CN1201044A - Production process for polyether ester acetate-amine elastic body and elastic fiber - Google Patents
Production process for polyether ester acetate-amine elastic body and elastic fiber Download PDFInfo
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- CN1201044A CN1201044A CN 98101640 CN98101640A CN1201044A CN 1201044 A CN1201044 A CN 1201044A CN 98101640 CN98101640 CN 98101640 CN 98101640 A CN98101640 A CN 98101640A CN 1201044 A CN1201044 A CN 1201044A
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Abstract
The invention is about a kind of production method of polyetherester amide elastic body and elastic fiber: Heat to melt the reactant of polyether glycol, diacid and lactum seperately in the dissolving tank, pump the molten reactant seperatly by gear pump into a high-efficiency static stirrer, for esterifying prepolymerization between polyether glycol and diacid and ring-opening prepolymerization reactions of lactum and then pour the prepolymer from the stirrer into membrane evaporator for high-polymerization for 3 to 30 minutes to get the said elastic body. The elastic body as raw material is fused and spun to produce the elastic polyether ester amide fiber. This method can raise productivity and low the cost of production.
Description
The present invention relates to a method for producing polyether ester amide elastomer and elastic fiber, particularly to a method for producing polyether ester amide elastomer by continuous process and producing melt spinning elastic fiber by using polyether ester amine elastomer as raw material; belongs to the technical field of methods for manufacturing artificial fibers.
Ether ester Amide (Polyether-ester Amide) elastomer is the most notable one of high-performance thermoplastic elastomers, and is mainly used in high-grade sports equipment, electrical equipment and pipes, and because of its good mechanical strength, high (low) temperature stability and excellent molding processability, it has been increasingly used.
The traditional elastic fiber manufacturing method is most famous by DuPont's dry method, which must synthesize Polyurethane (PU) elastomer, extrude out of spinning nozzle in solution mode, blow off solvent by heated nitrogen gas, leave elastomer to form elastic fiber; such processes involve the use of solvents [ e.g.: the volatilization of Dimethylformamide (DMF) or Dimethylacetamide (DMAC) causes harm to human body and environment, which requires huge investment in solvent recovery, and thus the cost of the elastic fiber produced by this method is too high, which is not favorable for market promotion and competition.
In recent years, a technique for producing elastic fibers by melt spinning has been developed in japan, and its main results include: nisshinbo, Kanebo and Kuraray melt-spin Polyurethane (PU) to produce elastic fiber, and Teijin and Unitika melt-spin Polyether ester (Polyether-ester) elastomer to produce elastic fiber, unlike DuPont's dry process, which produces elastic fiber by melt-spinning process, the process of producing elastic fiber by melt-spinning is not a solvent recovery problem, resulting in lower production cost, but on the other hand, PU and Polyether ester have poor heat resistance, and their physical properties are greatly degraded after high-temperature melt-spinning, and the resulting elastic fiber must undergo changes such as heating, dyeing and finishing steps in the subsequent processing procedures, and thus the melt-spinning process developed in Japan is very limited in use and has physical properties far lower than those of DuPont's elastic fiber.
The main objective of the present invention is to provide a method for producing Polyether ester amide elastomer (Polyether-ester amide elastomer) by continuous process, wherein the reactants of Polyether glycol, diacid and lactam are heated in their melting tanks respectively, and then injected into a high efficiency static mixer by a gear pump after melting, the esterification prepolymerization reaction of Polyether glycol and diacid and the ring opening prepolymerization reaction of lactam are performed in the high efficiency static mixer, and the prepolymerization product obtained from the high efficiency static mixer is introduced into a thin film evaporator for high polymerization reaction for 3-30 minutes. Thereby achieving the purposes of improving the yield and reducing the manufacturing cost.
In view of the above, the present invention relates to the production of continuous polyetheresteramide elastomers by tank prepolymerization, followed by heating the prepolymer in a thin film evaporator for a short time and removing water, unreacted materials and oligomers in a high vacuum. The product is pulled and cut into particles through an outlet below the thin film evaporator. The invention improves the defects of batch reactors, and has the flow characteristics as follows:
firstly, according to the physical property requirement of the finished product, the proportion of poly (tetra methyl ether) glycol (PTMG), caprolactam epsilon-Caprolactam (CPL) and adipic Acid Adiplicated (AA) can be directly adjusted and changed, and the operation is quite easy.
And (II) mixing PTMG, CPL and AA with a high-efficiency static stirrer, heating and pre-polymerizing in a first-in first-out mode, wherein the viscosity of the pre-polymer is determined by the time of staying in the reactor,and feeding the pre-polymer into a film evaporator by a quantitative pump.
And (III) rapidly heating the prepolymer by using a film evaporator, and rapidly pumping out water, unreacted substances and oligomer in the esterification reaction by using high vacuum when a film is formed so as to complete the high polymerization reaction in a short time.
And fourthly, performing high polymerization reaction by using a thin film evaporator in a first-in first-out mode, and controlling the viscosity of the product according to the retention time.
And fifthly, sending the product after high polymerization into a water tank for cooling through a gear pump from an outlet below the thin film evaporator, and stretching the product into strips and cutting the strips into particles through a cutting machine.
It is a further object of the present invention to provide a process for producing polyetheresteramide elastic fibers from the elastomers produced in the above-described manner.
In view of the above-mentioned objects, the present invention relates to the production of polyether ester amide elastic fiber, which uses the polyether ester amide elastomer of the previous process as the raw material, and the raw material is heated and melted by a drying extruder, and then fed into a two-piece (two piece) spinneret to be extruded into fiber, and then the fiber is passed through two middle wheels to proceed forward at high speed, and then the finished product is wound up by a winding machine; the process flow of the invention is characterized as follows:
(one) elastic fiber is made of polyether ester amide elastomer, which is different from Japanese polyurethane elastic fiber and polyether ester elastic fiber.
Secondly, the melted elastomer is spun by a double-sheet spinneret to form double-pass forward opportunities, thereby increasing the strength of the fiber.
And (III) the fiber is made to be highly forward by the double middle wheels at the elongation rate ratio of 1to 4 times, the crystallization is promoted, and the strength of the elastic fiber is increased.
And (IV) winding the elastic fiber by high-speed spinning (1500-3000 m/min), which is different from the low-speed spinning (less than 1500 m/min) of polyurethane elastic fiber, not only improving the yield and reducing the cost, but also increasing the strength due to the high-speed spinning.
The invention has the advantages that: low production cost, high efficiency and good product quality.
The invention relates to a method for producing polyether ester amide elastomer by a continuous process, which is characterized in that: respectively heating Polyether glycol (Polyether glycol), diacid (diacid) and lactam (lactam) reactants in a melting tank, and respectively injecting the reactants into a high-efficiency static stirrer by a gear pump after the reactants are melted; performing esterification prepolymerization of polyether glycol and diacid and ring-opening prepolymerization of lactam in the high-efficiency static mixer, and introducing the prepolymerization product obtained from the high-efficiency static mixer into a thin film evaporator for high polymerization for 3-30 min.
Wherein, the polyether diol, diacid and lactam are PTMG, CPL and AA respectively, the molar ratio of AA to PTMG is 1.01-1.06 to 1, and the molar ratio of CPL to PTMG is 5-20 to 1.
Wherein the PTMG used has a molecular weight of from 500g/mole to 3000 g/mole.
Wherein the high efficiency static mixer is maintained at a temperature of 200 ℃ to 260 ℃, a vacuum of 10torr to atmospheric pressure, and a residence time of the reactant therein is 1to 4 hours.
Wherein the thin film evaporator is maintained at a temperature of 240 to 280 ℃, a vacuum of 0.1to 50torr, and a residence time of the reactant therein is 3 to 30 minutes.
A method for producing polyether ester amide elastic fiber by using polyether ester amide elastomer as raw material is characterized in that: the polyether ester amide elastic fiber is produced by melt spinning with the polyether ester amide elastic fiber as raw material.
Wherein the molten elastomer is extruded through two spinning ports in series to be twice forward.
Wherein, the specification of the first spinneret is L/D-2, and the specification of the second spinneret is L/D-3.
Wherein the spun yarn from the second spinning opening is cooled and extended by 1-4 times through two intermediate wheels.
Wherein, a high-speed coiling machine is used for coiling the extended spinning, and the coiling speed is 1500 m/min to 300 m/min.
The invention has the following drawings:
FIG. 1 is a block diagram of the process for preparing a polyetheresteramide elastomer of the present invention.
FIG. 2 is a schematic diagram of the preparation process of polyether ester amide elastomer according to the present invention.
FIG. 3 is a schematic diagram of a thin film evaporator.
Figure 4 is a schematic cross-sectional view of the thin film evaporator taken along line 4-4 of figure 3.
FIG. 5 is a block diagram of the process for producing polyetheresteramide elastic fiber according to the present invention.
FIG. 6 is a schematic flow chart of melt spinning.
FIG. 7 is a schematic illustration (ratio 3: 1, dimension scale in mm) of the two-piece spinneret of FIG. 6.
The numbers in the figures are as follows:
1PTMG melting tank 2CPL melting tank 3AA melting tank
4 high efficiency static mixer (static mixer) 5 thin film evaporator
6 motor 7 feeding 8 heating medium outlet
9 extraction 10 blade 11 heat medium inlet
12 inner cylinder 13 jacket 14 gear pump
15 polymer goes out 16 particle drying equipment 17 extruder
18 spinneret group 19 cooling bellows (Quench duct)
20 spinning tube (Spin tube) 21, first intermediate wheel 22, second intermediate wheel
23 windup machine 24 first spinning 25 second spinning opening
The middle and English names and the abbreviation of the polymer are as follows:
chinese name and English name
Polyether ester Amide elastomer Polyether-ester Amide ether TPAE
Caprolactam epsilon-Caprolactam CPL
Adipic Acid AA
Polyether alcohol Poly (tetra methyl ether) glycou PTMG
Polyurethane PU
Polyether ester elastomer Ploy (ether-ester) elastomer TPEE
Dimethyl formamide DME
Dimethyl acetamide DMAC
The embodiments are described in detail below with reference tothe accompanying drawings:
this invention relates to a method for producing polyether ester amide elastomer and elastic fiber; referring to FIGS. 1 and 2, the production method of polyether ester amide elastomer is described in terms of the following steps:
A. preparing reactants:
firstly, heating main reactants such as PTMG, CPL and AA in melting tanks 1, 2 and 3 respectively, wherein the molar ratio of AA to PTMG is 1.01-1.06 to 1, and the molar ratio of CPL to PTMG is 5-20 to 1; the molecular weight of PTMG used in the present invention is from 500g/mole to 3000g/mole, which can be adjusted according to the physical property requirement of the product, and the stabilizer required in the reaction and the catalyst in the first stage are also added into the melting tanks 1, 2, 3 by a metering gear pump (not shown) for sufficient mixing.
B. Preparation of prepolymer:
after each reactant is melted by each molten angle groove 1, 2, 3, the reactants are respectively injected into a high-efficiency static stirrer 4 by a gear pump, the injection amount and the injection proportion can be respectively adjusted by the gear pump according to the required physical properties, meanwhile, the reactants are heated to start the esterification reaction according to the principle of first-in first-out from top to bottom, simultaneously, the water generated by the esterification drives the ring opening reaction of CPL (caprolactam), the prepolymer is gradually formed by proper time control, and the prepolymer is injected into a film evaporator 5 from a lower outlet; wherein the temperature adopted in the prepolymerization stage is 200-260 ℃, the vacuum degree is 10torr to normal pressure, and the reactant inlet and outlet time is 1-4 hours.
C. Synthesis of polyether ester amide elastomer:
the prepolymer is pumped into the thin film evaporator 5 via a gear pump, and the catalyst required for the high polymerization reaction is also fed into the thin film evaporator 5 via a micro gear pump (not shown); as shown in FIGS. 3 and 4, the structure and the basic principle of the thin film evaporator 5 are that the prepolymer is fed into the inner tube 12 through the feed inlet 7, the blades 10 of several sets of coaxial devices are driven by the motor 6 to rotate at high speed, the prepolymer is scraped into a thin film between the blades 10 and the wall of the inner tube 12, the heated heating medium is fed into the jacket 13 through the heating medium inlet 11 to heat the thin film of the inner tube 12 and promote the reaction, meanwhile, the inner cylinder 12 is vacuumized to be in an extremely low pressure state, when the prepolymer is in a film, reduced pressure and heated state, the by-product of the prepolymerization and the water can be quickly pumped out from the extract outlet 9, simultaneously, a small part of unreacted substances and oligomeric compounds are extracted from an extract outlet 9, the high polymerization reaction is rapidly carried out, the esterified substances generated by the prepolymerization and the CPL ring-opening substances are rapidly combined, the viscosity of the product is rapidly increased, and the high polymerization of the prepolymer is carried out within 3-30 minutes according to the required physical property conditions; wherein the high polymerization temperature is 240-280 ℃, the vacuum degree is 0.1-50 torr, and the reactant inlet and outlet time is 3-30 minutes.
The chemical reactions involved in the above B and C preparations can be seen in FIG. 8. Finally, the product is sent out from a polymer outlet 15, quenched by cooling water and pulled into strips by a granulator to be cut into granules, and the preparation of the polyether ester amide elastomer is finished; wherein the finished product of polyetherester amide elastomer can be made of elastomer such as Nylon6, Nylon11, Nylon12 and Nylon 66.
Referring to FIGS. 5, 6 and 7, the production method of the polyether ester amide elastic fiber is described as follows according to the production flow:
a. drying the polyether ester amide elastomer:
referring to fig. 5, 6 and 7, the polyether ester amide elastomer prepared in the previous stage is used as a raw material and is dried in a material drying device 16, because the glass transition point of the polyether ester amide elastomer is lower than room temperature, the temperature is not too high during drying, the temperature is set according to the content of CPL in the elastomer itself, and the drying nitrogen is used to assist in removing water, the drying time is 24-48 hours, and the water content after drying is preferably below 300 ppm.
b. Extruder setting:
the melting point of the polyetheresteramide elastomer is 195 ℃ to 205 ℃ depending on the composition, so that the temperature of the extruder 17 is set to 220 ℃ to 240 ℃ and the pressure is set to 160 to 200kg/cm2The rotation speed is set to 2-50 rpm and is set according to the spinning specification.
c. Setting a spinneret set:
the invention uses a double-sheet spinneret 18 (the output end of the double-sheet spinneret is sequentially connected with a cooling fan 19 and a spinning pipe 20), the specification of a first spinneret 24 is L/D2, and the specification of a second spinneret 25 is L/D3, so that the fused elastomer has two forward opportunities, and the strength is increased.
d. Setting the rotating speed of the middle wheel:
the rotation speed ratio of the first intermediate wheel 21 to the second intermediate wheel 22 is 1/1to 1/3, so that the extended fiber has a forward action, and simultaneously, the crystallinity is improved, and the physical properties of the fiber are increased; wherein the extension ratio of the two intermediate wheels 21, 22 is 1to 4 times.
e. And (4) winding a finished product:
because the polyether ester amide elastomer has higher viscosity and melting point, the polyether ester amide elastomer is suitable for high-speed spinning, the actual operation can reach 1500 m/min-3000 m/min, the yield is effectively improved, the cost is reduced, while the general PU elastomer can only operate at low speed (300 m/min-700 m/min), and the production capacity is quite low; therefore, the elastic fiber produced by the invention has low cost and better physical and chemical properties than PU elastic fiber.
Referring to Table (I) and Table (II), typical reaction recipes and reaction conditions are shown, respectively, for the present invention, along with the physical properties of the elastomer and the elastic fiber.
In conclusion, the present invention develops polyetheresteramide elastomer by an original continuous process, which has stable quality and can be adjusted in diversity, and greatly reduces the production cost by a high-efficiency production method; in addition, the present invention develops melt-spun elastic fiber with the produced polyether ester amide elastomer, which not only has excellent quality, low production cost, but also has no environmental problem, and can further enhance market competitiveness.
Table one: typical reaction recipe and reaction conditions
| Feed Rate (g/min) | Mole ratio of | Pre-polymerization | High polymerization of thin film | ||||
| Model (A) of Example (b) | PTMG (g/mole) | PTMG | AA | CPL | PTMG/AA/CPL | Reaction time/temperature/vacuum (hours) (° c) (torr) | Reaction time/temperature/vacuum (hours) (° c) (torr) |
| 1 | 1000 | 22.0 | 3.3 | 12.4 | 1/1.03/5 | 3.5/240/60 | 10/250/1 |
| 2 | 1000 | 16.5 | 2.5 | 18.7 | 1/1.03/10 | 3.5/240/60 | 10/260/1 |
| 3 | 1000 | 13.3 | 2.0 | 22.4 | 1/1.03/15 | 3.5/240/60 | 10/260/1 |
| 4 | 1000 | 11.1 | 1.7 | 24.9 | 1/1.03/20 | 3.5/240/60 | 10/260/1 |
| 5 | 1000 | 33.0 | 5.0 | 18.6 | 1/1.03/5 | 2.4/240/60 | 10/260/1 |
| 6 | 1000 | 24.8 | 3.7 | 28.1 | 1/1.03/10 | 2.4/240/60 | 10/260/1 |
| 7 | 1000 | 19.9 | 3.0 | 33.7 | 1/1.03/15 | 2.4/240/60 | 10/260/1 |
| 8 | 1000 | 16.7 | 2.6 | 37.3 | 1/1.03/20 | 2.4/240/60 | 10/260/1 |
| 9 | 2000 | 24.5 | 1.9 | 6.9 | 1/1.05/5 | 4/240/40 | 10/260/1 |
| 10 | 2000 | 20.2 | 1.5 | 11.6 | 1/1.05/10 | 4/240/40 | 10/260/1 |
| 11 | 2000 | 17.3 | 1.3 | 14.7 | 1/1.05/15 | 4/240/40 | 10/260/1 |
| 12 | 2000 | 15.1 | 1.1 | 17.1 | 1/1.05/20 | 4/240/40 | 10/260/1 |
| 13 | 2000 | 33.2 | 3.0 | 11.1 | 1/1.05/5 | 2.5/240/40 | 10/260/1 |
| 14 | 2000 | 32.3 | 2.4 | 18.6 | 1/1.05/10 | 2.5/240/40 | 10/260/1 |
| 15 | 2000 | 27.7 | 2.1 | 23.5 | 1/1.05/15 | 2.5/240/40 | 10/260/1 |
| 16 | 2000 | 24.2 | 2.9 | 26.2 | 1/1.05/20 | 2.5/240/40 | 10/260/1 |
| 17 | 1000 | 22.0 | 3.3 | 12.4 | 1/1.03/5 | 3.5/240/60 | 20/260/1 |
| 18 | 1000 | 16.5 | 2.5 | 18.7 | 1/1.03/10 | 3.5/240/60 | 20/260/1 |
| 19 | 1000 | 13.3 | 2.0 | 22.4 | 1/1.03/15 | 3.5/240/60 | 20/260/1 |
| 20 | 1000 | 11.1 | 1.7 | 24.9 | 1/1.03/20 | 3.5/240/60 | 20/260/1 |
| 21 | 2000 | 33.0 | 5.0 | 18.6 | 1/1.05/5 | 4/240/40 | 20/260/1 |
| 22 | 2000 | 24.8 | 3.7 | 28.1 | 1/1.05/10 | 4/240/40 | 20/260/1 |
| 23 | 2000 | 19.9 | 3.0 | 33.7 | 1/1.05/15 | 4/240/40 | 20/260/1 |
| 24 | 2000 | 16.7 | 2.6 | 37.3 | 1/1.05/20 | 4/240/40 | 20/260/1 |
Table two: physical Properties of elastomer and physical Properties of elastic fiber
| Physical Properties of elastomer | Physical Properties of elastic fiber | ||||||||
| Model (A) of Example (b) | Relative viscosity (0.5%) IN O-chloropheol 25℃ | Melting Point ℃ | Tensile strength kg/cm2 | Elongation rate ％ | Denny (4f) | Strength of g/d | Elongation rate ％ | 100％ Recovery rate of elongation | Relative viscosity of silk (0.5%) IN O-chlorophenol 25℃ |
| 1 | 1.93 | 191 | 550 | 632 | 100 | 1.10 | 526 | 93.9％ | 1.87 |
| 2 | 2.05 | 193 | 587 | 597 | 100 | 1.17 | 497 | 94.4％ | 1.93 |
| 3 | 2.07 | 199 | 613 | 425 | 100 | 1.22 | 354 | 96.5％ | 1.94 |
| 4 | 2.13 | 209 | 680 | 320 | 100 | 1.36 | 269 | 99.5％ | 1.97 |
| 5 | 1.87 | 190 | 510 | 617 | 100 | 1.02 | 514 | 93.7％ | 1.84 |
| 6 | 1.96 | 191 | 547 | 583 | 100 | 1.09 | 486 | 94.2％ | 1.89 |
| 7 | 2.03 | 195 | 602 | 410 | 100 | 1.20 | 372 | 96.6％ | 1.92 |
| 8 | 2.05 | 206 | 632 | 310 | 100 | 1.26 | 285 | 99.0％ | 1.93 |
| 9 | 1.78 | 183 | 470 | 780 | 100 | 0.94 | 650 | 92.7％ | 1.73 |
| 10 | 1.81 | 187 | 487 | 653 | 100 | 0.97 | 544 | 93.4％ | 1.80 |
| 11 | 1.97 | 193 | 503 | 597 | 100 | 1.00 | 497 | 93.8％ | 1.89 |
| 12 | 2.01 | 195 | 530 | 530 | 100 | 1.06 | 441 | 94.5％ | 1.91 |
| 13 | 1.70 | 181 | 420 | 760 | 100 | 0.84 | 633 | 92.5％ | 1.69 |
| 14 | 1.74 | 183 | 450 | 589 | 100 | 0.91 | 491 | 93.4％ | 1.71 |
| 15 | 1.89 | 185 | 495 | 537 | 100 | 0.99 | 448 | 94.1％ | 1.78 |
| 16 | 1.97 | 190 | 517 | 495 | 100 | 1.03 | 413 | 95.1％ | 1.89 |
| 17 | 1.95 | 192 | 560 | 568 | 100 | 1.12 | 473 | 95.3％ | 1.88 |
| 18 | 2.10 | 194 | 591 | 503 | 100 | 1.18 | 419 | 95.7％ | 1.95 |
| 19 | 2.13 | 201 | 617 | 410 | 100 | 1.23 | 341 | 96.8％ | 1.97 |
| 20 | 2.20 | 208 | 695 | 280 | 100 | 1.39 | 254 | 99.0％ | 2.00 |
| 21 | 1.89 | 187 | 490 | 793 | 100 | 0.98 | 660 | 92.3％ | 1.85 |
| 22 | 1.93 | 192 | 503 | 701 | 100 | 1.01 | 584 | 93.2％ | 1.87 |
| 23 | 2.07 | 195 | 523 | 623 | 100 | 1.05 | 519 | 93.7％ | 1.94 |
| 24 | 2.10 | 199 | 554 | 587 | 100 | 1.11 | 490 | 94.2％ | 1.96 |
The polymerization equation of the invention is as follows: prepolymerization (1) esterification
(2) Esterification prepolymerization reaction
(3) Opening reaction of caprolactam
(4) Caprolactam prepolymerization(II) high polymerization reaction (5) Polyamide reaction
(6) High polymerization of polyetheresteramide segmented copolymers (polyester reaction) Note ① [ A]].[B].[C].[D].[E]Are the products of the reaction formulae (1), (2), (3), (4), (5), respectively.
② X.Y.Z is apositive integer.
Claims (10)
1. A method for producing polyether ester amide elastomer by continuous process, which is characterized in that: polyether glycol (Polyether glycol), diacid (diacid) and lactam (lactam) reactants are respectively heated in a melting tank, and are respectively injected into a high-efficiency static stirrer by a gear pump after being melted; performing esterification prepolymerization of polyether glycol and diacid and ring-opening prepolymerization of lactam in the high-efficiency static mixer, and introducing the prepolymerization product obtained from the high-efficiency static mixer into a thin film evaporator for high polymerization for 3-30 min.
2. The method for producing a polyether ester amide elastomer according to claim 1, wherein: wherein the polyether diol, diacid and lactam are PTMG, CPL and AA respectively, and the molar ratio of AA to PTMG is 1.01-1.06 to 1, and the molar ratio of CPL to PTMG is 5-20 to 1.
3. The method for producing a polyether ester amide elastomer according to claim 1, wherein: wherein PTMG having a molecular weight of from 500g/mole to 3000g/mole is used.
4. The method for producing a polyether ester amide elastomer according to claim 1, wherein: wherein the high efficiency static mixer is maintained at a temperature of 200 ℃ to 260 ℃, a vacuum of 10torr to atmospheric pressure, and a residence time of the reactants therein is 1to 4 hours.
5. The method for producing a polyether ester amide elastomer according to claim 1, wherein: wherein the thin film evaporator is maintained at a temperatureof 240 to 280 ℃ under a vacuum of 0.1to 50torr, and a residence time of the reactant therein is 3 to 30 minutes.
6. A method for producing polyether ester amide elastic fiber by using polyether ester amide elastomer as raw material is characterized in that: the polyether ester amide elastic fiber is produced by melt spinning with the polyether ester amide elastic fiber as raw material.
7. The method for producing polyetheresteramide elastic fiber according to claim 6, wherein: wherein the molten elastomer is extruded through two spinning ports in series to be twice forward.
8. The method for producing polyetheresteramide elastic fiber according to claim 6, wherein: wherein the specification of the first spinneret is L/D2, and the specification of the second spinneret is L/D3.
9. The method for producing polyetheresteramide elastic fiber according to claim 8, wherein: wherein the spun yarn from the second spinning opening is cooled and extended by 1-4 times through two intermediate wheels.
10. The method for producing polyetheresteramide elastic fiber according to claim 9, wherein: wherein a high-speed winding machine is used for winding the extended spinning, and the winding speed is 1500 m/min-300 m/min.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103524732A (en) * | 2013-09-22 | 2014-01-22 | 株洲时代新材料科技股份有限公司 | Production method of polyether ester amide and application of polyether ester amide prepared with production method |
| CN104583473A (en) * | 2012-08-14 | 2015-04-29 | 三菱瓦斯化学株式会社 | Polyether polyamide fiber |
| CN109651592A (en) * | 2018-12-21 | 2019-04-19 | 山东诺威聚氨酯股份有限公司 | Essential anti-static thermoplastic polyurethane elastomer and preparation method thereof |
Family Cites Families (2)
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| JPS6164752A (en) * | 1984-09-07 | 1986-04-03 | Toray Ind Inc | Polyether ester amide resin composition |
| JPH09255744A (en) * | 1996-03-25 | 1997-09-30 | Sumitomo Bakelite Co Ltd | Production of phenol resin |
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1998
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104583473A (en) * | 2012-08-14 | 2015-04-29 | 三菱瓦斯化学株式会社 | Polyether polyamide fiber |
| TWI580830B (en) * | 2012-08-14 | 2017-05-01 | 三菱瓦斯化學股份有限公司 | Polyether polyamide fiber |
| CN103524732A (en) * | 2013-09-22 | 2014-01-22 | 株洲时代新材料科技股份有限公司 | Production method of polyether ester amide and application of polyether ester amide prepared with production method |
| CN103524732B (en) * | 2013-09-22 | 2015-12-09 | 株洲时代新材料科技股份有限公司 | The production method of polyether ester amides and the application of polyether ester amides obtained thus |
| CN109651592A (en) * | 2018-12-21 | 2019-04-19 | 山东诺威聚氨酯股份有限公司 | Essential anti-static thermoplastic polyurethane elastomer and preparation method thereof |
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