CN1389605A - Direct melt spinning process of elastic polyurethane fiber - Google Patents
Direct melt spinning process of elastic polyurethane fiber Download PDFInfo
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- CN1389605A CN1389605A CN 01114032 CN01114032A CN1389605A CN 1389605 A CN1389605 A CN 1389605A CN 01114032 CN01114032 CN 01114032 CN 01114032 A CN01114032 A CN 01114032A CN 1389605 A CN1389605 A CN 1389605A
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- spinning
- melt spinning
- direct melt
- elastomeric fiber
- polyurethane elastomeric
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Abstract
There is a manufacturing method of PU stretched fibre which has simple technology and not create grain and has successive process to ensure the functions, and has low cost and not need poisonous solvent. It put PTMG, MOCA, DA-4.4-DI with the mole ratio of 1:1-2:2-3 into the double-spiral shaft reaction press machine. The axis direction temperature is divided to 11 sections at the temperature condition of 100 C-210 C with the control accuracy of minus or plus 1 deg.C. The speed is 100-150 r.p.m. The polymer enters the spinning system through the spinning measure bump directly and then makes the product.
Description
The invention belongs to the production of chemical fibre method, particularly a kind of method of direct melt spinning polyurethane elastomeric fiber.
Polyurethane elastomeric fiber, China is called " spandex ".The method of spinning at present spandex in the world has four kinds, i.e. dry method, wet method, chemical method and fusion method.The output of dry production polyurethane elastomer accounts for more than 80% of world's spandex total output, the existing trend that is eliminated of wet method and chemical method.Complex process, the equipment investment of dry spinning are big, thereby the production cost height.And, seriously jeopardize the healthy of direct labor, and surrounding environment is caused severe contamination because dry spinning uses the bigger dimethyl formamide of toxicity as solvent.
Fusion method spins the method for polyurethane elastomeric fiber, can avoid the various deficiencies of dry spinning.It makes a polyalcohol and vulcabond step composite yarn type polyurethane elastomer in double screw extruder with chain extender earlier; Then, with fusion method its fusing is spun into spandex again.This method because signs of degradation can take place in elastomer fusion once more, descends the performance of spun polyurethane elastomer to some extent.
The object of the present invention is to provide a kind of technology, operation simplified to carry out continuously, enhancing product performance, to reduce equipment investment, reduce production costs and need not toxic solvent, to guarantee the healthy of direct labor and to prevent the method for the direct melt spinning polyurethane elastomeric fiber of contaminated environment.
Principal character of the present invention is spun spandex section for do not need to produce to melt in advance, and makes the direct and spinning system docking of slurry after its polymerization, finishes spinning process.
Its concrete technical solution is for carrying out continuously according to following steps successively: adopt oxolane polyethers or poly-hexanedioic acid glycol ester, chain extender, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, 1: 1 in molar ratio～2: 2～3, being injected into draw ratio by measuring pump is in 42～48: 1 the double screw rod extruder, the screw axial temperature is divided 11 sections controls, temperature range is 100～210 ℃, control accuracy is ± 1 ℃, screw speed is 100～150 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters spinning machine and carries out spinning, promptly makes finished product.
According to the method for above-mentioned direct melt spinning polyurethane elastomeric fiber, in the reactive polymeric thing of extruding through double screw extruder, also add the performed polymer that accounts for reactive polymeric thing weight 5～10%, so that the performance of spun polyurethane elastomeric fiber further improves.
Method according to above-mentioned direct melt spinning polyurethane elastomeric fiber, said screw axial temperature is controlled to be 100 ℃, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃ for 11 sections, and control accuracy is ± 1 ℃.
According to the method for above-mentioned direct melt spinning polyurethane elastomeric fiber, said chain extender is 1.4-butanediol or m-phenylene diamine (MPD).
Because oxolane polyethers or poly-hexanedioic acid glycol ester, chain extender, the reactive polymeric thing that diphenyl methane-three kinds of raw materials of 4.4`-vulcabond are extruded through double screw extruder directly enter spinning machine without granulation, thereby avoid the difficulty of the pelletizing moulding of polymer, also can avoid before reeling off raw silk from cocoons again with resin drying and fusion again; Simultaneously, in the reactive polymeric thing, add the operation give aggressiveness and also greatly simplify, thereby the performance of polyurethane elastomer is greatly improved, and can reduce equipment investment, reduce production costs.In addition,, make the direct labor need not to contact toxic solvent, guarantee the healthy of direct labor, prevent contaminated environment in the method without any need for solvent.And the spandex of producing no longer contains residual toxic solvents, and this is to dress and use this polyurethane elastomeric fiber person more comfortable and healthy.
Embodiments of the invention are provided below:
Embodiment 1:
With the oxolane polyethers of molecular weight 1000 or the poly-hexanedioic acid glycol ester of molecular weight 1770,1.4-butanediol, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, be injected into double screw extruder by measuring pump in 1: 1: 2 in molar ratio, said screw diameter is 72, draw ratio 48: 1, the screw axial temperature is controlled to be 100 ℃ respectively for 11 sections, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃, precision is ± 1 ℃, screw speed is 100 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters spinning machine through spinning pump and carries out spinning, promptly makes finished product.After testing, its fiber number 44-70 dawn, intensity 1.5-1.6CN/ dawn (wherein CN is 1/10 newton), percentage elongation 600---700%, 300% recovery rate 96.2% that stretches surely.
Embodiment 2:
With the oxolane polyethers of molecular weight 2000 or the poly-hexanedioic acid glycol ester of molecular weight 1770,1.4-butanediol, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, be injected into double screw extruder by measuring pump in 1: 2: 3 in molar ratio, said screw diameter is 72, draw ratio 42: 1, the screw axial temperature is controlled to be 100 ℃ respectively for 11 sections, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃, precision is ± 1 ℃, screw speed is 150 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters spinning machine through spinning pump and carries out spinning, promptly makes finished product.After testing, its fibre strength 1.4CN/ dawn (wherein CN is 1/10 newton), percentage elongation 696.4%, 300% recovery rate 95% that stretches surely.
Embodiment 3:
With the poly-hexanedioic acid glycol ester of molecular weight 1770 or the oxolane polyethers of molecular weight 1000-2000,1.4-butanediol, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, be injected into double screw extruder by measuring pump in 1: 2: 3 in molar ratio, said screw diameter is 72, draw ratio 46: 1, the screw axial temperature is controlled to be 100 ℃ respectively for 11 sections, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃, precision is ± 1 ℃, screw speed is 120 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters spinning machine through spinning pump and carries out spinning, promptly makes finished product.After testing, made fibre strength 1.2CN/ dawn (wherein CN is 1/10 newton), percentage elongation 500-550%, 300% recovery rate 94.7% that stretches surely.
Embodiment 4:
Oxolane polyethers or molecular weight 1770 poly-hexanedioic acid glycol esters with molecular weight 1000-2000,1.4-butanediol, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, be injected into double screw extruder by measuring pump in 1: 1.5: 2.5 in molar ratio, said screw diameter is 72, draw ratio 45: 1, the screw axial temperature is controlled to be 100 ℃ respectively for 11 sections, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃, precision ± 1 ℃, screw speed is 125 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters the spinning machine system through spinning pump and carries out spinning, promptly makes finished product.After testing, made 44 dawn of fibre number, the intensity 1.4-1.6CN/ dawn (wherein CN is 1/10 newton), percentage elongation 600-700%, 100% stretches recovery rate 98%, 300% surely stretches recovery rate 96.2% surely.
Embodiment 5:
According to embodiment 1～4, in the reactive polymeric thing that double screw extruder is extruded, add the performed polymer that accounts for reactive polymeric thing 5% (weight ratio), enter the spinning machine system through spinning pump again and carry out spinning, other is with embodiment 1～4.
Embodiment 6:
According to embodiment 1～4, in the reactive polymeric thing that double screw extruder is extruded, add the performed polymer that accounts for reactive polymeric thing weight 10% (weight ratio), enter the spinning machine system through spinning pump again and carry out spinning, other is with embodiment 1～4.
Embodiment 7:
According to embodiment 1～4, in the reactive polymeric thing that double screw extruder is extruded, add the performed polymer that accounts for reactive polymeric thing weight 8% (weight ratio), enter the spinning machine system through spinning pump again and carry out spinning, other is with embodiment 1～4.
Embodiment 8:
1.4 butanediols in embodiment 1～7 replace with m-phenylene diamine (MPD), and other is with embodiment 1～7.
Claims (4)
1, a kind of method of direct melt spinning polyurethane elastomeric fiber, it is characterized in that, carry out continuously according to following steps successively: adopt oxolane polyethers or poly-hexanedioic acid glycol ester, chain extender, diphenyl methane-three kinds of raw materials of 4.4`-vulcabond, 1: 1 in molar ratio～2: 2～3, being injected into draw ratio by measuring pump is in 42～48: 1 the double screw rod extruder, the screw axial temperature is divided 11 sections controls, temperature range is 100～210 ℃, control accuracy is ± 1 ℃, screw speed is 100～150 rev/mins, the reactive polymeric thing that double screw extruder is extruded directly enters spinning machine and carries out spinning, promptly makes finished product.
2, the method for direct melt spinning polyurethane elastomeric fiber according to claim 1 is characterized in that, also adds the performed polymer that accounts for reactive polymeric thing weight 5～10% in the reactive polymeric thing of extruding through double screw extruder.
3, the method for direct melt spinning polyurethane elastomeric fiber according to claim 1 and 2, it is characterized in that, said screw axial temperature is controlled to be 100 ℃, 160 ℃, 170 ℃, 180 ℃, 190 ℃, 195 ℃, 195 ℃, 195 ℃, 195 ℃, 200 ℃, 210 ℃ for 11 sections, and control accuracy is ± 1 ℃.
4, the method for direct melt spinning polyurethane elastomeric fiber according to claim 1 is characterized in that, said chain extender is 1.4-butanediol or m-phenylene diamine (MPD).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011140321A CN1172038C (en) | 2001-06-01 | 2001-06-01 | Direct melt spinning process of elastic polyurethane fiber |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011140321A CN1172038C (en) | 2001-06-01 | 2001-06-01 | Direct melt spinning process of elastic polyurethane fiber |
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| CN1389605A true CN1389605A (en) | 2003-01-08 |
| CN1172038C CN1172038C (en) | 2004-10-20 |
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| CNB011140321A Expired - Fee Related CN1172038C (en) | 2001-06-01 | 2001-06-01 | Direct melt spinning process of elastic polyurethane fiber |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1303122C (en) * | 2003-08-28 | 2007-03-07 | 冯鹰 | Production equipment of polyurethane fibre chip and application method of said polyurethane fibre chip |
| CN102051705A (en) * | 2010-12-10 | 2011-05-11 | 太仓市金祥氨纶纤维有限公司 | Method for producing direct melt filtration fused direct spun ultrafine denier polyurethane fibers |
| CN102080274A (en) * | 2010-12-10 | 2011-06-01 | 太仓市金祥氨纶纤维有限公司 | Melt spinning method of superfine denier spandex fibers through reaction in single static reaction kettle |
| CN102115919A (en) * | 2010-12-10 | 2011-07-06 | 太仓市金祥氨纶纤维有限公司 | Melting and direct-spinning superfine denier (4.6-5.5 denier) high-elastic modulus polyurethane fiber equipment |
| CN101481830B (en) * | 2008-01-08 | 2012-11-14 | 吴张江 | Engaging double-screw rod spinning pearl functional fibre and manufacturing process thereof |
| CN107881573A (en) * | 2017-12-19 | 2018-04-06 | 广东蒙泰高新纤维股份有限公司 | A kind of low melting point high-tension ternary polymerization PP TPU core-sheath monofilament and preparation method thereof |
| CN109853071A (en) * | 2018-12-27 | 2019-06-07 | 无锡金通高纤股份有限公司 | A kind of preparation method of thermoplastic polyurethane monofilament |
| CN114690307A (en) * | 2020-12-31 | 2022-07-01 | 三芳化学工业股份有限公司 | Thermoplastic polyurethane light-conducting fiber and manufacturing method thereof |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102051698B (en) * | 2010-12-10 | 2012-07-25 | 太仓市金祥氨纶纤维有限公司 | Equipment for producing direct melt filtration fused direct spun ultrafine denier polyurethane fibers |
| CN102021672B (en) * | 2010-12-10 | 2012-07-25 | 太仓市金祥氨纶纤维有限公司 | Fused direct spinning hyperfine denier polyurethane fibre device in single static agitated reactor |
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2001
- 2001-06-01 CN CNB011140321A patent/CN1172038C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1303122C (en) * | 2003-08-28 | 2007-03-07 | 冯鹰 | Production equipment of polyurethane fibre chip and application method of said polyurethane fibre chip |
| CN101481830B (en) * | 2008-01-08 | 2012-11-14 | 吴张江 | Engaging double-screw rod spinning pearl functional fibre and manufacturing process thereof |
| CN102051705A (en) * | 2010-12-10 | 2011-05-11 | 太仓市金祥氨纶纤维有限公司 | Method for producing direct melt filtration fused direct spun ultrafine denier polyurethane fibers |
| CN102080274A (en) * | 2010-12-10 | 2011-06-01 | 太仓市金祥氨纶纤维有限公司 | Melt spinning method of superfine denier spandex fibers through reaction in single static reaction kettle |
| CN102115919A (en) * | 2010-12-10 | 2011-07-06 | 太仓市金祥氨纶纤维有限公司 | Melting and direct-spinning superfine denier (4.6-5.5 denier) high-elastic modulus polyurethane fiber equipment |
| CN102051705B (en) * | 2010-12-10 | 2012-05-30 | 太仓市金祥氨纶纤维有限公司 | Method for producing direct melt filtration fused direct spun ultrafine denier polyurethane fibers |
| CN102080274B (en) * | 2010-12-10 | 2012-08-08 | 太仓市金祥氨纶纤维有限公司 | Melt spinning method of superfine denier spandex fibers through reaction in single static reaction kettle |
| CN102115919B (en) * | 2010-12-10 | 2013-02-13 | 太仓市金祥氨纶纤维有限公司 | Melting and direct-spinning superfine denier (4.6-5.5 denier) high-elastic modulus polyurethane fiber equipment |
| CN107881573A (en) * | 2017-12-19 | 2018-04-06 | 广东蒙泰高新纤维股份有限公司 | A kind of low melting point high-tension ternary polymerization PP TPU core-sheath monofilament and preparation method thereof |
| CN109853071A (en) * | 2018-12-27 | 2019-06-07 | 无锡金通高纤股份有限公司 | A kind of preparation method of thermoplastic polyurethane monofilament |
| CN114690307A (en) * | 2020-12-31 | 2022-07-01 | 三芳化学工业股份有限公司 | Thermoplastic polyurethane light-conducting fiber and manufacturing method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1172038C (en) | 2004-10-20 |
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Owner name: JILIN SAINUOSI INDUSTRY CO.,LTD. Free format text: FORMER OWNER: FENG YING; YAO YU; GUO DASHENG; MA HUI Effective date: 20061208 |
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Effective date of registration: 20061208 Address after: 132021 No. 3 Hanyang South Street, Longtan District, Jilin, Jilin Patentee after: Jilin sainuosi Co., Ltd. Address before: 121000 Jinzhou City, Liaoning province Linghe District Yunfei street two No. 40 Co-patentee before: Tao Yu Patentee before: Feng Ying Co-patentee before: Guo Dasheng Co-patentee before: Ma Hui |
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