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WO1990011403A1 - Procede de blanchiment servant a la production de pulpes tres claires - Google Patents

Procede de blanchiment servant a la production de pulpes tres claires Download PDF

Info

Publication number
WO1990011403A1
WO1990011403A1 PCT/CA1990/000097 CA9000097W WO9011403A1 WO 1990011403 A1 WO1990011403 A1 WO 1990011403A1 CA 9000097 W CA9000097 W CA 9000097W WO 9011403 A1 WO9011403 A1 WO 9011403A1
Authority
WO
WIPO (PCT)
Prior art keywords
pulp
bleaching
stage
sodium
peroxide
Prior art date
Application number
PCT/CA1990/000097
Other languages
English (en)
Inventor
Michel Barbe
Carole Gagne
Céline LEDUC
Claude Daneault
Original Assignee
Hymac Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hymac Ltd. filed Critical Hymac Ltd.
Priority to DE69009750T priority Critical patent/DE69009750D1/de
Priority to EP90905400A priority patent/EP0464110B1/fr
Publication of WO1990011403A1 publication Critical patent/WO1990011403A1/fr

Links

Classifications

    • 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

Definitions

  • This invention relates to a multistage bleaching process in which reducing agents and oxidizing agents are used sequentially to bleach mechanical and chemimechanical pulps to high brightness levels and partially remove their yellow shade.
  • the process is usually carried out in an aqueous phase at 3 to 5% consistency, a pH of 4.5 to 6.0, a temperature of about 60°C and a retention time of up to one hour.
  • a chelating or sequestering agent such as sodium tripolyphosphate (STPP) to remove naturally occuring trace metals is recommended. This agent is being added to the pulp prior to the addition of the reducing agent or is incorporated in the bleaching solution.
  • peroxide (P) is the most commonly employed oxidizing agent for bleaching mechanical and chemimechanical pulps. This alkaline process is normally carried out in a single stage or in a double stage. In both cases, the bleaching is done at a pulp consistency of 15 to 35%, moderate temperatures of 50 to 70°C, and retention times of 2 to 3 hours for each stage.
  • stabilizers such as sodium silicate and magnesium sulfate are added to the bleach liquor to prevent decomposition of the oxidizing agent.
  • Sodium hydroxide is also used to maintain an alkaline pH of 9.5 to 11 so as to increase the concentration of the perhydroxyl ion OOH- which is beleived to be the active bleaching agent.
  • pulps are normally pretreated at low consistency with organic chelating agents such as sodium diethylenetriamine penta-acetate (DTPA) to remove naturally occuring trace metals. Additional quantities are added in the bleach liquor to complex trace metals that are desorbed from the pulp as a result of the reaction of the bleaching agents with the chromophores of the pulp.
  • organic chelating agents such as sodium diethylenetriamine penta-acetate (DTPA)
  • DTPA sodium diethylenetriamine penta-acetate
  • a method for the bleaching of high yield or ultra high yield pulp which comprises the steps of sequentially treating the lignocellulosic fibres with a reducing compound and subsequently treating the same fibres with peroxide in two successive stages.
  • the method or process includes three stages where the wood pulp is subjected to bleaching operations.
  • the wood pulp which may be utilized is any high yield or ultra yield pulp such as mechanical, chemimechanical, chemithermomechanical, groundwood, refiner mechanical pulp, thermomechanical pulp, high yield and ultra high yield sulfite pulps.
  • the wood pulp is treated with a reducing compound which may be chosen from many such reducing compounds known to those skilled in the art.
  • a reducing compound which may be chosen from many such reducing compounds known to those skilled in the art.
  • preferred reaction conditions include:
  • reaction temperature of from about 60°C to 100°C
  • the pulp is bleached with a peroxygen compound.
  • Preferred conditions of bleaching include:
  • a peroxygen compound charge of about 0.1% to about 5% by weight of oven dried pulp in the presence of sodium hydroxide, sodium silicate, magnesium sulfate and DTPA;
  • reaction temperature of between about 60°C to about 100°C
  • reaction time of from about 4 minutes to about 180 minutes
  • a peroxygen compound is utilized which is similar to the one used in the second stage.
  • the preferred reaction conditions include:
  • reaction temperature of from about 60°C to about 100°C
  • reducing compounds utilized in the process of the present invention may be selected from among these well known to those skilled in the art.
  • the reducing compounds may be chosen from commercially inorganic reducing agents such as sodium or zinc hydrosulfite (dithionite), sodium or magnesium bisulfite, sodium borohydride, Borol* (a solution of sodium borohydride and sodium hydroxide), thiourea dioxide, ammonium borohydride, hydrazine and organic reducing agents such as amine-boranes and phosphine- boranes. It will be noted that some of these reducing agents are sold commercially with a chelating agent mixed therewith.
  • peroxide compound utilized in the second and third stages may include conventional inorganic peroxides such as hydrogen and sodium peroxide and also organic peroxides such as benzyl peroxide, ditertiary-butyl peroxide and peracetic acid.
  • the process flow diagram of figure 1 illustrates the various steps of a continuous operation in which pulps are bleached in multistage according to the present invention.
  • the pulp is first washed with a dewatering device (1) such as, but not exclusively, a standard screw press, a displacement washing screw press, a twin wire press, a disc filter or a twin roll press.
  • a dewatering device (1) such as, but not exclusively, a standard screw press, a displacement washing screw press, a twin wire press, a disc filter or a twin roll press.
  • These devices allow for water removal from the pulp slurry as well as for washing of contaminants such as sodium sulfite, metal ions, organic extractives, dissolved solids, etc., which are known to impair on the bleaching reactions between the bleaching agents and lignocellulosic fibres.
  • the pulp is mixed with the bleaching liquor containing the reducing agent.
  • Mixing devices (2) such as single or double shaft mixers, refiner type mixers, high shear mixers and medium or low consistency pumps can be used. It is important in this stage of the process to disperse the bleaching liquor uniformly onto the fibre surface so that bleaching reactions can prevail over darkening reactions that also occur when lignocellulosic fibres are submitted to high temperature. After this pulp mixing stage the reducing agent reacts with the pulp in an upflow tower or steaming tube (3). A chemical charge of 0.75 to 1.25% sodium hydrosulfite and of 0.3 to 0.5% of sodium borohydride by weight of oven dried pulp are the preferred charges.
  • a reaction terminating pH of about 4.5 to 5.0 for sodium hydrosulfite and of about 10.0 to 10.5 for sodium borohydride is also recommended.
  • the pulp is mixed with the peroxide bleaching liquor in a mixer (5).
  • Other devices such as those described previously and used in position (2) can also be used.
  • the efficiency of the mixer is important at this stage of the process to disperse the bleaching liquor uniformly onto the fibre surface so that oxidizing bleaching reactions of the chromophoric groups on the lignocellulosic fibres occur and prevail over darkening reactions that also occur when pulps are submitted to high temperatures.
  • a mixer (5) which allows for the addition of steam and the peroxide bleaching liquor simultaneously. Following this mixing stage the pulp is transferred to a bleaching tower (6).
  • the most preferred charge of the peroxygen compound in this second stage bleaching is in amount equal to the charge of the last bleaching tower or to one third of the charge of the last bleaching tower.
  • Sodium hydroxide, sodium silicate and magnesium sulfate are preferably added in charge ranges of 0.5-3.0%, 0.0 to 3.0% and 0.01-0.05% respectively. It is also preferable to add small amounts of DTPA between 0.1-0.4%. All these components stabilize the peroxygen compound, in the form of the perhydroxyl ion, initiate and maintain a stable bleaching reaction.
  • the peroxide bleaching liquor mixed with the pulp at this stage can be either prepared from fresh commercial components dissolved in water in separate tanks or it can be a residual bleaching liquor solution from the last stage bleaching tower (9).
  • the size of the second bleaching tower (6) is to be determined considering the production rate, reaction time and pulp consistency selected or desired. We have found that a consistency in the 10-12% range, a retention time of 60 to 90 minutes and a temperature of 65 to 70°C are preferable to minimize the bleaching cost of the process disclosed.
  • figure 1 we show a schematic of a tower which is discharged with a medium consistency pump so as to have an operation with an efficient control over the bleaching conditions.
  • the pulp is dewatered and washed with a dewatering device (7) such as those described previously and used in position (1) and (4).
  • the purpose is to wash the byproducts produced from the bleaching reactions which occured in the second stage bleaching tower, avoid their carry over to the next bleaching stage and eliminate these from the bleach plant with an adequate white water recirculation strategy.
  • the pulp is mixed with the peroxide bleaching liquor in a mixer (8).
  • the mixer used and its efficiency are important at this stage for the same reasons as those elaborated previously above.
  • the pulp is transferred to a bleaching tower (9).
  • the preferred charge of the peroxygen compound in this third stage bleaching is 3 to 10% by weight of oven dried pulps.
  • Sodium hydroxide, sodium silicate and magnesium sulfate are preferably added in charge ranges of 0.25-0.3%, 0.01% to 3.0% and 0.01-0.05% respectively. It is also preferable to add small amounts of DTPA between 0.2-0.4%.
  • This bleaching liquor is normally prepared from fresh commercial components which are dissolved in water in separate tanks. In addition to this fresh liquor, a small quantity of the residual bleaching liquor solution from the same tower (9) can also be used. The residual bleaching liquor is recovered with the last pair of dewatering presses (11 and 12). We have found that high charges of peroxide are required in this last bleaching tower to achieve high brightness levels.
  • the size of the third bleaching tower (9) is to be determined considering the production rate, reaction time and pulp consistency selected or desired. We have found that a consistency in the 20-35% range is preferable to have high effective concentrations of the oxidizing agents so as to minimize the bleaching cost of the process disclosed.
  • figure 1 we show a schematic of a tower which is discharged in a transfer chest (10) with a screw conveyer.
  • This device allows for a positive displacement out of the tower so as to provide an efficient control over the operating and bleaching conditions of the pulp in the tower.
  • the pulp is washed and dewatered with dewatering devices, (11) and (12), such as those described previously.
  • dewatering devices (11) and (12)
  • the pulp is pressed so as to recover the unreacted peroxide bleaching liquor and to reuse it in the process as shown in figure 1.
  • the bleaching chemicals were mixed by hand with a 20-g pulp sample, while the pulp consistency was simultaneously adjusted with demineralized water. Subsequently, the bags were sealed and immersed in a thermostatically controlled bath for the bleaching reactions to occur. After bleaching, the pulps were neutralized to destroy the bleaching agents and to adjust the pulp pH to minimize brightness reversion. For hydrogen peroxide bleaching, sodium metabisulfide was used, while sulfuric acid was used for the other bleaching agents. The pulps were neutralized by diluting the pulp to 3% consistency with the neutralizing agent, mixing the slurry for 5 minutes, and pressing the pulp to 18% consistency. After neutralization, two samples of 3.5g each were used to make the handsheets.
  • the pulps were disintegrated for 2 minutes at a consistency of approximately 0.3%.
  • the sheets were made with demineralized water on a British handsheet machine following the procedures prescribed by the Canadian Pulp and Paper Association. The sheets were pressed for 2 minutes at 50 psig and dried for 24 h at 23°C and 50% RH.
  • the brightness was measured with an Elrepho spectrophotometer. Reflectance measurements with Filter Nos. 8, 9, 10, and 11 were made and used to calculate the color coordinates (CIE LAB) reference system.
  • ISO brightness reported are the reflectance values at 457 nm using filter No. 8. in the multistage bleaching experiments, each stage was similar to the single stage. However, the two-stage experiments were carried out with 30-g pulp samples, and 40-g samples were used for three stages. In all cases, a 7-g sample was taken at the end of each stage and was processed to obtain brightness values.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Paper (AREA)
  • Detergent Compositions (AREA)
  • Treatment Of Fiber Materials (AREA)

Abstract

Le procédé décrit, qui sert à blanchir des pulpes mécaniques et des pulpes chimiomécaniques consiste à soumettre dans une première phase la pulpe à un traitement utilisant un agent de réduction, puis à soumettre dans une seconde phase la même pulpe à un autre traitement utilisant un composé de peroxygène, suivi dans une troisième phase par un traitement ultérieur utilisant un composé de peroxygène.
PCT/CA1990/000097 1989-03-23 1990-03-22 Procede de blanchiment servant a la production de pulpes tres claires WO1990011403A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DE69009750T DE69009750D1 (de) 1989-03-23 1990-03-22 Bleichverfahren zur herstellung von hochweissem zellstoff.
EP90905400A EP0464110B1 (fr) 1989-03-23 1990-03-22 Procede de blanchiment servant a la production de pulpes tres claires

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CA000594763A CA1340348C (fr) 1989-03-23 1989-03-23 Procede de blanchiment pour la production de pates tres blanches
CA594,763 1989-03-23

Publications (1)

Publication Number Publication Date
WO1990011403A1 true WO1990011403A1 (fr) 1990-10-04

Family

ID=4139806

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CA1990/000097 WO1990011403A1 (fr) 1989-03-23 1990-03-22 Procede de blanchiment servant a la production de pulpes tres claires

Country Status (5)

Country Link
EP (1) EP0464110B1 (fr)
AT (1) ATE106961T1 (fr)
CA (1) CA1340348C (fr)
DE (1) DE69009750D1 (fr)
WO (1) WO1990011403A1 (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
USH1690H (en) * 1995-07-20 1997-11-04 Nye; Jeffrey Process for bleaching kraft pulp
WO1997045585A1 (fr) * 1996-05-30 1997-12-04 Kemira Chemicals Oy Procede de blanchiment de pate a papier a haut rendement ou de pate a papier recycle
EP1258559A1 (fr) * 2001-05-09 2002-11-20 Rohm And Haas Company Procede de blanchiment des pates mecaniques
EP1418269A1 (fr) * 2002-11-05 2004-05-12 Rohm And Haas Company Procédé de blanchiment des pates mecaniques
WO2005080673A3 (fr) * 2004-02-25 2005-11-10 Kemira Oyj Procede de traitement d'un materiau fibreux et nouvelle composition
WO2005108673A1 (fr) 2004-05-12 2005-11-17 Kemira Oyj Composition et procede pour le traitement d'une matiere fibreuse
WO2007143182A3 (fr) * 2006-06-02 2008-03-06 Int Paper Co Procédé amélioré de fabrication de pulpe, de papier et de produits en carton
WO2010104725A1 (fr) 2009-03-09 2010-09-16 Nalco Company Procédé et composition chimique pour améliorer le rendement de pâte mécanique
CN104237211A (zh) * 2014-09-23 2014-12-24 中国科学院长春应用化学研究所 一种鲁米诺化学发光体系和鲁米诺、二氧化硫脲、钴离子浓度的测定方法
US9932709B2 (en) 2013-03-15 2018-04-03 Ecolab Usa Inc. Processes and compositions for brightness improvement in paper production

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0187477A1 (fr) * 1984-12-21 1986-07-16 Pulp and Paper Research Institute of Canada Blanchiment multistade de pâtes de bois à haut et très haut rendement
EP0191756A1 (fr) * 1985-02-15 1986-08-20 Kamyr Ab Blanchiment à étapes multiples au péroxyde, d'une pâte mécanique

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0187477A1 (fr) * 1984-12-21 1986-07-16 Pulp and Paper Research Institute of Canada Blanchiment multistade de pâtes de bois à haut et très haut rendement
EP0191756A1 (fr) * 1985-02-15 1986-08-20 Kamyr Ab Blanchiment à étapes multiples au péroxyde, d'une pâte mécanique

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
BULLETIN OF THE INSTITUTE OF PAPER CHEMISTRY. vol. 53, no. 2, August 1982, APPLETON US page 260 M.YOTSUYA et al.: "Peroxide bleaching of high-yield pulp." see the whole document *

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
USH1690H (en) * 1995-07-20 1997-11-04 Nye; Jeffrey Process for bleaching kraft pulp
WO1997045585A1 (fr) * 1996-05-30 1997-12-04 Kemira Chemicals Oy Procede de blanchiment de pate a papier a haut rendement ou de pate a papier recycle
EP1258559A1 (fr) * 2001-05-09 2002-11-20 Rohm And Haas Company Procede de blanchiment des pates mecaniques
US7163564B2 (en) 2002-11-05 2007-01-16 Jean Luc Sibiet Method for brightening virgin mechanical pulp
EP1418269A1 (fr) * 2002-11-05 2004-05-12 Rohm And Haas Company Procédé de blanchiment des pates mecaniques
WO2005080673A3 (fr) * 2004-02-25 2005-11-10 Kemira Oyj Procede de traitement d'un materiau fibreux et nouvelle composition
US7988821B2 (en) 2004-02-25 2011-08-02 Kemira Oyj Process for the treatment of fibre material and new composition
WO2005108673A1 (fr) 2004-05-12 2005-11-17 Kemira Oyj Composition et procede pour le traitement d'une matiere fibreuse
US8048264B2 (en) 2004-05-12 2011-11-01 Kemira Oyj Composition and process for the treatment of fibre material
WO2007143182A3 (fr) * 2006-06-02 2008-03-06 Int Paper Co Procédé amélioré de fabrication de pulpe, de papier et de produits en carton
US7967948B2 (en) 2006-06-02 2011-06-28 International Paper Company Process for non-chlorine oxidative bleaching of mechanical pulp in the presence of optical brightening agents
WO2010104725A1 (fr) 2009-03-09 2010-09-16 Nalco Company Procédé et composition chimique pour améliorer le rendement de pâte mécanique
US9932709B2 (en) 2013-03-15 2018-04-03 Ecolab Usa Inc. Processes and compositions for brightness improvement in paper production
CN104237211A (zh) * 2014-09-23 2014-12-24 中国科学院长春应用化学研究所 一种鲁米诺化学发光体系和鲁米诺、二氧化硫脲、钴离子浓度的测定方法

Also Published As

Publication number Publication date
EP0464110A1 (fr) 1992-01-08
DE69009750D1 (de) 1994-07-14
EP0464110B1 (fr) 1994-06-08
CA1340348C (fr) 1999-01-26
ATE106961T1 (de) 1994-06-15

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