh molecular weight polyethylene resin powder, a solvent and an auxiliary agent, swelling, and then putting into a screw to dissolve to obtain an ultrahigh molecular weight polyethylene solution;
s2: homogenizing the ultra-high molecular weight polyethylene solution obtained in the step S1 for preset time, and then feeding the solution into a spinning manifold;
s3: and (3) extruding and molding the solution obtained in the step (S2) through a spinning manifold to obtain gel strands, and then removing the solvent and performing hot stretching to obtain the ultra-high molecular weight polyethylene fibers.
2. The method for preparing the ultra-high molecular weight polyethylene fiber with high uniformity as claimed in claim 1, wherein in S1, the screw is a co-rotating twin screw, and the conveying section screw thread at the screw outlet is subjected to volume compression at least twice, so that the output pressure of the ultra-high molecular weight polyethylene solution is not less than 5MPa.
3. The method for preparing the ultra-high molecular weight polyethylene fiber with high uniformity as claimed in claim 1, wherein in S1, the swelling mode is kettle-type swelling, and the swelling temperature is 110 +/-5 ℃.
4. The method of claim 1, wherein in S1, the viscosity-average molecular weight of the ultra-high molecular weight polyethylene resin powder is 400 to 1000 ten thousand,
3-7 and the proportion of the ultrahigh molecular weight polyethylene resin powder particles with the particle size of 120-220 mu m is more than or equal to 70 percent.
5. The method of claim 1, wherein the solvent in S1 is selected from the group consisting of halogenated hydrocarbons, mineral oil, decalin, tetralin, naphthalene, xylene, toluene, dodecane, undecane, decane, nonane, octene, chlorobenzene, petroleum ether, and low molecular weight polyethylene wax.
6. The method of claim 1, wherein in S1, the auxiliary agent is selected from one or more of an antioxidant, a flow promoter, a thermal stabilizer, a colorant, and a functional powder.
7. The method as claimed in claim 1, wherein the step of homogenizing S2 is performed in a melt tube for no less than 10min.
8. The method of claim 1, wherein in step S2, the homogenization process is a constant temperature process, and the temperature of the melt channel is 3-5 ℃ lower than the temperature of the solution in the channel.
9. The method of claim 1, wherein in step S2, one or more static mixers are used in combination to eliminate the difference caused by flow shear in the solution, and the static mixer is used to prolong the residence time of the solution in the tube, so that the size of the gel particles that are not completely dissolved is reduced or the number of the gel particles is reduced under heating.
10. An ultra high molecular weight polyethylene fiber prepared by the method of any one of claims 1 to 9, wherein the dry heat shrinkage of the ultra high molecular weight polyethylene fiber is 2% or less at 100 ℃ and 3% or less at 120 ℃.
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