CN105729745A - Spinning production equipment for polylactic acid bi-component complex fibers - Google Patents
Spinning production equipment for polylactic acid bi-component complex fibers Download PDFInfo
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- CN105729745A CN105729745A CN201610233406.3A CN201610233406A CN105729745A CN 105729745 A CN105729745 A CN 105729745A CN 201610233406 A CN201610233406 A CN 201610233406A CN 105729745 A CN105729745 A CN 105729745A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/25—Component parts, details or accessories; Auxiliary operations
- B29C48/285—Feeding the extrusion material to the extruder
- B29C48/288—Feeding the extrusion material to the extruder in solid form, e.g. powder or granules
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
- B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
- B29C48/00—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor
- B29C48/03—Extrusion moulding, i.e. expressing the moulding material through a die or nozzle which imparts the desired form; Apparatus therefor characterised by the shape of the extruded material at extrusion
- B29C48/05—Filamentary, e.g. strands
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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
- D01D1/00—Treatment of filament-forming or like material
- D01D1/04—Melting filament-forming substances
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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
- D01D1/00—Treatment of filament-forming or like material
- D01D1/06—Feeding liquid to the spinning head
- D01D1/065—Addition and mixing of substances to the spinning solution or to the melt; Homogenising
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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
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- 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
- D01F1/00—General methods for the manufacture of artificial filaments or the like
- D01F1/02—Addition of substances to the spinning solution or to the melt
- D01F1/10—Other agents for modifying properties
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- 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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- D—TEXTILES; PAPER
- D03—WEAVING
- D03D—WOVEN FABRICS; METHODS OF WEAVING; LOOMS
- D03D13/00—Woven fabrics characterised by the special disposition of the warp or weft threads, e.g. with curved weft threads, with discontinuous warp threads, with diagonal warp or weft
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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
- D01D5/28—Formation of filaments, threads, or the like while mixing different spinning solutions or melts during the spinning operation; Spinnerette packs therefor
- D01D5/30—Conjugate filaments; Spinnerette packs therefor
- D01D5/32—Side-by-side structure; Spinnerette packs therefor
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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)
- Manufacturing & Machinery (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
Abstract
Spinning production equipment for polylactic acid bi-component complex fibers comprises a polymerization frame, a drying tower, a material bin, a spinning screw extruder and a spinning manifold; the polymerization frame is sequentially provided with a stirring tank, an initial polymerization tank and a final polymerization tank from top to bottom, the bottom of the stirring tank is connected to the top of the initial polymerization tank through a first conveying pipe, and the first conveying pipe is provided with a polylactic acid pre-polymerization mixing device; a first spinning metering pump, a second spinning metering pump and a double-spraying hole parallel spinning assembly are arranged inside the spinning manifold; a first flux pipeline and a second flux pipeline are each provided with a dynamic-static integrated pipeline type mixing device. According to the spinning production equipment, flux in pre-polymerization pipes can flow downwards at a constant speed, and the temperature of the flux in the pre-polymerization pipes is basically uniform; there is no need to install a mixing system on a conveying pipeline because a plurality of mixing units can be directly arranged on the first flux pipeline, and therefore the cost can be saved, uniform mixing can be realized, and the conveying efficiency and the mixing efficiency can be greatly improved.
Description
Technical field
The invention belongs to polylactic acid spinning production technical field, particularly relate to a kind of polylactic acid bi-component composite fiber spinning and produce equipment.
Background technology
Polylactic acid (PLA) fiber is a kind of degradable biological fiber, the similar polyester fiber of its production method, but, the production process of acid fiber by polylactic very easily degrades, especially drying process, according to knowhow, reach the aridity of spinning technique requirement, polylactic acid dry section (PLA) moisture content must at below 30PPm, according to experiment；The hot air temperature of drying material it is generally required to 100～110 DEG C, 6～8 hours drying times.
Find according to the polylactic acid slice of dry front and back being carried out chemical examination；Polylactic acid reaches more than 1/3rd to dried viscosity drop before drying.Although this illustrates the hydrolytic degradation caused because water content is too high to be avoided to react through the polylactic acid slice of super-dry, but dry run has also significantly caused the degraded of polylactic acid slice.Have a strong impact on the brute force of fiber.
The production of polylactic acid bi-component composite fiber needs the melt of two groups of different molecular weights (melt viscosity), namely；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 more high, 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 poly-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 steadily flow down to from the top 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 place that flow downward is fast, and the temperature of the temperature at prepolymerization tube wall place and prepolymerization tube hub also has difference.And desirably situation is；1, melt flows downward under constant speed state；2, when in prepolymerization pipe, melt flows downward, the tube wall of each aspect is desirably also the same with the solution temperature of prepolymerization tube hub；3, owing to the conveyance conduit being used for carrying polylactic acid after gathering eventually is longer, big especially 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 having influence on spinning quality.For reaching this purpose, need assembling array batch mixing preheater in prepolymerization pipe, to meet the requirement of polymerization technique.
Summary of the invention
The present invention is 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 poly-rear melt course of conveying eventually.
For solving above-mentioned technical problem, the present invention 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, aggregation framework is sequentially provided with agitator tank from top to bottom, just poly-tank and eventually poly-tank, it is connected with just 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, just 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; two spray orifice parallel type filament spinning component in spinning manifold, the discharging opening of the first spinning pump and the second spinning pump is connected with the charging aperture of double; two spray orifice parallel type filament spinning components respectively；
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；
First melt pipe is sequentially provided with the first filter, the 3rd dosing pump and the first sound integrated pipeline formula mixing device along melt flows direction, 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 structure of the sharp-pointed closure in bottom, 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 right-hand member Flange joint of the left end of dynamic mixture pipeline and 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 dynamically 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 be 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 under tube wall melt circulation road lower end and the outside of circulation road upper end intersection under blend melt.
Upper shunting cone cylinder and lower shunting cone cylinder be internally formed preheating cavity, preheating cavity under being internally formed of the first inferior pyramidal guide shell and the second inferior pyramidal guide shell, upper preheating cavity and all passed into hot circulating fluid medium in lower preheating cavity；Heating agent conduit is inner and upper preheating cavity connects, and heating agent external catheter end stretches out outside prepolymerization pipe.
nullAdopt 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，The melt A at prepolymerization tube hub place enters into shunt cylinder along upper shunting cone surface，Melt A flows circulation road lower end and the outside of the intersection of circulation road upper end under blend melt under tube wall melt automatically again through isocon，Meanwhile，Melt B near prepolymerization tube wall enters under tube wall melt in circulation road through the first upper conical guide shell，Stream is positioned at the top of melt A behind circulation road lower end under tube wall melt，Namely melt A and melt B enter under 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 stream export to circulation road lower end under blend melt，Melt B is positioned in the middle of melt A，Namely 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，In transposition process，Melt A and melt B have been also carried out mixing definitely.
In melt mixed transposition process, in upper preheating cavity and lower preheating cavity, all pass into hot circulating fluid medium, hot circulating fluid medium can according to technological requirement add thermal medium as；Biphenyl Ether, heat conduction wet goods, preheat melt, to facilitate control prepolymerization process.The present invention 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.
In the present invention, the technique of direct fabrics after relatively small molecular weight polylactic acid raw material employing polymerization, eliminates the defect that relatively small molecular weight polylactic acid slice is dried rear indirect spinning.First melt pipe arranges the first sound integrated pipeline formula mixing device, 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 time, 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, rarer melt that obtains in the middle of the viscous melt scraped and dynamic mixture pipeline mixes, and push ahead the 3rd semicircle helical duct in static batch mixing pipeline and mix in the 4th semicircle helical duct, enter back into after mixing and in dynamic mixture pipeline, repeat above-mentioned batch mixing process, after some groups of batch mixing unit, enter into the first spinning pump in spinning manifold；
In the present invention, larger molecular weight polylactic acid raw material adopts polylactic acid slice indirect spinning technique, and owing to baking temperature becomes positive correlation with the molecular weight of polylactic acid slice, molecular weight is more high, then can have higher baking temperature, thus improves drying efficiency and effect.First polylactic acid slice being dried, 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 time, 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, rarer melt that obtains in the middle of the viscous melt scraped and dynamic mixture pipeline mixes, and push ahead the 3rd semicircle helical duct in static batch mixing pipeline and mix in the 4th semicircle helical duct, enter back into after mixing and in dynamic mixture pipeline, repeat above-mentioned batch mixing process, 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, two 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, two 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, two spray orifice parallel type filament spinning components, spinneret finally by double, two 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 all in the axial direction for first sound integrated pipeline formula mixing device and the second sound integrated pipeline formula mixing device, thus when pressurized melt is passed through, dynamic screw dividing plate can be driven to rotate；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 improving 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, principle of the invention science, reasonable in design, simple in construction, the melt guaranteed in prepolymerization pipe flows downward under constant speed state, and make melt in prepolymerization pipe when flowing downward the tube wall of each aspect also basically identical with the solution temperature of prepolymerization tube hub, thus meeting 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.The present invention is by after carrying out after poly-lactic acid in high molecular weight chip drying melting, filter, mixing and be transported to double; two spray orifice parallel type filament spinning component and carry out spinning, to be transported to after low molecular weight polymerizable raw material, filtration, mixing in double; two spray orifice parallel type filament spinning component, this pair of spray orifice parallel type filament spinning component is number of patent application is the disclosed technical scheme of the invention of CN201510042184.2 simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention；
Fig. 2 is the structural representation of the present invention 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, the polylactic acid bi-component composite fiber spinning of the present invention produces equipment, including aggregation framework 16, drying tower 18, feed bin 30, spinning screw extruder 32 and spinning manifold 17, aggregation framework 16 is sequentially provided with agitator tank 19 from top to bottom, just poly-tank 20 and eventually poly-tank 21, it is connected with just 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, just it is connected with poly-tank 21 top eventually by the second conveying pipeline 25 bottom 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; two 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 is connected with the charging aperture of double; two spray orifice parallel type filament spinning components 35 respectively；
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；
First melt pipe 28 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, 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 right-hand member Flange joint of the left end of dynamic mixture pipeline 3 and 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 dynamically 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 dynamically 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 be 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 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 the present invention, 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 under tube wall melt circulation road 48 lower end and the outside of circulation road 49 upper end intersection under blend melt.
Upper shunting cone cylinder 46 is internally formed preheating cavity 53 with lower shunting cone cylinder 47, preheating cavity 54 under being internally formed of the first inferior pyramidal guide shell 44 and the second inferior pyramidal guide shell 45, upper preheating cavity 53 and all passed into hot circulating fluid medium in 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.Hot circulating fluid medium in upper preheating cavity 53 is circulated water conservancy diversion by heating agent conduit, and plays the effect supporting location upper shunting cone cylinder 46 and 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 under tube wall melt and the outside of the intersection of circulation road 49 upper end under blend melt automatically again through isocon 52，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，Stream is positioned at the top of melt A behind circulation road 48 lower end under tube wall melt，Namely melt A and melt B enter under 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 stream export to circulation road under blend melt 49 lower end，Melt B is positioned in the middle of melt A，Namely 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，In transposition process，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.
In melt mixed transposition process, in upper preheating cavity 53 and lower preheating cavity 54, all pass into hot circulating fluid medium, hot circulating fluid medium can according to technological requirement add thermal medium as；Biphenyl Ether, heat conduction wet goods, preheat melt, to facilitate control prepolymerization process.The present invention 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.
In the present invention, the technique of direct fabrics after relatively small molecular weight polylactic acid raw material employing polymerization, eliminates the defect that relatively small molecular weight polylactic acid slice is dried rear indirect spinning.nullFirst melt pipe 28 arranges the first sound integrated pipeline formula mixing device 31，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 time，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，Rarer melt that obtains in the middle of the viscous melt scraped and dynamic mixture pipeline 3 mixes，And push ahead the 3rd semicircle helical duct 8 in static batch mixing pipeline 2 and mix in the 4th semicircle helical duct 9，Enter back into after mixing and in dynamic mixture pipeline 3, repeat above-mentioned batch mixing process，After some groups of batch mixing unit，Enter into the first spinning pump 33 in spinning manifold 17；
In the present invention, larger molecular weight polylactic acid raw material adopts polylactic acid slice indirect spinning technique, and owing to baking temperature becomes positive correlation with the molecular weight of polylactic acid slice, molecular weight is more high, then can have higher baking temperature, thus improves drying efficiency and effect.First polylactic acid slice being dried, 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 time，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，Rarer melt that obtains in the middle of the viscous melt scraped and dynamic mixture pipeline 3 mixes，And push ahead the 3rd semicircle helical duct 8 in static batch mixing pipeline 2 and mix in the 4th semicircle helical duct 9，Enter back into after mixing and in dynamic mixture pipeline 3, repeat above-mentioned batch mixing process，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, two 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, two 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, two spray orifice parallel type filament spinning components 35, spinneret finally by double, two 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).
Owing to logical 6 roads of the first semicircle helical duct 5 and the second semicircle spiral are longer and arrange for the hand of spiral all in the axial direction, thus can when pressurized melt be passed through, driving dynamic screw dividing plate 4 rotates；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 improving 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 the spinning production technology of the present invention adopted 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；Meanwhile, the polylactic acid slice of higher molecular weight being sent in drying tower 18 and be dried, dried polylactic acid slice is stored in feed bin 30；
(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 tank 20 poly-at the beginning of the first conveying pipeline 22 drops into, preliminary polymerization operation is temperature is 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 just gathered bottom tank 20, is opened, by the second dosing pump 27 low molecular weight melt dropped into through the second conveying pipeline 25 and be eventually finally polymerized operation in poly-tank 21, final polymerization operation is temperature is 150～280 DEG C, the final time being polymerized operation is 1～6h, and pressure is 0.3MPa；Dry for polylactic acid section 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 gathered eventually bottom 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, and then low molecular weight pdlla melt enters in the first spinning pump 33 in 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 macromolecule polylactic acid melt is mixed；
(5), the polylactic acid melt supercharging of lower molecular weight is sent to double; two 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; two 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; two spray orifice parallel type filament spinning components 35, spinneret finally by double; two spray orifice parallel type filament spinning components 35 sprays, and produces PLA Composite Fiber.
The shape of the present invention, material, structure etc. are not done any pro forma restriction by the present embodiment; every any simple modification, equivalent variations and modification above example made according to the technical spirit of the present invention, belongs to the protection domain of technical solution of the present invention.
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, aggregation framework is sequentially provided with agitator tank, just poly-tank from top to bottom and gathers tank eventually, it is connected with just 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, just 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; two spray orifice parallel type filament spinning component in spinning manifold, the discharging opening of the first spinning pump and the second spinning pump is connected with the charging aperture of double; two spray orifice parallel type filament spinning components respectively；
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；
First melt pipe is sequentially provided with the first filter, the 3rd dosing pump and the first sound integrated pipeline formula mixing device along melt flows direction, 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 structure of the sharp-pointed closure in bottom, 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.
2. polylactic acid bi-component composite fiber spinning 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 right-hand member Flange joint of the left end of dynamic mixture pipeline and 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 dynamically 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.
3. polylactic acid bi-component composite fiber spinning according to claim 2 produces equipment, it is characterized in that: the quantity of batch mixing unit is be 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. the polylactic acid bi-component composite fiber spinning according to Claims 2 or 3 produces equipment, it is characterised in that: the length of static batch mixing pipeline is less than the length of dynamic mixture pipeline.
5. polylactic acid bi-component composite fiber spinning 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 under tube wall melt circulation road lower end and the outside of circulation road upper end intersection under blend melt.
6. polylactic acid bi-component composite fiber spinning 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, preheating cavity under being internally formed of the first inferior pyramidal guide shell and the second inferior pyramidal guide shell, upper preheating cavity and all passed into hot circulating fluid medium in lower preheating cavity；Heating agent conduit is inner and upper preheating cavity connects, and heating agent external catheter end stretches out outside prepolymerization pipe.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108950705A (en) * | 2018-09-14 | 2018-12-07 | 安徽丰原生物材料股份有限公司 | A kind of polylactic acid manifold |
| CN113279085A (en) * | 2021-03-17 | 2021-08-20 | 中国纺织科学研究院有限公司 | Dope-colored fully-stereo composite polylactic acid fiber, preparation method, crystallization behavior testing method, device, storage medium and equipment |
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| WO2011031251A1 (en) * | 2009-09-10 | 2011-03-17 | International Fibers, Ltd. | Apparatus and process for preparing superior carbon fibers |
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