US20110036523A1 - Method for manufacturing mechanical pulp - Google Patents

Method for manufacturing mechanical pulp Download PDF

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Publication number
US20110036523A1
US20110036523A1 US12/158,222 US15822207A US2011036523A1 US 20110036523 A1 US20110036523 A1 US 20110036523A1 US 15822207 A US15822207 A US 15822207A US 2011036523 A1 US2011036523 A1 US 2011036523A1
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Prior art keywords
stock
rejected
accepted
pulp
mechanical pulp
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Abandoned
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US12/158,222
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English (en)
Inventor
Esko Härkönen
Taisto Tienvieri
Jouko H. Lehto
Markku Gummerus
Folke Örså
Liisa Pirinen
Mia Piirainen
Jean-Cristophe Hostachy
Serge Kocimski
Ernst-Martin Billing
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UPM Kymmene Oy
ITT Manufacturing Enterprises LLC
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UPM Kymmene Oy
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Application filed by UPM Kymmene Oy filed Critical UPM Kymmene Oy
Assigned to ITT MANUFACTURING ENTERPRISES, INC., UPM-KYMMENE CORPORATION reassignment ITT MANUFACTURING ENTERPRISES, INC. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: KOCIMSKI, SERGE, HOSTACHY, JEAN-CRISTOPHE, PIIRAINEN, MIA, GUMMERUS, MARKKU, PIRINEN, LIISA, BILLING, ERNST-MARTIN, LEHTO, JOUKO H., ORSA, FOLKE, HARKONEN, ESKO, TIENVIERI, TAISTO
Publication of US20110036523A1 publication Critical patent/US20110036523A1/en
Abandoned legal-status Critical Current

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    • 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
    • D21B1/14—Disintegrating in mills
    • D21B1/16—Disintegrating in mills in the presence of chemical agents
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/147—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications
    • D21C9/153—Bleaching ; Apparatus therefor with oxygen or its allotropic modifications with ozone

Definitions

  • Publication F161926 and corresponding publication DE 2444475 disclose a process in which pulp is treated with ozone. It is possible that the pH of the pulp is adjusted after the ozonation.
  • Publication F167412 and corresponding publication CA 1083870 disclose a process in which pulp is fractionated and one fraction, possibly the coarse fraction, is treated with ozone. During the ozonation alkali is fed into the process.
  • a problem related to the ozonation process is that it produces strong organic acids.
  • the organic acids lower the pH of the pulp, which causes problems in a bleaching process, e.g. by precipitating ferrous substances from the process water.
  • the organic acids also deteriorate process devices by causing corrosion.
  • the above-mentioned drawbacks can be overcome by the method of the invention.
  • the method comprises
  • raw material of the mechanical pulp is introduced in a process.
  • the raw material can be softwood species, such as pine ( Pinus sylvestris ), Southern pine (genus Pinus , several different species), spruce ( Picea abies ), or mixtures of pine and spruce. Hardwood species and their mixtures with softwood species are also possible raw materials.
  • the raw material can be in form of wood chips.
  • the starting raw material can also be logs which are ground in a PGW (pressure groundwood) process.
  • the raw material such as wood chips, which are dewatered in order to reach a consistency which is from 25% to 35%, typically 30%, is fed in a refiner in which it is refined in a first refining stage.
  • the refiner can be a disc refiner or a disc refiner with a conical section.
  • the raw material is refined at an elevated temperature and under pressure in the refiner in order to form mechanical pulp.
  • the first refining stage can also be accomplished by a hammer mill.
  • the preferred raw material is pine because the method of the invention is the most advantageous compared to other processes when the raw material is pine. It is commonly known that the refining ability of pine is poor. However, by using ozone it can be improved. Pulp treated with ozone contains less fines and shives compared to pulp which is not treated with ozone. The ozone treatment has also a beneficial effect on a pitch removal which is important in connection with the pine raw material.
  • the first stage refining is rather mild; the pulp is refined to a freeness of 600-700 ml CSF.
  • the upper limit can be even higher than 700 ml CSF.
  • the pulp can be sorted to a first accepted stock and a first rejected stock, and the rejected stock is led to the alkali treatment reactor.
  • the whole mechanical pulp is led to the alkali treatment reactor in order to achieve a certain pH level.
  • the mechanical pulp is treated with alkali, such as sodium hydroxide (NaOH), sodium bicarbonate (Na 2 CO 3 ), magnesium hydroxide (Mg(OH) 2 ), or calcium hydroxide (Ca(OH) 2 ).
  • alkali such as sodium hydroxide (NaOH), sodium bicarbonate (Na 2 CO 3 ), magnesium hydroxide (Mg(OH) 2 ), or calcium hydroxide (Ca(OH) 2 ).
  • the process in the alkali treatment reactor is arranged so that there is a process delay, i.e. the pulp stays in the reactor for at least 0.5 hours, typically from 1 to 2 hours.
  • the process delay is necessary because the alkali should penetrate from the surface of the fibers of the pulp to the inner parts of the fibers (or fiber aggregates, depending on how coarse the pulp is), i.e. also the inner parts of the fibers and/or fiber aggregates shall
  • the pulp After the pulp is treated in the alkali treatment reactor, it is led to a sorter, such as a screen or a cyclone.
  • the pulp is sorted to a first accepted stock and a first rejected stock.
  • the sorting step takes place in a consistency of from 0.5 to 1.5 percent, typically about one percent, and the first accepted stock remains in that consistency after sorting.
  • the ratio accepted stock/rejected stock may be approximately 20/80.
  • the ratio accepted stock/rejected stock may also be 60/40 or 50/50.
  • the accepted stock may be between 20 and 60 percent of the total amount of the pulp, or even between 15 and 65 percent of the total amount of the pulp.
  • the first rejected stock is first dewatered so that the consistency of the first rejected stock is preferably higher than 30%.
  • the consistency is more preferably higher than 35%.
  • Excess liquid is circulated back to the process.
  • the first rejected stock is led in the above-mentioned consistency to an ozone reactor in which the first rejected stock is fluffed and ozonated.
  • the ozonation process is arranged so that the amount of ozone is between 0.5 and 10% and preferably between 1 and 4% of the weight of the pulp.
  • the process temperature is between 20 and 90° C. Strong organic acids form in the ozonation process, but the alkali by which the first rejected stock has been treated neutralizes those strong organic acids.
  • the strong organic acids and the alkali form a buffer solution whose pH can be kept on a certain level for a long time although the ozonation process constantly produces organic acids.
  • the pH of the rejected stock is between 5 and 7, which is a beneficial range in regard to the following process steps.
  • the first rejected stock is refined in a main line refining which may comprise sequential refiners. It is possible that that the first rejected stock is sorted to a second accepted stock and a second rejected stock.
  • the second rejected stock can be conveyed for further refining, i.e. to a third refining stage, but it is also possible that it is just removed from the process. If there is the third refining stage it is accomplished in the same manner as the preceding refining stages.
  • the first accepted stock and the accepted amount of the first rejected stock are combined after the above-mentioned process stages.
  • the accepted amount of the first rejected stock refers to all accepted stocks which have been obtained after the pulp has been sorted to the first accepted stock and the first rejected stock.
  • the first accepted stock is treated with ozone and the ozone treated pulps are combined. It is also possible that some alkali is added to the first accepted stock after it has been treated with ozone. The alkali may be the same that is added before the ozonation. Further, it is possible that the accepted stock which has not been ozonated is treated with the alkali before it is combined with the accepted amount of the first rejected stock.
  • the freeness of the resulting stock may be between 90 and 150 ml CSF but it is also possible that the lower limit is 30 or 40 ml CSF. Naturally, the above-mentioned freeness depends on the desired paper quality.
  • the pulp is sorted in a sorter, such as a screen or a cyclone, to a first accepted stock and a first rejected stock.
  • the consistency in the sorter is between 1 and 2%.
  • the ratio accepted stock/rejected stock may be approximately 20/80.
  • the ratio accepted stock/rejected stock may also be 60/40 or 50/50.
  • the accepted stock may be between 20 and 60 percent of the total amount of the pulp, or even between 15 and 65 percent of the total amount of the pulp.
  • the first rejected stock is treated with alkali, such as sodium hydroxide (NaOH), sodium bicarbonate (Na 2 CO 3 ), magnesium hydroxide (Mg(OH) 2 ), or calcium hydroxide (Ca(OH) 2 ), in an alkali treatment reactor.
  • alkali such as sodium hydroxide (NaOH), sodium bicarbonate (Na 2 CO 3 ), magnesium hydroxide (Mg(OH) 2 ), or calcium hydroxide (Ca(OH) 2
  • the pH of the first rejected stock is elevated to a level which is between 9 and 11 depending on the ozone amount to be applied and the raw material to be treated.
  • After that liquid is removed from the first rejected stock so that a consistency which is preferably higher than 30% is achieved.
  • the consistency is more preferably higher than 35%. Excess liquid is circulated back to the process.
  • the first rejected stock is led in the above-mentioned consistency to an ozone reactor in which the first rejected stock is fluffed and ozonated.
  • the ozonation process is arranged so that the amount ozone is between 0.5 and 10% and preferably between 1 and 4% of the weight of the pulp.
  • the process temperature is between 20 and 90° C.
  • Strong organic acids form in the ozonation process, but the alkali by which the first rejected stock has been treated neutralizes those strong organic acids.
  • the strong organic acids and the alkali form a buffer solution whose pH can be kept on a certain level for a long time although the ozonation process constantly produces organic acids.
  • the pH of the rejected stock is between 5 and 7, which is a beneficial range in regard to the following process steps.
  • the first rejected stock is led to a refiner in order to accomplish a second refining stage.
  • the first rejected stock is conveyed from the refiner to a sorter which sorts the first rejected stock to a second accepted stock and a second rejected stock.
  • the freeness of the accepted stocks i.e. the stock consisting of the first accepted stock and the second accepted stock, may be between 90 and 150 ml CSF but it is also possible that the lower limit is 30 or 40 ml CSF. Naturally, the above-mentioned freeness depends on the desired paper quality.
  • the second rejected stock can be conveyed for further refining, i.e. to the third refining stage, but it is also possible that it is just removed from the process. If there is the third refining stage, it is accomplished in the same manner as the preceding refining stages.
  • the first accepted stock may be removed from the process and used for other purposes, but it is also possible that the first accepted stock and the second accepted stock are combined so that they can be led as one stock to the following process step, which is usually a bleaching step.
  • the stock obtained from the second refining stage has a pH that is between 5 and 7, and the first accepted stock has about the same pH, so no further steps are required to adjust the pH level.
  • Harmful wood extractives are soluble in the water in which the alkali is added.
  • the mechanical pulp obtained from the present method (the above-mentioned first and second main options) is utilized in a paper product manufacturing process.
  • the paper product may be a paper containing mechanical pulp, such as a printing paper containing mechanical pulp, or it may be a cardboard.
  • FIG. 1 shows a schematic view of a first process
  • FIG. 2 shows a schematic view of a second process
  • FIG. 3 shows schematic views of third and fourth processes
  • FIG. 4 shows tensile index as a function of SEC (specific energy consumption).
  • FIG. 5 shows tear index as a function of tensile index.
  • Points 1 and 2 correspond to the results achieved from a normal TMP refining in which pine is used as the raw material.
  • Point 5 in FIGS. 5 and 6 corresponds to the results achieved from a process in which an ozonated pine reject is mixed with a non-ozonated pine accept. No alkali is added.
  • Point 7 in FIGS. 5 and 6 corresponds to the results achieved from a process in which an ozonated pine reject is mixed with an ozonated pine accept. No alkali is added.
  • Raw material of mechanical pulp is first dewatered, for example, in a thickener 1 , such as a screw press, and after that the raw material is fed into a refiner 2 , in which the raw material, such as pine chips, is refined in a first stage refining at an elevated temperature and under pressure in order to form mechanical pulp.
  • the consistency during the refining is about 30%.
  • the preferred raw material is pine because the method of the invention is the most advantageous compared to other processes when the raw material is pine.
  • the first stage refining is rather mild; The pulp is refined to a freeness of 600-700 ml CSF. It is possible that the freeness value is even higher than 700 ml CSF.
  • the pulp is treated with an alkali, such as sodium hydroxide, in an alkali treatment reactor 3 .
  • the pH of the first rejected stock is elevated to a level which is between 9 and 11.
  • There is a delay in the alkali treatment reactor 3 so that the pulp remains inside the alkali treatment reactor for at least 0.5 hours, typically from 1 to 2 hours.
  • the pulp is also diluted in the alkali treatment reactor so that its consistency is between 0.5 and 1.5%.
  • the pulp is sorted in a sorter 4 , such as a screen, to a first accepted stock A 1 and a first rejected stock R 1 .
  • a sorter 4 such as a screen
  • the ratio accepted stock/rejected stock is approximately 20/80, but also other ratios, which are described in the general description, are suitable.
  • the first rejected stock R 1 is led to a thickener 5 , such as a screw press, which removes liquid from the stock in such a manner that a consistency which is higher than 35% has been achieved. Excess liquid 9 is circulated back to the process.
  • the first rejected stock R 1 is led in the above-mentioned consistency to an ozone reactor 6 in which the first rejected R 1 stock is ozonated. Strong organic acids form in the ozonation process but the alkali by which the first rejected stock has been treated neutralizes those strong organic acids.
  • the strong organic acids and the alkali form a buffer solution whose pH can be kept on a certain level for a long time although the ozonation process constantly produces organic acids.
  • the pH of the rejected stock is between 5 and 7, which is a beneficial range in regard to the following process steps.
  • the first rejected stock R 1 is led to a refiner 7 .
  • the first rejected stock R 1 has been treated with ozone, its properties have been changed so that the refining stage consumes much less energy compared to stocks which are not treated with ozone.
  • the first rejected stock R 1 may be conveyed from the refiner 7 to another refiner 8 . It is also possible that the first rejected stock is led to a sorter (not shown) which sorts the first rejected stock to a second accepted stock and a second rejected stock.
  • the second rejected stock can be conveyed for further refining but it is also possible that it is just removed from the process.
  • the first accepted stock and the accepted amount of the first rejected stock may be combined after the first rejected stock has been treated in the above-mentioned manner so that they can be led as one stock to the following process step, which is usually a bleaching step.
  • the obtained stock has the pH which is between 5 and 7.
  • Point 4 in FIGS. 4 and 5 corresponds to the result which is achieved from the above-described process.
  • Raw material of mechanical pulp is first dewatered, for example, in a thickener 1 , such as a screw press, and after that the raw material is fed into a refiner 2 , in which the raw material, such as pine chips, is refined in a first stage refining at an elevated temperature and under pressure in order to form mechanical pulp.
  • the consistency of the pulp is about 30%.
  • the preferred raw material is pine because the method of the invention is the most advantageous compared to other processes when the raw material is pine.
  • the first stage refining is rather mild; the pulp is refined to a freeness of 600-700 ml CSF.
  • the pulp is treated with an alkali, such as sodium hydroxide, in an alkali treatment reactor 3 .
  • the pH of the first rejected stock is elevated to a level which is between 9 and 11.
  • There is a delay in the alkali treatment reactor 3 so that the pulp remains inside the alkali treatment reactor for at least 0.5 hours, typically from 1 to 2 hours.
  • the pulp is diluted to a consistency which is between 0.5 and 1.5%.
  • the pulp is sorted in a sorter 4 , such as a screen, to a first accepted stock A 1 and a first rejected stock R 1 .
  • a sorter 4 such as a screen
  • the ratio accepted stock/rejected stock is approximately 20/80, but also other ratios are suitable.
  • the first rejected stock R 1 is led to a thickener 5 , such as a screw press, which removes liquid from the stock in such a manner that a consistency which is higher than 35% has been achieved. Excess liquid 9 is circulated back to the process.
  • the first rejected stock R 1 is led in the above-mentioned consistency to an ozone reactor 6 in which the first rejected R 1 stock is ozonated.
  • the amount of ozone is between 0.5 and 10% and preferably between 1 and 4% of the weight of the pulp.
  • the temperature during the ozonation is between 20° C. and 90° C.
  • the first rejected stock R 1 is led to a refiner 7 .
  • the first rejected stock R 1 has been treated with ozone, its properties have been changed so that the second refining stage consumes much less energy compared to stocks which are not treated with ozone.
  • the first rejected stock R 1 may be conveyed from the refiner 7 to another refiner 8 . It is also possible that the first rejected stock is led to a sorter (not shown) which sorts the first rejected stock to a second accepted stock and a second rejected stock.
  • the second rejected stock can be conveyed for further refining, but it is also possible that it is just removed from the process.
  • the first accepted stock A 1 is led to an ozone reactor 11 at a consistency which is between 0.5 and 1.5%.
  • the first accepted stock A 1 is ozonated in the ozone reactor 11 .
  • Ozone may be injected to the first accepted stock A 1 .
  • the first accepted stock A 1 and the accepted amount of the first rejected stock R 1 are combined after the first stocks have been treated in the above-mentioned manner so that they can be led as one stock to the following process step, which is usually a bleaching step.
  • the obtained stock has a pH which is between 5 and 7.
  • Point 6 in FIGS. 4 and 5 corresponds to the result which is achieved from the above-described process option.
  • the third process is similar to that in example 2, except that the first accepted stock is treated with alkali after the ozonation in a mixing reactor 13 .
  • the amount of the alkali was 0.5 wt.-% of the total amount of the dry first accepted stock (for example, 0.5 wt.-% of 100% NaOH).
  • a process delay is arranged to the mixing reactor 13 . The pulp stays in the reactor 13 at least for 0.5 hours.
  • Point 8 in FIGS. 4 and 5 corresponds to the result which is achieved from the above-described process option.
  • the fourth process is similar to that in example 2, except that the first accepted stock is treated with alkali after the ozonation in a mixing reactor 13 .
  • the amount of the alkali was 2 wt.-% of the total amount of the dry first accepted stock (for example, 2 wt.-% of 100% NaOH).
  • a process delay is arranged to the mixing reactor 13 .
  • the pulp stays in the reactor 13 at least for 0.5 hours.
  • Point 9 in FIGS. 4 and 5 corresponds to the result which is achieved from the above-described process option.

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  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Paper (AREA)
US12/158,222 2006-12-28 2007-12-27 Method for manufacturing mechanical pulp Abandoned US20110036523A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FI20065860A FI119062B (fi) 2006-12-28 2006-12-28 Menetelmä mekaanisen massan valmistamiseksi
FI20065860 2006-12-28
PCT/FI2007/050721 WO2008081078A1 (en) 2006-12-28 2007-12-27 A method for manufacturing mechanical pulp

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US20110036523A1 true US20110036523A1 (en) 2011-02-17

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US12/158,222 Abandoned US20110036523A1 (en) 2006-12-28 2007-12-27 Method for manufacturing mechanical pulp

Country Status (9)

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US (1) US20110036523A1 (ru)
EP (1) EP2097582A4 (ru)
JP (1) JP4882090B2 (ru)
CN (1) CN101389808B (ru)
BR (1) BRPI0707368A2 (ru)
CA (1) CA2633800C (ru)
FI (1) FI119062B (ru)
RU (1) RU2373313C1 (ru)
WO (1) WO2008081078A1 (ru)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8877007B2 (en) 2012-08-21 2014-11-04 University Of New Brunswick System and method for reclaiming rejects in sulfite pulping
US20150122430A1 (en) * 2012-05-21 2015-05-07 Oji Holdings Corporation Method for producing fine fibers and sheet containing fine fibers
JP2017538044A (ja) * 2014-11-21 2017-12-21 インヴェンティア・アクチボラゲットＩｎｎｖｅｎｔｉａ Ａｂ 処理パルプの製造方法

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI123113B (fi) * 2008-09-10 2012-11-15 Upm Kymmene Corp Menetelmä mekaanisen massan valmistamiseksi ja mekaanisen massan käyttö
FR2937656B1 (fr) * 2008-10-24 2010-11-19 Arkema France Procede de fabrication de pate a papier
JP5729095B2 (ja) * 2011-03-31 2015-06-03 日本製紙株式会社 広葉樹機械パルプの製造方法
FR2980805B1 (fr) 2011-09-30 2013-09-20 Arkema France Pretraitement enzymatique de bois dans un procede de fabrication de pate a papier mecanique
EP3502348B1 (en) * 2017-12-21 2020-06-24 BillerudKorsnäs AB Fibre fractionation

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Publication number Priority date Publication date Assignee Title
US3013932A (en) * 1958-01-14 1961-12-19 Hawaiian Dev Company Ltd Printing paper and process of making the same
US4279694A (en) * 1977-10-17 1981-07-21 Myrens Verksted A/S Method for treating refined mechanical pulp and thermo mechanical pulp with ozone
US4718980A (en) * 1985-12-30 1988-01-12 Weyerhaeuser Company Interstage treatment of mechanical pulp
US5503709A (en) * 1994-07-27 1996-04-02 Burton; Steven W. Environmentally improved process for preparing recycled lignocellulosic materials for bleaching

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NO131996C (ru) 1973-10-04 1975-09-03 Papirind Forskningsinst
FI67412C (fi) 1977-04-27 1985-03-11 Myrens Verksted As Foerfarande foer behandling av cellulosahaltig massa
JP2825346B2 (ja) * 1990-05-17 1998-11-18 ユニオン キャンプ コーポレイション リグノセルロース物質の環境上改良された漂白方法
SE520707C2 (sv) * 2001-12-05 2003-08-12 Metso Paper Inc Metod och system för behandling av massa vid ozonblekning
FI121792B (fi) * 2003-06-30 2011-04-15 Andritz Oy Menetelmä massan käsittelemiseksi kemiallisen massan valkaisun yhteydessä
CN1263923C (zh) * 2004-09-15 2006-07-12 中国科学院广州化学研究所 木塑复合材料用甘蔗渣的超声化学前处理方法

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3013932A (en) * 1958-01-14 1961-12-19 Hawaiian Dev Company Ltd Printing paper and process of making the same
US4279694A (en) * 1977-10-17 1981-07-21 Myrens Verksted A/S Method for treating refined mechanical pulp and thermo mechanical pulp with ozone
US4718980A (en) * 1985-12-30 1988-01-12 Weyerhaeuser Company Interstage treatment of mechanical pulp
US5503709A (en) * 1994-07-27 1996-04-02 Burton; Steven W. Environmentally improved process for preparing recycled lignocellulosic materials for bleaching

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150122430A1 (en) * 2012-05-21 2015-05-07 Oji Holdings Corporation Method for producing fine fibers and sheet containing fine fibers
US9982387B2 (en) * 2012-05-21 2018-05-29 Oji Holdings Corporation Method for producing fine fibers and sheet containing fine fibers
US8877007B2 (en) 2012-08-21 2014-11-04 University Of New Brunswick System and method for reclaiming rejects in sulfite pulping
JP2017538044A (ja) * 2014-11-21 2017-12-21 インヴェンティア・アクチボラゲットＩｎｎｖｅｎｔｉａ Ａｂ 処理パルプの製造方法

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EP2097582A4 (en) 2013-12-25
BRPI0707368A2 (pt) 2011-05-03
JP2009530508A (ja) 2009-08-27
FI20065860A0 (fi) 2006-12-28
CN101389808A (zh) 2009-03-18
CN101389808B (zh) 2011-05-11
CA2633800A1 (en) 2008-06-28
WO2008081078A1 (en) 2008-07-10
FI119062B (fi) 2008-07-15
JP4882090B2 (ja) 2012-02-22
EP2097582A1 (en) 2009-09-09
CA2633800C (en) 2011-08-02
RU2373313C1 (ru) 2009-11-20

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