EP0884415B1 - Verfahren zum Waschen von Zellstoff beim Bleichen - Google Patents

Verfahren zum Waschen von Zellstoff beim Bleichen Download PDF

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EP0884415B1
EP0884415B1 EP98113684A EP98113684A EP0884415B1 EP 0884415 B1 EP0884415 B1 EP 0884415B1 EP 98113684 A EP98113684 A EP 98113684A EP 98113684 A EP98113684 A EP 98113684A EP 0884415 B1 EP0884415 B1 EP 0884415B1
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Prior art keywords
washer
bleaching
stage
pulp
recited
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French (fr)
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EP0884415A1 (de
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Kaj Henricson
Bertil Stromberg
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Andritz Oy
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Andritz Oy
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1026—Other features in bleaching processes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/02—Washing ; Displacing cooking or pulp-treating liquors contained in the pulp by fluids, e.g. wash water or other pulp-treating agents
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1026—Other features in bleaching processes
    • D21C9/1036—Use of compounds accelerating or improving the efficiency of the processes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1026—Other features in bleaching processes
    • D21C9/1042—Use of chelating agents
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1057—Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
    • D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/16—Bleaching ; Apparatus therefor with per compounds
    • D21C9/163—Bleaching ; Apparatus therefor with per compounds with peroxides

Definitions

  • the present invention relates to a method of washing pulp in connection with bleaching.
  • the invention is especially related to ozone bleaching of pulp without preceding removal of heavy metals.
  • Typical bleaching sequences by which pulp has earlier been bleached are, for example, OOAZEZPZ, OAZEZPZ, OOAZEZP and OAZEZP. These sequences thus include one or more oxygen bleaching stages (O), an A-stage (acid washing), an ozone stage (Z), an extraction stage (E), a second ozone stage (Z) and a peroxide stage (P), and possibly a third ozone stage (Z).
  • the extraction stage (E) may be an oxidizing peroxide extraction stage or a conventional oxidizing extraction stage.
  • the ozone bleaching stages are preferably carried out with pulp having the consistency of about 5-18%.
  • washing stages in other words bleaching stages alternate with washing stages, i.e. washers, by which the chemicals separated from the fibers as reaction products or otherwise in each bleaching stage are removed from the suspension. Since the washers form a considerable part of the investment costs in a bleaching plant, the number of the washers should, of course, be limited as much as possible, if it is only possible without risking the quality of the final product.
  • EP-A-0 426 652 discloses several bleaching sequences where ozone has been used in combination with peroxide and oxygen. For instance, sequences like EOP-Z-PE-Z-PE, EOP-Z-PE, O-Z-EO-Z-P, O-Z-EOP-Z-P and O-Z-EO-Z-D were discussed. However, the publication does not take into account the presence of heavy metals in the pulp in spite of the fact that at least one of the examples discusses bleaching of kraft pulp by means of a peroxide containing compound.
  • EP-A-0 512 978 discloses a multi-stage bleaching process using both ozone and peroxide for bleaching pulp. The document does not pay any attention to the removal of heavy metals from pulp before bleaching with peroxide.
  • EP-A-0 402 335 discloses a process for bleaching lignocellulose-containing pulps by means of peroxide containing substance.
  • the main teaching of the document is to alter the trace metal profile of the pulp by means of a separate treatment with a complexing agent.
  • the document teaches the importance of treating pulp prior to a peroxide stage in a separate metal removing stage.
  • the treatment comprises a washing stage between the treatment with complex formers and the peroxide stage.
  • US-A-4 310 384 describes ozone bleaching with stages before and after it. The pulp is washed after each stage with counterflow of the wash filtrate.
  • a conventional bleaching + screening plant has thus included four or five bleaching stages and one screening and/or vortex cleaning stage, which the washing stage separates from each other.
  • the present invention compresses these five to six stages into three stages and thus almost halves the investment costs of a bleaching plant and a screening plant.
  • the method in accordance with the present invention involves that pulp is bleached with a sequence beginning with ozone and without the removal of heavy metals preceding the ozone stage.
  • a bleaching sequence is provided using a high consistency pulp tower 10, from which pulp is discharged and fed, for example, with an MC® (i.e. fluidizing) pump 12 into an ozone reactor 14, from which pulp is preferably discharged by means of a gas separator 16 into a first reaction tower 18.
  • Pulp is preferably discharged from tower 18 into a washer 22 by means of an MC® pump 20.
  • the washer may be a conventional DRUM DISPLACERTM washer or a conventional pressure diffuser. Pulp is preferably pumped from washer 22 by an MC® pump 24 into an oxygen reactor 26, and from reactor 26 into a second reaction tower 28.
  • a second washer 32 preferably a DRUM DISPLACERTM washer
  • ozone in a carrier gas
  • oxygen may be mixed prior to the oxygen reactor 26 with mixer 62 and the mixture of ozone and carrier gas prior to the second ozone reactor 36.
  • the mixers 60, 62, 64 are preferably AHLMIXERTM type fluidizing mixers, which are able to mix very large amounts of gas into fiber suspensions, including medium consistency suspensions.
  • Fig. 1 teaches how, in order to adjust the pH value of the pulp for the first ozone stage and the removal of heavy metals subsequent thereto, acid may be supplied into the pulp, for example, in the pump 12.
  • complex formers such as EDTA, and/or alkali may be added to the pulp. If too much magnesium is removed from the pulp by washer 22, it may be added, for example, with the alkali either in pump 24 and/or in the discharge from the oxygen reactor 26, or in any other appropriate way.
  • Another possibility to adjust the pH of the pulp for the second ozone treatment is to feed acid subsequent to the second washer 32 in pump 34 or in some other suitable way.
  • peroxide and/or magnesium may be added into the pulp, as illustrated in Fig. 1.
  • All the reaction towers 18, 28 and 40 in Fig. 1 are shown as of the down flow type. Alternatively, they may be of the up flow type, as is shown in Fig. 2.
  • the only significant difference between Figs. 1 and 2 is the flow direction of the reaction towers.
  • components functionally equivalent to or the same as the components in the Fig. 1 embodiment are illustrated by the same reference numeral, only preceded by a "1".
  • pumps 20, 30 and 42 of Fig. 1 are replaced by pumps 120', 130' and 142' of Fig.2, because they have been relocated at the other side of the reaction tower, in other words instead of feeding washers 22, 32 and 44 as illustrated in Fig. 1 they feed pulp to the reaction towers 118, 128 and 140 in the embodiments of Fig. 2.
  • pulp is cooked, for example with a continuous EMCC digester, sold by Kamyr Inc., of Glens Falls, New York, to a low kappa number, whereafter the kappa number is further decreased by oxygen bleaching to a value of about 14 or below.
  • a continuous EMCC digester sold by Kamyr Inc., of Glens Falls, New York
  • oxygen bleaching to a value of about 14 or below.
  • hot alkali extraction and oxygen bleaching a kappa range of 14 - 5 is obtained both with soft wood and birch.
  • a kappa number of 14 is sufficient in order to carry out the final bleaching with chlorine-free bleaching chemicals and yet reach a full brightness defined by ISO 86 (preferably ISO 88).
  • ISO 86 preferably ISO 88
  • the kraft pulp is bleached subsequent to the pulp washing and according to the invention without a separate removal of heavy metals, for example, with a sequence in accordance with Fig. 1, which is described more in detail below.
  • Pulp may be treated, if so required, with enzymes prior to the sequence in accordance with the present invention.
  • Pulp is brought from the high consistency pulp tower 10 to the first bleaching stage, which is a (ZT) stage.
  • the first bleaching stage which is a (ZT) stage.
  • pulp is bleached with ozone, the dosing being about 2-10 kg/adt, pH about 2- 7, and temperature about 40-70°C.
  • the pH value of pulp is adjusted by adding acid to the bottom of the high consistency tower 10, pump 12 (or the discharge to pump 12 as seen in Fig. 1), or chemical mixer 60.
  • the ozone having reacted, the residual gas is removed from the pulp preferably in a gas separator 16 and the treatment of heavy metals begins in the first reaction tower 18 in the T portion
  • the T portion of the (ZT) stage may be carried out, for example, in the following ways.
  • the first alternative is to allow the pH value of the pulp to decrease to the range of 2 - 4, whereby the majority of the heavy metals are dissolved into the filtrate phase and may be washed off in the thickener or washer 22 following that stage.
  • the disadvantage here is that the majority of the magnesium (Mg) is also discharged, so that it is possible that magnesium must be added to the pulp, mostly in the form of magnesium sulphate, for the oxygen and/or peroxide stages following later on in the sequence.
  • T portion of the (ZT) stage Another way to carry out the T portion of the (ZT) stage is to use complex formers, for example, EDTA.
  • the T portion of the (ZT) stage is then carried out in the pH range of about 4-7 and it is advantageous also to have the pH of Z portion of the (ZT) stage preceding T portion above 4.
  • manganese which is harmful in the oxygen stages
  • Filtrate S 1 of the washer 22 subsequent to the (ZT) stage may be brought to pulp washing prior to the (ZT) stage, or passed to the sewer or to the recovery of cooking chemicals.
  • the (ZT) stage is followed in Fig. 1 by an (EOP) stage.
  • the oxygen dose is about 2-6 kg/adt and the peroxide dose about 10-20 kg/adt. In some special cases it is possible to run the process completely without oxygen.
  • Temperature in the (EOP) stage is about 60-95°C, pH about 9-12, and the duration is about 2-8 hours. If required, magnesium may be added as a protective chemical.
  • the (EOP) stage is followed by washing, which gives filtrate S 2 .
  • the filtrate S 2 may be taken to pulp washing prior to or subsequent to the (ZT) stage, to sewer, or to recovery of chemicals.
  • the (EOP) stage is followed in Fig. 1 by a second ozone bleaching stage, i.e. an (ZP) stage.
  • the ozone portion of the (ZP) stage is normally carried out in the processes in accordance with the prior art in cold, acid conditions in order to have the ozone react properly.
  • the P portion of the (ZP) stage is carried out according to the teachings of the prior art in hot, alkali conditions in order to have the peroxide react properly.
  • the combination thereof in an economically advantageous way according to the present concepts is conventionally considered impossible.
  • the ozone dose is small, below 3 kg/adt and the purpose of the ozone is only to activate. Although disadvantageous conditions are used and a part of the ozone reacts poorly, this is insignificant, because the dose is small. Ozone is thus mainly used for the activation of the bleaching stage.
  • the temperature in the ozone stage may be 50-80°C, preferably, for example, 60-70°C.
  • the pH is 4-10, preferably about 6- 10.
  • the dose in the P portion of the (ZP) stage is also small, usually less than 10 kg/adt. Normally about 3-7 kg/adt is sufficient.
  • the temperature in the peroxide stage may be dropped to the range of 60-80°C, preferably to 70-80°C.
  • the pH is 9-11, preferably about 10.
  • the duration is about 1-6 hours.
  • the pulp is washed and a filtrate S 3 is obtained.
  • the filtrate S 3 may be used for the washing of pulp in connection with the earlier bleaching stages, discharged to the sewer, or led to the recovery of cooking chemicals.
  • a vortex cleaner 66 and/or a screening plant may be added according to Fig. 3 to the last stage of the bleaching plant to precede the thickener/washer 68, which in this case does not have to be an MC® washer, as in the earlier embodiments.
  • Pulp is diluted to the consistency range of about 0.5-1.5 % after the P-tower 140, when vortex cleaning or screening with a slotted screen is used. On the other hand, when screening with a perforated screen, a dilution to about 2-4% is usually sufficient.
  • the pulp is thickened and washed - usually with a suction filter 68. Previously pulp had to be diluted after washing to a screening consistency and thickened again after screening to a medium consistency.
  • FIG. 5 illustrates an oxygen delignification stage 80, which is followed by a two-stage washing 82. Pulp is transferred from the washing stage to the (ZT) stage 83, and from there via washing 84 to (EOP) stage 85, and from there via washing 86 to the (ZP) stage 87, which is followed by a washing stage 88.
  • the amount of effluent, which is brought to the effluent clarification, discharge channel 90, is 0-5 m3/adt. Part of the effluent may alternatively be transferred to the manufacture of cooking chemicals, via discharge channel 92, to be used instead of fresh water. Thus the amount of effluent that must be treated is minimized.
  • Fig. 5 may further be intensified by dividing the filtrates from the washer into two fractions with different pH according to Fig. 6.
  • Fig. 6 utilizes the reference numbers of Fig. 5 with a preceding "1".
  • the washers used in Fig. 6 are manufactured and marketed by A. Ahlstrom Corporation, and known as DRUM DISPLACERTM washers.
  • the pulp for the last washer 188 comes from the alkali (ZP) stage.
  • ZP alkali
  • the first outwashed filtrate 1881 is clearly alkaline and the filtrate 1882 coming out later is less alkaline or even neutral, because water 1880 flowing to the last washer 188 is generally neutral or slightly acid.
  • the pH of the filtrates may also be adjusted by adding acid or alkali to them before they are used again. In some cases it may, for example, be necessary to add alkali to the filtrates prior to their being brought to the brown stock washing or it may be necessary to add acid in order to maintain the pH low during the removal of the metals in the (ZT) stage (point 1840). It is possible that heavy metals are thickened again and attach to the fibers, if the pH increases during washing. Thus heavy metals are entrained to the P portion of the (ZP) stage following the Z portion and disturb the peroxide stage. Preferably the pH value is maintained less than 4, or at least maintained at 4, during the removal of heavy metals.
  • the pH values of the filtrates are close to the respective pH values of the entering and exiting pulp, preferably closer to these than to each other.
  • the present invention also includes a new method of arranging the screening subsequent to the pulp bleaching in such a way that a separate washing between the last washing stage and screening/vortex cleaning is unnecessary, but only dilution to screening/cleaning consistency is needed.

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Claims (17)

  1. Verfahren fürs Waschen von Zellstoff in Verbindung mit der Bleiche, bei welchem Verfahren der Zellstoff mit einer Sequenz gebleicht wird, die mit Sauerstoff beginnt und ohne Entfernung von Schwermetallen vor der Ozonstufe (83) in einer ersten Bleichanordnung, bestehend aus der Ozonstufe (83), der wahlweise eine Stufe (85) mit Peroxid unter alkalischen Verhältnissen oder Sauerstoff folgt, in einem ersten Wäscher (84; 184) gewaschen wird, und wahlweise in einem nachfolgenden Wäscher (86; 186) gewaschen wird, in einer zweiten Bleichanordnung (87) gebleicht wird und in einem zweiten Wäscher (88; 188) auf solche Weise gewaschen wird, dass die Waschflüssigkeit vom zweiten Wäscher (88; 188) zum ersten Wäscher (84; 184) im Gegenstrom zum Stoffstrom zurückgeführt wird, Waschflüssigkeit (1880) zum zweiten Wäscher (88; 188) zur Wäsche des von der zweiten Bleichanordnung (87) kommenden Zellstoffs eingeführt wird, dadurch gekennzeichnet, dass durch die Waschflüssigkeit zumindest zwei verschiedene Filtrate (1881, 1882) mit unterschiedlichen pH-Werten verdrängt werden, die zumindest zwei verschiedenen Filtrate (1881, 1882) getrennt aufgefangen werden und die zumindest zwei Filtrate (1881, 1882) getrennt stromaufwärts vom zweiten Wäscher (88; 188) als Waschflüssigkeiten und zur Einstellung des pH-Werts des Zellstoffs verwendet werden.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass aus dem zweiten Wäscher ein erstes Filtrat und ein zweites Filtrat eingesammelt werden und das erste und das zweite Filtrat als erste und zweite Waschflüssigkeit dem ersten Wäscher zugeführt werden.
  3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, dass es sich bei der zweiten Bleichanordnung um eine kombinierte ZP-Stufe handelt, wo das erste Filtrat vom zweiten Wäscher alkalisch ist und als erste Waschflüssigkeit dem ersten Wäscher zugeführt wird.
  4. Verfahren nach Anspruch, 1, dadurch gekennzeichnet, dass ein erstes Filtrat und ein zweites Filtrat mit unterschiedlichen pH-Werten vom zweiten Wäscher eingesammelt werden und das erste und das zweite Filtrat als zweite und erste Waschflüssigkeit, also in umgekehrter Reihenfolge, dem ersten Wäscher zugeführt werden.
  5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass die zweite Bleichanordnung eine Peroxidbleichstufe ist, wobei ein vom zweiten Wäscher eingesammeltes erstes Filtrat als zweite/letzte Waschflüssigkeit dem ersten Wäscher zugeführt wird.
  6. Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass die zweite Bleichanordnung eine Ozonbleichstufe ist, wobei ein vom zweiten Wäscher eingesammeltes erstes Filtrat als zweite/letzte Waschflüssigkeit dem ersten Wäscher zugeführt wird.
  7. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass eine zusätzliche Bleichanordnung (80) und ein zusätzlicher Wäscher (82; 182) stromaufwärts von der ersten Bleichanordnung (83, 85) vorgesehen sind.
  8. Verfahren nach Anspruch 7, dadurch gekennzeichnet, dass vom ersten Wäscher (184) zumindest zwei verschiedene Filtrate (1842, 1843) getrennt erhalten werden und die zumindest zwei verschiedenen Filtrate (1842, 1843) getrennt dem zusätzlichen Wäscher (182) zur Wäsche des von der zusätzlichen Bleichanordnung (80) kommenden Zellstoffs zugeführt werden.
  9. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Wäscher einstufige Wäscher sind.
  10. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die zweite Bleichanordnung einen Peroxidbleichturm umfasst, von wo der Zellstoff in den zweiten Wäscher eingeführt wird.
  11. Verfahren nach Anspruch 10, dadurch gekennzeichnet, dass die zweite Bleichanordnung eine vom Peroxidbleichturm stromaufwärts angeschlossene Ozonbleichstufe umfasst.
  12. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die erste Bleichanordnung einen Peroxidbleichturm umfasst.
  13. Verfahren nach Anspruch 7, dadurch gekennzeichnet, dass die zusätzliche Bleichanordnung (80) eine Sauerstoffbleichstufe umfasst.
  14. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass dem zweiten Wäscher frische Waschflüssigkeit zugeführt wird.
  15. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die zumindest zwei Filtrate in der gleichen Reihenfolge dem ersten Wäscher als Waschflüssigkeiten zugeführt werden.
  16. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die zumindest zwei Filtrate in der umgekehrten Reihenfolge dem ersten Wäscher als Waschflüssigkeiten zugeführt werden.
  17. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der pH von zumindest einem der Filtrate durch Zugabe von Säure oder Alkali vor der Einführung des Filtrats als Waschflüssigkeit in den ersten Wäscher eingestellt wird.
EP98113684A 1993-03-03 1993-05-25 Verfahren zum Waschen von Zellstoff beim Bleichen Expired - Lifetime EP0884415B1 (de)

Applications Claiming Priority (3)

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FI930954 1993-03-03
FI930954A FI93232C (fi) 1993-03-03 1993-03-03 Menetelmä massan valkaisemiseksi kloorivapailla kemikaaleilla
EP93910051A EP0687321B1 (de) 1993-03-03 1993-05-25 Verfahren zum bleichen von zellstoff mit chlorfreien chemikalien

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EP93910051A Division EP0687321B1 (de) 1993-03-03 1993-05-25 Verfahren zum bleichen von zellstoff mit chlorfreien chemikalien

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EP0884415A1 EP0884415A1 (de) 1998-12-16
EP0884415B1 true EP0884415B1 (de) 2002-11-20

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EP98113684A Expired - Lifetime EP0884415B1 (de) 1993-03-03 1993-05-25 Verfahren zum Waschen von Zellstoff beim Bleichen
EP93910051A Expired - Lifetime EP0687321B1 (de) 1993-03-03 1993-05-25 Verfahren zum bleichen von zellstoff mit chlorfreien chemikalien

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EP (2) EP0884415B1 (de)
JP (1) JP3276083B2 (de)
AT (2) ATE176808T1 (de)
AU (1) AU5370594A (de)
BR (1) BR9307858A (de)
CA (1) CA2157109C (de)
DE (2) DE69332508T2 (de)
ES (2) ES2130260T3 (de)
FI (3) FI93232C (de)
NO (1) NO953444L (de)
PT (1) PT884415E (de)
RU (1) RU2126471C1 (de)
WO (1) WO1994020673A1 (de)

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FI103818B1 (fi) * 1995-02-21 1999-09-30 Ahlstrom Machinery Oy Menetelmä massan valkaisemiseksi
US20080110584A1 (en) * 2006-11-15 2008-05-15 Caifang Yin Bleaching process with at least one extraction stage
FR2910027B1 (fr) * 2006-12-13 2009-11-06 Itt Mfg Enterprises Inc Procede de blanchiment des pates papeteries chimiques par traitement final a l'ozone a haute temperature
CN104060491B (zh) 2009-05-28 2017-04-12 Gp纤维素股份有限公司 来自化学牛皮纸纤维的改性纤维素及其制造和使用方法
US9719208B2 (en) 2011-05-23 2017-08-01 Gp Cellulose Gmbh Low viscosity kraft fiber having reduced yellowing properties and methods of making and using the same
CN104302831A (zh) 2012-01-12 2015-01-21 Gp纤维素股份有限公司 具有降低的黄变特性的低粘性牛皮纸纤维及其制造和使用方法
AU2013249725B2 (en) 2012-04-18 2017-04-20 Gp Cellulose Gmbh The use of surfactant to treat pulp and improve the incorporation of kraft pulp into fiber for the production of viscose and other secondary fiber products
BR112015018492A2 (pt) 2013-02-08 2017-07-18 Gp Cellulose Gmbh fibra kraft e método para fazer polpa kraft oxidada
MX364379B (es) 2013-03-14 2019-04-24 Gp Cellulose Gmbh Un metodo para preparar una fibra kraft altamente funcional y de baja viscosidad, usando una secuencia de blanqueamiento acido, y una fibra hecha por el proceso.
EP2971338A2 (de) 2013-03-15 2016-01-20 GP Cellulose GmbH Niedrigviskose kraftfaser mit verbessertem carboxylgehalt und verfahren zur herstellung und verwendung davon
FR3007044B1 (fr) * 2013-06-13 2016-01-15 Air Liquide Procede de traitement des pates papetieres chimiques par traitement a l'ozone en presence d'ions magnesium
AT515152B1 (de) * 2013-11-26 2015-12-15 Chemiefaser Lenzing Ag Verfahren zum Vorbehandeln von rückgewonnenen Baumwollfasern zur Verwendung bei der Herstellung von Formkörpern aus regenerierter Cellulose
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BR9307858A (pt) 1996-02-27
CA2157109A1 (en) 1994-09-15
WO1994020673A1 (en) 1994-09-15
FI954093A (fi) 1995-10-17
DE69332508D1 (de) 2003-01-02
EP0687321B1 (de) 1999-02-17
FI930954A (fi) 1994-09-04
JPH08509781A (ja) 1996-10-15
EP0687321A1 (de) 1995-12-20
NO953444D0 (no) 1995-09-01
FI934036A (fi) 1994-09-04
FI93232C (fi) 1995-03-10
DE69332508T2 (de) 2003-07-03
ATE228181T1 (de) 2002-12-15
CA2157109C (en) 2002-09-03
JP3276083B2 (ja) 2002-04-22
DE69323566T2 (de) 1999-07-15
FI930954A0 (fi) 1993-03-03
PT884415E (pt) 2003-03-31
RU2126471C1 (ru) 1999-02-20
FI954093A0 (fi) 1995-08-30
FI934036A0 (fi) 1993-09-15
FI98223B (fi) 1997-01-31
DE69323566D1 (de) 1999-03-25
ES2130260T3 (es) 1999-07-01
EP0884415A1 (de) 1998-12-16
NO953444L (no) 1995-10-19
AU5370594A (en) 1994-09-26
ES2186948T3 (es) 2003-05-16
ATE176808T1 (de) 1999-03-15
FI93232B (fi) 1994-11-30

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