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EP0263040A1 - Verfahren zum Bleichen von Lignocellulose-Materialien - Google Patents

Verfahren zum Bleichen von Lignocellulose-Materialien Download PDF

Info

Publication number
EP0263040A1
EP0263040A1 EP87420244A EP87420244A EP0263040A1 EP 0263040 A1 EP0263040 A1 EP 0263040A1 EP 87420244 A EP87420244 A EP 87420244A EP 87420244 A EP87420244 A EP 87420244A EP 0263040 A1 EP0263040 A1 EP 0263040A1
Authority
EP
European Patent Office
Prior art keywords
sodium
carried out
bleaching
agent
washing
Prior art date
Legal status (The legal status 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 status listed.)
Granted
Application number
EP87420244A
Other languages
English (en)
French (fr)
Other versions
EP0263040B1 (de
Inventor
Michel Devic
Robert Cen. Tech. De L'ind. Des Papiers Angelier
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Arkema France SA
Original Assignee
Atochem SA
Elf Atochem SA
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 Atochem SA, Elf Atochem SA filed Critical Atochem SA
Publication of EP0263040A1 publication Critical patent/EP0263040A1/de
Application granted granted Critical
Publication of EP0263040B1 publication Critical patent/EP0263040B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • DTEXTILES; PAPER
    • D21PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21CPRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00After-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
    • D21C9/10Bleaching ; Apparatus therefor
    • D21C9/1057Multistage, with compounds cited in more than one sub-group D21C9/10, D21C9/12, D21C9/16

Definitions

  • the present invention relates to a process for bleaching lignocellulosic materials
  • lignocellulosic materials to which the process of the invention applies denotes here paper pulps of mechanical, thermomechanical, chemo-mechanical, chemo-thermomechanical origin as well as wood in the form of shavings being transformed into one of these types of pulp by treatment. in a machine as described for example in the French patent published under the number 2319737, the French certificate of addition to this patent published under the number 2436844, the French patents published under the numbers 2418295 and 2451963, all from the company CREUSOT- LOIRE.
  • Such lignocellulosic materials need to be bleached so that the products finally produced from them, such as for example the paper intended for the printing of newspapers and magazines, have the required quality.
  • the process of the invention relates more particularly to a process for bleaching these materials in which a bleaching treatment using a reducing agent and a bleaching treatment using an oxidizing agent are combined.
  • an oxidizing agent such as, for example, chlorine dioxide, peracetic acid, ozone and, above all, hydrogen peroxide.
  • hydrosulfite and that of hydrogen peroxide are for example described by R.R. KINDRON, "PULP & PAPER", Nov. 1980, 54 (11), 127-130.
  • hydrosulfite generated from borohydride is for example described by John W. GERRIE, "PULP & PAPER MAGA ZINE of CANADA "Vol 75 No. 7 / July 1974 89-92 and by Robert G. GUESS,” PULP & PAPER ", June 1979, 53 (6), 74-81
  • complexing or sequestering agents for example, sodium tripolyphosphate, sodium tetrapyrophosphate, diethylenetriaminepentaacetic and ethylenediaminetetraacetic acids in the form of sodium salts are used.
  • complexing or sequestering agents can take place either simultaneously or prior to that of the bleaching agent.
  • the material to be bleached is subjected to a pretreatment by the complexing or sequestering agent.
  • the conditions such as those especially of pH, under which this reagent exerts its action at best can be essentially different: acid medium, for example for dithionite, alkaline medium, for example for borohydride.
  • the present invention not only offers such a process but also leads, within the framework of its generality, to whitening effects superior to those achieved to date by known processes based on a combination of oxidative whitening and whitening. reducer.
  • the process of the invention is characterized in that the lignocellulosic material, after pretreatment by means of at least one metal complexing or sequestering agent, is subjected to a washing of efficiency greater than 96% before undergoing successively a treatment of bleaching using a reducing agent at a pH between 8 and 12, washing to remove the reducing agent and bleaching treatment using an oxidizing agent.
  • washing is meant the operation consisting in eliminating more or less completely from the lignocellulosic material the liquid phase present in it, thanks for example to a concentration of the lignocellulosic material for example by pressing on a filter, or thanks to a sequence, repeated or no, dilution, most often with water, then concentration of the lignocellulosic material, for example by pressing on a filter.
  • efficiency is meant, expressed in percent, the degree of elimination of the liquid phase present before washing in the lignocellulosic material.
  • the washing which follows the pretreatment of the lignocellulosic material with the complexing or sequestering agent in the process of the invention is most often carried out in practice by diluting the lignocellulosic material with water and concentration by pressing on a filter, a temperature generally between about 20 ° C and 90 ° C, often between about 20 ° C and 60 ° C for economic reasons.
  • this is carried out at a rate of approximately 0.1% to 1% by weight of the weight of lignocellulosic material in the dry state. Unless specified or evident, it is also in percent by weight of the weight of lignocellulosic material in the dry state that the quantities of reactants are expressed in all that follows.
  • the complexing or sequestering agent is most often chosen from sodium tripolyphosphate, sodium tetrapyrophosphate, sodium salts of acetic, nitrilotriacetic, ethylenediaminetetraacetic, diethylenetriaminepentaacetic acids.
  • the pretreatment with the complexing or sequestering agent is most often carried out at a temperature between about 20 ° C and 100 ° C, preferably between 50 ° C and 95 ° C so as not to have to work under pressure while keeping a Sufficiently fast complexation or sequestration speed.
  • the consistency, content in% of the treatment medium in lignocellulosic material in the dry state can be equaled in the pretreatment to a value between fairly wide limits, about 5% to 50% but it is generally not higher about 25% in the case of pasta and most often remains between 10% and 40% in the case of chips to reconcile economy and efficiency of subsequent washing.
  • the duration depends on the other parameters and the equipment used. Generally between about 5 minutes and 2 hours in the case of pasta it can be reduced to a few minutes and even a few tens of seconds in the case of chips as defined here.
  • the bleaching treatment which follows the washing with an efficiency greater than 96% is carried out by means of a reducing agent chosen most often from sodium dithionite, thiourea dioxide, sodium borohydride.
  • the latter is advantageously used at a rate of approximately 0.05% 0.7% in the presence of sodium hydroxide, for example in the form of approximately 0.4 to 6% of the alkaline solution of sodium borohydride containing 12% by weight of this product and marketed under the name of BOROL (R) by the company VENTRON Corporation.
  • sodium hydroxide for example in the form of approximately 0.4 to 6% of the alkaline solution of sodium borohydride containing 12% by weight of this product and marketed under the name of BOROL (R) by the company VENTRON Corporation.
  • Sodium dithionite to present the best activity in the required pH range, is preferably used at a rate of about 1% to 10%, with about 0.5% to 5% of sodium hydroxide and an amount sodium silicate corresponding to about 1% to 4% of an aqueous solution of this product with a density equal to 1.33, so that the weight ratio of sodium dithionite / sodium hydroxide is between about 1.5 and 2.5 and that the weight ratio sodium silicate solution, density 1.33 / sodium hydroxide is between approximately 1 and 2.
  • thiourea dioxide still for carrying out the invention in a preferred manner, it is used at a rate of approximately 1% to 10% in the presence of approximately 0.5% to 5% of sodium hydroxide.
  • the consistency in the reduction whitening treatment is most generally between approximately 5 and 50%, practically between approximately 5% and 25% in the case of pasta.
  • the reducing bleaching treatment is carried out at a temperature between about 30 ° C and 90 ° C which, although having relatively little influence in the range chosen, is preferably between about 40 ° C and 60 ° C.
  • the reducing whitening treatment generally lasts between about 0.5 hours and 2 hours.
  • the treatment by means of an oxidizing agent is carried out, the oxidizing agent being most generally chosen from chlorine dioxide peracetic acid, ozone, peroxide hydrogen.
  • the invention authorizes not to involve again an agent, complexing or sequestering before or during oxidative bleaching, contrary to the practice currently recommended.
  • the oxidative bleaching is preferably carried out by means of hydrogen peroxide engaged for example at a rate of about 0.5, to 10, 'in the presence of sodium silicate, at a pH between about 9 and 11, at a temperature between about 60 ° C and 90 ° C usually lasting about 0.5 hour to 2 hours with a consistency generally between about 15% and 30%.
  • the process of the invention can be carried out in any apparatus combining devices known in the paper industry to be suitable for pretreatment, washing, bleaching operations such as among other mixers, filters, presses.
  • Such a machine essentially consists of two helical surfaces penetrating into one another, wound around parallel shafts, driven in synchronous rotation in the same direction inside a sheath enveloping them, and determining the upstream downstream in the direction of advancement of the material, a succession of zones for driving and braking the material.
  • the quantities of reagents used are expressed in percent by weight of the weight of lignocellu material.
  • the terms washing and efficiency have the meanings indicated above, the term sodium silicate denotes a commercial solution of sodium silicate with a density equal to 1.33, the pH during the reducing whitening is each time between 9 and 12 and the degrees of whiteness of the pastes (457 nm) are measured in percent using a KARL ZEIS spectrophotometer of the ELREPHO type.
  • the dough thus obtained is brought to a consistency of 15% in order to be bleached in a mixer under a nitrogen atmosphere using 1.25% sodium dithionite in the presence of 0.75, sodium hydroxide and 1% of sodium silicate, for 1 hour at a temperature equal to 90 ° C.
  • the dough is bleached in a mixer at a consistency equal to 20% using 3% hydrogen peroxide in the presence of 1.5% sodium hydroxide and 4% sodium silicate for 2 hours at 90 ° C.
  • the pulp resulting from the above treatments has a degree of whiteness equal to 81% while only 55% of the hydrogen peroxide used is consumed.
  • the example is repeated, omitting to wash the dough after the pretreatment.
  • Example 1 is repeated with the exception that the amounts of reactants involved in the reducing bleaching are 5% sodium dithionite, 2% sodium hydroxide and 3% silicate.
  • the degree of whiteness finally reached is equal to 83% for a consumption of hydrogen peroxide which only amounts to 56% of the hydrogen peroxide used.
  • the paste is then washed to remove the reducing agent, then bleached in a mixer for 2 hours at 90 ° C at a consistency equal to 20%, using 10% hydrogen peroxide, in the presence of 3% hydroxide sodium and 4% sodium silicate.
  • the bleached pulp obtained has an excellent whitening degree since it is equal to 89% while only 40% of the hydrogen peroxide used is consumed.
  • Example 4 By doubling in Example 4 the amounts of thiourea dioxide and sodium hydroxide but by committing during oxidative bleaching only 1% of hydrogen peroxide accompanied by 0.5% of sodium hydroxide and 2 % of sodium silicate, the pulp, due to the bleaching ability acquired during the process of the invention, has, at the end of it, a degree of whiteness equal to 82%, reached for consumption of hydrogen peroxide equal to 64% of the hydrogen peroxide used.
  • the bleaching treatment is then carried out on the pretreated and washed dough brought to a consistency equal to 20% in a mixer under nitrogen atmosphere, using 5% BOROL (R) in the presence of 5% sodium silicate, during 1 hour at a temperature of 50 ° C.
  • the oxidative bleaching is finally carried out at the consistency of 20%, using 3% hydrogen peroxide, 1.5% sodium hydroxide and 4% sodium silicate for 2 hours at a temperature of 90 ° C.
  • the degree of whiteness of the pulp thus bleached reaches a value equal to 85.3% for a consumption of 53.2% of the quantity of hydrogen peroxide used.
  • the pretreatment using 0.5% of a 40% sodium salt solution of diethylenetriaminepentaacetic acid takes place for 1 minute in the first training zone and in the first braking zone at a temperature 85 ° C, the temperature at which the whole process is carried out.
  • Water is introduced downstream of the first braking zone so as to carry out the washing in the second training zone with a consistency equal to 10%.
  • the evacuation of the liquid expressed by compression of the dough into the third braking zone brings the consistency to a value equal to 40% downstream of this zone when 5% of sodium dithionite, 2% of sodium hydroxide are added. and 3.5% of sodium silicate with water to operate the reducing bleaching in the fourth training zone and the fourth braking zone at a consistency equal to 35%.
  • the dough On leaving the first machine, the dough stays for 1 hour at the same consistency in a tank under a water vapor atmosphere before being introduced into a second machine of the same design as the first where the reducing agent is eliminated by dilution, compression, filtration in the first three parts of the machine, each part consisting of a drive zone and a material braking zone.
  • the oxidative bleaching takes place in the fourth part of the machine, then in a tank during a stay of 1 hour, at a consistency of 25%, using 4.7% of hydrogen peroxide, 2% of hydroxide. sodium, 4% sodium silicate and 0.1% of the 40% sodium salt solution of diethylenetriaminepentaacetic acid introduced into the fourth training zone.
  • the dough is finally passed through a two-disc refiner from BAUER and has a whiteness level of 78.5%.
  • Example 7 is repeated, omitting to carry out the washing after pretreatment in the first machine.
  • the degree of whiteness of the paste finally obtained is then only 76.5%.
  • the paste thus pretreated and washed in a highly efficient manner is subjected in a mixer under nitrogen atmosphere, with a consistency of 15%, to a reducing bleaching treatment using 5% sodium dithionite in the presence of 2% d sodium hydroxide and 3% sodium silicate for 1 hour at 90 ° C.
  • the dough washed to remove the reducing agent, is then treated in a kneader using 2% hydrogen peroxide in the presence of 1% sodium hydroxide and 3% sodium silicate, to an equal consistency. at 20%, for 2 hours at 90 ° C.
  • the bleached pulp obtained has a degree of whiteness equal to 72% while 75% of the hydrogen peroxide used is consumed.
  • Example 9 is repeated except that the reducing bleaching treatment follows the pretreatment without washing the pretreated dough.
  • the bleached pulp finally obtained only has a degree of whiteness equal to 67% for a significant consumption of hydrogen peroxide, reaching 95% of the quantity committed.
  • the mechanical properties of the bleached pulp in this example are also lower than those of the bleached pulp according to the invention.
  • the breaking length is 1.25 times higher when proceeding according to example 9 than when proceeding according to example 10.
  • Example 9 By operating as in Example 9, and therefore ensuring in particular a highly effective washing of the dough between the pretreatment and the reducing bleaching, but ending with a bleaching by means of 10% hydrogen peroxide, 3% d sodium hydroxide and 4% sodium silicate, the whiteness of the bleached chemothermomechanical pulp obtained reaches 80% while 75% of the quantity of hydrogen peroxide used is transformed.
  • the process according to the invention offers a general method for obtaining milled mechanical type pasta, with a high degree of whiteness and 25% to 35% absolute greater than the degree of whiteness of the original unbleached pasta, convincingng, having regard to this strong whitening effect, only a reduced consumption of an oxidizing bleaching agent such as hydrogen peroxide.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Paper (AREA)
EP87420244A 1986-09-23 1987-09-18 Verfahren zum Bleichen von Lignocellulose-Materialien Expired - Lifetime EP0263040B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8613546A FR2604197B1 (fr) 1986-09-23 1986-09-23 Procede de blanchiment de matieres lignocellulosiques.
FR8613546 1986-09-23

Publications (2)

Publication Number Publication Date
EP0263040A1 true EP0263040A1 (de) 1988-04-06
EP0263040B1 EP0263040B1 (de) 1991-01-09

Family

ID=9339347

Family Applications (1)

Application Number Title Priority Date Filing Date
EP87420244A Expired - Lifetime EP0263040B1 (de) 1986-09-23 1987-09-18 Verfahren zum Bleichen von Lignocellulose-Materialien

Country Status (7)

Country Link
US (1) US4812206A (de)
EP (1) EP0263040B1 (de)
JP (1) JPS6399388A (de)
CA (1) CA1302018C (de)
ES (1) ES2002249B3 (de)
FI (1) FI86443C (de)
FR (1) FR2604197B1 (de)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0311356A1 (de) * 1987-10-05 1989-04-12 FMC Corporation Verfahren zum Bleichen von mechanischer Pulpe
FR2639371A1 (fr) * 1988-11-24 1990-05-25 Atochem Procede de blanchiment de pates desencrees
EP0446110A1 (de) * 1990-03-07 1991-09-11 Elf Atochem S.A. Verfahren zur Herstellung von gebleichtem Zellstoff mit hoher Ausbeute
AU641858B2 (en) * 1991-04-30 1993-09-30 Eka Nobel Ab Process for bleaching of lignocellulose-containing material

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2583226B2 (ja) * 1987-02-24 1997-02-19 新王子製紙株式会社 中性紙の製造方法
US5169555A (en) * 1990-11-09 1992-12-08 Morton International, Inc. Pulp bleaching solution
US5213836A (en) * 1991-09-18 1993-05-25 American Crystal Sugar Company Method of preparation of sugar beet fiber material
AU1357097A (en) * 1996-02-27 1997-09-16 Tetra Laval Holdings & Finance Sa Process for sanitizing post-consumer paper fibers and product formed therefrom
US7001484B2 (en) * 2000-05-04 2006-02-21 University Of New Brunswick Peroxide bleaching of wood pulp using stabilizers and sodium hydrosulfide reducing agent
US6881299B2 (en) * 2001-05-16 2005-04-19 North American Paper Corporation Refiner bleaching with magnesium oxide and hydrogen peroxide
US6743332B2 (en) * 2001-05-16 2004-06-01 Weyerhaeuser Company High temperature peroxide bleaching of mechanical pulps
US7384502B2 (en) * 2002-12-24 2008-06-10 Nippon Paper Industries Co., Ltd. Process for impregnating, refining, and bleaching wood chips having low bleachability to prepare mechanical pulps having high brightness
SE528348C2 (sv) * 2004-09-21 2006-10-24 Noss Ab Förfarande och anordning för att tillverka cellulosamassa
JP4517933B2 (ja) * 2005-04-27 2010-08-04 王子製紙株式会社 コールドセット型オフセット用新聞用紙
US8262851B2 (en) * 2006-08-10 2012-09-11 Andritz Inc. Processes and systems for the pulping of lignocellulosic materials

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2290601A (en) * 1940-02-16 1942-07-21 Du Pont Bleaching of ground wood pulp with preliminary bisulphite treatment
DE834808C (de) * 1950-08-31 1952-03-24 Degussa Verfahren zum Bleichen von mechanisch erzeugten, schwer bleichbaren Faserstoffen, insbesondere Holzschliff
FR1201712A (fr) * 1958-07-11 1960-01-05 Fr Du Xylon Soc Perfectionnements au blanchiment des pâtes cellulosiques
DE1173172B (de) * 1962-04-11 1964-07-02 Siemens Ag Verfahren zur Abschaltung einpolig erdschlussbehafteter unbelasteter Drehstrom-leitungen mit Spannungen hoeher 5 kV und niederohmig induktiv geerdetem Sternpunkt
FR2285489A1 (fr) * 1974-09-23 1976-04-16 Mo Och Domsjoe Ab Procede de fabrication de pates de cellulose avec des rendements eleves
EP0017544A1 (de) * 1979-03-22 1980-10-15 Creusot-Loire Verfahren zur Herstellung einer Papierpulpe
EP0187477A1 (de) * 1984-12-21 1986-07-16 Pulp and Paper Research Institute of Canada Mehrstufige Aufhellung von Holzpulpen die mit hoher und ultrahoher Ausbeute gewonnen sind

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1171723B (de) * 1958-11-27 1964-06-04 Mo Och Domsjoe Ab Verfahren zum Veredeln von cellulose-haltigem Material

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2290601A (en) * 1940-02-16 1942-07-21 Du Pont Bleaching of ground wood pulp with preliminary bisulphite treatment
DE834808C (de) * 1950-08-31 1952-03-24 Degussa Verfahren zum Bleichen von mechanisch erzeugten, schwer bleichbaren Faserstoffen, insbesondere Holzschliff
FR1201712A (fr) * 1958-07-11 1960-01-05 Fr Du Xylon Soc Perfectionnements au blanchiment des pâtes cellulosiques
DE1173172B (de) * 1962-04-11 1964-07-02 Siemens Ag Verfahren zur Abschaltung einpolig erdschlussbehafteter unbelasteter Drehstrom-leitungen mit Spannungen hoeher 5 kV und niederohmig induktiv geerdetem Sternpunkt
FR2285489A1 (fr) * 1974-09-23 1976-04-16 Mo Och Domsjoe Ab Procede de fabrication de pates de cellulose avec des rendements eleves
EP0017544A1 (de) * 1979-03-22 1980-10-15 Creusot-Loire Verfahren zur Herstellung einer Papierpulpe
EP0187477A1 (de) * 1984-12-21 1986-07-16 Pulp and Paper Research Institute of Canada Mehrstufige Aufhellung von Holzpulpen die mit hoher und ultrahoher Ausbeute gewonnen sind

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
ABSTRACT BULLETIN OF THE INSTITUTE OF PAPER CHEMISTRY, vol. 53, no. 2, août 1982, page 260, résumé no. 2296, Appleton, Wisconsin, US; & JP-A-5 99 282 (MITSUBISHI GAS CHEMICAL CO. INC.) 12-01-1982 *

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0311356A1 (de) * 1987-10-05 1989-04-12 FMC Corporation Verfahren zum Bleichen von mechanischer Pulpe
FR2639371A1 (fr) * 1988-11-24 1990-05-25 Atochem Procede de blanchiment de pates desencrees
EP0374057A2 (de) * 1988-11-24 1990-06-20 Elf Atochem S.A. Verfahren zum Bleichen von tintenfreiem Zellstoff
EP0374057A3 (de) * 1988-11-24 1991-07-10 Elf Atochem S.A. Verfahren zum Bleichen von tintenfreiem Zellstoff
EP0446110A1 (de) * 1990-03-07 1991-09-11 Elf Atochem S.A. Verfahren zur Herstellung von gebleichtem Zellstoff mit hoher Ausbeute
FR2659363A1 (fr) * 1990-03-07 1991-09-13 Atochem Procede de preparation de pates a haut rendement blanchies.
AU641858B2 (en) * 1991-04-30 1993-09-30 Eka Nobel Ab Process for bleaching of lignocellulose-containing material

Also Published As

Publication number Publication date
FR2604197B1 (fr) 1988-11-18
FR2604197A1 (fr) 1988-03-25
CA1302018C (fr) 1992-06-02
FI874141A (fi) 1988-03-24
EP0263040B1 (de) 1991-01-09
FI874141A0 (fi) 1987-09-22
JPS6399388A (ja) 1988-04-30
ES2002249B3 (es) 1991-11-16
FI86443C (fi) 1992-08-25
US4812206A (en) 1989-03-14
FI86443B (fi) 1992-05-15
JPH0210275B2 (de) 1990-03-07
ES2002249A4 (es) 1988-08-01

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