CN101092755A - Method for producing uniporous fine denier filament of urethane elastic fiber - Google Patents
Method for producing uniporous fine denier filament of urethane elastic fiber Download PDFInfo
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- CN101092755A CN101092755A CN 200710015255 CN200710015255A CN101092755A CN 101092755 A CN101092755 A CN 101092755A CN 200710015255 CN200710015255 CN 200710015255 CN 200710015255 A CN200710015255 A CN 200710015255A CN 101092755 A CN101092755 A CN 101092755A
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Abstract
This invention relates to a production technology of spandex single hole fine wire characterizing in applying a spandex semi-continuous polymerization dry spinning method including pre-polymerization, polymerization and spinning, in which the pre-polymerization is carried out in a reactor, the polymerization is done continuously in a dynamic compression screw mixer and a static mixer and the spinning process includes: a polymerized solution is shifted to a storage tank to be aged, filtered and deaerated to enter into the spinning tank then to be pressed by nitrogen and boosted with a gear pump to spit out solution by a measuring pump to be filtered in a spinning component and distributed to a spinneret to be ejected then to be evaporated in a spinning corridor to remove solvent in it and form spandex wires to be guided and oiled then winded to a roll on a winding machine.
Description
One, technical field
The present invention relates to a kind of producing uniporous fine denier filament of urethane elastic fiber, belong to spandex silk technical field of producing.
Two, background technology
Spandex is a kind of elastomeric elastomeric fibre, is that the linear polymeric material of polyurethanes segment accounts for the synthetic fiber of constitutional chemistry structure more than 85%.Spandex has very high percentage elongation and elasticity, in many traditional textiless, only need to add a spot of spandex, the class of fabric is greatly improved, embody soft, comfortable, attractive in appearance, graceful style, feel very comfortable, become the indispensable special textile fabric of the high-grade elasticity textile product of development in recent years, have using value and development prospect quite widely.Spinning process is the place of spandex fibre moulding, evaporates by solvent in spinning process polymerization stoste, finally forms spandex fibre, and the process conditions of forming process have determined the quality of spandex fibre.
Present domestic 20D silk all is to adopt 2 hole spinneretss and 3 hole spinnerets spinning, and its weak point is: spinning speed is slow, and unit production efficiency is low, specific yield cost height.
Three, summary of the invention
The technical problem to be solved in the present invention is the deficiency at existing spandex fiber technology, a kind of single hole spinnerets spinning that is applicable to is provided, can improves spinning speed greatly, increase production efficiency, reduce specific yield cost height, increase the producing uniporous fine denier filament of urethane elastic fiber of spandex production capacity.
The technical problem to be solved in the present invention is to realize by following scheme:
A kind of producing uniporous fine denier filament of urethane elastic fiber is characterized in adopting spandex semi-continuous polymerization dry spinning technology, comprises prepolymerization, polymerization and spinning process,
Prepolymerization is carried out in reactor, presses a mole proportioning 1: (1.5-2.0) will gather four subunit ethers, two pure and mild vulcabond raw materials and add in the reactors, and mix in reactor, react and cool off, and obtain prepolymer;
Be aggregated in the screw rod extruding dynamic mixer and carry out continuously, prepolymer solution and mixed amine solution are continuously added in the screw rod extruding dynamic mixer carry out the amine reaction, obtain polymerization stoste; Polymerization stoste is input in the basin of polymer, reservoir capacity is enough stored the polymerization stoste more than 12 hours, slowly stirs, and time 20-40 minute, temperature remained on about 30-50 ℃ in the basin;
Spinning process is, is transferred to storage tank through the stoste of polymerisation, stores after the slaking more after filtration, deaeration enters spinning tank, by the nitrogen force feed, after the gear pump supercharging, by measuring pump spue stoste in filament spinning component after filtration, be dispensed to spinnerets ejection, in spinning shaft behind the evaporative removal solvent, form the spandex silk, through seal wire, oil, package becomes the silk volume of constant weight on up-coiler again.
Prepolymerized reaction temperature is controlled at about 70 ℃, provides required reaction temperature to raw material, and the time was controlled at 2～3 hours, and to guarantee that the enough hybrid reaction time is arranged, cooled temperature is controlled at 35～41 ℃, and the time was controlled at 1.5～2.5 hours;
The temperature of the polymerisation of carrying out in screw rod extruding dynamic mixer is controlled at 60-80 ℃, and the time is controlled at 40-75 second, and the solid content of polymer is controlled at 30～35%, and even with the molecular weight that guarantees polymer, the polymerization viscosity Control is about 400-450Pa.S;
For adapting to the single hole spinning fine denier filament, should strictly control storage tank, the actual outlet temperature of circulatory mediator solves the spinning air quantity in spinning tank and the pipeline that the joins companion thermic devices thereof, and the homogeneity of wind-warm syndrome and stability improve solvent evaporates speed.
Be increased to 15～20kg/cm2 by the pressure of gear pump supercharging before with measuring pump, wherein all be provided with companion's thermic devices on storage tank, spinning tank and the pipeline that joins thereof, companion's thermic devices adopts circulating heat exchange medium, and control heat exchange outlet medium temperature is 35～50 ℃;
The technical problem to be solved in the present invention can also come further to realize by the following technical programs, the hot temperature of the companion in last path is 210～230 ℃, it is 180～200 ℃ that hot temperature is accompanied in middle path, insulation companion thermal technology improves, select conduction oil as heat medium, by regulating the furnace outlet temperature and the heat conduction oil mass is controlled, the hot temperature of companion in middle path.
The technical problem to be solved in the present invention can also come further to realize by the following technical programs, spinnerets is a single orifice plate, has 24, and per 12 are positioned on the base, spinnerets is divided into two rows on each piece base, the spinnerets setting of staggering mutually between two rows.
A kind of producing uniporous fine denier filament of urethane elastic fiber of the present invention, be a kind of new technology of spandex fiber that is applicable to the spinning of single hole spinnerets, compare with intermittence type polymerization, the present invention adopts the continuous uninterrupted feeding manner, make mixing of materials evenly, reaction evenly, thereby make the molecular weight of the polymerization stoste that obtains also uniform and stable, the spinnability of polymerization stoste improves widely, thereby can improve spinning speed greatly, improve about 80%, increase production efficiency than batch (-type).
Four, description of drawings
Fig. 1: a kind of producing uniporous fine denier filament of urethane elastic fiber schematic flow sheet of the embodiment of the invention.
Five, the specific embodiment
The present invention is described in further detail below in conjunction with embodiment, but these embodiment must not be interpreted as the limitation of the present invention that goes up in all senses.
Embodiment 1:
Spandex production mainly is divided into processes such as polymerization, spinning silk winding and post processing, and current spinning process has four kinds: dry spinning, wet spinning, melt spinning and reaction method spinning, spinning new technology of the present invention are 24 dry spinnings of single hole.
To add respectively in the reactor through the poly-four subunit ether glycol (PTG) and vulcabond (MDI) raw material of accurate measurement, under 47 ℃ of conditions, mix, after 1 hour, temperature is reached about 70 ℃ greatly, under reaction temperature, kept about 3 hours.At this moment prepolymerization reaction is finished substantially.Logical water quench in reactor jacket then, cooling reactor temperature to 41 ℃, the time is about 1.5 hours, obtains prepolymer after supercooling, adds dimethylacetylamide, and prepolymer is dissolved.Then prepolymer solution is transported in the basin, prepolymer solution approximately stopped 8 hours in basin.
Secondly, is that 5% the mixed amine solution that contains 80% ethylenediamine, 18% propane diamine, 2% diethylamine continuously adds in screw rod extruding dynamic mixer and the static mixer with the speed of 500Kg/h, 200Kg/h respectively and reacts by proportioning with prepolymer solution and concentration, the temperature of reaction is controlled at 75 ℃, about 60 seconds of time, get polymerization stoste.Former fluid solid content is 32.50%, and the polymerization viscosity Control is about 400Pa.S.Polymerization stoste is input in the basin of polymer, reservoir capacity is enough stored the polymerization stoste more than 12 hours, stirs at a slow speed, and temperature remains on about 45 ℃ in the basin.
Again, the polymerization stoste in the basin is flowed to spinning, after filtration, deaeration enters spinning tank, by the nitrogen force feed, after the gear pump supercharging, by measuring pump spue stoste in filament spinning component after filtration, be dispensed to spinnerets ejection, in spinning shaft behind the evaporative removal solvent wherein, be frozen into the spandex silk, through seal wire, oil, package becomes the silk volume of constant weight on up-coiler again.
Embodiment 2:
At first, to add respectively in the reactor through the poly-four subunit ether glycol (PTG) and vulcabond (MDI) raw material of accurate measurement, under 44 ℃ of conditions, mix, greatly after 0.6 hour, temperature is reached about 70 ℃, under reaction temperature, kept about 2.5 hours.At this moment prepolymerization reaction is finished substantially.Logical water quench in reactor jacket then, cooling reactor temperature to 37 ℃, the time is about 2.5 hours, obtains prepolymer after supercooling, adds dimethylacetylamide, and prepolymer is dissolved.Prepolymer solution is transported in the basin, and prepolymer solution approximately stopped 8 hours in basin.
Secondly, is that 5% the mixed amine solution that contains 80% ethylenediamine, 18% propane diamine, 2% diethylamine continuously adds in screw rod extruding dynamic mixer and the static mixer with the speed of 500Kg/h, 200Kg/h respectively and reacts by proportioning with prepolymer solution and concentration, the temperature of reaction is controlled at 72 ℃, about 50 seconds of time, get polymerization stoste.Former fluid solid content is 32.80%, and the polymerization viscosity Control is about 450Pa.S.Polymerization stoste is input in the basin of polymer, reservoir capacity is enough stored the polymerization stoste more than 12 hours, stirs at a slow speed, and temperature remains on about 40 ℃ in the basin.
Again, the polymerization stoste in the basin is flowed to spinning, after filtration, deaeration enters spinning tank, by the nitrogen force feed, after the gear pump supercharging, by measuring pump spue stoste in filament spinning component after filtration, be dispensed to spinnerets ejection, in spinning shaft behind the evaporative removal solvent wherein, be frozen into the spandex silk, through seal wire, oil, package becomes the silk volume of constant weight on up-coiler again.
Embodiment 3:
At first, to add respectively in the reactor through the poly-four subunit ether glycol (PTG) and vulcabond (MDI) raw material of accurate measurement, under 45 ℃ of conditions, mix, greatly after 0.8 hour, temperature is reached about 70 ℃, under reaction temperature, kept about 2 hours.At this moment prepolymerization reaction is finished substantially.Logical water quench in reactor jacket then, cooling reactor temperature to 39 ℃, the time is about 2.2 hours, obtains prepolymer after supercooling, adds dimethylacetylamide, and prepolymer is dissolved.Prepolymer solution is transported in the basin, and prepolymer solution approximately stopped 8 hours in basin.
Secondly, is that 5% contain 80% ethylenediamine, 18% propane diamine, 2% diethylamine solution continuously add in screw rod extruding dynamic mixer and the static mixer with the speed of 500Kg/h, 200Kg/h respectively and react by proportioning with prepolymer solution and concentration, the temperature of reaction is controlled at 73 ℃, about 55 seconds of time, get polymerization stoste.Former fluid solid content is 32.65%, and the polymerization viscosity Control is about 430Pa.S.Polymerization stoste is input in the basin of polymer, reservoir capacity is enough stored the polymerization stoste more than 12 hours, stirs at a slow speed, and temperature remains on about 42 ℃ in the basin.
Again, the polymerization stoste in the basin is flowed to spinning, after filtration, deaeration enters spinning tank, by the nitrogen force feed, after the gear pump supercharging, by measuring pump spue stoste in filament spinning component after filtration, be dispensed to spinnerets ejection, in spinning shaft behind the evaporative removal solvent wherein, be frozen into the spandex silk, through seal wire, oil, package becomes the silk volume of constant weight on up-coiler again.Be increased to 20-25kg/cm by the pressure of gear pump supercharging before with measuring pump.
Spinnerets is 1 orifice plate, and each position is provided with 24, and per 12 are positioned on the base, and spinnerets is divided into two rows on each piece base, the spinnerets setting of staggering mutually between two rows.
A kind of producing uniporous fine denier filament of urethane elastic fiber of above embodiment, all can reach purpose of the present invention, compare with intermittence type polymerization, adopt the continuous uninterrupted feeding manner, make mixing of materials evenly, reaction evenly, thereby make the molecular weight of the polymerization stoste that obtains also uniform and stable, the spinnability of polymerization stoste improves widely, thereby can improve spinning speed greatly, improve about 80%, increase production efficiency than batch (-type).
Claims (7)
1, a kind of producing uniporous fine denier filament of urethane elastic fiber is characterized in that: adopts spandex semi-continuous polymerization dry spinning technology, comprises prepolymerization, polymerization and spinning process,
The prepolymerization operation is carried out in reactor continuously, and in molar ratio 1: (1.5-2.0) will gather four subunit ethers, two pure and mild vulcabond raw materials and add in the reactors, and in reactor, mix, react and cool off, and obtain prepolymer;
Be aggregated in the screw rod extruding dynamic mixer and carry out continuously, pre-polymer solution and mixed amine solution are continuously added in the screw rod extruding dynamic mixer react, obtain polymerization stoste; Polymerization stoste is input in the basin of polymer, reservoir capacity is enough stored the polymerization stoste more than 12 hours, slowly stirs, and time 20-40 minute, temperature remained on about 30-50 ℃ in the basin;
Spinning process is, is transferred to storage tank through the stoste of polymerisation, stores after the slaking more after filtration, deaeration enters spinning tank, by the nitrogen force feed, after the gear pump supercharging, by measuring pump spue stoste in filament spinning component after filtration, be dispensed to spinnerets ejection, in spinning shaft behind the evaporative removal solvent wherein, form the spandex silk, through seal wire, oil, package becomes the silk volume of constant weight on up-coiler again.
2, according to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 1, it is characterized in that,
Prepolymerized reaction temperature is controlled at about 70 ℃, and the time was controlled at 2～3 hours, and cooled temperature is controlled at 35～41 ℃, and the time was controlled at 1.5～2.5 hours.
3, according to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 1, it is characterized in that, the temperature of the polymerisation of carrying out in screw rod extruding dynamic mixer is controlled at 60-80 ℃, time is controlled at 40-75 second, the solid content of polymer is controlled at 30～35%, and the polymerization viscosity Control is at 400-450PaS.
4, according to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 1, it is characterized in that,
Be increased to 15～20kg/cm by the pressure of gear pump supercharging before with measuring pump
2, wherein on storage tank, spinning tank and the pipeline that joins thereof, all being provided with companion's thermic devices, companion's thermic devices adopts circulating heat exchange medium, and control heat exchange outlet medium temperature is 35～50 ℃.
5, according to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 1, it is characterized in that,
The hot temperature of the companion in last path is 210～230 ℃, and it is 180～200 ℃ that hot temperature is accompanied in middle path, selects conduction oil as heat medium.
According to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 1, it is characterized in that 6, spinnerets is a single orifice plate.
7, according to the described a kind of producing uniporous fine denier filament of urethane elastic fiber of claim 6, it is characterized in that,
Spinnerets is provided with 24, and per 12 are positioned on the base, and spinnerets is divided into two rows on each piece base, the spinnerets setting of staggering mutually between two rows.
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| CN 200710015255 CN101092755A (en) | 2007-07-06 | 2007-07-06 | Method for producing uniporous fine denier filament of urethane elastic fiber |
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| CN 200710015255 CN101092755A (en) | 2007-07-06 | 2007-07-06 | Method for producing uniporous fine denier filament of urethane elastic fiber |
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Cited By (14)
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|---|---|---|---|---|
| CN102021673A (en) * | 2010-12-10 | 2011-04-20 | 太仓市金祥氨纶纤维有限公司 | Method for producing melt direct spinning superfine (4.6-5.5) denier high elastic modulus polyurethane fibers |
| CN102021672A (en) * | 2010-12-10 | 2011-04-20 | 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 |
| CN102051698A (en) * | 2010-12-10 | 2011-05-11 | 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 |
| 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 |
| CN101760798B (en) * | 2009-12-24 | 2012-07-18 | 烟台泰和新材料股份有限公司 | Manufacturing method of spandex heavy denier yarn |
| CN102926007A (en) * | 2011-08-13 | 2013-02-13 | 苏州敏喆机械有限公司 | Vertical pump base |
| CN103194814A (en) * | 2013-04-07 | 2013-07-10 | 浙江四海氨纶纤维有限公司 | Polymer for increasing speed for spinning fine-denier filaments in Nisshinbo dry process |
| CN108950850A (en) * | 2018-09-27 | 2018-12-07 | 福建省大嘉针织有限责任公司 | A kind of production method stretching discoloration polyester-cotton blend spandex blended knitted fabric |
| CN109338547A (en) * | 2018-11-21 | 2019-02-15 | 湖南康宝源科技实业有限公司 | A kind of preparation facilities of the high-elastic super thermal fiber of fine-denier |
| CN110331467A (en) * | 2019-06-24 | 2019-10-15 | 郑州中远氨纶工程技术有限公司 | A kind of super fine denier spandex and preparation method thereof to interweave with terylene |
| CN112725929A (en) * | 2020-12-29 | 2021-04-30 | 宁夏宁东泰和新材有限公司 | Spinning control method for high-temperature-resistant polyurethane elastic fiber |
| CN114700001A (en) * | 2022-03-18 | 2022-07-05 | 江阴中绿化纤工艺技术有限公司 | Anti-caking continuous polymerization reaction device |
| CN114775074A (en) * | 2022-03-29 | 2022-07-22 | 东华大学 | Uniform and continuous hybrid gel filament forming equipment |
| CN117468102A (en) * | 2023-12-28 | 2024-01-30 | 烟台泰和新材高分子新材料研究院有限公司 | Coupling type anti-doubling spandex spinning channel and method |
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2007
- 2007-07-06 CN CN 200710015255 patent/CN101092755A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101760798B (en) * | 2009-12-24 | 2012-07-18 | 烟台泰和新材料股份有限公司 | Manufacturing method of spandex heavy denier yarn |
| CN102021673A (en) * | 2010-12-10 | 2011-04-20 | 太仓市金祥氨纶纤维有限公司 | Method for producing melt direct spinning superfine (4.6-5.5) denier high elastic modulus polyurethane fibers |
| CN102021672A (en) * | 2010-12-10 | 2011-04-20 | 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 |
| CN102051698A (en) * | 2010-12-10 | 2011-05-11 | 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 |
| 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 |
| 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 |
| 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 |
| 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 |
| CN102926007A (en) * | 2011-08-13 | 2013-02-13 | 苏州敏喆机械有限公司 | Vertical pump base |
| CN103194814A (en) * | 2013-04-07 | 2013-07-10 | 浙江四海氨纶纤维有限公司 | Polymer for increasing speed for spinning fine-denier filaments in Nisshinbo dry process |
| CN108950850A (en) * | 2018-09-27 | 2018-12-07 | 福建省大嘉针织有限责任公司 | A kind of production method stretching discoloration polyester-cotton blend spandex blended knitted fabric |
| CN109338547A (en) * | 2018-11-21 | 2019-02-15 | 湖南康宝源科技实业有限公司 | A kind of preparation facilities of the high-elastic super thermal fiber of fine-denier |
| CN110331467A (en) * | 2019-06-24 | 2019-10-15 | 郑州中远氨纶工程技术有限公司 | A kind of super fine denier spandex and preparation method thereof to interweave with terylene |
| CN110331467B (en) * | 2019-06-24 | 2021-10-26 | 郑州中远氨纶工程技术有限公司 | Superfine denier spandex interwoven with terylene and preparation method thereof |
| CN112725929A (en) * | 2020-12-29 | 2021-04-30 | 宁夏宁东泰和新材有限公司 | Spinning control method for high-temperature-resistant polyurethane elastic fiber |
| CN112725929B (en) * | 2020-12-29 | 2022-05-17 | 宁夏宁东泰和新材有限公司 | Spinning control method for high-temperature-resistant polyurethane elastic fiber |
| CN114700001A (en) * | 2022-03-18 | 2022-07-05 | 江阴中绿化纤工艺技术有限公司 | Anti-caking continuous polymerization reaction device |
| CN114775074A (en) * | 2022-03-29 | 2022-07-22 | 东华大学 | Uniform and continuous hybrid gel filament forming equipment |
| CN114775074B (en) * | 2022-03-29 | 2023-07-04 | 东华大学 | Uniform and continuous hybrid gel filament forming equipment |
| CN117468102A (en) * | 2023-12-28 | 2024-01-30 | 烟台泰和新材高分子新材料研究院有限公司 | Coupling type anti-doubling spandex spinning channel and method |
| CN117468102B (en) * | 2023-12-28 | 2024-04-12 | 烟台泰和新材高分子新材料研究院有限公司 | Coupling type anti-doubling spandex spinning channel and method |
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