EP0617742B1 - Dispositif et procede de production de matieres fibreuses a base d'amidon - Google Patents

Dispositif et procede de production de matieres fibreuses a base d'amidon Download PDF

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Publication number
EP0617742B1
EP0617742B1 EP93922545A EP93922545A EP0617742B1 EP 0617742 B1 EP0617742 B1 EP 0617742B1 EP 93922545 A EP93922545 A EP 93922545A EP 93922545 A EP93922545 A EP 93922545A EP 0617742 B1 EP0617742 B1 EP 0617742B1
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Prior art keywords
starch
starch material
chamber
section
solution
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German (de)
English (en)
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EP0617742A1 (fr
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Catia Bastioli
Bruno Casale
Gino Zanardi
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Cerestar Holding BV
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Cerestar Holding BV
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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
    • D01F9/00—Artificial filaments or the like of other substances; Manufacture thereof; Apparatus specially adapted for the manufacture of carbon filaments
    • 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
    • D01D5/40—Formation of filaments, threads, or the like by applying a shearing force to a dispersion or solution of filament formable polymers, e.g. by stirring

Definitions

  • the present invention refers to a device and process for production of fibrous starch materials particularly destined for use in the production of paper and cardboard.
  • aqueous colloid dispersions of starch in typical concentrations of between 5 and 40% by weight of anhydrous solid, is brought into contact with non-solvents (for example a saline solution of ammonium sulphate), it coagulates forming flakes of gel.
  • non-solvents for example a saline solution of ammonium sulphate
  • US-A-4,243,480 describes such a process.
  • GB-A-2258251 describes a process for producing a starch pulp comprising jet cooking an aqueous starch suspension, injecting this into a primary flux of a coagulating agent to obtain the pulp and subjecting the pulp to maturing in its own mother liquors.
  • US Patent No. 4,340,442 describes a process for the formation of fibrils which, in order to improve the hydrophobic properties of the fibrils, uses starch insoluble in water having a high amylose content (50-80% by weight), which is coagulated in a saline solution, in particular ammonium sulphate.
  • Said starch which is substantially insoluble in water requires a stage in which it is dissolved in alkaline solution which causes problems in the coagulation stage and problems with respect to disposal of sulphates different from ammonium salts, which are formed in said stage.
  • US Patent No. 4,139,699 describes a process for the production of a product having starch fibre morphology, through extrusion of a colloidal starch dispersion having a high amylopectin content in a coagulating agent.
  • a starch having a amylopectin content of less than approximately 95% it is necessary to chemically modify the starch to ensure the colloidal dispersion thereof in the aqueous system or, alternatively, the starch must be dissolved in the presence of alkaline hydroxides.
  • alkaline hydroxides particularly sodium hydroxide
  • the use of alkaline hydroxides, particularly sodium hydroxide makes the industrial application of the process described difficult, in that the coagulation stage carried out using ammonium sulphate results in the production of ammonia and formation of large quantities of sodium sulphate preventing coagulation and causing problems with respect to disposal.
  • US Patent No. 4,243,480 describes a process that uses the product obtained according to the process described in US Patent No. 4,139,699, for the production of paper or cardboard according to conventional paper making technology.
  • Said product has a short fibre morphology having a diameter of between 10 and 500 microns and a length of between 0.1 and 3 mm, obtained by extruding the starch dispersion via a die into a moving coagulation bath.
  • US Patent No. 4,853,168 describes a process of the type described in US Patent No. 4,139,699, in which the colloidal starch dispersion adapted to be extruded is obtained by cooking an aqueous starch dispersion containing the coagulating saline solution.
  • the object of this invention is a process for the preparation of fibres of starch material which comprises preparing an aqueous dispersion or solution of starch material and extruding this into a solution of a saline coagulating agent characterised in that the aqueous dispersion or solution of starch material is extruded through a microporous tubular wall of a chamber circularly ringed with said microporous wall into an annular change through which the solution of coagulating agent is caused to flow whereby the contact of the flowing coagulating agent solution with the extruded starch material dispersion or solution coagulates the starch material to form a fibrous structure.
  • Another object of the invention is a fibre making device characterised by the fact that it comprises:
  • 1 indicates a stirred dispersion for the preparation of the starch suspension in water with a dry weight typically from 5 to 50% by weight and preferably 10-40% by weight.
  • the starch used for the preparation of the suspension is preferably natural starch such as starch from maize, rice, tapioca, potato having a amylopectin content from 30 to 100%. Particularly prefered is maize starch, widely available on the market, having a typical amylopectin content of from 64-80% by weight.
  • starch with a high content of amylose, such as amylomaize and chemically or physically modified starch can be used.
  • the starch suspension can also contain additives such as salts (e.g. saline coagulating agents as described in US Patent No. 4,853,168) alkaline agents, organic fillers or minerals, crosslinking agents, plasticisers, polyoxyethylene, polyvinyl alcohol, ionomeric polymers such as copolymers of ethylene and acrylic acid and/or maleic anhydride, polyacrylates, polyamides, lubricants such as lecithin, fatty acids, esters and amides of fatty acids.
  • salts e.g. saline coagulating agents as described in US Patent No. 4,853,168
  • alkaline agents organic fillers or minerals
  • crosslinking agents plasticisers
  • polyoxyethylene polyvinyl alcohol
  • ionomeric polymers such as copolymers of ethylene and acrylic acid and/or maleic anhydride
  • polyacrylates polyamides
  • lubricants such as lecithin, fatty acids, esters and amides of fatty acids.
  • the jet cooking process is known per se and involves instantaneous heating of the aqueous suspension with process steam and then maintaining the heated liquid for a predetermined period.
  • the cooking temperature generally between 90 and 180°C, is selected according to the specific starch used in the course of the process. In particular, care should be taken to avoid an excessively high temperature causing degradation of the starch material, while ensuring that the temperature, the shearing time applied and the standing time are such that it is possible to obtain a dispersion close to complete gelation.
  • the starch dispersion or solution subject to cooking is collected whilst stirring in a lined stirred reactor 4, water circulating at a temperature of about 100°C in the casing thereof.
  • a flash is effected in this lined tank in order to free the excess steam and to return the starch/water concentrations close to the initial concentrations.
  • the starch is pumped via a pump 5, in a heat exchanger 6 where it is brought to a temperature of between 20 and 100°C, preferably from 40 to 70°C. From the heat exchanger, the starch is fed to a fibre making device of the types illustrated in figures 2 and 3, described in the following, in which a saline coagulating solution is also injected.
  • the salts that can be used in the scope of the present invention comprise ammonium sulphate, magnesium sulphate, aluminium sulphate, ammonium phosphate, potassium chloride, sodium sulphate, sodium carbonate, sodium bicarbonate, and ammonium chloride.
  • the preferred saline solution is a saturated solution of ammonium sulphate, although it is not necessary to reach saturated levels of the above mentioned salts and it is equally possible to use concentrations lower than saturation levels.
  • the starch fibres obtained from the fibre making device are collected in a stirred reactor 8 in order to be subjected to maturing and subsequently decanting. Once the decanting has been effected the clarified substance is recycled, by means of a pump 9, and mixed with a saturated saline solution of the coagulating agent before being reused for drawing the starch.
  • the clarified substance which circulates in the installation as a coagulating agent contains the saline solution and the finest fibres which, due to their small dimensions are not decanted in the collecting container.
  • the mass of fibres from reactor 8 is pumped by means of pump 10 on to filter 11.
  • the fibres are then collected in a container 12, while the filtrate is fed to container 13 where it is mixed with the clarified substance from pump 9, with subsequent addition of sulphate in order to recycle the saline solution adapted to be fed into fibre making device 7.
  • the fibre making device 7 in the embodiement in figure 2, comprises a tubular body 14 having at least one inlet 15 which, under normal conditions, is used for feeding the starch material, an inlet 16 designed to feed the coagulating agent and a outlet 17 for discharging the starch fibres produced after the coagulation.
  • the starch material is immersed in a tubular duct 18 which partially terminates in a wall 19 supplied with radial holes.
  • the holey wall part 19 acts as the distributor of the starch material flow towards a feeding chamber 21.
  • the tubular element with microporous walls suitable for extruding the starch material from the feeding chamber 21 into the annular chamber 23 coaxially thereto is indicated.
  • the chamber 23 is separated from the radially external surface of the element 22 and the radially internal surface of body 14.
  • the tubular element 22 can consist of a body of porous sintered metal material in which the distribution of the porous dimension is preferably comprised between 10 and 500 microns.
  • the tubular element 22 is a body of metal material, for example stainless steel, provided with a number of radially passing holes obtained by mechanical working and having at least a narrow flow section with openings having a dimension preferably comprised between 10 and 500 microns.
  • said radial holes have a cross section as illustrated in figure 4 with a portion 24 of the inlet for the starch material having a narrow opening, typically from 10 to 500 microns, and a portion 25 on the outlet of the starch material with an larger size opening, preferably comprised between 0.5 and 1.5 mm.
  • the opening density on the extrusion surface (intended as the surface of the tubular element in contact with the coagulating agent), expressed as a ratio of number of holes to surface area is preferably comprised between 4 and 0.05 holes/mm 2 .
  • the coagulating agent fed through the inlet opening 16 flows through the annular element 26 having a crown of axial holes 27, acting as distributor, and is fed into the first annular chamber 28 defined by the walls 14 of the fibre making device and a tubular element coaxial to the body 29. From chamber 28 the flow is fed into the annular chamber of outlet 23, parallel to the radially external surface of the microporous tubular element 22, where the flow of coagulating agent interacts with the extrusion flow of the starch material.
  • the starch material is extruded in the form of a variety of threads which surround the extrusion surface in the guise of a tubular film.
  • the flow speed of the saline coagulating agent in the annular section of the outlet chamber 23 is maintained between 1 and 15 m/s.
  • the drawing ratio intended as ratio of flow speed of the coagulating agent in the annular section of the chamber 23 and the speed of the starch material at the outlet of the holes of the microporous wall (defined as the ratio between the flow rate of the starch material and the total section in the holes of the outlet) is generally comprised between 1-1000, preferably between 100-1000.
  • the axial length of the outlet chamber 23 is such that a stay time of the starch material comprised between 5 and 15 milliseconds is obtained. In any case the axial length of the chamber 23 in which the starch material undergoes drawing must be such to cause an orientation of the starch material allowing at the same time a complete phase inversion.
  • the flow of starch materials is fed through an inlet 31 to an annular chamber 32 defined by the walls of body 14 and the microporous walled tubular element 33.
  • the flow of the starch material follows the radial direction towards the inside through the walls of element 33 into the annular outlet chamber 34 comprised between the tubular element 33 and a central nucleus 35 coaxial to the body.
  • the flow of the coagulating agent is fed across an inlet 36 and into a prechamber 37, it flows into a chamber 40 across holes 39 of an annular element 38 and from chamber 40 is fed to the outlet chamber 34 having a narrow cross section in the flow direction.
  • the section of holes of the microporous element 33 remains the same as figure 4. In this case, however, the flow of the starch material advances from a bigger to a smaller cross section, which brings an increase in the starch flow speed and necking down of the starch threads.
  • the material leaving the holes is coagulated by the coagulation agent flow in the annular chamber 34. It has been observed that the best conditions of coagulation are when the drawing ratio is comprised preferably between 1 and 150, with an emission speed of the starch material from the holes in the microporous walls 33 comprises preferably between 0.1 and 1 m/s.
  • the fibre making device subject of the present invention presents notable advantages such as:
  • starch fibres were obtained having the following size distribution measured according to the Bauer McNett apparatus expressed in percent by weight: 595 ⁇ m (28 mesh)% 0.3 297 ⁇ m (40 mesh)% 3.1 149 ⁇ m (100 mesh)% 68.5 74 ⁇ m (200 mesh)% 21.3 above 200 mesh X 100 6.8
  • the dispersion obtained is filtered on Bruckner with a diameter of 30 cm in the presence of a paper filter under vacuum of 10 mm Hg.
  • the liquid is filtered twice on the same panel.
  • the panel is then washed with 500 ml of H 2 O.
  • the ratio of starch to water in the washing is 1:10.
  • the solubility determination is carried out on the filtered product, in order to separate it from the water and washed to remove the coagulant.
  • the product is dispersed in water in a conventional laboratory pulper (dry concentration 0.2% rotation speed 3000 rpm); a sample was removed after 4 hours and after filtered on a 8 micron filter paper, the starch is measured in solution with the reagent "ANTHRONE" (solution 0.2% of ANTHRONE in 96% H 2 SO 4 ).
  • the solubility value determined by the above cited method on the filter panels obtained according to the example, is less than 1.5%.
  • the test according to example 1 has been repeated varying only the characteristics of the microporous sintered filter consisted, in this case of a sintered metal tube with pores having an average diameter of 100 ⁇ m. Fibres were obtained having the following size distribution expressed in terms of percentage by weight: 595 ⁇ m (28 mesh)% : 0.3 297 ⁇ m (40 mesh)% : 0.9 149 ⁇ m (100 mesh)% : 63 74 ⁇ m (200 mesh)% : 25.2 above 200 mesh X 100 : 10.6
  • solubility values obtained according to the method of example 1 are once again less than 1.5% like in the preceding case.
  • the characteristics of the fibres obtained by the test in example 1 are compared to the fibrids obtained with the other fibre making devices, in particular ejector and spinneret.
  • the process conditions are the same as for example 1.
  • the first fibre making device consists of an ejector equipped with 8 holes in a 1 mm diameter, for the starch inlet with an inclination of 45° with respect to ejector axis placed in the groove.
  • the speed of the coagulating agent (ammonium sulphate) in the thinner section is equal to 31 m/s and the draw ratio, (defined as the ratio between the maximum speed of the sulphate to that of the starch leaving the holes) is equal to 47.
  • the second fibre making device consists of a spinneret equipped with 113 holes having a diameter of 0.5mm; this spinneret is placed in a circular duct and the annular crown separated from the external surface of the spinneret and the internal walls of the circular duct is fed with the coagulating agent, ammonium sulphate: the speed of the ammonium sulphate and that of the starch material exiting the holes are parallel.
  • the starch material is contacted with the coagulating agent; the suspension formed then enters in a convergent (having a minimum diameter of 4 mm which corresponds to a sulphate speed of 30 m/s) in which the high turbulence completes the coagulation.
  • Table 1 reports the comparison of the fibre distribution for the various products; as can be noted, with the ejection fibres there is a high percentage of fine particles (80%) which reduces when passing to the spinneret and the tubular.
  • the distribution curve is also different for these two fibre making device: very narrow for the tubular (90% of the particles between 100 and 200 mesh), larger for the spinneret.
  • Table 2 reports the percentage of starch retained on the sheet of paper prepared in the laboratory with the Rapid-Koethen apparatus, after dispersion of the cellulose - starch material paste (at 10 % of the latter) in the pulper for 2 hours at 3000 rpm at ambient temperature. As noted the highest retention is with the product from the tubular fibre making device.
  • Table 3 finally highlights the behaviour of the two different products when filtered from the slurry after the coagulation and washing until the ammonium sulphate has been eliminated, the concentrations of the slurry and the maturing time being equal.
  • the products obtained from the tubular fibre making device show a double productivity with respect to those of the spinneret.
  • starch fibres obtainable through the previously described method that present the characteristic of having a solubility of less than 2% and a dimension distribution as such of 90% has a dimension such as to enter in the range of from 100 to 200 mesh, after classification by the Bauer-McNett apparatus.
  • Fibre making device Distribution (% w/w) 28 50 100 200 >200 spinneret 0.1 7.6 35.3 31.0 26 ejector 0.3 0.4 4.2 14.6 80.5 tubular 0.3 3.1 68.5 21.3 6.8 Retention of starch fibres/fibrids in the paper Fibre making device Retention % Spinneret 87.5 Ejector 77 Tubular >99 Filtering capacity of various starch fibres/fibrids Fibre making device Filtered solid (Kg/h) tubular 20 spinneret 10

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Textile Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Chemical & Material Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Artificial Filaments (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
  • Paper (AREA)
  • Yarns And Mechanical Finishing Of Yarns Or Ropes (AREA)

Claims (14)

  1. Procédé pour la préparation de fibres d'une matière de type ou à base d'amidon ou de fécule, ce procédé comprenant la préparation d'une dispersion ou solution aqueuse d'amidon ou de fécule et l'extrusion de cette dispersion ou solution dans une solution d'un agent salin de coagulation, procédé caractérisé en ce que la dispersion ou solution aqueuse de la matière du type ou à base d'amidon ou de fécule est extrudée à travers une paroi tubulaire microporeuse d'une chambre entourée circulairement par ladite paroi microporeuse dans une chambre annulaire à travers laquelle la solution de l'agent de coagulation est obligée de s'écouler, de sorte que le contact de la solution d'agent de coagulation en circulation avec la dispersion ou solution de la matière de type ou à base d'amidon ou de fécule extrudée coagule la matière de type ou à base d'amidon ou de fécule pour former une structure fibreuse.
  2. Procédé selon la revendication 1, dans lequel la dispersion ou solution aqueuse de la matière à base ou du type amidon ou fécule est extrudée à travers une paroi microporeuse qui présente des trous ayant au moins une section d'un diamètre moyen compris entre 10 500 micromètres, et qui a une densité de trou(s) dans la surface d'extrusion comprise entre 4 et 0,05 trou/mm2.
  3. Procédé selon la revendication 2, dans lequel la dispersion ou solution aqueuse de matière de type ou à base d'amidon ou de fécule est extrudée à travers une paroi tubulaire microporeuse ayant une section d'entrée étroite et ayant une taille d'ouverture de 10 à 500 micromètres dans une sortie plus large ayant une taille d'ouverture ou une lumière supérieure à ladite section étroite, le rapport ou taux d'étirage étant compris entre 100 et 1000.
  4. Procédé selon la revendication 2, dans lequel la solution ou dispersion aqueuse de matière de type ou à base d'amidon ou de fécule est extrudée à travers une paroi tubulaire microporeuse ayant une section d'entrée étroite et ayant une taille d'ouverture ou lumière de 10 à 500 micromètres et qui est inférieure à la taille d'ouverture de ladite section plus grande, procédé dans lequel le rapport ou taux d'étirage est compris entre 1 et 150.
  5. Procédé selon l'une quelconque des revendications 1 à 4 précédentes, dans lequel le temps de séjour de la matière de type ou à base d'amidon ou de fécule dans ladite chambre annulaire est compris entre 5 et 15 millisecondes.
  6. Dispositif de production de fibres, en particulier pour la production de fibres d'amidon ou de fécule par extrusion d'un courant de matière de type ou à base d'amidon ou de fécule dans un agent coagulant en écoulement, dispositif caractérisé en ce qu'il comprend:
    un corps tubulaire (14) comprenant un premier moyen d'entrée (15, 31) pour l'introduction du flux de la matière de type ou à base d'amidon ou de fécule;
    une chambre d'alimentation en la matière de type ou à base d'amidon ou de fécule (21, 32) connectée audit premier moyen d'entrée;
    une chambre annulaire de sortie (23, 34) de la matière du type ou à base d'amidon ou de fécule;
    un élément tubulaire (22, 33) comportant des parois poreuses disposées coaxialement avec ladite chambre de sortie (23, 34) et interposé entre cette chambre et la chambre d'alimentation (21, 32), cet élément convenant pour une extrusion à travers lesdites parois poreuses dans ladite chambre de sortie de divers fils de matière à base d'amidon ou de fécule;
    un second moyen d'entrée (16, 36) reliant ladite chambre de sortie pour introduire un courant d'agent de coagulation; et
    un moyen de décharge (17, 30) disposé en aval de la chambre annulaire de sortie et relié à cette chambre.
  7. Dispositif de production de fibres selon la revendication 6, caractérisé en ce que ledit élément tubulaire comportant une paroi poreuse (22, 33) est constitué d'un métal fritté ayant des pores présentant une distribution des tailles comprise entre 10 et 500 micromètres.
  8. Dispositif de fabrication de fibres selon la revendication 6, caractérisé en ce que ledit élément tubulaire (22, 33) comportant une paroi microporeuse est un élément cylindrique présentant des parois foraminées ayant plusieurs trous (24, 25) passant radialement et ayant au moins une section étroite de dimension comprise entre 10 et 500 micromètres.
  9. Dispositif selon la revendication 7 ou 8, dans lequel lesdits pores présentent, par rapport à la surface d'extrusion, une densité surfacique de 4 à 0,05 trou/mm2.
  10. Dispositif de fabrication de fibres selon la revendication 8, dans lequel ladite chambre annulaire de sortie (23) de la matière de type ou à base d'amidon ou de fécule est coaxiale et radialement externe par rapport à ladite chambre d'alimentation (21).
  11. Dispositif selon la revendication 10, dans lequel lesdits trous radiaux comprennent un tronçon ou une section (24) en liaison avec la chambre d'alimentation (21), ayant une taille d'ouverture ou lumière comprise entre 10 et 500 micromètres et un tronçon ou section (25) de liaison avec ladite chambre de sortie ayant une taille d'ouverture ou lumière plus grande que la taille de l'ouverture de ladite section ou dudit tronçon (24).
  12. Dispositif selon la revendication 8, dans lequel ladite chambre annulaire (34) de sortie est coaxiale et radialement intérieure par rapport à ladite chambre (32) d'alimentation.
  13. Dispositif selon la revendication 12, dans lequel lesdits trous radiaux comprennent un tronçon ou une section (24) de liaison avec la chambre de sortie (34) ayant une taille d'ouverture ou lumière comprise entre 10 et 500 micromètres et un tronçon ou section (25) de liaison avec la chambre d'alimentation (32) ayant une taille d'ouverture ou lumière plus grande que la taille d'ouverture de ladite section ou dudit tronçon (24).
  14. Fibres de fécule ou d'amidon, obtenues à l'aide d'un procédé selon l'une quelconque des revendications 1 à 5, ayant une solubilité inférieure à 2% et une distribution de taille telle que 90% des fibres ont une dimension leur permettant de pénétrer dans les mailles d'une toile de tamis numéro 100 à 200, après classification par l'appareil de Bauer-McNett.
EP93922545A 1992-10-16 1993-10-11 Dispositif et procede de production de matieres fibreuses a base d'amidon Expired - Lifetime EP0617742B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
ITTO920837A IT1256971B (it) 1992-10-16 1992-10-16 Dispositivo e procedimento per la produzione di fibre di materiale amidaceo.
ITTO920837 1992-10-16
PCT/EP1993/002782 WO1994009190A1 (fr) 1992-10-16 1993-10-11 Dispositif et procede de production de matieres fibreuses a base d'amidon

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EP0617742A1 EP0617742A1 (fr) 1994-10-05
EP0617742B1 true EP0617742B1 (fr) 1998-01-21

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EP (1) EP0617742B1 (fr)
JP (1) JP3345013B2 (fr)
AT (1) ATE162561T1 (fr)
AU (1) AU669225B2 (fr)
BR (1) BR9305678A (fr)
CA (1) CA2125977C (fr)
DE (1) DE69316585T2 (fr)
DK (1) DK0617742T3 (fr)
ES (1) ES2111186T3 (fr)
FI (1) FI102772B (fr)
IT (1) IT1256971B (fr)
NO (1) NO942255D0 (fr)
RU (1) RU2113559C1 (fr)
WO (1) WO1994009190A1 (fr)

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DE4409465A1 (de) * 1994-03-19 1995-09-21 Kinkel Werner Helmut Biologisch abbaubare Vliese und Vliesverbundmaterialien
EP2246472A1 (fr) 2009-03-24 2010-11-03 Mondi Limited South Africa Procédé pour la préparation de particules de gel de polysaccharides et fourniture de pâte pour la fabrication de papier
BR112015008315B1 (pt) * 2012-10-22 2021-11-16 Innventia Ab Método de fibras de fiação ou extrusão
GB2518199A (en) * 2013-09-13 2015-03-18 Xiros Ltd Method of producing a swellable polymer fibre
BR112017023152B1 (pt) 2015-04-28 2023-02-23 Spinnova Oyj Método e sistema para fabricar fios fibrosos

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US2988782A (en) * 1958-12-09 1961-06-20 Du Pont Process for producing fibrids by precipitation and violent agitation
US4205025A (en) * 1975-12-22 1980-05-27 Champion International Corporation Synthetic polymeric fibrids, fibrid products and process for their production
US4243480A (en) * 1977-10-17 1981-01-06 National Starch And Chemical Corporation Process for the production of paper containing starch fibers and the paper produced thereby
IT1249972B (it) * 1991-07-31 1995-03-30 Ferruzzi Ricerca & Tec Polpa d'amido, procedimento per la sua preparazione e suo impiego nella fabbricazione di carta e cartone.

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FI942851A0 (fi) 1994-06-15
FI102772B1 (fi) 1999-02-15
FI942851A (fi) 1994-06-15
ITTO920837A1 (it) 1994-04-16
NO942255L (no) 1994-06-15
FI102772B (fi) 1999-02-15
DE69316585D1 (de) 1998-02-26
IT1256971B (it) 1995-12-27
BR9305678A (pt) 1994-11-22
JPH07502312A (ja) 1995-03-09
CA2125977A1 (fr) 1994-04-28
AU5150693A (en) 1994-05-09
ES2111186T3 (es) 1998-03-01
RU2113559C1 (ru) 1998-06-20
CA2125977C (fr) 2003-09-30
NO942255D0 (no) 1994-06-15
DE69316585T2 (de) 1998-04-23
DK0617742T3 (da) 1998-03-30
ITTO920837A0 (it) 1992-10-16
AU669225B2 (en) 1996-05-30
ATE162561T1 (de) 1998-02-15
JP3345013B2 (ja) 2002-11-18
WO1994009190A1 (fr) 1994-04-28
EP0617742A1 (fr) 1994-10-05

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