CN205522385U - Two ingredient composite fiber spinning production facilities of polylactic acid - Google Patents
Two ingredient composite fiber spinning production facilities of polylactic acid Download PDFInfo
- Publication number
- CN205522385U CN205522385U CN201620315032.5U CN201620315032U CN205522385U CN 205522385 U CN205522385 U CN 205522385U CN 201620315032 U CN201620315032 U CN 201620315032U CN 205522385 U CN205522385 U CN 205522385U
- Authority
- CN
- China
- Prior art keywords
- guide shell
- melt
- spinning
- pipeline
- batch mixing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn - After Issue
Links
Landscapes
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
Abstract
Two ingredient composite fiber spinning production facilities of polylactic acid, including aggregation framework, drying tower, feed bin, spinning screw extruder and spinning box, the last top -down of aggregation framework is equipped with the agitator tank in proper order, just gathers jar and gather eventually the jar, bottom the agitator tank through first conveying pipeline with just gather tank deck portion and be connected, be equipped with polylactic acid pre -polymerization compounding device on the first conveying pipeline, it ties for type spinning subassembly to be equipped with a spinning pump, the 2nd spinning pump and two orifice in the spinning box, all be equipped with the integrative pipeline formula compounding device of sound on first fuse -element pipeline and the second fuse -element pipeline. The utility model discloses ensure the downward flow under the constant speed state of the intraductal fuse -element of prepolymerization to it is also unanimous basically to make the intraductal fuse -element temperature of prepolymerization, the utility model discloses direct set up on first fuse -element pipeline a plurality of groups compounding unit can, saved installation compounding system on pipeline, practiced thrift the cost, reach the purpose of even compounding, transport and compounding efficiency improve greatly.
Description
Technical field
This utility model belongs to polylactic acid spinning production technical field, particularly relates to a kind of polylactic acid bi-component composite fiber spinning and produces equipment.
Background technology
Polylactic acid (PLA) fiber is a kind of degradable biological fiber, its production method is similar to polyester fiber, but, the production process of acid fiber by polylactic easily degrades, especially drying process, according to knowhow, the aridity of spinning technique requirement to be reached, polylactic acid dry section (PLA) moisture content must be at below 30PPm, according to experiment；The hot air temperature of drying material it is generally required to 100～110 DEG C, drying time 6～8 hours.
Find according to the polylactic acid slice before and after being dried is carried out chemical examination；Polylactic acid reaches more than 1/3rd to dried viscosity drop before being dried.Although this explanation can avoid the hydrolytic degradation reaction caused because water content is too high through the polylactic acid slice being dried, but dry run has also significantly caused the degraded of polylactic acid slice.Have a strong impact on the strength of fiber.
The production of polylactic acid bi-component composite fiber needs the melt of two groups of different molecular weights (melt viscosity), i.e.；A kind of melt for higher degrees of polymerization, another kind is the melt of low degree.
If carrying out melt spinning by traditional indirect spinning method, then can run into a difficult problem for the degraded that low molecular weight pdlla section causes because of chip drying.Owing to baking temperature becomes positive correlation with the molecular weight of polylactic acid slice, molecular weight is the highest, then can there is higher baking temperature, molecular weight is relatively low, can not use higher baking temperature, owing to the gasification temperature of moisture at ambient pressure is 100 DEG C, if the hot-air using less than 100 DEG C is dried process, then it is extremely difficult to drying effect.Therefore, the section of lower molecular weight, be difficult to be dried process.
It addition, poly lactic acid polymerized operation includes pre-polymerization and gathers eventually.The melt needing polymerization first has to through pre-polymerization, and the equipment of pre-polymerization is the tank body of a vertical type cylinder shape, and tank body top is vertically provided with prepolymerization pipe.Prepolymerized melt is needed quantitatively to enter in prepolymerization pipe from the upper end of prepolymerization pipe, by self gravitation and the most steadily flow down in tank body.Due to the friction factor of melt Yu prepolymerization tube wall, the melt of the prepolymerization tube hub speed flowing velocity more downward than the melt at prepolymerization tube wall that flow downward is fast, and the temperature of the temperature at prepolymerization tube wall and prepolymerization tube hub also has difference.And preferably situation is；1, melt flows downward under constant speed state；2, when in prepolymerization pipe, melt flows downward, the tube wall of each aspect and the solution temperature of prepolymerization tube hub are desirably also；3, due to longer for carrying the conveyance conduit of polylactic acid after gathering eventually, the biggest near the high polymer molten viscosity of tube wall, molecular weight of high polymer wider distribution (uneven) problem that polylactic acid melt causes because melt flow is uneven in course of conveying, impurity can not effectively filter out, thus has influence on spinning quality.For reaching this purpose, need in prepolymerization pipe to assemble array batch mixing preheater, to meet the requirement of polymerization technique.
Utility model content
This utility model is in order to solve weak point of the prior art, it is provided that a kind of basic constant speed can be kept to flow downward prepolymerization inside pipe wall and the melt of center and prepolymerization inside pipe wall can be swapped mixing with the melt of center keeping temperature polylactic acid bi-component composite fiber spinning production equipment consistent, that mix homogeneously in the most poly-rear melt course of conveying.
For solving above-mentioned technical problem, this utility model adopts the following technical scheme that polylactic acid bi-component composite fiber spinning produces equipment, including aggregation framework, drying tower, feed bin, spinning screw extruder and spinning manifold, agitator tank it is sequentially provided with from top to bottom in aggregation framework, first poly-tank and eventually poly-tank, it is connected with first poly-tank top by the first conveying pipeline bottom agitator tank, first conveying pipeline is provided with polylactic acid pre-polymerization mixing device, first autocontrol valve and the first dosing pump, first poly-pot bottom is connected with poly-tank top eventually by the second conveying pipeline, second conveying pipeline is provided with the second autocontrol valve and the second dosing pump；
Being provided with the first spinning pump, the second spinning pump and double spray orifice parallel type filament spinning component in spinning manifold, the discharging opening of the first spinning pump and the second spinning pump charging aperture with double spray orifice parallel type filament spinning components respectively is connected；
Poly-pot bottom is connected by the charging aperture of the first melt pipe and the first spinning pump eventually；
The outlet of drying tower is connected with the import of feed bin, the outlet of feed bin is connected by the import of tremie pipe with spinning screw extruder, tremie pipe is provided with quantifier, and the discharging opening of spinning screw extruder is connected by the charging aperture of the second melt pipe and the second spinning pump；
It is sequentially provided with the first filter, the 3rd dosing pump and the first sound integrated pipeline formula mixing device along melt flows direction on first melt pipe, be sequentially provided with the second filter and the second sound integrated pipeline formula mixing device on second melt pipe along melt flows direction, the structure of the first sound integrated pipeline formula mixing device and the second sound integrated pipeline formula mixing device is identical；
Polylactic acid pre-polymerization mixing device includes the prepolymerization pipe being arranged in vertical, and from top to bottom at least provided with two batch mixing preheaters in prepolymerization pipe, all of equal structure of batch mixing preheater is identical；
Each batch mixing preheater all includes having the first upper conical guide shell of same centrage, the second upper conical guide shell, the first inferior pyramidal guide shell, the second inferior pyramidal guide shell, upper shunting cone cylinder and lower shunting cone cylinder；
nullFirst upper conical guide shell and the first inferior pyramidal guide shell are upper coarse and lower fine and upper and lower permeable structures，First upper conical guide shell bottom diameter is more than the second upper conical guide shell bottom diameter，Second upper conical guide shell and the second inferior pyramidal guide shell are up-thin-low-thick and upper and lower permeable structures，First upper conical guide shell bottom diameter and the second upper conical guide shell upper-end inner diameter are equal，First inferior pyramidal guide shell bottom diameter and the second inferior pyramidal guide shell upper-end inner diameter are equal，First outer, upper conical guide shell upper end、Second outer, upper conical guide shell lower end、First edge, inferior pyramidal guide shell upper end and the second edge, inferior pyramidal guide shell lower end are fixedly connected with at prepolymerization inside pipe wall，The fixing connection in first upper conical edge, guide shell lower end and the second edge, upper conical guide shell upper end，The fixing connection in first upper conical edge, guide shell lower end and the second edge, upper conical guide shell upper end，The fixing connection in first edge, inferior pyramidal guide shell lower end and the second edge, inferior pyramidal guide shell upper end；
Upper shunting cone cylinder is the structure that top sharply blocks, bottom is uncovered, lower shunting cone cylinder is the sharp-pointed closure in bottom, the structure of open top, upper shunting cone cylinder bottom diameter is equal to lower shunting cone cylinder upper-end inner diameter, upper shunting cone cylinder bottom diameter is less than prepolymerization bore, and edge, upper shunting cone cylinder lower end is fixing with edge, lower shunting cone cylinder upper end to be connected；Upper shunting cone cylinder and lower spreader drum outer wall are connected by heating agent conduit and prepolymerization inside pipe wall are fixing；
The upper end of upper shunting cone cylinder is higher than the first edge, upper conical guide shell upper end, and the lower end of lower shunting cone cylinder flushes with the second edge, inferior pyramidal guide shell upper end；
Form circulation road under tube wall melt between upper spreader tube outer surface and the first inferior pyramidal guide shell outer surface, between lower spreader tube outer surface and the first inferior pyramidal guide shell outer surface, form circulation road under blend melt；
Upper spreader tube outer surface is provided with central melt flow dividing structure, and the lower end of central melt flow dividing structure crosses with circulation road lower end under tube wall melt.
First sound integrated pipeline formula mixing device includes fixed-piping and batch mixing unit, batch mixing unit includes static batch mixing pipeline and the dynamic mixture pipeline of coaxial setting, the left end of dynamic mixture pipeline and the right-hand member Flange joint of static batch mixing pipeline, dynamic screw dividing plate it is provided with in dynamic mixture pipeline, dynamic mixture pipe interior is in axial direction separated into the first semicircle helical duct and the second semicircle helical duct, dynamic screw dividing plate and dynamic mixture inner-walls of duct matched in clearance by dynamic screw dividing plate；Being provided with static ribbon dividing plate in static batch mixing pipeline, static state batch mixing pipeline axially inside direction is separated into the 3rd semicircle helical duct and the 4th semicircle helical duct by static ribbon dividing plate, and static ribbon dividing plate is fixing with static batch mixing inner-walls of duct to be connected；
The plane at the place, both ends of dynamic screw dividing plate and static ribbon dividing plate is each perpendicular to the central axis of dynamic mixture pipeline, center, dynamic screw dividing plate right part is provided with dynamic cone tank, center, dynamic screw dividing plate left part is provided with the most top, center, static ribbon dividing plate right part is provided with static cone tank, center, static ribbon dividing plate left part is provided with static top, and dynamic top left end withstands in static cone tank；
Fixed-piping left end and dynamic mixture pipeline right-hand member Flange joint, be provided with support in fixed-piping, support is provided with stationary center, and stationary center left end withstands in dynamic cone tank.
The quantity of batch mixing unit is more than or equal to two groups, and Flange joint between two adjacent groups batch mixing unit, the top left end of static state of one group of batch mixing unit withstands in the dynamic cone tank of adjacent one group batch mixing unit, and fixed-piping is connected with one group of batch mixing unit of low order end.
The length of static batch mixing pipeline is less than the length of dynamic mixture pipeline.
Central melt flow dividing structure includes a shunt cylinder and several isocons, shunt cylinder and isocon are each provided in shunting cone cylinder, shunt cylinder open top, edge, shunt cylinder upper end level, isocon is wide at the top and narrow at the bottom, the all isocons of isocon are evenly arranged along upper shunting cone cylinder circumferencial direction, and isocon upper end connects with shunt cylinder lower end, and isocon lower port is positioned at circulation road lower end and the outside of circulation road upper end intersection under blend melt under tube wall melt.
Upper shunting cone cylinder is internally formed preheating cavity with lower shunting cone cylinder, and preheating cavity under being internally formed of the first inferior pyramidal guide shell and the second inferior pyramidal guide shell has all been passed through hot circulating fluid medium in upper preheating cavity and lower preheating cavity；Heating agent conduit is inner and upper preheating cavity connects, and heating agent external catheter end stretches out outside prepolymerization pipe.
nullUse technique scheme，First conveying pipeline arranges polylactic acid pre-polymerization mixing device carry out batch mixing warm and be: melt flows downward in prepolymerization pipe，Melt A at prepolymerization tube hub enters into shunt cylinder along upper shunting cone surface，Melt A flows to circulation road lower end and the outside of the intersection of circulation road upper end under blend melt under tube wall melt automatically by isocon again，Meanwhile，Melt B near prepolymerization tube wall enters under tube wall melt in circulation road through the first upper conical guide shell，Flow to be positioned at behind circulation road lower end under tube wall melt the top of melt A，Under i.e. melt A and melt B entrance blend melt after circulation road，Melt A is positioned at lower floor，Melt B is positioned at upper strata，Until melt A and melt B flow to circulation road lower end outlet under blend melt，Melt B is positioned in the middle of melt A，I.e. melt A is transformed into by center and continues to flow downward along tube wall，Melt B is transformed into center and continues to flow downward by being close to tube wall，During transposition，Melt A and melt B have been also carried out mixing definitely.
During melt mixed replaces, being all passed through hot circulating fluid medium in upper preheating cavity and lower preheating cavity, hot circulating fluid medium can add thermal medium such as according to technological requirement；Biphenyl Ether, conduction oil etc., preheat melt, to facilitate control prepolymerization process.This utility model all takes in the junction of all parts and designs without dead angle.Many group batch mixing preheaters can be installed in a piece prepolymerization pipe from top to bottom.
After in this utility model, relatively small molecular weight polylactic acid raw material uses polymerization, the technique of direct fabrics, eliminates the defect that relatively small molecular weight polylactic acid slice is dried rear indirect spinning.First sound integrated pipeline formula mixing device is set on the first melt pipe, have the advantages that under the effect of the 3rd dosing pump, polylactic acid melt after polymerization is entered by fixed-piping, when the melt of thickness under high pressure passes through dynamic mixture pipeline when, dynamic screw dividing plate starts to rotate under the promotion of melt, the dynamic screw dividing plate that viscous melt on the inwall of dynamic mixture pipeline is rotated scrapes, the viscous melt scraped is diluter that melt mixes with dynamic mixture pipeline centre, and mix in pushing ahead the 3rd semicircle helical duct in static batch mixing pipeline and the 4th semicircle helical duct, above-mentioned batch mixing process is repeated in entering back into dynamic mixture pipeline after mixing, after some groups of batch mixing unit, enter into the first spinning pump in spinning manifold；
In this utility model, larger molecular weight polylactic acid raw material uses polylactic acid slice indirect spinning technique, owing to baking temperature becomes positive correlation with the molecular weight of polylactic acid slice, molecular weight is the highest, then can have higher baking temperature, thus improve drying efficiency and effect.First being dried polylactic acid slice, dried polylactic acid slice stores in feed bin, and is entered in spinning screw extruder by the metering of quantifier；
Second melt pipe is provided with the second sound integrated pipeline formula mixing device, have the advantages that under the effect of spinning screw extruder, polylactic acid melt is entered by the second melt pipe, when the melt of thickness under high pressure passes through dynamic mixture pipeline when, dynamic screw dividing plate starts to rotate under the promotion of melt, the dynamic screw dividing plate that viscous melt on the inwall of dynamic mixture pipeline is rotated scrapes, the viscous melt scraped is diluter that melt mixes with dynamic mixture pipeline centre, and mix in pushing ahead the 3rd semicircle helical duct in static batch mixing pipeline and the 4th semicircle helical duct, above-mentioned batch mixing process is repeated in entering back into dynamic mixture pipeline after mixing, after some groups of batch mixing unit, enter into the second spinning pump in spinning manifold；
The polylactic acid melt supercharging of lower molecular weight is sent to double spray orifice parallel type filament spinning component by the first spinning pump, the polylactic acid melt supercharging of higher molecular weight is sent to double spray orifice parallel type filament spinning component by the second spinning pump simultaneously, the polylactic acid melt of lower molecular weight and the polylactic acid melt of higher molecular weight mix homogeneously in double spray orifice parallel type filament spinning components, spinneret finally by double spray orifice parallel type filament spinning components sprays, produce the PLA Composite Fiber (polylactic acid melt that cross section half is lower molecular weight of single composite fibre, second half is the polylactic acid melt of higher molecular weight).
Due to the first semicircle helical duct and the second semicircle helical duct is longer and arranges for the hand of spiral the most in the axial direction for first sound integrated pipeline formula mixing device and the second sound integrated pipeline formula mixing device, thus dynamic screw dividing plate can be driven to rotate when pressurized melt is passed through；The top form with the press-fit of cone tank top of rotary material of dynamic screw dividing plate, is not only easy to manufacture and assembling, and frictional force is less in rotary course, thus improve the efficiency of dynamic screw dividing plate scraper.The length of static batch mixing pipeline, less than the length of dynamic mixture pipeline, so can make most of length of the pipeline of whole conveying polylactic acid all can be wiped off by king-sized for the viscosity adhered on tube wall polylactic acid, fully improves the uniformity of mixing.
In sum, this utility model scientific in principle, reasonable in design, simple in construction, guarantee that the melt in prepolymerization pipe flows downward under constant speed state, and when making melt in prepolymerization pipe flow downward, the tube wall of each aspect is the most basically identical with the solution temperature of prepolymerization tube hub, thus meet the requirement of polymerization technique.Directly arranging some groups of batch mixing unit on the first melt pipe, eliminate installation mixing system on conveyance conduit, saved cost, reach the purpose of uniform batch mixing, conveying and batch mixing efficiency are greatly improved.After this utility model will carry out after poly-lactic acid in high molecular weight chip drying melting, filter, mix and be transported to double spray orifice parallel type filament spinning component and carry out spinning, simultaneously by low molecular weight polymerizable raw material, filter, mix after be transported in double spray orifice parallel type filament spinning component, this pair of spray orifice parallel type filament spinning component be number of patent application be the technical scheme disclosed in the utility model of CN201510042184.2.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model；
Fig. 2 is the structural representation of the present utility model in Fig. 1 with one group of batch mixing unit；
Fig. 3 is the perspective view of dynamic screw dividing plate in Fig. 2；
Fig. 4 is the perspective view of static ribbon dividing plate in Fig. 2；
Fig. 5 is the structural representation of polylactic acid pre-polymerization mixing device in Fig. 1；
Fig. 6 is the top view of the central melt flow dividing structure in Fig. 5.
Detailed description of the invention
As shown in figure-Fig. 6, polylactic acid bi-component composite fiber spinning of the present utility model produces equipment, including aggregation framework 16, drying tower 18, feed bin 30, spinning screw extruder 32 and spinning manifold 17, agitator tank 19 it is sequentially provided with from top to bottom in aggregation framework 16, first poly-tank 20 and eventually poly-tank 21, it is connected with first poly-tank 20 top by the first conveying pipeline 22 bottom agitator tank 19, first conveying pipeline 22 is provided with polylactic acid pre-polymerization mixing device 40, first autocontrol valve 23 and the first dosing pump 24, it is connected with poly-tank 21 top eventually by the second conveying pipeline 25 bottom first poly-tank 20, second conveying pipeline 25 is provided with the second autocontrol valve 26 and the second dosing pump 27.
Being provided with first spinning pump the 33, second spinning pump 34 and double spray orifice parallel type filament spinning component 35 in spinning manifold 17, the discharging opening of the first spinning pump 33 and the second spinning pump 34 charging aperture with double spray orifice parallel type filament spinning components 35 respectively is connected；
It is connected with the charging aperture of the first spinning pump 33 by the first melt pipe 28 bottom poly-tank 21 eventually；
The outlet of drying tower 18 is connected with the import of feed bin 30, the outlet of feed bin 30 is connected by the import of tremie pipe 36 with spinning screw extruder 32, tremie pipe 36 is provided with quantifier 37, and the discharging opening of spinning screw extruder 32 is connected with the charging aperture of the second spinning pump 34 by the second melt pipe 38；
It is sequentially provided with the first filter the 39, the 3rd dosing pump 29 and the first sound integrated pipeline formula mixing device 31 along melt flows direction on first melt pipe 28, be sequentially provided with the second filter 60 and the second sound integrated pipeline formula mixing device 61 on second melt pipe 38 along melt flows direction, the first sound integrated pipeline formula mixing device 31 is identical with the structure of the second sound integrated pipeline formula mixing device 61.
First sound integrated pipeline formula mixing device 31 includes fixed-piping 1 and batch mixing unit, batch mixing unit includes static batch mixing pipeline 2 and the dynamic mixture pipeline 3 of coaxial setting, the left end of dynamic mixture pipeline 3 and the right-hand member Flange joint of static batch mixing pipeline 2, dynamic screw dividing plate 4 it is provided with in dynamic mixture pipeline 3, dynamic mixture pipeline 3 axially inside direction is separated into the first semicircle helical duct 5 and the second semicircle helical duct 6, dynamic screw dividing plate 4 and dynamic mixture pipeline 3 inwall matched in clearance by dynamic screw dividing plate 4；Being provided with static ribbon dividing plate 7 in static batch mixing pipeline 2, static state batch mixing pipeline 2 axially inside direction is separated into the 3rd semicircle helical duct 8 and the 4th semicircle helical duct 9 by static ribbon dividing plate 7, and static ribbon dividing plate 7 is fixing with static batch mixing pipeline 2 inwall to be connected.
The plane at the place, both ends of dynamic screw dividing plate 4 and static ribbon dividing plate 7 is each perpendicular to the central axis of dynamic mixture pipeline 3, center, dynamic screw dividing plate 4 right part is provided with dynamic cone tank 10, center, dynamic screw dividing plate 4 left part is provided with the most top 11, center, static ribbon dividing plate 7 right part is provided with static cone tank 12, center, static ribbon dividing plate 7 left part is provided with static top 13, and the most top 11 left ends withstand in static cone tank 12.
Fixed-piping 1 left end and dynamic mixture pipeline 3 right-hand member Flange joint, be provided with support 14 in fixed-piping 1, support 14 is provided with stationary center 15, and stationary center 15 left end withstands in dynamic cone tank 10.
The quantity of batch mixing unit is more than or equal to two groups, and Flange joint between two adjacent groups batch mixing unit, top 13 left ends of static state of one group of batch mixing unit withstand in the dynamic cone tank 10 of adjacent one group batch mixing unit, and fixed-piping 1 is connected with one group of batch mixing unit of low order end.The length of static batch mixing pipeline 2 is less than the length of dynamic mixture pipeline 4.
Polylactic acid pre-polymerization mixing device 40 includes the prepolymerization pipe 41 being arranged in vertical, prepolymerization pipe 41 two ends are fixedly connected on the first conveying pipeline 22, or can be using the first conveying pipeline 22 as prepolymerization pipe 41, from top to bottom at least provided with two batch mixing preheaters in prepolymerization pipe 41, all of equal structure of batch mixing preheater is identical；In this utility model, prepolymerization pipe 41 can use the first conveying pipeline 22 to replace；
Each batch mixing preheater all includes having first upper conical guide shell 42, second upper conical guide shell the 43, first inferior pyramidal guide shell the 44, second inferior pyramidal guide shell 45 of same centrage, upper shunting cone cylinder 46 and lower shunting cone cylinder 47；
nullFirst upper conical guide shell 42 and the first inferior pyramidal guide shell 44 are upper coarse and lower fine and upper and lower permeable structures，First upper conical guide shell 42 bottom diameter is more than the second upper conical guide shell 43 bottom diameter，Second upper conical guide shell 43 and the second inferior pyramidal guide shell 45 are up-thin-low-thick and upper and lower permeable structures，First upper conical guide shell 42 bottom diameter and the second upper conical guide shell 43 upper-end inner diameter are equal，First inferior pyramidal guide shell 44 bottom diameter and the second inferior pyramidal guide shell 45 upper-end inner diameter are equal，First outer, upper conical guide shell 42 upper end、Second outer, upper conical guide shell 43 lower end、First edge, inferior pyramidal guide shell 44 upper end and the second edge, inferior pyramidal guide shell 45 lower end are fixedly connected with at prepolymerization pipe 41 inwall，The fixing connection in first upper conical edge, guide shell 42 lower end and the second edge, upper conical guide shell 43 upper end，The fixing connection in first upper conical edge, guide shell 42 lower end and the second edge, upper conical guide shell 43 upper end，The fixing connection in first edge, inferior pyramidal guide shell 44 lower end and the second edge, inferior pyramidal guide shell 45 upper end；
The structure that upper shunting cone cylinder 46 sharply blocks for top, bottom is uncovered, lower shunting cone cylinder 47 sharply blocks for bottom, the structure of open top, upper shunting cone cylinder 46 bottom diameter is equal to lower shunting cone cylinder 47 upper-end inner diameter, upper shunting cone cylinder 46 bottom diameter is less than prepolymerization pipe 41 internal diameter, and edge, upper shunting cone cylinder 46 lower end is fixing with edge, lower shunting cone cylinder 47 upper end to be connected；Upper shunting cone cylinder 46 and lower shunting cone cylinder 47 outer wall are connected by heating agent conduit and prepolymerization pipe 41 inwall are fixing；
The upper end of upper shunting cone cylinder 46 is higher than the first edge, upper conical guide shell 42 upper end, and the lower end of lower shunting cone cylinder 47 flushes with the second edge, inferior pyramidal guide shell 45 upper end；
Form circulation road 48 under tube wall melt between upper shunting cone cylinder 46 outer surface and the first inferior pyramidal guide shell 44 outer surface, between lower shunting cone cylinder 47 outer surface and the first inferior pyramidal guide shell 44 outer surface, form circulation road 49 under blend melt；
Upper shunting cone cylinder 46 outer surface is provided with central melt flow dividing structure 50, and the lower end of central melt flow dividing structure 50 crosses with circulation road 48 lower end under tube wall melt.
Central melt flow dividing structure 50 includes a shunt cylinder 51 and several isocons 52, shunt cylinder 51 and isocon 52 are each provided in shunting cone cylinder 46, shunt cylinder 51 open top, edge, shunt cylinder 51 upper end level, isocon 52 is wide at the top and narrow at the bottom, the all isocons of isocon 52 52 are evenly arranged along upper shunting cone cylinder 46 circumferencial direction, isocon 52 upper end connects with shunt cylinder 51 lower end, and isocon 52 lower port is positioned at circulation road 48 lower end and the outside of circulation road 49 upper end intersection under blend melt under tube wall melt.
Upper shunting cone cylinder 46 is internally formed preheating cavity 53, preheating cavity 54 under being internally formed of the first inferior pyramidal guide shell 44 and the second inferior pyramidal guide shell 45 with lower shunting cone cylinder 47, has all been passed through hot circulating fluid medium in upper preheating cavity 53 and lower preheating cavity 54.Heating agent conduit is inner and upper preheating cavity 53 connects, and heating agent external catheter end stretches out outside prepolymerization pipe.Heating agent conduit is circulated water conservancy diversion to the hot circulating fluid medium in upper preheating cavity 53, and plays support location upper shunting cone cylinder 46 and the effect of lower shunting cone cylinder 47.Wherein heating agent conduit is not illustrated out in the drawings.
nullFirst conveying pipeline arranges polylactic acid pre-polymerization mixing device 40 carry out batch mixing warm and be: melt flows downward in prepolymerization pipe 41，The melt A of prepolymerization pipe 41 center enters into shunt cylinder 51 along upper shunting cone cylinder 46 surface，Melt A flows to circulation road 48 lower end and the outside of the intersection of circulation road 49 upper end under blend melt under tube wall melt automatically by isocon 52 again，Meanwhile，Melt B near prepolymerization pipe 41 tube wall enters under tube wall melt in circulation road 48 through the first upper conical guide shell 42，Flow to be positioned at behind circulation road 48 lower end under tube wall melt the top of melt A，Under i.e. melt A and melt B entrance blend melt after circulation road 49，Melt A is positioned at lower floor，Melt B is positioned at upper strata，Until melt A and melt B flow to circulation road 49 lower end outlet under blend melt，Melt B is positioned in the middle of melt A，I.e. melt A is transformed into by center and continues to flow downward along tube wall，Melt B is transformed into center and continues to flow downward by being close to tube wall，During transposition，Melt A and melt B have been also carried out mixing definitely.The flow direction being oriented to melt A of Fig. 5 hollow core arrow, the flow direction being oriented to melt B of filled arrows.
During melt mixed replaces, being all passed through hot circulating fluid medium in upper preheating cavity 53 and lower preheating cavity 54, hot circulating fluid medium can add thermal medium such as according to technological requirement；Biphenyl Ether, conduction oil etc., preheat melt, to facilitate control prepolymerization process.This utility model all takes in the junction of all parts and designs without dead angle.Many group batch mixing preheaters can be installed in a piece prepolymerization pipe 41 from top to bottom.
After in this utility model, relatively small molecular weight polylactic acid raw material uses polymerization, the technique of direct fabrics, eliminates the defect that relatively small molecular weight polylactic acid slice is dried rear indirect spinning.nullFirst sound integrated pipeline formula mixing device 31 is set on first melt pipe 28，Have the advantages that under the effect of the 3rd dosing pump 29，Polylactic acid after polymerization is entered by fixed-piping 1，When the melt of thickness under high pressure passes through dynamic mixture pipeline 3 when，Dynamic screw dividing plate 4 starts to rotate under the promotion of melt，The dynamic screw dividing plate 4 that viscous melt on the inwall of dynamic mixture pipeline 3 is rotated scrapes，The viscous melt scraped is diluter that melt mixes with dynamic mixture pipeline 3 centre，And mix in pushing ahead the 3rd semicircle helical duct 8 in static batch mixing pipeline 2 and the 4th semicircle helical duct 9，Above-mentioned batch mixing process is repeated in entering back into dynamic mixture pipeline 3 after mixing，After some groups of batch mixing unit，Enter into the first spinning pump 33 in spinning manifold 17；
In this utility model, larger molecular weight polylactic acid raw material uses polylactic acid slice indirect spinning technique, owing to baking temperature becomes positive correlation with the molecular weight of polylactic acid slice, molecular weight is the highest, then can have higher baking temperature, thus improve drying efficiency and effect.First being dried polylactic acid slice, dried polylactic acid slice stores in feed bin 30, and is entered in spinning screw extruder 32 by the metering of quantifier 37；
nullSecond melt pipe 38 is provided with the second sound integrated pipeline formula mixing device 61，Have the advantages that under the effect of spinning screw extruder 32，The polylactic acid melt of higher molecular weight is entered by the second melt pipe 38，When the melt of thickness under high pressure passes through dynamic mixture pipeline 3 when，Dynamic screw dividing plate 4 starts to rotate under the promotion of melt，The dynamic screw dividing plate 4 that viscous melt on the inwall of dynamic mixture pipeline 3 is rotated scrapes，The viscous melt scraped is diluter that melt mixes with dynamic mixture pipeline 3 centre，And mix in pushing ahead the 3rd semicircle helical duct 8 in static batch mixing pipeline 2 and the 4th semicircle helical duct 9，Above-mentioned batch mixing process is repeated in entering back into dynamic mixture pipeline 3 after mixing，After some groups of batch mixing unit，Enter into the second spinning pump 34 in spinning manifold 17；
The polylactic acid melt supercharging of lower molecular weight is sent to double spray orifice parallel type filament spinning component 35 by the first spinning pump 33, the polylactic acid melt supercharging of higher molecular weight is sent to double spray orifice parallel type filament spinning component 35 by the second spinning pump 34 simultaneously, the polylactic acid melt of lower molecular weight and the polylactic acid melt of higher molecular weight mix homogeneously in double spray orifice parallel type filament spinning components 35, spinneret finally by double spray orifice parallel type filament spinning components 35 sprays, produce the PLA Composite Fiber (polylactic acid melt that cross section half is lower molecular weight of single composite fibre, second half is the polylactic acid melt of higher molecular weight).
Due to the first semicircle helical duct 5 and the second semicircle spiral lead to 6 roads longer and the most in the axial direction for the hand of spiral arrange, thus can when pressurized melt is passed through, drive dynamic screw dividing plate 4 rotate；The top form with the press-fit of cone tank top of rotary material of dynamic screw dividing plate 4, is not only easy to manufacture and assembling, and frictional force is less in rotary course, thus improve the efficiency of dynamic screw dividing plate 4 scraper.The length of static batch mixing pipeline 2 is less than the length of dynamic mixture pipeline 3, whole first melt pipe 28(so can be made to be made up of static batch mixing pipeline 2 and dynamic mixture pipeline 3) most of length all king-sized for viscosity adhere on tube wall polylactic acid can be wiped off, fully improve the uniformity mixed.
What spinning production technology of the present utility model was used specifically comprises the following steps that
(1), the catalyst of participation polymerization, the fusion of stabilizer equal solvent are become suspension, suspension is injected in agitator tank 19, in agitator tank 19, injects the lactide melt of lower molecular weight simultaneously, open agitator tank work, stirring melt 20～40min, until stopping stirring after mix homogeneously；, being dried in the polylactic acid slice of higher molecular weight is sent to drying tower 18, dried polylactic acid slice is stored in feed bin 30 meanwhile；
(2) the first autocontrol valve 23 bottom agitator tank 19, is opened, by the first dosing pump 24, lactide melt mixture is carried out preliminary polymerization operation in the first conveying pipeline 22 drops into first poly-tank 20, preliminary polymerization operation be temperature be 100～150 DEG C, the time of preliminary polymerization operation is 1～2h, pressure is 0.2MPa, after preliminary polymerization operation, the mixture of lactide, titanium dioxide and solvent is aggregated into the polylactic acid melt into thickness；Meanwhile, the polylactic acid slice in feed bin 30 is first measured by tremie pipe 36, drops in spinning screw extruder 32 after metering；
(3), the second autocontrol valve 26 bottom first poly-tank 20 is opened, by the second dosing pump 27, low molecular weight melt is finally polymerized operation in the second conveying pipeline 25 drops into whole poly-tank 21, final polymerization operation be temperature be 150～280 DEG C, the time of final polymerization operation is 1～6h, and pressure is 0.3MPa；Polylactic acid is done section and is heated to 200-300 DEG C and makes poly-lactic acid in high molecular weight melt by spinning screw extruder 32；
(4), the 3rd autocontrol valve bottom whole poly-tank 21 is opened, low molecular weight pdlla melt in poly-tank 21 is discharged through the first melt pipe 28 eventually, the 3rd dosing pump 29 on first melt pipe 28 provides metering and the power of conveying for low molecular weight pdlla melt, and by the filtration of the first filter 39, low molecular weight pdlla melt is mixed by the first sound integrated pipeline formula mixing device 31, in the first spinning pump 33 in then low molecular weight pdlla melt enters into spinning manifold 17；Simultaneously, under the effect of spinning screw extruder 32, macromolecule polylactic acid melt is entered by the second melt pipe 38, in the filtration of the second filter 60, the second spinning pump 34 that the second sound integrated pipeline formula mixing device 61 enters in spinning manifold 17 after mixing macromolecule polylactic acid melt；
(5), the polylactic acid melt supercharging of lower molecular weight is sent to double spray orifice parallel type filament spinning component 35 by the first spinning pump 33, the polylactic acid melt supercharging of higher molecular weight is sent to double spray orifice parallel type filament spinning component 35 by the second spinning pump 34 simultaneously, the polylactic acid melt of lower molecular weight and the polylactic acid melt of higher molecular weight mix homogeneously in double spray orifice parallel type filament spinning components 35, spinneret finally by double spray orifice parallel type filament spinning components 35 sprays, and produces PLA Composite Fiber.
Shape of the present utility model, material, structure etc. are not made any pro forma restriction by the present embodiment; every any simple modification, equivalent variations and modification made above example according to technical spirit of the present utility model, belongs to the protection domain of technical solutions of the utility model.
Claims (6)
1. the spinning of polylactic acid bi-component composite fiber produces equipment, it is characterized in that: include aggregation framework, drying tower, feed bin, spinning screw extruder and spinning manifold, agitator tank, first poly-tank and whole poly-tank it is sequentially provided with from top to bottom in aggregation framework, it is connected with first poly-tank top by the first conveying pipeline bottom agitator tank, first conveying pipeline is provided with polylactic acid pre-polymerization mixing device, the first autocontrol valve and the first dosing pump, first poly-pot bottom is connected with poly-tank top eventually by the second conveying pipeline, and the second conveying pipeline is provided with the second autocontrol valve and the second dosing pump；
Being provided with the first spinning pump, the second spinning pump and double spray orifice parallel type filament spinning component in spinning manifold, the discharging opening of the first spinning pump and the second spinning pump charging aperture with double spray orifice parallel type filament spinning components respectively is connected；
Poly-pot bottom is connected by the charging aperture of the first melt pipe and the first spinning pump eventually；
The outlet of drying tower is connected with the import of feed bin, the outlet of feed bin is connected by the import of tremie pipe with spinning screw extruder, tremie pipe is provided with quantifier, and the discharging opening of spinning screw extruder is connected by the charging aperture of the second melt pipe and the second spinning pump；
It is sequentially provided with the first filter, the 3rd dosing pump and the first sound integrated pipeline formula mixing device along melt flows direction on first melt pipe, be sequentially provided with the second filter and the second sound integrated pipeline formula mixing device on second melt pipe along melt flows direction, the structure of the first sound integrated pipeline formula mixing device and the second sound integrated pipeline formula mixing device is identical；
Polylactic acid pre-polymerization mixing device includes the prepolymerization pipe being arranged in vertical, and from top to bottom at least provided with two batch mixing preheaters in prepolymerization pipe, all of equal structure of batch mixing preheater is identical；
Each batch mixing preheater all includes having the first upper conical guide shell of same centrage, the second upper conical guide shell, the first inferior pyramidal guide shell, the second inferior pyramidal guide shell, upper shunting cone cylinder and lower shunting cone cylinder；
nullFirst upper conical guide shell and the first inferior pyramidal guide shell are upper coarse and lower fine and upper and lower permeable structures，First upper conical guide shell bottom diameter is more than the second upper conical guide shell bottom diameter，Second upper conical guide shell and the second inferior pyramidal guide shell are up-thin-low-thick and upper and lower permeable structures，First upper conical guide shell bottom diameter and the second upper conical guide shell upper-end inner diameter are equal，First inferior pyramidal guide shell bottom diameter and the second inferior pyramidal guide shell upper-end inner diameter are equal，First outer, upper conical guide shell upper end、Second outer, upper conical guide shell lower end、First edge, inferior pyramidal guide shell upper end and the second edge, inferior pyramidal guide shell lower end are fixedly connected with at prepolymerization inside pipe wall，The fixing connection in first upper conical edge, guide shell lower end and the second edge, upper conical guide shell upper end，The fixing connection in first upper conical edge, guide shell lower end and the second edge, upper conical guide shell upper end，The fixing connection in first edge, inferior pyramidal guide shell lower end and the second edge, inferior pyramidal guide shell upper end；
Upper shunting cone cylinder is the structure that top sharply blocks, bottom is uncovered, lower shunting cone cylinder is the sharp-pointed closure in bottom, the structure of open top, upper shunting cone cylinder bottom diameter is equal to lower shunting cone cylinder upper-end inner diameter, upper shunting cone cylinder bottom diameter is less than prepolymerization bore, and edge, upper shunting cone cylinder lower end is fixing with edge, lower shunting cone cylinder upper end to be connected；Upper shunting cone cylinder and lower spreader drum outer wall are connected by heating agent conduit and prepolymerization inside pipe wall are fixing；
The upper end of upper shunting cone cylinder is higher than the first edge, upper conical guide shell upper end, and the lower end of lower shunting cone cylinder flushes with the second edge, inferior pyramidal guide shell upper end；
Form circulation road under tube wall melt between upper spreader tube outer surface and the first inferior pyramidal guide shell outer surface, between lower spreader tube outer surface and the first inferior pyramidal guide shell outer surface, form circulation road under blend melt；
Upper spreader tube outer surface is provided with central melt flow dividing structure, and the lower end of central melt flow dividing structure crosses with circulation road lower end under tube wall melt.
Polylactic acid bi-component composite fiber spinning the most according to claim 1 produces equipment, it is characterized in that: the first sound integrated pipeline formula mixing device includes fixed-piping and batch mixing unit, batch mixing unit includes static batch mixing pipeline and the dynamic mixture pipeline of coaxial setting, the left end of dynamic mixture pipeline and the right-hand member Flange joint of static batch mixing pipeline, dynamic screw dividing plate it is provided with in dynamic mixture pipeline, dynamic mixture pipe interior is in axial direction separated into the first semicircle helical duct and the second semicircle helical duct by dynamic screw dividing plate, dynamic screw dividing plate and dynamic mixture inner-walls of duct matched in clearance；Being provided with static ribbon dividing plate in static batch mixing pipeline, static state batch mixing pipeline axially inside direction is separated into the 3rd semicircle helical duct and the 4th semicircle helical duct by static ribbon dividing plate, and static ribbon dividing plate is fixing with static batch mixing inner-walls of duct to be connected；
The plane at the place, both ends of dynamic screw dividing plate and static ribbon dividing plate is each perpendicular to the central axis of dynamic mixture pipeline, center, dynamic screw dividing plate right part is provided with dynamic cone tank, center, dynamic screw dividing plate left part is provided with the most top, center, static ribbon dividing plate right part is provided with static cone tank, center, static ribbon dividing plate left part is provided with static top, and dynamic top left end withstands in static cone tank；
Fixed-piping left end and dynamic mixture pipeline right-hand member Flange joint, be provided with support in fixed-piping, support is provided with stationary center, and stationary center left end withstands in dynamic cone tank.
Polylactic acid bi-component composite fiber spinning the most according to claim 2 produces equipment, it is characterized in that: the quantity of batch mixing unit is more than or equal to two groups, Flange joint between two adjacent groups batch mixing unit, the top left end of static state of one group of batch mixing unit withstands in the dynamic cone tank of adjacent one group batch mixing unit, and fixed-piping is connected with one group of batch mixing unit of low order end.
4. produce equipment according to the polylactic acid bi-component composite fiber spinning described in Claims 2 or 3, it is characterised in that: the length of static batch mixing pipeline is less than the length of dynamic mixture pipeline.
Polylactic acid bi-component composite fiber spinning the most according to claim 1 produces equipment, it is characterized in that: central melt flow dividing structure includes a shunt cylinder and several isocons, shunt cylinder and isocon are each provided in shunting cone cylinder, shunt cylinder open top, edge, shunt cylinder upper end level, isocon is wide at the top and narrow at the bottom, the all isocons of isocon are evenly arranged along upper shunting cone cylinder circumferencial direction, isocon upper end connects with shunt cylinder lower end, and isocon lower port is positioned at circulation road lower end and the outside of circulation road upper end intersection under blend melt under tube wall melt.
Polylactic acid bi-component composite fiber spinning the most according to claim 5 produces equipment, it is characterized in that: above shunting cone cylinder and lower shunting cone cylinder be internally formed preheating cavity, hot circulating fluid medium all it has been passed through in preheating cavity under being internally formed of the first inferior pyramidal guide shell and the second inferior pyramidal guide shell, upper preheating cavity and lower preheating cavity；Heating agent conduit is inner and upper preheating cavity connects, and heating agent external catheter end stretches out outside prepolymerization pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620315032.5U CN205522385U (en) | 2016-04-15 | 2016-04-15 | Two ingredient composite fiber spinning production facilities of polylactic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620315032.5U CN205522385U (en) | 2016-04-15 | 2016-04-15 | Two ingredient composite fiber spinning production facilities of polylactic acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205522385U true CN205522385U (en) | 2016-08-31 |
Family
ID=56792966
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620315032.5U Withdrawn - After Issue CN205522385U (en) | 2016-04-15 | 2016-04-15 | Two ingredient composite fiber spinning production facilities of polylactic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205522385U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105729745A (en) * | 2016-04-15 | 2016-07-06 | 河南省龙都生物科技有限公司 | Spinning production equipment for polylactic acid bi-component complex fibers |
| CN111155180A (en) * | 2020-01-14 | 2020-05-15 | 北京服装学院 | Polylactic acid parallel composite fiber and preparation method thereof |
-
2016
- 2016-04-15 CN CN201620315032.5U patent/CN205522385U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105729745A (en) * | 2016-04-15 | 2016-07-06 | 河南省龙都生物科技有限公司 | Spinning production equipment for polylactic acid bi-component complex fibers |
| CN111155180A (en) * | 2020-01-14 | 2020-05-15 | 北京服装学院 | Polylactic acid parallel composite fiber and preparation method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105734701B (en) | Polylactic acid slice adds titanium dioxide delustring spinning production technology | |
| CN105463588B (en) | Bamboo charcoal polylactic acid melt direct spinning | |
| DE112013007170B4 (en) | Process of melt polycondensation reaction, reactor for the same and its falling film tube | |
| CN205522385U (en) | Two ingredient composite fiber spinning production facilities of polylactic acid | |
| CN1060543C (en) | Method and apparatus for continuous making superhigh molecula polyethylene fibre | |
| CN105714391A (en) | Polylactic acid double-component composite fiber spinning process | |
| CN104258795A (en) | Exchange reaction system, modified polyester production system containing exchange reaction system as well as modified polyester production method | |
| CN105463589B (en) | Bamboo charcoal particles of polylactic acid spinning technique | |
| CN105803565B (en) | PLA delustering fibre direct fabrics production technology | |
| CN105729745B (en) | PLA bi-component composite fiber spinning production equipment | |
| CN108642584A (en) | Combination machine is led in the fine female silk spinning of one kind point | |
| CN105734702B (en) | PLA delustering fibre direct fabrics system | |
| CN205529171U (en) | Polylactic acid delustered fiber direct spinning system | |
| CN105729660B (en) | PLA delustring section production technology | |
| CN205522079U (en) | Polylactic acid extinction section production system | |
| CN205522386U (en) | Titanium dioxide extinction spinning production system is added in polylactic acid section | |
| CN206266759U (en) | A kind of spunbond spinning system of double-component | |
| CN105690702B (en) | Polylactic acid slice adds titanium dioxide delustring spinning production system | |
| CN205329219U (en) | Mixed melt direct spinning system of bamboo charcoal polylactic acid | |
| CN105818291B (en) | PLA delustring section production system | |
| CN107754646A (en) | A kind of cosmetic solution matches mixing arrangement | |
| CN205326047U (en) | Bamboo charcoal polylactic acid section manufacturing system | |
| CN210496191U (en) | Horizontal self-rotating airflow plastic stirring machine | |
| CN105671648B (en) | Bamboo charcoal micropowder polylactic acid slice produces fibre technology | |
| CN205522056U (en) | Polylactic acid pre -polymerization compounding device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20160831 Effective date of abandoning: 20171114 |
|
| AV01 | Patent right actively abandoned |