CN108085756A - A kind of PBT fused mass directly spinnings fibre technology - Google Patents
A kind of PBT fused mass directly spinnings fibre technology Download PDFInfo
- Publication number
- CN108085756A CN108085756A CN201810082933.8A CN201810082933A CN108085756A CN 108085756 A CN108085756 A CN 108085756A CN 201810082933 A CN201810082933 A CN 201810082933A CN 108085756 A CN108085756 A CN 108085756A
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- melt
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/08—Melt spinning methods
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D1/00—Treatment of filament-forming or like material
- D01D1/04—Melting filament-forming substances
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D1/00—Treatment of filament-forming or like material
- D01D1/06—Feeding liquid to the spinning head
- D01D1/09—Control of pressure, temperature or feeding rate
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
- D01F6/62—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyesters
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/88—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polycondensation products as major constituent with other polymers or low-molecular-weight compounds
- D01F6/92—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from mixtures of polycondensation products as major constituent with other polymers or low-molecular-weight compounds of polyesters
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- Engineering & Computer Science (AREA)
- Textile Engineering (AREA)
- Mechanical Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
- Artificial Filaments (AREA)
Abstract
The present invention relates to a kind of PBT fused mass directly spinnings fibre technologies, it includes slurry preparation, esterification, preshrunk is reacted, prepolymer obtained is delivered to poly- reactor eventually after prepolymer filter and prepolymer cooler are filtered cooling treatment successively, the height of whole poly- reactor discharge port glues melt and melt is delivered to heating controller along utilidor by booster pump, it is finally delivered to straight spinning equipment and carries out spinning, melt heating and temperature control is at 237 272 DEG C in heating controller, residence time is in 10 40min, heated adjuster treated melt, poly- reactor outlet viscosity is controlled with no silk noil differences in viscosity in 0.06 0.17 dl/g eventually, no silk noil content of carboxyl end group control is in 25 45mol/t, pressure control is in 85 100bar before device for spinning metering pump.The present invention can the viscous conveyings of PBT high be straight spins, and small investment is easy to operate.
Description
Technical field
The invention belongs to the production technical fields of PBT fibers, and in particular to a kind of PBT fused mass directly spinnings technique.
Background technology
At present, there are two types of the production methods of polyester fiber, section is spun and fused mass directly spinning.Section spinning process, mainly passes through
Polyester slice is dried, the remelted extrusion of screw rod heating to the production of spinning manifold progress fiber, the polyester fiber of early stage
Production is more in this way；Due in section spinning technique there are the shortcomings that high energy consumption, long flow path, unstable product quality, closely
PET sections are spun over year is gradually replaced by fused mass directly spinning.
PET melt directly spin the technological process that generally uses for：Melt conveying pumps, and -- fondant filter -- booster pump -- cools down
Device -- static mixer -- distributor -- spinning.
In PET melt is directly spun, 0.64 or so, melt conveying temperature is controlled in 280-- the control of the inherent viscosity of melt
285 DEG C, melt pressure control 25Mpa, heat medium temperature is controlled 295 or so.Melt pass through booster pump and melt pipe, temperature by
Gradually rise, so as to which melt viscosity be caused to decline, since spinning and after-processing technology are determined in the range of normal viscosity, so
When melt viscosity runaways, i.e., excessive viscosity drop can cause to generate more gel particles in melt, deteriorate and spin
Strand part, the silk that floats broken end increases, therefore PET melt directly spin it is crucial that reduce melt viscosity drop, improve spinning for melt
Property, generally requirement but viscosity drop cannot be more than 0.02, must there is the reason for cooler place in directly being spun here it is PET melt.
Compared with PET, PBT determines that it has better elasticity, better dress ornament is more next due to its molecular structure feature
More favored be subject to people.Meanwhile molecular structure feature also determines that the viscosity needed for its spinning is higher, further, since PBT
Fusing point well below PET, and PBT melts are more sensitive to heat, therefore can not possibly be carried out by the carrying method of PET melt defeated
It send.At present be useful for PBT long filaments production fused mass directly spinning technique and device, the device include be sequentially connected slurry preparation,
Esterifier, preshrunk reactor, prepolymer filter, eventually prepolymer cooler, poly- reactor, fondant filter, liquid phase increasing
Viscous reactor and straight spinning equipment, fused mass directly spinning feature are to use to convey low viscosity melt to liquid-phase tackifying reaction by Melt Pump
Device, then by secondary liquid-phase tackifying melt viscosity is made to reach spinning technique needs, the discharge port of liquid-phase tackifying reactor is directly logical
The feed inlet that delivery pipe is crossed with straight spinning equipment is connected.
Fused mass directly spinning technique compared with section spinning process for, though production cost or product quality have it is larger into
Step, but also need to before melt conveying to spinning manifold low viscosity melt further to be reacted the need that its viscosity is enable to meet spinning
It asks, investment is larger, operation is cumbersome, and energy consumption is still higher.
The content of the invention
Goal of the invention：The purpose of the invention is to overcome deficiency of the prior art, it is straight to provide a kind of viscous conveyings of PBT high
It spins, small investment, fibre manufacturing technique easy to operate.
Technical solution：In order to solve the above-mentioned technical problem, a kind of PBT fused mass directly spinnings fibre technology of the present invention, it
Comprise the following steps,
（1）Load weighted raw material are put into slurry preparation and carry out slurry preparation, esterifier is put into after slurry preparation is good
Middle carry out esterification；
（2）Then carboxylate is put into and preshrunk reaction is carried out in preshrunk reactor, prepolymer obtained filters successively through prepolymer
Device and prepolymer cooler are delivered to poly- reactor eventually after being filtered cooling treatment；
（3）The height that poly- reactor outlet viscosity is 0.73-1.15dl/g eventually glue melt by booster pump by melt along utilidor
Heating controller is delivered to, straight spinning equipment is finally delivered to and carries out spinning；
Wherein, step（3）In, melt heating and temperature control is at 237-272 DEG C in heating controller, and the residence time is in 10-
40min, heated adjuster treated melt, eventually poly- reactor outlet viscosity with the control of no silk noil differences in viscosity in 0.06-
0.17 dl/g, no silk noil content of carboxyl end group control pressure before 25-45mol/t, device for spinning metering pump are controlled in 85-
100bar。
Step（3）In, melt heating and temperature control is at 245-266 DEG C in heating controller.
Step（2）In, it is equipped with online Viscosity Monitoring meter in the discharge outlet of poly- reactor eventually.
Wherein, heating controller adjustment melt temperature makes its melt generate proper amount of viscosity drop, so that melt quality accords with
Close the requirement of the dyeability of spinning fracture strength, elongation at break and following process product DTY, heating controller tune
The size of whole melt temperature is determined by the viscosity and content of carboxyl end group of no silk noil.
Step of the present invention（3）In, single dwell course refers to that high viscous melt comes out to heating from poly- reactor eventually and adjusts
Time course between device discharging, is equivalent to patent application document（Application number 2014100802765）In low viscous melt keeping the temperature
Time of delivery process in pipeline and the single dwell course in liquid-phase tackifying reactor；The residence time is 10- in the present invention
40min, time of delivery of the low viscous melt in utilidor is 0.5-0.7h in patent application document, in liquid-phase tackifying reactor
The interior residence time is 0.5-1.3h, so, for the present invention compared with patent application document, melt residence time reduction 1.5 is left when small
It is right.
Present invention and patent application file（Application number 2014100802765）Performance detection comparison see the table below：
Using the present invention since viscosity is easier to go to control according to the requirement of spinning, the uniformity of spinning (POY) is more preferable,
Compared with the POY products of liquid-phase tackifying method production, the fineness-unevenness rate of POY produced by the invention, fracture strength irregularity and
Extension at break irregularity is substantially reduced, and fracture strength and elongation at break significantly improve；And the dye of the downstream product DTY of POY
Color uniformity is also increased to 95% by 92%.
Advantageous effect：Compared with prior art, the present invention its remarkable advantage is：PBT high is viscous molten before the present invention breaches
Body can not convey the limitation directly spun, by by melt conveying in poly- reactor eventually to heating controller, then heated adjuster tune
Whole melt temperature is fed directly to straight spinning equipment after making it have suitable viscosity drop（Spinning manifold）, make product not only have compared with
Good fracture strength and elongation at break, and its later product has preferable dyeability, and the melt conveying time is more existing
The fused mass directly spinning technique of low viscous conveying liquid-phase tackifying again compare, melt residence time reduce 1.5 it is small when or so, the present invention with it is existing
There is section spinning process to compare, 30-50%, of the invention and existing direct spinning process are saved in the production of equivalent specifications, the electricity consumption of finished product per ton
It compares, the production of equivalent specifications, 20-30% is saved in the electricity consumption of finished product per ton, greatly reduces production cost, reduces equipment throwing
Money, achieves preferable economic benefit.
Description of the drawings
Fig. 1 is the process flow chart of the present invention.
Specific embodiment
With reference to embodiment and attached drawing, the present invention is further illustrated.
Embodiment 1
A kind of PBT fused mass directly spinnings fibre technology of the present invention, it comprises the following steps,
（1）Load weighted raw material are put into slurry preparation and carry out slurry preparation, esterifier is put into after slurry preparation is good
Middle carry out esterification；
（2）Then carboxylate is put into and preshrunk reaction is carried out in preshrunk reactor, prepolymer obtained filters successively through prepolymer
Device and prepolymer cooler are delivered to poly- reactor eventually after being filtered cooling treatment；
（3）The height of whole poly- reactor discharge port glues melt and melt is delivered to heating controller along utilidor by booster pump,
It is finally delivered to straight spinning equipment and carries out spinning；
Wherein, step（3）In, melt heating temperature is 245 DEG C, residence time 10.8min in heating controller, heated tune
Device treated melt is saved, poly- reactor outlet viscosity and no silk noil differences in viscosity are 0.082dl/g eventually, no silk noil content of carboxyl end group
For 36.3mol/t, pressure is 88.7bar before device for spinning metering pump.
Step（2）In, it is equipped with online Viscosity Monitoring meter in the discharge outlet of poly- reactor eventually.
Embodiment 2
A kind of PBT fused mass directly spinnings fibre technology of the present invention, it comprises the following steps,
（1）Load weighted raw material are put into slurry preparation and carry out slurry preparation, esterifier is put into after slurry preparation is good
Middle carry out esterification；
（2）Then carboxylate is put into and preshrunk reaction is carried out in preshrunk reactor, prepolymer obtained filters successively through prepolymer
Device and prepolymer cooler are delivered to poly- reactor eventually after being filtered cooling treatment；
（3）The height of whole poly- reactor discharge port glues melt and melt is delivered to heating controller along utilidor by booster pump,
It is finally delivered to straight spinning equipment and carries out spinning；
Wherein, step（3）In, melt heating temperature is 248 DEG C, residence time 13.6min in heating controller, heated tune
Device treated melt is saved, poly- reactor outlet viscosity and no silk noil differences in viscosity are 0.093dl/g eventually, no silk noil content of carboxyl end group
For 40.5mol/t, pressure is 90.9bar before device for spinning metering pump.
Step（2）In, it is equipped with online Viscosity Monitoring meter in the discharge outlet of poly- reactor eventually.
Embodiment 3
A kind of PBT fused mass directly spinnings fibre technology of the present invention, it comprises the following steps,
（1）Load weighted raw material are put into slurry preparation and carry out slurry preparation, esterifier is put into after slurry preparation is good
Middle carry out esterification；
（2）Then carboxylate is put into and preshrunk reaction is carried out in preshrunk reactor, prepolymer obtained filters successively through prepolymer
Device and prepolymer cooler are delivered to poly- reactor eventually after being filtered cooling treatment；
（3）The height of whole poly- reactor discharge port glues melt and melt is delivered to heating controller along utilidor by booster pump,
It is finally delivered to straight spinning equipment and carries out spinning；
Wherein, step（3）In, melt heating temperature is 250 DEG C, residence time 16.7min in heating controller, heated tune
Device treated melt is saved, poly- reactor outlet viscosity and no silk noil differences in viscosity are 0.105l/g eventually, no silk noil content of carboxyl end group
For 43.8mol/t, pressure is 93.6bar before device for spinning metering pump.
Step（2）In, it is equipped with online Viscosity Monitoring meter in the discharge outlet of poly- reactor eventually.
By the parameter visual representation of above-described embodiment in the following table
The present invention, which breaches former PBT high and glues melt, can not convey the limitation directly spun, by by melt conveying in poly- reactor eventually
To heating controller, then heated adjuster adjustment melt temperature, it is fed directly to directly spin dress after making it have suitable viscosity drop
It puts（Spinning manifold）, make product that not only there is preferable fracture strength and elongation at break, but also its later product has preferably
Dyeability, the melt conveying time fused mass directly spinning technique of more existing low viscous conveying liquid-phase tackifying again compares, Melt residence
It is of the invention compared with existing section spinning process when time reduction 1.5 is small or so, the production of equivalent specifications, the electricity consumption of finished product per ton
30-50%, of the invention compared with existing direct spinning process, the production of equivalent specifications are saved, 20-30% is saved in the electricity consumption of finished product per ton,
Production cost is greatly reduced, reduces equipment investment, achieves preferable economic benefit.
The present invention provides a kind of thinking and method, it is many to implement method and the approach of the technical solution, more than institute
State only is the preferred embodiment of the present invention, it is noted that for those skilled in the art, is not being departed from
On the premise of the principle of the invention, several improvements and modifications can also be made, these improvements and modifications also should be regarded as the guarantor of the present invention
Scope is protected, all undefined components in this embodiment can be implemented in the prior art.
Claims (3)
1. a kind of PBT fused mass directly spinnings fibre technology, it is characterised in that：It comprises the following steps,
（1）Load weighted raw material are put into slurry preparation and carry out slurry preparation, esterifier is put into after slurry preparation is good
Middle carry out esterification；
（2）Then carboxylate is put into and preshrunk reaction is carried out in preshrunk reactor, prepolymer obtained filters successively through prepolymer
Device and prepolymer cooler are delivered to poly- reactor eventually after being filtered cooling treatment；
（3）The height that poly- reactor outlet viscosity is 0.73-1.15dl/g eventually glue melt by booster pump by melt along utilidor
Heating controller is delivered to, straight spinning equipment is finally delivered to and carries out spinning；
Wherein, step（3）In, melt heating and temperature control is at 237-272 DEG C in heating controller, and the residence time is in 10-
40min, heated adjuster treated melt, eventually poly- reactor outlet viscosity with the control of no silk noil differences in viscosity in 0.06-
0.17 dl/g, no silk noil content of carboxyl end group control pressure before 25-45mol/t, device for spinning metering pump are controlled in 85-
100bar。
2. PBT fused mass directly spinnings fibre technology according to claim 1, it is characterised in that：Step（3）In, heating controller
Interior melt heating and temperature control is at 245-266 DEG C.
3. PBT fused mass directly spinnings fibre technology according to claim 1, it is characterised in that：Step（2）In, in poly- reaction eventually
The discharge outlet of device is equipped with online Viscosity Monitoring meter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2018/117675 WO2019144695A1 (en) | 2017-12-27 | 2018-11-27 | Process for directly spinning pbt melt into fibers |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711441027 | 2017-12-27 | ||
| CN2017114410274 | 2017-12-27 |
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| CN108085756A true CN108085756A (en) | 2018-05-29 |
| CN108085756B CN108085756B (en) | 2018-11-13 |
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| CN201810082933.8A Active CN108085756B (en) | 2017-12-27 | 2018-01-29 | A kind of PBT fused mass directly spinnings fibre technology |
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| WO (1) | WO2019144695A1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019144695A1 (en) * | 2017-12-27 | 2019-08-01 | 无锡市兴盛新材料科技有限公司 | Process for directly spinning pbt melt into fibers |
| CN110938199A (en) * | 2019-12-08 | 2020-03-31 | 无锡市兴盛新材料科技有限公司 | Production process of PBT (polybutylene terephthalate) slices |
| CN115044997A (en) * | 2022-06-25 | 2022-09-13 | 无锡市兴盛新材料科技有限公司 | PBS melt direct spinning process |
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- 2018-11-27 WO PCT/CN2018/117675 patent/WO2019144695A1/en active Application Filing
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| DD159436A1 (en) * | 1981-06-03 | 1983-03-09 | Ewert Karl Heinz | PROCESS FOR PREPARING POLYESTERDRESSES FOR FLAEENGEBILDE |
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| CN102691130A (en) * | 2012-06-19 | 2012-09-26 | 福建经纬新纤科技实业有限公司 | Process for manufacturing fire-retardant polyester fiber |
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| CN110938199A (en) * | 2019-12-08 | 2020-03-31 | 无锡市兴盛新材料科技有限公司 | Production process of PBT (polybutylene terephthalate) slices |
| CN115044997A (en) * | 2022-06-25 | 2022-09-13 | 无锡市兴盛新材料科技有限公司 | PBS melt direct spinning process |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2019144695A1 (en) | 2019-08-01 |
| CN108085756B (en) | 2018-11-13 |
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