WO1999018285A1 - Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu - Google Patents

Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu Download PDF

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Publication number
WO1999018285A1
WO1999018285A1 PCT/US1998/020748 US9820748W WO9918285A1 WO 1999018285 A1 WO1999018285 A1 WO 1999018285A1 US 9820748 W US9820748 W US 9820748W WO 9918285 A1 WO9918285 A1 WO 9918285A1
Authority
WO
WIPO (PCT)
Prior art keywords
straw
mixture
pulp
chips
straw chips
Prior art date
Application number
PCT/US1998/020748
Other languages
English (en)
Inventor
Wayne H. Nay
William S. Fuller
Original Assignee
Weyerhaeuser Company
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 Weyerhaeuser Company filed Critical Weyerhaeuser Company
Priority to CA002304575A priority Critical patent/CA2304575A1/fr
Priority to EP98949727A priority patent/EP1021613A1/fr
Priority to JP2000515063A priority patent/JP2001519486A/ja
Priority to KR1020007003289A priority patent/KR20010030747A/ko
Priority to AU95992/98A priority patent/AU9599298A/en
Publication of WO1999018285A1 publication Critical patent/WO1999018285A1/fr

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/04—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres
    • D21B1/12—Fibrous raw materials or their mechanical treatment by dividing raw materials into small particles, e.g. fibres by wet methods, by the use of steam
    • D21B1/30—Defibrating by other means
    • D21B1/36—Explosive disintegration by sudden pressure reduction
    • 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
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate 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
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials

Definitions

  • This invention relates to a method for pre-processing and processing lignocellulosic material into pulp.
  • Emerson attempts to address the use of straw pulp in paper. Emerson teaches intertwining and crimping fibers into a paper web.
  • the present invention provides a method for pulping straw chips and forming a usable byproduct.
  • straw chips are mixed with steam and water to form a mixture.
  • the mixture is exposed to temperatures and pressures sufficient to significantly soften the straw chips to form straw pulp, lignins, and hemicellulose when exposed to a rapid decrease in pressure.
  • the mixture is washed to separate a portion of the lignins and hemicellulose from the straw pulp such that a usable byproduct of water, lignins and hemicellulose, referred to as black liquor, is formed and passed through a mechanical refiner.
  • the straw chips may be mixed with a caustic before the mixture of straw chips, steam and water is exposed to temperatures and pressures sufficient to significantly soften the straw chips to form straw pulp, lignins and hemicellulose in the mixture when exposed to a rapid decrease in pressure.
  • the caustic may be present in the mixture in about less than two percent by weight. It is more preferred that the caustic is present in the mixture in about less than one-half percent by weight.
  • the caustic may comprise sodium hydroxide. Also, the caustic may comprise potassium hydroxide.
  • the mixture may be exposed to temperatures and pressures sufficient to significantly soften the mixture when exposed to a rapid decrease in pressure for between about two and one-half minutes to about eight minutes.
  • At least about seventy percent by weight of the straw chips are formed into straw pulp.
  • the pressure sufficient to significantly soften the straw chips when exposed to a rapid decrease in pressure is between about 140 psig and about 200 psig.
  • the fiber chips may be selected from non- wood fibers such as ryegrass, wheat and a mixture of grain and cereal straws.
  • Straw chips for use in the method may be formed by chopping straw to form a mixture of straw chips, meal, ash and grit and screening the mixture to separate a substantial portion of the straw chips from the meal, ash and grit.
  • the meal, ash, and grit may be used as animal feed.
  • the meal, ash, and grit may be mixed with the black liquor byproduct to form animal feed.
  • the straw pulp formed by this method has a Canadian Standard Freeness between about 200 and about 600.
  • the present invention also provides a paper product made from wood pulp and straw pulp wherein the straw pulp is produced by mixing straw chips with steam and water to form a mixture of straw chips, steam and water. The mixture is exposed to temperatures and pressures sufficient to significantly soften the straw chips into straw pulp when exposed to decreased pressures. The mixture is then refined and a substantial portion of the straw pulp is separated from the mixture. A portion of the wood pulp and the paper product may be derived from processed post-consumer waste.
  • the straw chips may be formed by chopping straw to form a mixture of straw chips, meal, ash and grit and screening the mixture to separate a substantial portion of the straw chips from the meal, ash and grit.
  • the straw pulp has a Canadian Standard Freeness (CSF) of between about 200 and about 600 and an STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Fig. 1 is an elevational view of a rye grass plant
  • Fig. 2 is a flow diagram of a pre-processing plant constructed according to the method of the present invention.
  • Fig. 3 is a flow diagram of a pulping plant constructed according to the method of the present invention. BEST MODE FOR CARRYING OUT THE INVENTION
  • the present invention provides an improved method for pre-processing and processing various lignocellulosic source materials.
  • Suitable lignocellulosic materials include non-wood fibers such as grain and cereal straw, and corn stover.
  • the methods of the present invention have been found to be particularly suited for lignocellulosic material derived from grass and straw, such as annual ryegrass, fescue, and wheat.
  • straw chips may refer to chips derived from any non-wood fibers such as grain and cereal straw, grass and corn stover. However, for simplicity, all such chips shall be referred to as straw chips.
  • a ryegrass plant 10 is shown growing in soil 12.
  • the ryegrass plant 10 has seeds or kernels 14 held within ears 16, hollow stems or internodes 18 between joints or nodes 20, and an extensively branching fibrous root system 22. Sheath portions 24 are formed on the stems 18 and attach leaves 26 to the stems 18.
  • the ryegrass plants 10 are cut or swathed about three to six inches from the ground, generally below the first of the joints or nodes 20. Then, the cut ryegrass plants are left to cure in the fields for a few weeks. Seeds or kernels 14 may be harvested from the cut plants by use of a combine. After the combine has removed the seeds or kernels 14, the remainder of the ryegrass plants, generally known as straw 30, is dropped to the ground. The straw 30 may be recovered from the field and baled for storage prior to further processing.
  • straw 30 is fed into a tub grinder 28.
  • the straw 30 may be fed into the tub grinder 28 in bales.
  • the tub grinder 28 breaks up the bales and chops the straw into pieces averaging roughly one inch in length.
  • the chopped straw 32 includes nodes 20, leaves 26, sheath portion 24, and internodes 18, as well as ash, silica, and grit.
  • the chopped straw 32 is sent into a mill 34 to reduce the chopped straw 32 to pieces averaging roughly one-half inches in length.
  • the mill 34 grinds most of the nodes 20, leaves 26, and sheath portion 24 into powder.
  • the chopped straw 32 may be stored in a storage tank 35 before being sent to the mill 34 if the capacity of the mill 34 does not permit the chopped straw 32 to be fed directly from the tub 28 grinder to the mill 34.
  • milled mixture 36 is passed through multilayer screens
  • Meal 38 is dislodged and removed from straw chips 40 by passing the milled mixture 36 through the multilayer screens 37.
  • the meal 38 includes non-fibrous particles and ash, enriched with silica and grit.
  • the meal 38 may be used as an agricultural byproduct for feeding livestock.
  • the straw chips 40 are then ready for processing into pulp.
  • the straw chips 40 may be stored before further processing.
  • the pulp processing is to be carried out at a place remote from where the straw chips 40 have been preprocessed, the straw chips 40 may be transported by any manner used to transport bulk materials, such as by the use of containers.
  • the straw chips 40 are fed into a mixer 42 where they are mixed with steam and water 44 and any caustic or digestive additives 46.
  • the amount of digestive additives 46 utilized is calculated on a weight basis per amount of dry straw chips entering the system. Scales may be incorporated into the pulping process so that the straw chips 40 may be weighed as they enter the system and the amount of digestive additives 46 may be administered at the appropriate rate.
  • the amount of digestive additives 46 mixed with steam and water 44 and straw chips 40 is between about zero and about 2.0 percent by weight. However, it is more preferable that the amount of digestive additives 46 is between about zero and about 0.5 percent by weight.
  • Suitable digestive additives 46 for use in the present invention include sodium hydroxide and potassium hydroxide.
  • a stream 48 composed of straw chips 40, steam and water 44, and any digestive additives 46 is then fed into reactor 50.
  • stream 48 is exposed to temperatures and pressures sufficient for the steam 44 and any digestive additives 46 to penetrate the straw chips 40 such that when exposed to a rapid decrease in pressure, a mixture of softened chips, cellulose, lignins, hemicellulose and water is formed.
  • Suitable reactors for use in the present invention include continuous feed reactors such as those manufactured by Stake Technology, Ltd. of Oakville, Canada, and described in U.S. Patent Nos. 4,798,651 and 4,947,743, the contents of which are incorporated herein by reference.
  • reactor products 52 may be exposed to a rapid decrease in pressure by passing the reactor products 52 into a blow tank 56.
  • the reactor products 52 may be metered from the reactor 50 into the blow tank 56 by a blow valve 54.
  • the reactor products 52 include softened straw pulp mixed with lignins, hemicellulose and water. In other words, straw chips are steam exploded as they pass through the blow valve 54 when exiting the reactor 50 to form straw pulp, lignins and hemicellulose.
  • Stream 58 from the blow tank 56 is sent into a screw press 59 where stream 126 of a straw pulp mixture is separated from the steam exploded straw chips.
  • Stream 126 is composed substantially of black liquor and undissolved solids.
  • stream 126 is substantially composed of water, reacted lignins and hemicellulose.
  • Stream 126 is sent to a byproduct chest 142.
  • Stream 144 from byproduct chest 142 is passed through filtration system 128. Solids 130 removed at filtration system 128 are sent to blow tank 56.
  • Liquid stream 138 from filtration system 128 are collected in storage tank 140.
  • the black liquor collected in storage tank 140 constitutes a usable byproduct.
  • This byproduct has usefulness as an animal feed additive.
  • the byproduct may be mixed with meal 38 from preprocessing to form animal feed.
  • the animal feed may be formed into a mash or pellets by methods known in the art.
  • Stream 61 from screw press 59 is then defiberized.
  • the defiberization may be carried out by a mechanical refiner 60, such as an Ahlstrom MDR (frotopulper).
  • the pulp is then ready to be washed.
  • the pulp may be washed by any method, such as dilution and extraction.
  • the refined pulp mixture 62 may be sent to a dilution tank 64 where it is diluted with water 73.
  • diluted pulp mixture 66 from tank 64 may be thickened by use of a wash press 68. Weak black liquor in stream 69 from wash press 68 is sent to blow tank 56.
  • Thickened pulp 70 may then be screened to remove unwanted particles.
  • the thickened pulp 70 may be sent to a prescreening dilution tank 72 where it is mixed with water 73.
  • Diluted pulp 74 from the dilution tank 72 may then be passed into a primary screening 76.
  • Accepts 78 from the primary screening 76 may be collected in accepts tank 84.
  • Rejects 86 from primary screening 76 may be passed to a primary screen rejects tank 90.
  • Rejects 92 from rejects tank 90 may be passed to a secondary screening 80.
  • Accepts 82 from secondary screening 80 may be collected in accepts tank 84.
  • Rejects 88 from secondary screening 80 are sent to drainer 146.
  • Drained stream 148 is sent to a secondary rejects tank 150.
  • Stream 152 from secondary rejects tank 150 is sent to a rejects defiberizer 154.
  • Stream 156 from the rejects defiberizer 154 is collected in a tertiary screen feed tank 158.
  • Stream 160 from the tertiary screen feed tank 158 is passed through a tertiary screening 162.
  • Accepts 164 from tertiary screening 162 are collected in the rejects tank 90.
  • Rejects 166 from tertiary screening 162 are sent to the drainer 146.
  • the protein level of the straw is determined to be about three to four percent (3%-4%).
  • the moisture content of the rye grass straw is determined to be approximately ten percent (10%).
  • the annual rye grass straw is preprocessed and pulped according to the method described in the best mode of this application and as set forth herein.
  • Bales of the rye grass straw are fed into an agricultural tub grinder where the bales are broken up and the straw chopped into pieces averaging roughly one (1) inch in length.
  • the agricultural tub grinder has grate plates with round holes sized between about one half (0.5) inches and about two (2) inches.
  • the chopped straw is sent into a disc mill.
  • the disc mill is a United Milling Systems mill which has milling gaps of between about 0.6 mm and about 1.0 mm. In the disc mill, the chopped straw is reduced into approximately one-half inch pieces. Also, the disc mill grinds most of the hard node, leaf and sheath of the straw into a powder. Ash and grit are determined to compose approximately two to five percent (2%-5%) of the straw fed into the tub grinder.
  • the straw After leaving the milling machine, the straw is passed into a vibrating six-deck screen of 35 mesh.
  • the screen is a gyratory screen equipped with fine mesh and ball decks for cleaning fines and dirt from the surfaces of the screen.
  • Approximately eighteen percent (18%) of the straw mixture is removed at the screen as meal. Part of the meal removed is the powder formed in the disc mill by the hard node, leaf and sheath of the straw. The remainder of the straw chips leaving the screen averages approximately one half (V2) inch in size.
  • the meal has a protein level of about eight to thirteen percent (8%-13%).
  • the silica content is between about 8-15%. It is determined that the meal removed at the screen is usable as animal feed.
  • the preprocessed straw chips are then stored prior to pulping.
  • the straw chips are preprocessed at a site remote from the pulping system.
  • the preprocessed straw chips are transported to the pulping system in container trucks.
  • the preprocessed straw chips are fed into a pulping system at a rate consistent with the capacity of the pulping system.
  • the preprocessed straw chips are fed into a mixer where they are mixed with steam and water to achieve a moisture content of about 40-50% based on the charge of preprocessed straw chips to the mixer.
  • the preprocessed straw chips mixed with steam and water are fed into a Stake Digester steam explosion reactor. In the reactor, the preprocessed straw chips are exposed to pressure of about 160 psig for about five and a half (514) minutes.
  • Pulp from the reactor is metered into a blow tank by a blow valve. Pulp from the blow tank is passed through a screwpress where black liquor is separated from the pulp. Then the pulp is defiberized or refined in an Ahlstrom frotopulper mechanical refiner. The refined pulp is sent to a dilution tank where it is mixed with liquid at a dilution factor of about 2.5. The diluted pulp is then thickened by use of a wash press. The thickened pulp is screened in a two-stage pressure screen with about 0.010 inch slotted plates.
  • the straw pulp is determined to have a Canadian Canadian
  • CSF Standard Freeness
  • OCC pulp derived from recycled corrugated cardboard
  • CSF Canadian Standard Freeness
  • STFI Standard Freeness
  • OCC pulp derived from recycled corrugated cardboard
  • Kraft pulp is determined to have a Canadian Standard Freeness (CSF) of between about 450 and about 750 and STFI of between about 21 and about 26.
  • Straw pulp with a Canadian Standard Freeness (CSF) between about 200 and about 600 and STFI between about 14 and about 21 is suitable to be blended with Kraft pulp and OCC to make liner board in standard mill grades.
  • the straw pulp comprises about less than twenty percent (20%) of the liner board furnish.
  • Example 1 is repeated using about one-half percent (0.5%) by weight sodium hydroxide in the mixer. After exiting the process, the straw pulp is determined to have a Canadian
  • Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • Example 1 is repeated using about one percent (1%) by weight sodium hydroxide in the mixer.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated using two percent (2%) by weight sodium hydroxide in the mixer.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated using about one-half percent (0.5%) by weight potassium hydroxide in place of the sodium hydroxide in the mixer. After exiting the process, the straw pulp is determined to have a Canadian
  • Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • Example 1 is repeated using about one percent (1%) by weight potassium hydroxide in place of the sodium hydroxide in the mixer.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated using about two percent (2%) by weight potassium hydroxide in place of the sodium hydroxide in the mixer.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated allowing the preprocessed straw chips mixed water to remain in the reactor for about two and one-half minutes. After exiting the process, the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated allowing the preprocessed straw chips mixed water to remain in the reactor for about 4 minutes.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated allowing the preprocessed straw chips mixed with water to remain in the reactor for about six (6) minutes.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated allowing the preprocessed straw chips mixed water to remain in the reactor for about eight (8) minutes. After exiting the process, the straw pulp is determined to have a Canadian
  • Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • Example 1 is repeated with the preprocessed straw chips mixed with water to be exposed to a pressure of about 140 psig in the reactor.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated with the preprocessed straw chips mixed with water to be exposed to a pressure of about 180 psig in the reactor.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness
  • Example 1 is repeated with the preprocessed straw chips mixed with water to be exposed to a pressure of about 200 psig in the reactor.
  • the straw pulp is determined to have a Canadian Standard Freeness (CSF) of between about 200 and about 600 and STFI between about 14 and about 21.
  • CSF Canadian Standard Freeness

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Paper (AREA)

Abstract

La présente invention concerne le pré-traitement et le traitement de la pâte de paille et la formation d'un sous-produit convenant à la consommation animale. L'invention concerne également un produit de papeterie comprenant de la pâte de paille. Le procédé consiste à former la pâte de paille en soumettant à vapocraquage les copeaux de paille, soit en présence d'une faible quantité d'un caustique, soit en l'absence totale de caustique.
PCT/US1998/020748 1997-10-07 1998-09-30 Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu WO1999018285A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CA002304575A CA2304575A1 (fr) 1997-10-07 1998-09-30 Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu
EP98949727A EP1021613A1 (fr) 1997-10-07 1998-09-30 Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu
JP2000515063A JP2001519486A (ja) 1997-10-07 1998-09-30 わらを処理してパルプにする方法及びそれから得られる紙製品
KR1020007003289A KR20010030747A (ko) 1997-10-07 1998-09-30 짚을 펄프로 가공하는 방법 및 이로부터 제조된 종이제품
AU95992/98A AU9599298A (en) 1997-10-07 1998-09-30 Method for processing straw into pulp and paper product therefrom

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US94649797A 1997-10-07 1997-10-07
US08/946,497 1997-10-07

Publications (1)

Publication Number Publication Date
WO1999018285A1 true WO1999018285A1 (fr) 1999-04-15

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Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1998/020748 WO1999018285A1 (fr) 1997-10-07 1998-09-30 Transformation de la paille en pate a papier, et produit de papeterie ainsi obtenu

Country Status (8)

Country Link
US (1) US20020003032A1 (fr)
EP (1) EP1021613A1 (fr)
JP (1) JP2001519486A (fr)
KR (1) KR20010030747A (fr)
CN (1) CN1273618A (fr)
AU (1) AU9599298A (fr)
CA (1) CA2304575A1 (fr)
WO (1) WO1999018285A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1098389C (zh) * 1999-08-13 2003-01-08 中国科学院化工冶金研究所 利用低压汽爆秸秆类植物制纸浆的无污染方法
EP1450994A1 (fr) * 2001-11-06 2004-09-01 Lignotech Developments Limited Traitement de materiaux ligno-cellulosiques
WO2008141464A1 (fr) 2007-05-23 2008-11-27 Alberta Research Council Inc. Procédé de décortication
WO2011072718A1 (fr) * 2009-12-15 2011-06-23 Södra Cell Ab Procédé de fabrication de pâte
EP2762637A1 (fr) 2013-02-01 2014-08-06 Soremartec S.A. Carton multicouche comprenant des résidus agro-industriels
WO2023175175A1 (fr) 2022-03-18 2023-09-21 Anheuser-Busch Inbev S.A. Emballage fabriqué à partir de fibres végétales agricoles

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US7198925B2 (en) * 2004-09-30 2007-04-03 Iogen Energy Corporation Pre-treatment of bales of feedstock
BRPI0811760A2 (pt) * 2007-06-20 2014-11-11 Nagarjuna Energy Private Ltd Processo para separação de componentes de biomassa
BRPI0817084B1 (pt) * 2007-09-07 2019-05-21 Council Of Scientific & Industrial Research Processo para o fracionamento de bagaço de cana-de-açúcar em polpa de alfa-celulose superior, xilano e lignina
WO2009119956A1 (fr) * 2008-03-27 2009-10-01 Chan Oh Park Fibre herbacée et son procédé de fabrication, et raffineur pour sa fabrication
CA2638157C (fr) 2008-07-24 2013-05-28 Sunopta Bioprocess Inc. Methode et appareil permettant le transport d'une charge d'alimentation cellulosique
US8915644B2 (en) 2008-07-24 2014-12-23 Abengoa Bioenergy New Technologies, Llc. Method and apparatus for conveying a cellulosic feedstock
CA2638159C (fr) 2008-07-24 2012-09-11 Sunopta Bioprocess Inc. Methode et appareil permettant le traitement d'une charge d'alimentation cellulosique
US9127325B2 (en) 2008-07-24 2015-09-08 Abengoa Bioenergy New Technologies, Llc. Method and apparatus for treating a cellulosic feedstock
CA2638160C (fr) 2008-07-24 2015-02-17 Sunopta Bioprocess Inc. Methode et appareil permettant le transport d'une charge d'alimentation cellulosique
CA2650913C (fr) 2009-01-23 2013-10-15 Sunopta Bioprocess Inc. Methode et appareillage de transport de produits de depart cellulosiques
CA2650919C (fr) 2009-01-23 2014-04-22 Sunopta Bioprocess Inc. Methode et installation de transport de produit de depart cellulosique
CA2638150C (fr) 2008-07-24 2012-03-27 Sunopta Bioprocess Inc. Methode et appareil permettant le transport d'une charge d'alimentation cellulosique
BRPI1009093A2 (pt) 2009-08-24 2016-03-01 Abengoa Bioenergy New Technologies Inc "método para pré-tratamento do estoque de alimentação de biomassa celulósica que compreende celulose, hemicelulose, e lignina".
BRPI1100063A2 (pt) 2010-05-07 2017-04-04 Abengoa Bioenergy New Tech Inc processos para a recuperação de valores de uma massa de fermentação, e para extração de lignina e inorgânicos, e, produtos de sólidos ricos em lignina
CN103510418B (zh) 2012-06-25 2016-03-30 北京英力生科新材料技术有限公司 一种无黑液化学制浆工艺
JP6362732B1 (ja) * 2017-05-31 2018-07-25 日本製紙株式会社 反芻動物用飼料原料

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US131465A (en) * 1872-09-17 Improvement in processes of disintegrating vegetable fiber s
US5656129A (en) * 1995-05-31 1997-08-12 Masonite Corporation Method of producing fibers from a straw and board products made therefrom

Patent Citations (2)

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Publication number Priority date Publication date Assignee Title
US131465A (en) * 1872-09-17 Improvement in processes of disintegrating vegetable fiber s
US5656129A (en) * 1995-05-31 1997-08-12 Masonite Corporation Method of producing fibers from a straw and board products made therefrom

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1098389C (zh) * 1999-08-13 2003-01-08 中国科学院化工冶金研究所 利用低压汽爆秸秆类植物制纸浆的无污染方法
EP1450994A1 (fr) * 2001-11-06 2004-09-01 Lignotech Developments Limited Traitement de materiaux ligno-cellulosiques
EP1450994A4 (fr) * 2001-11-06 2005-06-01 Lignotech Developments Ltd Traitement de materiaux ligno-cellulosiques
WO2008141464A1 (fr) 2007-05-23 2008-11-27 Alberta Research Council Inc. Procédé de décortication
EP2152945A1 (fr) * 2007-05-23 2010-02-17 Alberta Research Council, Inc. Procédé de décortication
EP2152945A4 (fr) * 2007-05-23 2014-09-24 Alberta Innovates Technology Futures Procédé de décortication
WO2011072718A1 (fr) * 2009-12-15 2011-06-23 Södra Cell Ab Procédé de fabrication de pâte
EP2762637A1 (fr) 2013-02-01 2014-08-06 Soremartec S.A. Carton multicouche comprenant des résidus agro-industriels
WO2023175175A1 (fr) 2022-03-18 2023-09-21 Anheuser-Busch Inbev S.A. Emballage fabriqué à partir de fibres végétales agricoles

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CA2304575A1 (fr) 1999-04-15
AU9599298A (en) 1999-04-27
US20020003032A1 (en) 2002-01-10
KR20010030747A (ko) 2001-04-16
EP1021613A1 (fr) 2000-07-26
JP2001519486A (ja) 2001-10-23
CN1273618A (zh) 2000-11-15

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