US20080054516A1 - Method for Producing Cellulose Fiber - Google Patents

Method for Producing Cellulose Fiber Download PDF

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Publication number
US20080054516A1
US20080054516A1 US10/565,098 US56509805A US2008054516A1 US 20080054516 A1 US20080054516 A1 US 20080054516A1 US 56509805 A US56509805 A US 56509805A US 2008054516 A1 US2008054516 A1 US 2008054516A1
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Prior art keywords
cellulose
solution
nmmo
kneader
powder
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US10/565,098
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Ik-Hyun Kwon
Soo-myung Choi
Young-Soo Wang
Sung-Ryong Kim
Tae-jung Lee
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Hyosung Corp
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Individual
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Assigned to HYOSUNG CORPORATION reassignment HYOSUNG CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CHOI, SOO-MYUNG, KIM, SUNG-RYONG, KWON, IK-HYUN, LEE, TAE-JUNG, WANG, YOUNG-SOO
Publication of US20080054516A1 publication Critical patent/US20080054516A1/en
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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
    • D01F2/00—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof
    • 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
    • D01D1/02—Preparation of spinning solutions
    • 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
    • D—TEXTILES; PAPER
    • D04—BRAIDING; LACE-MAKING; KNITTING; TRIMMINGS; NON-WOVEN FABRICS
    • D04H—MAKING TEXTILE FABRICS, e.g. FROM FIBRES OR FILAMENTARY MATERIAL; FABRICS MADE BY SUCH PROCESSES OR APPARATUS, e.g. FELTS, NON-WOVEN FABRICS; COTTON-WOOL; WADDING ; NON-WOVEN FABRICS FROM STAPLE FIBRES, FILAMENTS OR YARNS, BONDED WITH AT LEAST ONE WEB-LIKE MATERIAL DURING THEIR CONSOLIDATION
    • D04H1/00—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres
    • D04H1/04—Non-woven fabrics formed wholly or mainly of staple fibres or like relatively short fibres from fleeces or layers composed of fibres having existing or potential cohesive properties, e.g. natural fibres, prestretched or fibrillated artificial fibres
    • D04H1/28—Regenerated cellulose series
    • D—TEXTILES; PAPER
    • D10—INDEXING SCHEME ASSOCIATED WITH SUBLASSES OF SECTION D, RELATING TO TEXTILES
    • D10B—INDEXING SCHEME ASSOCIATED WITH SUBLASSES OF SECTION D, RELATING TO TEXTILES
    • D10B2201/00—Cellulose-based fibres, e.g. vegetable fibres
    • D10B2201/20—Cellulose-derived artificial fibres

Definitions

  • the present invention relates to a method for producing a cellulose solution which is homogeneous at low temperatures, and to fiber produced by the method. More particularly, the invention relates to a production of a cellulose solution which is homogeneous at low temperatures, by dissolving a small amount of the cellulose powder in concentrated liquid-state N-methylmorpholine-N-oxide (NMMO) to lower the solidification temperature of NMMO, introducing the low-temperature, concentrated liquid-state NMMO solution having cellulose dissolved and the cellulose powder into a kneader, mixing and swelling the cellulose in the kneader without a process of reducing pressure to produce a paste, and then supplying the paste into an extruder to dissolve the paste in a homogeneous solution.
  • NMMO concentrated liquid-state N-methylmorpholine-N-oxide
  • the fiber produced from the cellulose solution has excellent tenacity and dimensional stability, and thus can be usefully used for making a single fiber or a filament for clothing, as well as for making an industrial filament fiber or a reinforcing material for rubber products such as a tire and a belt.
  • NMMO N-methylmorpholine-N-oxide
  • the process for production of cellulose fiber using the NMMO solvent is frequently used in the processes for production of cellulose-based products, from the perspectives that the solvent can be all recovered, recycling of the solvent involves a pollution-free process, and the fiber and film thus produced have high mechanical strength.
  • U.S. Pat. No. 3,447,935 discloses the process for production of cellulose fiber using the NMMO solvent.
  • U.S. Pat. Nos. 4,142,913, 4,144,080 disclose manufacturing methods for making cellulose solution by obtaining cellulose solution by under reduced pressure distillation of cellulose that is swelled and dispersed in NMMO hydrates, solidifying the cellulose solution to a precursor (solid-state) by cooling the cellulose solution(a kind if ‘making chips’ and melting in an extruder. These methods simplify the melting process by using an extruder, but require relatively long time and a large amount of energy because of the preceding ‘making chips’ And also, the precursor is hard to protect from heat and humidity.
  • U.S. Pat. No. 5,584,919 discloses a manufacturing method for making cellulose solution by preparing solid-state NMMO comprising 5 to 17% by weight water, feeding the solid-state NMMO with cellulose powder into a horizontal cylinder-type high speed mixer and mixing them to make a granule type precursor, and melting the precursor using an extruder.
  • This method has a disadvantage of a wide distribution of the obtained the precursor and low yield. If the volume of the raw material is larger, the distribution of the obtained precursor is more widened. And a complicated cooling apparatus is required to transfer and store the precursor. And also, the solid-state NMMO is hard to manufacture and store.
  • U.S. Pat. Nos. 5,094,690, 5,534,113 and 5,603,883 disclose a manufacturing method for making cellulose solution by dispersing cellulose in the NMMO comprising 40% by weight water to make slurry, removing the water from the slurry by using a Force-drive type thin-layer distillation apparatus that can form a thin, solution-layer, and obtaining the cellulose solution.
  • These methods have disadvantages of a low efficiency to the volume of the raw material because the slurry was distilled the water and melted by rotating of the rotor so slurry was downstreamed.
  • U.S. Pat. Nos. 5,421,525, 5,456,748, 5,534,113 and 5,888,288 disclose manufacturing methods cellulose solution by mixing pulp crashed into irregular flat type with NMMO comprising 22% by weight water in a horizontal cylinder-type mixer and swelling them, swelling again by stirring for hours in a storage hopper, removing the water form the high viscid solution by using a Force-drive type thin-layer distillation apparatus so as to obtain the melted cellulose solution.
  • These methods have a disadvantage of extra handling and feeding of dust pulp produced as by-product during when crash the pulp into irregular flat type pulp. And also, it is hard to operate the horizontal cylinder-type mixer to discharge the swelled solution.
  • U.S. Pat. No. 5,921,675 discloses a horizontal cylinder-type mixer comprising a conveyor screw at the outlet of the mixer.
  • U.S. Pat. No. 5,948,905 discloses a manufacturing method for making cellulose solution by distilling the water from a mixture of cellulose and NMMO hydrates comprising about 23% by weight.
  • the mixture was distilled under reduced pressure during passing the nozzle having 1.5 to 6.0 millimeter diameter.
  • the first-stage chamber has a small number of nozzles having relatively large diameter.
  • the number of nozzle is increased and the diameter of the hole of the nozzle is decreased so as to increase the cross-sectional area in order to upgrade the efficiency of water vaporization.
  • an extruder is used.
  • This method however, has a disadvantage of needing of a highly complicated apparatus that is composed of many chambers different each other and comprised too many screws for shifting the chambers and distilling stages.
  • PCT WO 1997/47790 discloses a manufacturing method for making cellulose solution by solving cellulose powder in the liquid-state NMMO directly in a twin-screw type extruder.
  • the cellulose solution is produced by feeding the liquid-state NMMO comprising 12% by weight water into the first barrel of the extruder maintaining an inner temperature of 100° C., feeding cellulose powder into the third barrel of the extruder maintaining an inner temperature of 75° C., shifting and mixing them, and obtaining the solution by rising the temperature to 120° C.
  • three barrel of the extruder is used for feeding the cellulose powder and NMMO, and another barrel is required for melting the cellulose.
  • there is a relatively short swelling zone so as to obtain cellulose solution comprising undissolved cellulose particles.
  • this method is effective to proceed relatively small amount of raw material, however, it is not proper to adapt a mass production of cellulose solution because there are too many undissolved moiety. And it is not proper economically because of requiring a lot of filter system. And also, this method has a disadvantage of too short spinning cycle. If the swelling zone of the extruder is increased by increasing the number of blocks and the L/D(length/diameter) of the screw, it is hard to control the swelling condition and the melting condition concurrently because the screws of the extruder are driven by single driving shaft.
  • Korean patent application laid-open publication No. 2002-24689 discloses a manufacturing method for making highly homogenized cellulose solution by obtaining a mixture of swelled cellulose pulp powder and liquid-state NMMO by using the liquid-state NMMO that is overcooled by cooling air and melting the mixture.
  • This method is hard to control the temperature of the overcooled NMMO by using the cooling air and to control the content of the NMMO because of exposing of the moisture contained in the cooling air.
  • the prior arts provided manufacturing methods for making cellulose solution by contacting cellulose with NMMO containing 20 to 40% by weight water firstly, then, distilling the water by using a variety of distillation apparatus, followed by swelling and melting the cellulose.
  • This method however, has a disadvantage of remaining undissolved moiety that caused by melting the cellulose immediately without swelling when the cellulose contacts with the NMMO maintaining at the temperature of 80° C.(the crystallization temperature of NMMO) or more that has too high reaction activation.
  • the holes (hereinafter, referred to as ‘pit’ that penetrate water and the thickness of the cell walls were distributed not uniformly. So, there are some areas that water can penetrate easily and other areas that water can penetrate hardly. And this made some differences to penetrate NMMO in the cellulose in a pre-determined time. And, these tendencies were showed in case of manufacturing pulp from wood fiber according to the kinds of wood fiber and processes used for making pulp. Consequently, to obtain fully homogenized cellulose solution, it is required that the solvent is fully penetrate to the cellulose wholly and swelled the cellulose.
  • Conventional methods for making cellulose solutions have problems such as complicated processes which are disadvantageous in mass production, undesirable addition of purification processes due to cellulose decomposition and NMMO discoloration occurring as the time for production of solution is lengthened, cellulose decomposition due to high temperature, and low homogeneity of the cellulose solution.
  • the NMMO solvent sufficiently penetrates into the macrostructure and the microstructure of cellulose over the entire surface area within a short period of time at a low temperature and a low shear force, thereby the NMMO solvent indefinitely swelling cellulose and then dissolving the cellulose.
  • the present invention solves such conventional problems and, thus provides a homogeneous cellulose solution even at low temperatures and a method for producing cellulose fiber from the cellulose solution.
  • NMMO N-methyl-morpholine-N-oxide
  • the invention is characterized in that when a kneader system is used, complete dissolution does not occur in the kneader, and a paste prepared by mixing and swelling the cellulose or by partially dissolving the cellulose is fed into an extruder, in which only the step of dissolution is carried out. Therefore, according to the invention, a large quantity of solution can be produced in a unit time, compared with the conventional method of using an extruder only, which is constituted of respective compartments for introducing raw materials employing NMMO of high concentration to dissolve cellulose, mixing, swelling, and dissolving.
  • the method of the present invention is advantageous in that a simple mechanical apparatus is used, compared with the conventional method of using a complicated apparatus in which NMMO of low concentration is used to mix and swell cellulose, and then the cellulose is dissolved while the solvent is concentrated by removing water.
  • the method for making a cellulose fiber from a homogeneous cellulose solution comprises the steps of (A) preparing an NMMO solution by dissolving a cellulose powder in concentrated liquid-state N-methylmorpholine-N-oxide (NMMO) to a small amount of 0.01 to 5% by weight; (B) introducing the NMMO solution having a small amount of the cellulose powder dissolved and the cellulose powder into a kneader, subsequently making a paste by mixing and swelling the cellulose in the kneader without reducing pressure, and then feeding the paste into an extruder; (C) spinning the cellulose solution by extrusion through a spinning nozzle, and then solidifying the spun cellulose solution which has passed through an air bed to reach a solidifying bath, to obtain a multifilament; and (D) washing, drying, oil-treating and winding the obtained multifilament.
  • NMMO concentrated liquid-state N-methylmorpholine-N-oxide
  • the liquid-state NMMO having a small amount of cellulose dissolved may be maintained at a temperature of 50° C. to 95° C. in the step (A).
  • the kneader into which the NMMO solution having the small amount of cellulose dissolved and the cellulose powder are introduced may be maintained at 50° C. to 95° C. in the step (B).
  • the NMMO solution at the step (A) may contain moisture in an amount of 10 to 18% by weight of the total weight of the NMMO solution.
  • the final cellulose solution may contain cellulose at a concentration of 5 to 20% by weight of the total weight of the cellulose solution.
  • the liquid-state NMMO having a small amount of cellulose dissolved at the step (B) may be fed to the kneader while being maintained at a temperature of 50° C. to 95° C.
  • the cellulose powder at the step (A) or the step (B) may be mixed with other polymer materials.
  • NMMO NMMO solution having a small amount of the cellulose powder dissolved in concentrated liquid-state NMMO
  • the solidification temperature of the NMMO is lowered, and NMMO can be introduced and mixed in definite amounts at a low temperature, thereby rapid generation of film on the surface of the cellulose powder or powder lumps possibly being prevented.
  • a homogeneous cellulose solution can be produced even at a low temperature, and upon spinning, a low temperature homogeneous cellulose solution can be used to inhibit the property of cellulose undergoing decomposition at high temperatures in the extruder, thus allowing production of cellulose molded articles having excellent flexibility and strength.
  • FIG. 1 is a scheme briefly illustrating the process for producing a homogeneous cellulose solution by dissolving a small amount of the cellulose powder in NMMO of the invention
  • FIG. 2 is a scheme illustrating the entire production process for according to the invention.
  • FIG. 3 is a diagram showing the change behavior of the solidification temperature of NMMO in accordance with the cellulose concentration.
  • FIG. 1 is a scheme briefly illustrating the procedure of the process for producing a homogeneous cellulose solution at a low temperature by dissolving a small amount of cellulose in NMMO according to an embodiment of the present invention.
  • the cellulose powder used in FIG. 1 is obtained by pulverizing by means of a pulverizer equipped with a knife bar, and has a particle size of 5000 mm or less, and more specifically 500 mm or less.
  • a pulverizer equipped with a knife bar When the size of the cellulose powder exceeds 5000 mm, it is difficult to uniformly disperse the cellulose powder, and thus there is a problem that the swelling process requires a long time.
  • a small amount of the cellulose powder having a particle size of 5000 mm or less is first dissolved.
  • the content of the cellulose powder is 0.01 to 5% by weight, and more specifically 0.1 to 3% by weight, with respect to the concentrated liquid-state NMMO.
  • the content of the cellulose powder is less than 0.01% by weight, the effect of the cellulose powder on the lowering of the solidification temperature of NMMO is negligible, thus not contributing to the swellability.
  • the content of the cellulose powder exceeds 5% by weight, the viscosity of the NMMO solution increases, thus the process of mixing and swelling in the kneader requiring a long time.
  • the NMMO solution at a concentration of 20 to 30% by weight is concentrated by a conventional method to produce concentrated liquid-state NMMO having a water content of 10 to 18% by weight.
  • the NMMO solution is concentrated to have a water content of less than 10% by weight, it is economically disadvantageous because of increased costs.
  • the solubility of the cellulose powder may be deteriorated.
  • the NMMO solution having a small amount of the cellulose powder dissolved is introduced into a kneader which has been maintained at 50 to 95° C.
  • the cellulose is mixed and swelled in the kneader without reducing pressure, to form a paste, and then the paste is fed to an extruder, where the paste is dissolved to a homogeneous state to form a homogeneous cellulose solution.
  • the NMMO solution having a small amount of the cellulose powder dissolved can be fed to the kneader by means of a gear pump or a screw type feeder, and is preferably introduced into the kneader by means of a screw type feeder.
  • the content of the cellulose powder in the cellulose solution mixed and swelled in the kneader is adjusted to 5 to 20% by weight, and more specifically 9 to 14% by weight, with respect to the total weight of the liquid-state NMMO solution in accordance with the degree of polymerization of the cellulose polymer.
  • the finally obtained fiber may not have the properties required from fiber.
  • the content of the cellulose powder exceeds 20% by weight, it is difficult to dissolve the cellulose powder in the liquid-state NMMO, and thus a homogeneous solution cannot be obtained.
  • cellulose is mixed and swelled in the kneader without a process of reducing pressure, to form a paste, and then the paste is fed to an extruder, where the paste is dissolved in a homogeneous state to produce a homogeneous solution.
  • the extruder used for this purpose is preferably a twin-screw type extruder, and the twin-screw type extruder may have 3 to 16 barrels or may have the ratio L/D of the screw in the range of 12 to 64.
  • the cellulose powder at the step (A) or step (B) may be mixed with other polymer materials or additives.
  • a polymer material such as polyvinyl alcohol, polyethylene, polyethylene glycol, polymethyl methacrylate or a cellulose derivative, or an additive such as titanium dioxide, silicon dioxide, carbon or ammonium chloride may be mixed into the cellulose solution, in order to impart stability or spinnability to the cellulose solution, or to impart functionality to the final molded product.
  • FIG. 2 is a scheme briefly illustrating the process of the invention for producing a highly homogeneous cellulose solution used for the production of lyocell, and the fiber.
  • a pulp sheet 1 is conveyed by a nip roller 5 to a pulverizer 6 .
  • the pulp sheet 1 is passed through a drying chamber 2 adjusted to a constant temperature and then is cooled by dry air 3 to be maintained at 25° C.
  • the dry temperature of the drying chamber 2 is controlled by a contact-type moisture content measuring device so that the moisture content may not exceed 7%.
  • Commonly supplied pulp has a moisture content of about 8 to 10%.
  • the moisture content of the powdered cellulose stored in a storage tank 10 after pulverization may vary depending on the seasonal changes in humidity and temperature.
  • the particle size of the powdered cellulose can be adjusted according to the size of the screen sieve disposed inside the pulverizer 6 equipped with a knife, and a powder having a size of 5000 mm or less, and more specifically, 500 mm or less, can be favorably used.
  • a powder having a size of 5000 mm or less, and more specifically, 500 mm or less can be favorably used.
  • the particle size of the powder is 5000 mm or greater, aggregation of the pulp may easily occur during the mixing with NMMO in the kneader, and such aggregated pulp may obstruct production of a homogeneous solution.
  • the powdered cellulose passing through the screen sieve of the pulverizer 6 is supplied through a blower system 7 to a backfilter 8 , while air is discharged out, with the powdered cellulose being fed to a powdered cellulose storage tank 10 through a rotary valve 9 .
  • the powdered cellulose is fed into a kneader 25 through a precise weight metering device 11 .
  • the used NMMO that is generated during the process is controlled at a concentration of 20 to 35% by weight in control bath 15 and fed to a purification column 17 , where ionic materials, carbide impurities and the like are removed, and the purified NMMO is stored in the supply tank 18 of a concentration column.
  • the NMMO is supplied in definite amounts from the supply tank of the concentration column sequentially to three falling film concentration columns 19 , and is produced into an aqueous solution of NMMO at a final concentration of 86 to 88% by weight.
  • the concentrated NMMO is fed to a jacketed storage tank 20 which is maintained at 95° C., and the liquid-state NMMO 20 and the cellulose powder 21 are metered to a dissolution tank 22 equipped with a combination mixer for high viscosity dissolution, in order to be produced into an NMMO solution having a small amount of 0.01 to 5% by weight of cellulose powder dissolved.
  • the produced solution is transported to a solution base tank 23 , and is supplied in definite amounts together with the cellulose powder 11 into the kneader 25 through a gear pump 24 .
  • the kneader 25 which is maintained at a desired temperature by heat medium jacketing can be adjusted to a temperature of about 50 to 95° C., and the suitable temperature may vary depending on the concentration of the cellulose dissolved in the introduced NMMO, the molecular weight of the cellulose powder used, and the final cellulose concentration.
  • NMMO When the low-temperature NMMO in which a small amount of cellulose is dissolved and the cellulose powder are mixed and kneaded in the kneader at 50 to 95° C., NMMO penetrates uniformly to the entire area of the cellulose, thereby forming a paste. As the paste is transported forward, the paste makes cellulose to swell and starts to partially dissolve the cellulose. The paste is supplied to a twin screw extruder 26 through a forced transporting device 12 . The internal temperature of the twin-screw type extruder is adjusted in the range of 60° C. to 105° C., and the cellulose in the paste is completely dissolved under the effects of the temperature increase and the shear force.
  • the obtained cellulose solution passes through a filter 27 and then is spun through a nozzle 28 , and the spun cellulose is solidified in solidifying bath 13 , washed in washing bath 14 , and then finally dried to be produced into a cellulose fiber in dryer 29 .
  • a concentration of the used NMMO that is generated during the solidifying and washing process is controlled in control bath 15 , and then the controlled NMMO is fed to the solidifying bath 13 by pump 16 .
  • FIG. 3 is a diagram illustrating the change behavior of the solidification temperature of NMMO in accordance with the cellulose concentration. Referring to FIG. 3 , it can be seen that even if a small amount (about 0.01 to 6%) of cellulose is dissolved, the solidification temperature of NMMO is remarkably lowered from 75° C. to 30° C.
  • a small amount of the cellulose powder is dissolved in concentrated liquid-state NMMO in order to lower the solidification temperature of the NMMO solution.
  • the NMMO solution can be fed to the kneader in the liquid state at a relatively low temperature.
  • the process can be carried out in a wide range of temperature, and also, the cellulose powder and the NMMO solution can be easily mixed and swelled at a low temperature. This prevents generation of film on the surface of the cellulose powder, and eventually, a cellulose solution which is homogeneous even at low temperatures can be produced.
  • a sample of the cellulose solution produced according to the invention was taken from the solution transport line immediately after passing through a kneader and being discharged from a twin-screw type extruder and was subjected to eye observation with a polarized microscope, and then the solubility of the cellulose solution was evaluated.
  • the extent of the dissolved state was classified into 5 grades.
  • the completely dissolved state was rated as Grade ‘1’, while an unspinnable state where a large quantity of undissolved components were present was rated as Grade ' 5 ′.
  • the intermediate grades were classified into Grades 2, 3 and 4 in accordance with the amount of residual undissolved cellulose.
  • the intrinsic viscosity [IV] of the dissolved cellulose is measured as follows. 0.5M cupriethylenediamine hydroxide solution in the range of 0.1 to 0.6 g/dl concentration obtained according to ASTM D539-51T is measured by using an Uberod viscometer at 25 ⁇ 0.01° C. The intrinsic viscosity is calculated from the specific viscosity by using the calculation method of extrapolation and then Mark-Hauwink's equation to obtain the degree of polymerization.
  • Dry strength strength after drying at 107° C. for 2 hours (g/d)
  • a cellulose sheet having a weight average degree of polymerization of 1,200 (V-81 available from Buckeye Technologies) was dried in a drying chamber to have a moisture content of 6.5 to 10%.
  • a cellulose powder having a particle size of 500 mm or less and a moisture content of 3.5 to 7% by weight was produced using a pulverizer equipped with a screen sieve having a mesh size of 500 mm, and liquid-state NMMO concentrated to 87.5% by weight in a falling film concentration column and maintained at 90° C. was produced.
  • liquid-state NMMO concentrated to 87.5% by weight in a falling film concentration column and maintained at 90° C. was produced.
  • 0.001% by weight, with respect to the concentrated liquid-state NMMO of an antioxidant was added and dissolved.
  • the liquid-state NMMO and the cellulose powder were metered into a dissolution tank equipped with a combination mixer for high viscosity dissolution, and a NMMO solution having cellulose powder dissolved to a small amount of 0.01 to 2.5% by weight was produced.
  • the produced NMMO solution was introduced in definite amounts to a kneader whose internal temperature was maintained at 50 to 95° C., by means of a gear pump.
  • the cellulose powder was metered by a precise weight metering device (K-tron feeder) and was introduced to the kneader, so that the final concentration of the cellulose paste was 11% by weight of the total solution.
  • the kneader used herein had a volume of about 30 L, and the speed of the rotating blade was 20 to 30 rpm.
  • the produced paste was transported by force to be fed into a co-rotating twin-screw type extruder.
  • the twin-screw type extruder used had a screw with a diameter of 47 mm(I and the barrel temperature at the initial feeding section was maintained at 60 to 70° C., while the barrel temperature at the final discharge section was maintained at 95 to 105° C.
  • the produced paste was swelled and dissolved, and was fed to a nozzle through a gear pump after passing through a filter.
  • sampling was done from the solution transport line immediately after discharge from the twin-screw type extruder.
  • the cellulose solution was discharged through a nozzle having 1,000 orifices, in which the orifice diameter was 150 mm, and the orifices's interval was 1.5 mm.
  • the length of the air bed was maintained to be 90 mm, and the temperature and relative humidity of the cooling air blown from the air bed to the filament were 25° C. and 45% RH, respectively.
  • the blowing speed was adjusted to 6.5 m/sec.
  • the filament entering a solidifying bath from the air bed was washed, dried, oil-treated and then wound. The fineness of the finally obtained multi-filament was adjusted to 1500 deniers.
  • a cellulose sheet having a weight average degree of polymerization of 850 (V-60 available from Buckeye Technologies) was dried in a drying chamber to have a moisture content of 6.5 to 10%.
  • a cellulose powder having a particle size of 500 mm or less and a moisture content of 3.5 to 7% by weight was produced using a pulverizer equipped with a screen sieve having a mesh size of 500 mm, and liquid-state NMMO concentrated to 87.5% by weight in a falling film concentration column and maintained at 85° C. was produced.
  • liquid-state NMMO concentrated to 87.5% by weight in a falling film concentration column and maintained at 85° C. was produced.
  • 0.001% by weight, with respect to the concentrated liquid-state NMMO of an antioxidant was added and dissolved.
  • the liquid-state NMMO and the cellulose powder were metered into a dissolution tank equipped with a combination mixer for high viscosity dissolution, and a NMMO solution having cellulose powder dissolved to a small amount of 0.1 to 5% by weight was produced.
  • the produced NMMO solution was introduced in definite amounts to a kneader whose internal temperature was maintained at 50 to 95° C., by means of a gear pump.
  • the cellulose powder was metered by a precise weight metering device and was introduced to the kneader, so that the final concentration of the cellulose paste was 13% by weight of the total solution.
  • the kneader used herein had a volume of about 30 L, and the speed of the rotating blade was 20 to 30 rpm.
  • the produced paste was transported by force to be fed into a co-rotating twin-screw type extruder.
  • the twin-screw type extruder used had a screw with a diameter of 47 mm ⁇ and the barrel temperature at the initial feeding section was maintained at 50 to 70° C., while the barrel temperature at the final discharge section was maintained at 95 to 105° C.
  • the produced paste was swelled and dissolved, and was fed to a nozzle through a gear pump after passing through a filter.
  • sampling was done from the solution transport line immediately after discharge from the twin-screw type extruder.
  • the cellulose solution was discharged through a nozzle having 50 orifices, in which the orifice diameter was 150 mm, and the orifices's interval was 2.5 mm.
  • the length of the air bed was maintained to be 60 mm, and the temperature and relative humidity of the cooling air blown from the air bed to the filament were 23° C. and 55% RH, respectively.
  • the blowing speed was adjusted to 7 m/sec.
  • the filament entering a solidifying bath from the air bed was washed, dried, oil-treated and then wound. The fineness of the finally obtained multi-filament was adjusted to 50 to 100 deniers.
  • Example 22 a multi-filament was produced by the same method as that used in Examples 13 to 21 , except that a cellulose sheet having an average weight degree of polymerization of 700 (Buckeye Technologies) was used.
  • Comparative Examples 6 through 8 unlike the Examples, only a twin-screw type extruder was used without using a kneader.
  • liquid-state NMMO at a concentration 86.5% by weight, which was maintained at 95° C. was introduced into a first barrel, and cellulose powder was introduced to a third barrel through a lateral twin-screw type feeder.
  • a cellulose solution was produced by mixing, swelling and dissolving the cellulose, while adjusting the temperature of the twin-screw type extruder.
  • Table 3 in comparison with those of Examples 1 through 22.
  • cellulose is pulverized by controlling the moisture content of a pulp sheet, and a small amount of the cellulose powder is dissolved in concentrated liquid-state NMMO to lower the solidification temperature of the NMMO.
  • an NMMO solution can be fed to a kneader at a relatively low temperature, and the cellulose powder and the NMMO solution can be easily mixed and swelled in the kneader at low temperatures.
  • NMMO solution When only a high-temperature NMMO solution is used, rapid swelling and dissolving at the surface of the cellulose powder or powder lumps may occur during the initial mixing and swelling process, and thus aggregation of the cellulose powder may occur.
  • a homogeneous cellulose solution can be produced even at a low temperature, and upon spinning, a low temperature homogeneous cellulose solution can be used to inhibit the property of cellulose undergoing decomposition at high temperatures in the extruder, thus allowing production of cellulose molded articles having excellent flexibility and strength.
  • pulp having low specific gravity can be easily introduced into a kneader having a high internal space as suggested in the present invention, and thus the output of the solution and the output of the cellulose molded articles can be increased.
  • direct introduction of concentrated NMMO at a concentration of about 86.5% by weight eliminates the need for a separate water evaporating unit utilizing reduced pressure, thus simplifying the structure of the apparatus.
  • the filter exchange interval is shortened.
  • a cellulose paste which has been preliminarily swelled is produced in the kneader and fed to a twin-screw type extruder in a state having the minimum volume, and thus screw arrangement inside the twin-screw type extruder is less stressful. That is to say, insertion of reverse screw elements or kneading discs can be minimized, and thus the residence time distribution for the cellulose solution in the extruder may be made narrow, thus decomposition of the cellulose being prevented.
  • a twin-screw type extruder having high shear force efficiency immediately after the kneader allows reduction of the dissolution time and dissolution temperature, and since reduction of the original degree of polymerization of pulp is minimized, the high molecular weight can be maintained.
  • a cellulose fiber having excellent properties can be produced by the method according to the present invention.

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  • Engineering & Computer Science (AREA)
  • Textile Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • Artificial Filaments (AREA)
  • Processes Of Treating Macromolecular Substances (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
US10/565,098 2004-12-30 2005-12-30 Method for Producing Cellulose Fiber Abandoned US20080054516A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
KR10-2004-0116907 2004-12-30
KR1020040116907A KR100575388B1 (ko) 2004-12-30 2004-12-30 고균질 셀룰로오스 용액 및 이로 부터 제조된 섬유
PCT/KR2005/004677 WO2006071101A1 (en) 2004-12-30 2005-12-30 Method for producing cellulose fiber

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EP (1) EP1841905B1 (ru)
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KR (1) KR100575388B1 (ru)
CN (1) CN100354461C (ru)
AT (1) ATE483044T1 (ru)
DE (1) DE602005023907D1 (ru)
RU (1) RU2362845C2 (ru)
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US20130037635A1 (en) * 2011-08-09 2013-02-14 Anirudh Singh Process for defiberizing pulp
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CN101353824B (zh) * 2008-09-10 2010-06-23 浙江大学 二次加溶剂物理溶解草植物纤维的方法
US20130037635A1 (en) * 2011-08-09 2013-02-14 Anirudh Singh Process for defiberizing pulp
US11866849B2 (en) * 2013-10-29 2024-01-09 Braskem America, Inc. System and method of dosing a polymer mixture with a first solvent, device, system and method of extracting solvent from at least one polymeric yarn, system and method of mechanical pre-recovery of at least one liquid in at least one polymeric yarn, and continuous system and method for producing at least one polymeric yarn
US20240026571A1 (en) * 2013-10-29 2024-01-25 Braskem America, Inc. System and method of dosing a polymer mixture with a first solvent, device, system and method of extracting solvent from at least one polymeric yarn, system and method of mechanical pre-recovery of at least one liquid in at least one polymeric yarn, and continuous system and method for producing at least one polymeric yarn
US10883196B2 (en) 2014-01-03 2021-01-05 Lenzing Aktiengesellschaft Cellulose fiber
CN116120597A (zh) * 2019-10-17 2023-05-16 武汉纺织大学 一种nmmo醇溶液快速溶解纤维素的方法
CN111892718A (zh) * 2020-06-22 2020-11-06 中国纺织科学研究院有限公司 一种干法溶解纤维素的方法
TWI826882B (zh) * 2021-01-04 2023-12-21 日商旭化成股份有限公司 纖維素纖維之製造方法及纖維素纖維
CN112779612A (zh) * 2021-01-07 2021-05-11 杭州融凯盛科技有限公司 一种莱赛尔纤维的高效生产制造方法及设备
CN115182096A (zh) * 2022-05-27 2022-10-14 杭州诺邦无纺股份有限公司 一种纤维素长丝非织造材料及其制备方法
CN115323501A (zh) * 2022-06-30 2022-11-11 武汉纺织大学 加工Lyocell纤维纺丝原液的成膜蒸发器和方法

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EP1841905B1 (en) 2010-09-29
RU2362845C2 (ru) 2009-07-27
TWI310386B (ru) 2009-06-01
ATE483044T1 (de) 2010-10-15
JP2006188806A (ja) 2006-07-20
JP4210285B2 (ja) 2009-01-14
WO2006071101A1 (en) 2006-07-06
EP1841905A1 (en) 2007-10-10
TW200626617A (en) 2006-08-01
CN100354461C (zh) 2007-12-12
RU2007124513A (ru) 2009-02-10
KR100575388B1 (ko) 2006-05-03
DE602005023907D1 (de) 2010-11-11
EP1841905A4 (en) 2009-08-19

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