Patent Application
20160017516
1. Technical Field
The present invention relates to a PET industrial yarn melt direct spinning manufacturing method and its device, specifically belonging to the technical field of PET industrial yarn manufacturing.
2. Description of Related Art
Currently, PET industrial yarn manufacturing implements a chip spinning process where PTA and EG are submitted to esterification, pre-polycondensation, final-polycondensation and quenching, and then cut into chips having intrinsic viscosity of 0.63˜0.68 dL/g. The chips are further processed through solid-state polycondensation so as to produce high-viscosity chips of 0.85˜1.05 dL/g. The high-viscosity chips are put into a screw extruder for melt spinning Finally, after drawing performed by heat rollers of multiple stages, the yarn is wound for formation. As mentioned herein, solid-state polycondensation refers to a process where polyester chips are submitted to polycondensation at a temperature that is 30° C. ˜60° C. lower than the melting point thereof in a vacuum environment or in inert atmosphere such as that of nitrogen, so as to make the polyester's molecular weight continuously increase. The process of polycondensation can take as long as 20 some hours. The existing process for manufacturing PET industrial yarn through solid-state polycondensation chip spinning has problems such as long production cycles, large facility investment, and high energy consumption. Hence, liquid tackifyingmelt direct spinning manufacturing has been a desire in the industry
Though there is technical breakthrough about liquid tackifying of polyester, two more technical problems have to be solved before large-scale melt direct spinning manufacturing of PET industrial yarn becomes possible. The first one is transportation of high-viscosity melt. PET industrial yarn requires melt having intrinsic viscosity of 0.90˜1.05 dL/g or even higher. Such high-viscosity melt has great kinematic viscosity, so it is necessary to properly arrange the piping transportation of the melt from liquid tackifying reactors to spinning boxes in order to prevent excessive viscosity drop and inconsistency.
The second problem is how to make the manufacturing flexible enough for multiple PET industrial yarns. For manufacturers, it is important to make melt direct spinning PET industrial yarns in a way that provides scale merit of polyester manufacturing and satisfies the market demand for multiple PET industrial yarns.
For solving the transportation problem of melt with high viscosity in a way that provides scale merit of polyester manufacturing and satisfies the market demand for multiple PET industrial yarns, the present invention discloses a PET industrial yarn melt direct spinning manufacturing method that is flexible and intensive, and also discloses a device using this method. The technical schemes implemented are described particularly as follows.
A PET industrial yarn melt direct spinning manufacturing device comprises:
a polymerizer using a high-capacity continuous polymerizing apparatus and used for preparing base polyester melt that is polyethylene terephthalate (PET) melt having intrinsic viscosity of 0.63˜0.68 dL/g;
2 to 10 liquid tackifying reactors each connected with the high-capacity continuous polymerizing apparatus through a split-flow pipeline, wherein the base polyester melt after tackified by the liquid tackifying reactor has the intrinsic viscosity reaching 0.90˜1.10 dL/g;
multi-head spinning units in a number ranging between 2 and 10 connected with each said liquid tackifying reactor, wherein each of the spinning units is connected with the corresponding liquid tackifying reactor through a melt pipeline and equipped with 2 to 4 spinning boxes.
The device further has the following configuration.
The high-capacity continuous polymerizing apparatus refers to a polyester reactor that has single-line capacity high enough to continuously supply material for multiple liquid tackifying reactors for esterification and polycondensation.
The liquid tackifying reactor is a vertical reactor with capacity of 30˜120 ton/day.
The spinning units are located below the liquid tackifying reactor and evenly distributed to center around the liquid tackifying reactor.
The spinning units are evenly distributed around a discharge gate of the liquid tackifying reactor, and all the melt pipelines between the spinning boxes and the discharge gate of the liquid tackifying reactor have an identical length of transportation.
The melt pipeline between the spinning unit and a discharge gate of the liquid tackifying reactor has a length of transportation not exceeding 15m and has a diameter of 25˜100 mm.
The spinning units and the liquid tackifying reactor are arranged into a “linear”, “asteroidal” or “symmetrically rectangular” pattern.
A PET industrial yarn melt direct spinning manufacturing method comprises the following steps:
(1) preparing base polyester melt: performing esterification and melt polycondensation on terephthalic acid and ethylene glycol in a high-capacity continuous polymerizing apparatus, so as to produce PET (polyethylene terephthalate) base polyester melt having intrinsic viscosity of 0.63˜0.68 dL/g, wherein parameters used include:
molar ratio between ethylene glycol and terephthalic acid of 1˜1.3; for esterification, temperature of 250˜265° C., pressure of 0.12˜0.18 Mpa, and time 3˜5 hours; for pre-polycondensation, temperature of 265˜275° C., pressure of 2500˜3000 Pa, and time of 1˜1.5 hours; and for polycondensation,
temperature of 275˜295° C., pressure of 50˜150 Pa, and time of 1.5˜2.5 hours;
(2) liquid tackifying: transporting the prepared base polyester melt to liquid tackifying reactors through split-flow pipelines respectively for polycondensation, so as to produce high-viscosity polyester melt having intrinsic viscosity of 0.90˜1.10 dL/g, wherein:
the liquid tackifying reactor is a vertical reactor, and parameters used for liquid tackifying include: temperature of 270˜285° C., pressure of 50˜130 Pa, time of 40˜90 min, so that the tackified intrinsic viscosity reaches 0.90˜1.1 dL/g, melt hue (b value) smaller than 4, and terminal carboxyl group content smaller than 30 mol/t;
(3) multi-head spinning: transporting the tackified high viscosity polyester melt to the spinning units through the melt pipelines respectively for multi-head spinning that is intensive spinning with 16˜24 heads, and submitting the high viscosity polyester melt to a process of metering using a metering pump, filtering, spinning at spinnerets, quenching through chimneys, clustering and oiling, drawing and setting, and interlacing and winding formation, thereby completing spinning.
The method further has the following limitation. The base polyester melt has intrinsic viscosity of 0.63˜0.68 dL/g, with deviation less than ±0.005 dL/g, and has terminal carboxyl group content smaller than 30 mol/t.
The high-viscosity polyester melt has intrinsic viscosity reaching 0.90˜1.1 dL/g, with melt hue (b value) smaller than 4 and terminal carboxyl group content smaller than 30 mol/t.
For transporting the high-viscosity polyester melt to the spinning boxes, the pipeline is no longer than 15 m, with diameter of 25˜100 mm, temperature of 290˜298° C., pressure of 25˜30 MPa, shear rate of 10˜18 m/s, retention time no longer than 8.0 min, and viscosity drop within 0.04˜0.08 dL/g.
For the multi-head spinning, each said spinning unit spins 16˜24 strands of yarn, namely each said spinning unit having 2 spinning boxes, and each said spinning box having 4˜6 spinning members. The spinning member is of a twin-cavity cup type and has two melt passages. Two melting cavities of the spinning member each have an independent melt-filter, and two streams of the melt for the two heads share a common spinneret that has a split structure. Each said spinning member spins two strands of yarn with spinning temperature of 290˜305° C., total denier count of each spinning position up to 20040 dtex, total draw ratio of 5.6˜6.2%, oil pick-up percentage of 0.4˜1.05%. For satisfying the need for multi-head spinning with small pitch and high capacity, said winding is performed using a parallel twin take-up machine running with winding speed of 2600˜3300 m/min.
The present invention has the following benefits:
The present invention adopts a flexible, one-head-multi-reactor-multi-tail manufacturing line and intensive melt direct spinning multi-head spinning.
1. Flexible, one-head-multi-reactor-multi-tail manufacturing line: a large-scale continuous polymerizing apparatus is used to prepare base melt for benefiting from its efficient energy use and material use and consistent melt quality due to mass manufacturing. The liquid tackifying reactor has manufacturing capacity of a proper range of 30˜120 ton/day. A polymerizing apparatus is downstream connected with 2 or more liquid tackifying reactors. Each of the liquid tackifying reactors supplies material to 2˜10 spinning units. Each of the spinning units is equipped with 2˜4 spinning boxes for spinning. Such configuration provides the benefits of batch polycondensation and is flexible enough to adapt to multiple PET industrial yarns as the market demands. Functional materials can be in-site added into the high-viscosity melt pipeline upstream the spinning system so as to produce various functional PET industrial yarns.
2. Intensive melt direct spinning multi-head spinning since the liquid tackifying reactors have proper manufacturing capability, and the spinning process involves intensive spinning with 16˜24 heads, the spinning system following each of the liquid tackifying reactor can have a compact layout where the length of the high-viscosity melt pipeline is limited to 15 m. This compact layout when working with reasonable piping parameter and transportation conditions helps to minimize the viscosity drop. The present invention is highly adaptive to market demand of various PET industrial yarns, and significantly increase spinning capacity. It also helps to significantly reduce investment per unit capacity and energy consumption during manufacturing.
The invention as well as a preferred mode of use, further objectives and advantages thereof will be best understood by reference to the following detailed description of illustrative embodiments when read in conjunction with the accompanying drawings.
in
Referring to
The polymerizer 10 uses a high-capacity continuous polymerizing apparatus and is used for preparing base polyester melt that is polyethylene terephthalate (PET) melt having intrinsic viscosity of 0.63˜0.68 dL/g.
Two to ten liquid tackifying reactors 20 are each connected with one said high-capacity continuous polymerizing apparatus through a split-flow pipeline 40. The base polyester melt after tackified by the liquid tackifying reactor 20 has the intrinsic viscosity reaching 0.90˜1.10 dL/g. The liquid tackifying reactor is preferably a vertical reactor having capacity of 30 to 120 ton/day.
Two to ten multi-head spinning units 30 are connected with each said liquid tackifying reactor 20. The spinning unit 30 is connected with the corresponding liquid tackifying reactor 20 through a melt pipeline 50 and equipped with 2 to 4 spinning boxes 60.
For achieving high efficiency of melt transportation and providing flexible and intensive production, the spinning units 30 are located below the liquid tackifying reactor 20 and evenly distributed to center around the liquid tackifying reactor 20. Particularly, the spinning units are evenly distributed around a discharge gate of the liquid tackifying reactor, and all the melt pipelines between the spinning boxes and the discharge gate of the liquid tackifying reactor have an identical length of transportation.
As proven by experiments, the best transportation efficiency is achieved when the length of the melt pipeline between the spinning unit and the discharge gate of the liquid tackifying reactor is not exceeding 15 m and the diameter of the melt pipeline ranges between 25 and 100 mm. Under these conditions, the melt transported can maintain desirable viscosity and consistency and the transportation speed is good.
The spinning units and the liquid tackifying reactors may be arranged into a “linear” pattern as shown in
The following manufacturing examples are provided for further describing the disclosed manufacturing device and the disclosed manufacturing method.
A polymerization device having annual capacity of 50,000 tons is selected to work with two liquid tackifying reactors. Each said liquid tackifying reactor corresponds to two spinning units. Each said spinning unit corresponds to 2-4 spinning positions. The arrangement between the liquid tackifying reactor and the spinning units as well as the design of the melt pipelines are shown in FIG. 3. The specific technical parameters used include:
(1) Liquid tackifying:
Low-viscosity polyester melt with intrinsic viscosity of 0.63˜0.68 dl/g is prepared using melt polycondensation and then pressurized by a booster pump and filtered by a filter before transported to tops of the vertical liquid tackifying reactors. The melt in the vertical liquid tackifying reactor falls naturally as an even film by gravity. Such a liquid tackifying process is conducted under temperature of 270˜285° C. and pressure of 50˜130Pa for 40˜90 minutes. After tackified, the melt has its intrinsic viscosity reaching 0.90˜1.1 dL/g, with melt hue (b value) smaller than 4 and terminal carboxyl group content smaller than 30 mol/t.
(2) Transportation of high-viscosity melt
During melt transportation, the length of transportation through the pipeline between the discharge gate of the liquid tackifying reactor and each said spinning box is identical and not exceeding 15m. Such pipeline is conducted using pipes having diameter of 25˜100 mm, with temperature of 280˜298° C., pressure of 25˜30 MPa, and shear rate of 10˜18 m/s, for retention time not exceeding 8.0 min, so as to control viscosity drop within 0.10 dL/g. The layout of the melt pipelines is as shown in
(3) Multi-head spinning
For the arrangement where one liquid tackifying reactor works for two spinning units, each said spinning unit may have 2-4 spinning positions. 16-24 heads of spinning may be achieved at each said spinning position. The total denier count at a spinning position is up to 20040 dtex. The high-viscosity polyester melt after the liquid tackifying process is transported to the spinning boxes at all the spinning positions and held at 290˜300° C. in the spinning boxes. The melt is then measured by a metering pump and filtered and comes out from the spinneret before quenched in the annealing area, clustered and oiled. For the metering pump, the pre- and post-pump pressures are 5˜8 MPa and 15˜20 MPa, respectively. The fineness of the filter is 15˜20 μm. In the annealing area, the temperature is 310˜350° C. For quenching, the air velocity is 0.3˜0.6 m/s, with temperature of 60˜80° C. and moisture of 70%˜80%. Oiling is performed at a site 30˜100 mm below the spinning chimney using two oil nozzles that draw oil form 2 oil pumps simultaneously. The oil pump is 0.05˜0.10 CC and has 1 oil inlet and 16 oil outlets, with oil pick-up percentage of 0.4˜1.05%.
(4) Drawing and heat setting:
This step is performed using a heat setting process including two stages of drawing and one stage of relaxation. The first pair of spinning rollers runs at 400˜600 m/min, with total draw ratio of 5.6˜6.2%.
(5) Winding formation:
The set fiber is input into an interlacing process for winding formation. Therein, the interlacer pressure is 0.3˜0.4 Mpa. Winding is achieved using a twin-type take-up machine, with winding speed of 2600˜3300 m/min, winding tension of 170˜230 cN, winding angle of 6.5°˜7.5°.
A polymerization device having annual capacity of 100,000 tons is selected to work with three liquid tackifying reactors. Each said liquid tackifying reactor corresponds to two spinning units. Each said spinning unit corresponds to 2-4 spinning positions. The arrangement between the liquid tackifying reactor and the spinning units as well as the design of the melt pipelines are shown in FIG. 4. The specific technical parameters used include:
(1) Liquid tackifying:
Low-viscosity polyester melt with intrinsic viscosity of 0.63˜0.68 dl/g is prepared using melt polycondensation and then pressurized by a booster pump and filtered by a filter before transported to tops of the vertical liquid tackifying reactors. The melt in the vertical liquid tackifying reactor falls naturally as an even film by gravity. Such a liquid tackifying process is conducted under temperature of 270˜285° C. and pressure of 50˜130 Pa for 40˜90 minutes. After tackified, the melt has its intrinsic viscosity reaching 0.90˜1.1 dL/g, with melt hue (b value) smaller than 4 and terminal carboxyl group content smaller than 30 mol/t.
(2) Transportation of high-viscosity melt
During melt transportation, the length of transportation through the pipeline between the discharge gate of the liquid tackifying reactor and each said spinning box is identical and not exceeding 15 m. Such pipeline is conducted using pipes having diameter of 25˜100 mm, with temperature of 280˜298° C., pressure of 25˜30 MPa, and shear rate of 10˜18 m/s, for retention time not exceeding 4.6˜7.0 min, so as to control viscosity drop within 0.10 dL/g. The layout of the melt pipelines is as shown in
(3) Multi-head spinning
For the arrangement where one liquid tackifying reactor works for two spinning units, each said spinning unit may have 2-4 spinning positions. 16-24 heads of spinning may be achieved at each said spinning position. The total denier count at a spinning position is up to 20040 dtex. The high-viscosity polyester melt after the liquid tackifying process is transported to the spinning boxes at all the spinning positions and held at 290˜300° C. in the spinning boxes. The melt is then measured by a metering pump and filtered and comes out from the spinneret before quenched in the annealing area, clustered and oiled. For the metering pump, the pre- and post-pump pressures are 5˜8 MPa and 15˜20 MPa, respectively. The fineness of the filter is 15˜20 μm. In the annealing area, the temperature is 310˜350° C. For quenching, the air velocity is 0.3˜0.6 m/s, with temperature of 60˜80° C. and moisture of 70%˜80%. Oiling is performed at a site 30˜100 mm below the spinning chimney using two oil nozzles that draw oil form 2 oil pumps simultaneously. The oil pump is 0.05˜0.10 CC and has 1 oil inlet and 16 oil outlets, with oil pick-up percentage of 0.4˜1.05%.
(4) Drawing and heat setting:
This step is performed using a heat setting process including two stages of drawing and one stage of relaxation. The first pair of spinning rollers runs at 400˜600 m/min, with total draw ratio of 5.6˜6.2%.
(5) Winding formation:
The set fiber is input into an interlacing process for winding formation. Therein, the interlacer pressure is 0.3˜0.4 Mpa. Winding is achieved using a twin-type take-up machine, with winding speed of 2600˜3300 m/min, winding tension of 170˜230 cN, winding angle of 6.5°˜7.5°.
A polymerization device having annual capacity of 200,000 tons is selected to work with four liquid tackifying reactors. Each said liquid tackifying reactor corresponds to two spinning units. Each said spinning unit corresponds to 2-4 spinning positions. The arrangement between the liquid tackifying reactor and the spinning units as well as the design of the melt pipelines are shown in
(1) Liquid tackifying:
Low-viscosity polyester melt with intrinsic viscosity of 0.63˜0.68 dl/g is prepared using melt polycondensation and then pressurized by a booster pump and filtered by a filter before transported to tops of the vertical liquid tackifying reactors. The melt in the vertical liquid tackifying reactor falls naturally as an even film by gravity. Such a liquid tackifying process is conducted under temperature of 270˜285° C. and pressure of 50˜130 Pa for 40˜90 minutes. After tackified, the melt has its intrinsic viscosity reaching 0.90˜1.1 dL/g, with melt hue (b value) smaller than 4 and terminal carboxyl group content smaller than 30 mol/t.
(2) Transportation of high-viscosity melt
During melt transportation, the length of transportation through the pipeline between the discharge gate of the liquid tackifying reactor and each said spinning box is identical and not exceeding 15 m. Such pipeline is conducted using pipes having diameter of 25˜100 mm, with temperature of 280˜298° C., pressure of 25˜30 MPa, and shear rate of 10˜18 m/s, for retention time not exceeding 4.6˜7.0 min, so as to control viscosity drop within 0.10 dL/g. The layout of the melt pipelines is as shown in
(3) Multi-head spinning
For the arrangement where one liquid tackifying reactor works for two spinning units, each said spinning unit may have 2-4 spinning positions. 16-24 heads of spinning may be achieved at each said spinning position. The total denier count at a spinning position is up to 20040 dtex. The high-viscosity polyester melt after the liquid tackifying process is transported to the spinning boxes at all the spinning positions and held at 290˜300° C. in the spinning boxes. The melt is then measured by a metering pump and filtered and comes out from the spinneret before quenched in the annealing area, clustered and oiled. For the metering pump, the pre- and post-pump pressures are 5˜8 MPa and 15˜20 MPa, respectively. The fineness of the filter is 15˜20 μm. In the annealing area, the temperature is 310˜350° C. For quenching, the air velocity is 0.3˜0.6 m/s, with temperature of 60˜80° C. and moisture of 70%˜80%. Oiling is performed at a site 30˜100 mm below the spinning chimney using two oil nozzles that draw oil form 2 oil pumps simultaneously. The oil pump is 0.05˜0.10 CC and has 1 oil inlet and 16 oil outlets, with oil pick-up percentage of 0.4˜1.05%.
(4) Drawing and heat setting:
This step is performed using a heat setting process including two stages of drawing and one stage of relaxation. The first pair of spinning rollers runs at 400˜600m/min, with total draw ratio of 5.6˜6.2%.
(5) Winding formation:
The set fiber is input into an interlacing process for winding formation. Therein, the interlacer pressure is 0.3˜0.4 Mpa. Winding is achieved using a twin-type take-up machine, with winding speed of 2600˜3300 m/min, winding tension of 170˜230 cN, winding angle of 6.5°˜7.5°.
| Number | Date | Country | Kind |
|---|---|---|---|
| 201310074295.2 | Mar 2013 | CN | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/CN2013/081811 | 8/20/2013 | WO | 00 |
