WO2001059203A2 - Procede de reduction en pate - Google Patents

Procede de reduction en pate Download PDF

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Publication number
WO2001059203A2
WO2001059203A2 PCT/SE2001/000257 SE0100257W WO0159203A2 WO 2001059203 A2 WO2001059203 A2 WO 2001059203A2 SE 0100257 W SE0100257 W SE 0100257W WO 0159203 A2 WO0159203 A2 WO 0159203A2
Authority
WO
WIPO (PCT)
Prior art keywords
gas
chlorine dioxide
containing material
process according
lignocellulose containing
Prior art date
Application number
PCT/SE2001/000257
Other languages
English (en)
Other versions
WO2001059203A3 (fr
Inventor
Patrick S. Bryant
John C. Sokol
Dwane S. Hutto
Original Assignee
Akzo Nobel N.V.
Eka Chemicals Ab
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
Priority claimed from EP00850037A external-priority patent/EP1130155A1/fr
Application filed by Akzo Nobel N.V., Eka Chemicals Ab filed Critical Akzo Nobel N.V.
Priority to NZ520518A priority Critical patent/NZ520518A/en
Priority to EP01904736A priority patent/EP1264038A2/fr
Priority to AU32561/01A priority patent/AU778689B2/en
Priority to JP2001558528A priority patent/JP2003522845A/ja
Priority to CA002399772A priority patent/CA2399772A1/fr
Publication of WO2001059203A2 publication Critical patent/WO2001059203A2/fr
Publication of WO2001059203A3 publication Critical patent/WO2001059203A3/fr
Priority to NO20023712A priority patent/NO20023712L/no

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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/04—Pretreatment of the finely-divided materials before digesting with acid reacting compounds
    • 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
    • D21C1/00—Pretreatment of the finely-divided materials before digesting

Definitions

  • the present invention relates to a process for the removal of Iignin from lignocellulose containing material comprising treating the lignocellulose containing material prior to a high-yield pulping process with a delignifying gas comprising gaseous compounds comprising at least one oxygen atom.
  • the objective is to disrupt the structure of the lignocellulosic containing material in fragments of variable dimensions by the use of mechanical treatment optionally in the presence of chemicals.
  • High-yield pulps are produced by grinding or refining of the lignocellulose containing material and thereby essentially all of the fibres constituents are retained in the pulp.
  • High-yield pulping processes encompasses grinding, screening and refining processes.
  • washed logs are forced against a rotating grinding disk to tear the lignocellulose containing material into small pieces which are then further processed by screening or refining to produce mechanical pulp.
  • screened washed chips pass between rotating disks or a rotating and stationary disk to shred the lignocellulose containing material into pulp. The resultant pulp may then be further refined, screened and cleaned to produce the desired mechanical pulp.
  • One aspect of high-yield pulping is to rip or shred the lignocellulose containing material into fibres which consumes energy. This energy is measured as the power required to rotate the grindstone or the refiner disk(s).
  • one advantage of the present invention is to provide a pretreatment process that softens or breaks the Iignin contained within the lignocellulose containing material resulting in a substantial reduction in the energy required to produce high yield pulp.
  • US 4172006 refers to the pretreatment of wood chips with oxygen prior to adding a cooking liquor.
  • US 4750973 relates to a process for reducing carbohydrate losses in sulphate pulping of wood using sodium hydroxides and sodium sulfide, wherein the wood is pretreated in presence of water with oxygen gas and nitrogen oxides.
  • GB 567774 discloses a process for the treatment of cellulosic raw material where wood chips are contacted with a aqueous solution of a wetting agent prior to subjecting the chips to a solution containing sodium chlorite thereby using sufficient acid to insure the liberation of chlorine dioxide.
  • WO 8908165 refers to a method for the pretreatment of wood chips with sulphur dioxide gas prior to alkaline deligification operations.
  • DE 1049220 discloses a method comprising subjecting wood chips to carbon acid before sulfite cooking.
  • JP 49020241 refers to a pulping process comprising the steps of reacting chlorine dioxide or a mixture consisting of chlorine dioxide and chlorine with wood chips in the presence of water soluble cellulose derivatives and thereafter removing inter alia the oxidised Iignin by extraction.
  • US 5474654 refers to a delignification process where chlorine dioxide gas is used on pulp obtained from pulping processes such as chemical kraft, sulfide or mechanical processes.
  • US 3591451 and US 3919041 disclose the use of gaseous chlorine dioxide subsequent a pretreatment step which may be either mechanical, chemical or a combination thereof. Summary of the invention In accordance with the present invention it has surprisingly been found that a substantial reduction in the energy required to produce high yield pulp can be obtained by providing a process according to the claims. More specifically, the invention relates to a process for the removal of Iignin from lignocellulose containing material comprising treating the lignocellulose containing material prior to a high-yield pulping process with a delignifying gas, wherein the gas comprises gaseous compounds comprising at least one oxygen atom. Detailed description of the invention
  • Suitable lignocellulose containing material used in the present invention can be any lignocellulose containing material derived from natural sources such as softwood, hardwood, gum, straw, bagasse and/or bamboo.
  • the physical state of the lignocellulose containing material is not critical, however, a physical state providing a large surface area is preferred that maximises penetration of the delignifying gas and optionally processing chemicals.
  • the lignocellulose containing material is in the form of chips with a size which is governed by the process equipment and process parameters.
  • the lignocellulose containing material is suitably treated according to any method known to the skilled artisan which renders the diffusion of the delignifying gas within the fibre source to the Iignin more effective such as steaming and/or evacuation.
  • the lignocellulosic material is treated with a delignifying gas comprising gaseous compounds comprising at least one oxygen atom.
  • the delignifying gas comprising chlorine dioxide, nitrogen oxides, carbon dioxide or sulphur dioxide or mixtures thereof.
  • Nitrogen oxides include nitrogen monoxide, nitrogen dioxide, polymeric oxides and double molecules thereof, e.g. N 2 O 4 or N 2 O 3 .
  • the delignifying gas mixture is suitably a non-liquid containing gas.
  • the delignifying gas comprises chlorine dioxide.
  • the chlorine dioxide containing gas may contain other gases such as nitrogen, oxygen, air or steam or mixtures thereof.
  • the chlorine dioxide containing gas may also contain small amounts of chlorine, however, the gas is suitably substantially free from chlorine, preferably having less than 10% by volume, more preferably less than 1% by volume of chlorine.
  • a delignifying gas such as a gas comprising chlorine dioxide overcomes several unsolved problems.
  • Treatment of the lignocellulosic containing material with solutions containing for example chlorine dioxide is limited by the rate of chlorine dioxide diffusion through the solution to the fibre source followed by the diffusion of the chlorine dioxide within the fibre source to the Iignin.
  • the result is a slow delignification process that works primarily on the fibre source surface and an aqueous effluent stream containing chlorine dioxide, dissolved fibre components and chlorides, which is difficult to treat in an environmentally correct manner.
  • a gas comprising chlorine dioxide does not have the diffusion barriers that limit the process when a solution is used.
  • the gas passes rapidly and uniformly into the fibre source resulting in even delignification throughout the material. Furthermore, there are no aqueous effluent streams.
  • the gas comprising chlorine dioxide is applied on lignocellulose containing material free from any surrounding aqueous solution.
  • the moisture content of the lignocellulose containing material is from about 30 weight % up to about 60 weight % based on oven dry material, more preferably from about 40 up to about 50 weight %.
  • the chlorine dioxide containing gas employed in the present invention is suitably produced using a chlorine dioxide generation process as described in the US patens US 4770868, US 5091166, US 5091197 and US 5380517, which all are incorporated by reference.
  • the concentration of chlorine dioxide in the gas is not critical for the invention.
  • the lignocellulose containing material may be treated with substantially pure chlorine dioxide gas.
  • the upper limit of the amount of chorine dioxide, i.e. chlorine dioxide comprised in the gas mixture, is purely set by safety considerations.
  • Suitable concentrations of chlorine dioxide comprised in the gas mixture are from about 0.05 up to about 100% by volume, more preferably from about 0.05 up to about 50 % by volume and most preferably from about 1 up to about 20 % by volume.
  • the gas comprising chlorine dioxide is generally applied in amounts which renders a reduction in the energy required for the production of pulp compared to a process where the lignocellulose containing material has not been subjected to chlorine dioxide prior to said high-yield process.
  • the charge of chlorine dioxide is from about 0.5 kg/tonne up to about 300 kg active Cl 2 per tonne of oven dry material, more preferably from about 2 kg up to about 100 kg active Cl 2 per tonne oven dry material and most preferably from about 30 kg/tonne up to about 50 kg active Cl 2 per tonne oven dry material.
  • the present invention may be performed at any location prior to high-yield pulping processes, i.e. mechanical pulping processes.
  • the treatment with the gas comprising gaseous compounds comprising at least one oxygen atom is carried out prior to a refining process, suitably prior to a first refining process.
  • the lignocellulose containing material may be treated with the delignifying gas in any type of equipment.
  • the equipment should be gas tight.
  • the treatment with the gas comprising chlorine dioxide may also be carried out in the same equipment (vessel) as is used for the subsequent pulping process.
  • the treatment is carried out in an equipment such as a vessel which is essentially free from an aqueous solution, i.e. the treatment is carried out in the absence of aqueous solutions.
  • a vessel which is essentially free from an aqueous solution
  • a gas comprising chlorine dioxide as long as the removal efficiency of Iignin is not significantly impaired, i.e.
  • the delignifying gas such as a gas comprising chlorine dioxide is suitably admixed with the lignocellulose containing material in an equipment which is at any suitable pressure including atmospheric, subatmospheric or superatmospheric pressures.
  • the treatment is carried out at a pressure ranging from about 10 kPa up to about 500 kPa, preferably from about 50 kPa up to about 250 kPa. The most preferred pressure ranges from about 80 kPa up to about 120 kPa.
  • the temperature during the treatment according to the present invention is not critical and can be carried out at surprisingly low temperatures including ambient temperatures.
  • the upper temperature level in the treatment is set by economical and safety considerations. Temperatures may range from about 10 °C up to about 400 °C, suitably from about 15 °C up to 200 ⁇ C, more preferably from 20 °C up to about 95 °C and most preferably from about 25 ⁇ C up to about 90 °C. Suitable temperature ranges are also those obtained by combining any of the lower temperature level of above ranges with any of the higher temperature levels.
  • the lignocellulose containing material is pretreated prior to being subjected to the gas comprising chlorine dioxide.
  • the pretreatment may be accomplished in the same equipment used for the delignifying gas, yet, the pretreatment can also be performed in any suitable equipment located upstream the treatment with the delignifying gas.
  • the pretreatment includes various steaming and/or evacuation processes. The pretreatment is believed to open up the lattice structure of the lignocellulose containing material thereby improving the diffusion of the delignifying gas into the material.
  • High-yield or mechanical pulping processes are generally pulping processes where the yield typically is from about 70 up to about nearly 100% by weight based on total lignocellulose containing material.
  • high-yield pulping processes are referred to as stone groundwood (SGW), pressurised groundwood (PGW), refiner mechanical pulp (RMP) and modifications thereof, thermomechanical pulp (TMP), chemithermomechanical pulp (CTMP) or chemimechanical pulp (CMP).
  • SGW stone groundwood
  • PGW pressurised groundwood
  • RMP refiner mechanical pulp
  • TMP thermomechanical pulp
  • CMP chemithermomechanical pulp
  • CMP chemimechanical pulp
  • the basic principle in high-yield pulping processes is to disrupt the wood structure in fragments of variable dimensions by the use of mechanical treatments optionally in conjunction with chemicals such as sulphite.
  • a refiner is used, where wood ships are fed between two metal disks, of which at least one disc is rotating, and the wood fibres are separated by the action of grooves and bars located on the surface of the two disks.
  • one advantage with the present invention is that by treating lignocellulose containing material prior to high-yield pulping processes the input of energy in said pulping processes can be significantly reduced.
  • Douglas Fir wood chips obtained from a commercial pulp supplier were used. The samples were pulled at random from the chip supply and were then mixed and separated into samples 1 and 2. There was no special handling, separation or classification of the chips prior to the experiment.
  • the chips of sample 1 were treated with the chlorine dioxide containing gas in a packed bed reactor with a gas containing approximately 3% to 5% chlorine dioxide on a volume basis. Approximately 20 grams of chlorine dioxide were used to treat 1 kg of wood chips.
  • the resulting treated wood chips were then pre-steamed and mechanically refined to specific Canadian Standard Freeness levels using a Sprout-Bauer 12-1 CP pressurized laboratory refiner.
  • the first stage refining involves size reduction from chips to matchstick material and was conducted at approximately 30% consistency. All subsequent refining stages were performed at 15% consistency.
  • Chip pre-steaming was conducted for 3 to 5 minutes by direct injection of 206,8 kPa (30 psig) steam.
  • the pulp was heated by steaming with low-pressure steam 13,8-20,7 kPa (2-3 psig) by direct injection to heat the wood to 100 °C.
  • the energy consumption at each CSF level was measured (table 1).
  • Wood chips from sample 2 which were not subjected to chlorine dioxide treatment were pre-steamed and refined to the same CSF levels using the same equipment and procedures as the wood of sample 1 to establish a base energy consumption for the refining process.
  • Table 1 shows the total energy requirement versus the CSF for wood chips not subjected to a chlorine dioxide containing gas (control) and wood chips treated with a chlorine dioxide containing gas as outlined above (treated).
  • Table 1 clearly shows a significant reduction in the energy requirement when producing mechanical pulp using wood chips treated with chlorine dioxide containing gas.
  • the energy requirement for the treated chips is approximately 45% lower than the untreated chips.

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  • Paper (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)

Abstract

La présente invention concerne un procédé permettant d'enlever la lignine de lignocellulose contenant de la matière. Avant le procédé de réduction en pâte à haut rendement, on traite la lignocellulose contenant de la matière avec un gaz de délignification contenant des composés gazeux renfermant au moins un atome d'oxygène, tel qu'un gaz contenant du bioxyde de chlore.
PCT/SE2001/000257 2000-02-09 2001-02-08 Procede de reduction en pate WO2001059203A2 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
NZ520518A NZ520518A (en) 2000-02-09 2001-02-08 Process to remove lignin from lignocellulose material by first treating with a oxygen containing delignifying gas before a mechanical pulping process
EP01904736A EP1264038A2 (fr) 2000-02-09 2001-02-08 Procede de reduction en pate
AU32561/01A AU778689B2 (en) 2000-02-09 2001-02-08 Pulping process
JP2001558528A JP2003522845A (ja) 2000-02-09 2001-02-08 パルプ化方法
CA002399772A CA2399772A1 (fr) 2000-02-09 2001-02-08 Procede de reduction en pate
NO20023712A NO20023712L (no) 2000-02-09 2002-08-06 Kokeprosess

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US50138400A 2000-02-09 2000-02-09
US09/501,384 2000-02-09
EP00850037A EP1130155A1 (fr) 2000-03-01 2000-03-01 Procédé de délignification
EP00850037.3 2000-03-01

Publications (2)

Publication Number Publication Date
WO2001059203A2 true WO2001059203A2 (fr) 2001-08-16
WO2001059203A3 WO2001059203A3 (fr) 2002-01-03

Family

ID=26074189

Family Applications (2)

Application Number Title Priority Date Filing Date
PCT/SE2001/000257 WO2001059203A2 (fr) 2000-02-09 2001-02-08 Procede de reduction en pate
PCT/SE2001/000256 WO2001059202A2 (fr) 2000-02-09 2001-02-08 Procede de reduction en pate

Family Applications After (1)

Application Number Title Priority Date Filing Date
PCT/SE2001/000256 WO2001059202A2 (fr) 2000-02-09 2001-02-08 Procede de reduction en pate

Country Status (7)

Country Link
EP (2) EP1264038A2 (fr)
JP (2) JP2003522845A (fr)
AU (2) AU778689B2 (fr)
CA (2) CA2399723A1 (fr)
NO (2) NO20023712L (fr)
NZ (1) NZ520518A (fr)
WO (2) WO2001059203A2 (fr)

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ATE527230T1 (de) 2004-12-23 2011-10-15 Shell Int Research Verfahren zur hydrierung eines lactons oder einer carbonsäure oder eines esters mit einer gamma- carbonylgruppe
US20070034345A1 (en) * 2005-06-15 2007-02-15 Leonardus Petrus Process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping
US8580978B2 (en) 2009-08-07 2013-11-12 Shell Oil Company Process for preparing a hydroxyacid or hydroxyester
ES2828623T3 (es) 2016-07-27 2021-05-27 Padlock Therapeutics Inc Inhibidores covalentes de PAD4
CN109972436A (zh) * 2017-12-28 2019-07-05 北京小池原品科技有限公司 一种竹料制造生活用纸的方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB567774A (en) * 1942-08-24 1945-03-02 George Brainard Fowler Improvements in or relating to processes of treating cellulosic raw material, and the improved cellulosic fibres resulting therefrom
US4211605A (en) * 1978-08-03 1980-07-08 Canadian International Paper Company High yield chemimechanical pulping processes
EP0433258A1 (fr) * 1989-12-12 1991-06-19 Enso-Gutzeit Oy Procédé de fabrication de pâte
WO1991019040A1 (fr) * 1990-06-07 1991-12-12 Stfi Procede de fabrication de pate de cellulose
WO1994018382A1 (fr) * 1993-02-09 1994-08-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de fabrication de pates a papier chimicothermomecaniques (ctmp)

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3591451A (en) * 1969-02-06 1971-07-06 Ethyl Corp Pretreatment of vegetable matter and delignification of the refined matter with chloring dioxide
SE450393B (sv) * 1981-10-27 1987-06-22 Mo Och Domsjoe Ab Forfarande for behandling av ved med kveveoxider och syrgas fore sulfatkokning
SU1416576A1 (ru) * 1986-08-14 1988-08-15 Ленинградская лесотехническая академия им.С.М.Кирова Способ получени целлюлозного полуфабриката
SE466964B (sv) * 1988-03-01 1992-05-04 Sca Pulp Ab Foerbehandling av flis medelst svaveldioxid vid framstaellning av sulfatmassa
AU655842B2 (en) * 1991-08-23 1995-01-12 Olin Corporation Delignifying wood pulp

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB567774A (en) * 1942-08-24 1945-03-02 George Brainard Fowler Improvements in or relating to processes of treating cellulosic raw material, and the improved cellulosic fibres resulting therefrom
US4211605A (en) * 1978-08-03 1980-07-08 Canadian International Paper Company High yield chemimechanical pulping processes
EP0433258A1 (fr) * 1989-12-12 1991-06-19 Enso-Gutzeit Oy Procédé de fabrication de pâte
WO1991019040A1 (fr) * 1990-06-07 1991-12-12 Stfi Procede de fabrication de pate de cellulose
WO1994018382A1 (fr) * 1993-02-09 1994-08-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procede de fabrication de pates a papier chimicothermomecaniques (ctmp)

Also Published As

Publication number Publication date
NO20023712L (no) 2002-10-04
WO2001059202A2 (fr) 2001-08-16
NZ520518A (en) 2004-02-27
AU779711B2 (en) 2005-02-10
AU3256001A (en) 2001-08-20
JP2003522844A (ja) 2003-07-29
EP1264037A2 (fr) 2002-12-11
NO20023712D0 (no) 2002-08-06
AU3256101A (en) 2001-08-20
EP1264038A2 (fr) 2002-12-11
NO20023711D0 (no) 2002-08-06
NO20023711L (no) 2002-10-04
WO2001059203A3 (fr) 2002-01-03
AU778689B2 (en) 2004-12-16
CA2399772A1 (fr) 2001-08-16
CA2399723A1 (fr) 2001-08-16
WO2001059202A3 (fr) 2002-01-03
JP2003522845A (ja) 2003-07-29

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