EP3472383B1 - Method for producing a fibrous material - Google Patents

Method for producing a fibrous material Download PDF

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Publication number
EP3472383B1
EP3472383B1 EP17724804.4A EP17724804A EP3472383B1 EP 3472383 B1 EP3472383 B1 EP 3472383B1 EP 17724804 A EP17724804 A EP 17724804A EP 3472383 B1 EP3472383 B1 EP 3472383B1
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Prior art keywords
chemicals
refiner
added
impregnation
sodium
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EP17724804.4A
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German (de)
French (fr)
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EP3472383A1 (en
Inventor
Oleg Shagaev
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Andritz AG
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Andritz AG
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    • 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
    • D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
    • D21B1/00—Fibrous raw materials or their mechanical treatment
    • D21B1/02—Pretreatment of the raw materials by chemical or physical means
    • D21B1/021—Pretreatment of the raw materials by chemical or physical means by chemical means
    • 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
    • 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
    • D21C3/04—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides
    • 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
    • D21C3/04—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides
    • D21C3/06—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides sulfur dioxide; sulfurous acid; bisulfites sulfites
    • D21C3/12—Pulping cellulose-containing materials with acids, acid salts or acid anhydrides sulfur dioxide; sulfurous acid; bisulfites sulfites sodium bisulfite
    • 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
    • D21C3/22—Other features of pulping processes
    • D21C3/26—Multistage processes
    • D21C3/266—Multistage processes the same pulping agent being used in all stages
    • 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
    • D21C9/001—Modification of pulp properties
    • D21C9/007—Modification of pulp properties by mechanical or physical means
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21D—TREATMENT OF THE MATERIALS BEFORE PASSING TO THE PAPER-MAKING MACHINE
    • D21D1/00—Methods of beating or refining; Beaters of the Hollander type
    • D21D1/20—Methods of refining

Definitions

  • the invention relates to a process for the production of wood pulp from lignocellulose, preferably in the form of wood chips, the lignocellulosic material being impregnated by chemicals from a mixture of sodium sulfite and sodium bisulfite and then subjected to a comminution process in a refiner.
  • Processes for the production of high-yield pulp are, for example, from the CA 1051618 known.
  • chemicals for removing the lignin are added in a pretreatment for the impregnation.
  • the WO2007 / 012350 A1 describes a process for the production of wood-based products, in which the wood before gluing z. B. is treated in the stove or in the refiner with bisulfite.
  • the EP 0199481 A1 describes a process for the production of pulp, in which chemicals from the sodium sulfite family are used for impregnation. The use of sulfur compounds in wood chips but also annual plants is well known and is used to save energy in comminution and to improve the quality of the pulp in mechanical pulp. Mixtures of sodium sulfite and sodium bisulfite at temperatures of 100 - 150 ° C are usually used as chemicals, with the pulp spending a certain time in a container after being impregnated by the chemicals.
  • Sodium sulfite and sodium bisulfite are present together, with the equilibrium shifting depending on the pH. At a low pH (approx. 4 - 5.5) the larger proportion of sodium bisulfite is present, while at a higher pH (approx. 6 - 7.5) the majority of the mixture is in the form of sodium sulfite. In order to avoid SO 2 emissions, a pH of less than 5.5 is often used, and often less than 4.0.
  • the gaseous SO 2 as a product of bisulfite decomposition can also occur in the pretreatment stage during comminution. Free SO 2 can also condense with water vapor and cause corrosion on colder parts of the apparatus.
  • the aim of the invention is to prevent corrosion on the one hand and the formation of deposits on the refiner plates on the other. This is achieved by additionally introducing chemicals from a mixture of sodium sulfite and sodium bisulfite directly into the refiner, the chemicals having a pH of 6.0-7.5, preferably 6.5-7.0, of Impregnation are supplied and the additional chemicals with a pH of 4.0-5.5, preferably 4.2-4.5, are added to the refiner.
  • An advantageous embodiment of the invention is characterized in that 60-80% of the chemicals are added to the impregnation and 20-40% of the chemicals are added to the refiner. A particularly good use of the chemicals is thus achieved.
  • a favorable further development of the invention is characterized in that the impregnation is carried out at a temperature of 80-170 ° C, preferably 130-140 ° C. In this temperature range, a particularly good and quick implementation of the chemicals can be achieved.
  • a favorable further development of the invention is characterized in that the total amount of chemicals added is 1-20 kg / t, preferably 10-15 kg / t. This enables the specific energy consumption of the process, in particular the size reduction in the refiner, to be significantly reduced.
  • FIG. 1 shows a flow diagram of a pretreatment system with impregnation and subsequent comminution in the refiner.
  • Wood chips which may already have been pretreated, are fed from a storage container 1 to a reactor 2 for impregnation.
  • a chemical is supplied via a line 3. This is a mixture of sodium sulfite and sodium bisulfite.
  • the chemical supplied here has a pH of approx. 6.5 -7.0 and is approx. 60 - 80% of the total amount of chemicals to be added. It has been shown that at a pH of 6.5-7.0, 60-80% of the reaction is complete after a short time, often after a few seconds of reaction time. In principle, the pH value can be 6.0 - 7.5.
  • the impregnated chips are fed to a refiner 5 for comminution.
  • the remaining amount of approximately 20-40% of the chemicals which in turn consist of a mixture of sodium sulfite and sodium bisulfite, is fed in here via a line 6.
  • the addition can also be introduced into the shredding zone with the dilution water through holes in the grinding plates of the stators.
  • the invention is not restricted to the examples described. Rather, it can be used for both hardwood and softwood.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Paper (AREA)

Description

Die Erfindung betrifft ein Verfahren zur Herstellung von Faserstoff aus Lignozellulose aus Holz, vorzugsweise in Form von Hackschnitzeln, wobei das lignozellulose Material durch Chemikalien aus einer Mischung von Natriumsulfit und Natriumbisulfit imprägniert und anschließend einem Zerkleinerungsprozess in einem Refiner unterworfen wird.The invention relates to a process for the production of wood pulp from lignocellulose, preferably in the form of wood chips, the lignocellulosic material being impregnated by chemicals from a mixture of sodium sulfite and sodium bisulfite and then subjected to a comminution process in a refiner.

Verfahren zur Herstellung von Hochausbeutezellstoff sind z.B. aus der CA 1051618 bekannt. Hier werden bei chemischem Zellstoff, mechanischem Zellstoff, chemimechanischem Zellstoff, thermomechanischem Zellstoff etc. in einer Vorbehandlung zur Imprägnation Chemikalien zur Entfernung des Lignin zugesetzt.Processes for the production of high-yield pulp are, for example, from the CA 1051618 known. In the case of chemical pulp, mechanical pulp, chemimechanical pulp, thermomechanical pulp etc., chemicals for removing the lignin are added in a pretreatment for the impregnation.

Die WO2007/012350 A1 beschreibt ein Verfahren zur Herstellung von Holzwerkstoff-Artikeln, bei der das Holz vor der Verleimung z. B. im Kocher oder im Refiner mit Bisulfit behandelt wird. Die EP 0199481 A1 beschreibt einen Prozess zur Herstellung von Zellstoff, bei dem zur Imprägnation u.a. Chemikalien aus der Familie der Natriumsulfite eingesetzt werden. Der Einsatz von Schwefelverbindungen bei Hackschnitzeln aber auch Jahrespflanzen ist gut bekannt und wird angewandt um Energie bei der Zerkleinerung einzusparen und die Qualität des Zellstoffs bei mechanischem Zellstoff zu verbessern. Als Chemikalien werden hier meist Mischungen aus Natriumsulfit und Natriumbisulfit bei Temperaturen von 100 - 150 °C eingesetzt, wobei der Zellstoff nach der Imprägnierung durch die Chemikalien eine gewisse Verweilzeit in einem Behälter verbringt. Natriumsulfit und Natriumbisulfit liegen gemeinsam vor, wobei sich das Gleichgewicht abhängig vom pH-Wert verschiebt. So liegt bei einem niedrigen pH-Wert (ca. 4 - 5,5) der größere Anteil an Natriumbisulfit vor, während bei einem höheren pH-Wert (ca. 6 - 7,5) der Großteil der Mischung als Natriumsulfit vorliegt. Um SO2 Emissionen zu vermeiden wird meist bei einem pH-Wert kleiner 5,5 oft auch kleiner 4,0 gearbeitet. Das gasförmige SO2 als Produkt einer Bisulfitzersetzung kann bei der Vorbehandlungsstufe aber auch bei der Zerkleinerung auftreten. Freies SO2 kann auch mit Wasserdampf kondensieren und an kälteren Teilen der Apparate Korrosion erzeugen. Bei den höheren pH-Wert Bedingungen tritt aber ein Belag auf den Refinerplatten auf, der die Lebensdauer der Refinerplatten stark verkürzt. Auch kann es zu Verstopfungen der Kanäle der Refinerplatten durch Kalziumsalze kommen. Bei geringeren pH-Werten kann Korrosion auftreten und auch SO2 Emissionen im bzw. nach dem Refiner erfolgen.
Ziel der Erfindung ist es Korrosion einerseits und Belagbildung auf den Refinerplatten andererseits zu vermeiden.
Dies wird dadurch erreicht, dass zusätzlich Chemikalien aus einer Mischung von Natriumsulfit und Natriumbisulfit direkt in den Refiner eingebracht werden, wobei die Chemikalien mit einem pH-Wert von 6,0 - 7,5, vorzugsweise von 6,5 - 7,0, der Imprägnation zugeführt werden und die zusätzlichen Chemikalien mit einem pH-Wert von 4,0 - 5,5, vorzugsweise 4,2-4,5, in den Refiner zugegeben werden. Damit können die Bedingungen der Zugabe zur Imprägnation und in den Refiner unterschiedlich gestaltet und speziell die pH-Werte optimal angepasst werden, um Korrosion und Belagbildung zu vermeiden. Damit kann man die Korrosion durch mit Wasserdampf kondensiertes freiwerdendes SO2 in den Hauptaggregaten vermeiden und es ermöglicht, dass die Belagbildung auf den Refinerplatten stark reduziert oder vermieden werden kann und dadurch die Lebensdauer der Platten erheblich verlängert wird, was zu enormen Kostenersparnissen führt. Auch wird dadurch die Salzbildung, insbesondere von Kalziumsalzen, im Wesentlichen vermieden.
Eine vorteilhafte Ausgestaltung der Erfindung ist dadurch gekennzeichnet, dass 60 - 80 % der Chemikalien in die Imprägnation und 20 - 40 % der Chemikalien in den Refiner gegeben werden. Damit wird eine besonders gute Ausnützung der Chemikalien erreicht.
Eine günstige Weiterbildung der Erfindung ist dadurch gekennzeichnet, dass die Imprägnation bei einer Temperatur von 80 - 170 °C, vorzugsweise von 130- 140°C, durchgeführt wird. In diesem Temperaturbereich ist eine besonders gute und schnelle Umsetzung der Chemikalien erreichbar.The WO2007 / 012350 A1 describes a process for the production of wood-based products, in which the wood before gluing z. B. is treated in the stove or in the refiner with bisulfite. The EP 0199481 A1 describes a process for the production of pulp, in which chemicals from the sodium sulfite family are used for impregnation. The use of sulfur compounds in wood chips but also annual plants is well known and is used to save energy in comminution and to improve the quality of the pulp in mechanical pulp. Mixtures of sodium sulfite and sodium bisulfite at temperatures of 100 - 150 ° C are usually used as chemicals, with the pulp spending a certain time in a container after being impregnated by the chemicals. Sodium sulfite and sodium bisulfite are present together, with the equilibrium shifting depending on the pH. At a low pH (approx. 4 - 5.5) the larger proportion of sodium bisulfite is present, while at a higher pH (approx. 6 - 7.5) the majority of the mixture is in the form of sodium sulfite. In order to avoid SO 2 emissions, a pH of less than 5.5 is often used, and often less than 4.0. The gaseous SO 2 as a product of bisulfite decomposition can also occur in the pretreatment stage during comminution. Free SO 2 can also condense with water vapor and cause corrosion on colder parts of the apparatus. At the higher pH conditions, however, a coating appears on the refiner plates, which greatly shortens the life of the refiner plates. Can too calcium channels block the channels of the refiner plates. At lower pH values, corrosion can occur and SO 2 emissions can also occur in or after the refiner.
The aim of the invention is to prevent corrosion on the one hand and the formation of deposits on the refiner plates on the other.
This is achieved by additionally introducing chemicals from a mixture of sodium sulfite and sodium bisulfite directly into the refiner, the chemicals having a pH of 6.0-7.5, preferably 6.5-7.0, of Impregnation are supplied and the additional chemicals with a pH of 4.0-5.5, preferably 4.2-4.5, are added to the refiner. This means that the conditions of addition to the impregnation and in the refiner can be designed differently and the pH values can be optimally adjusted in order to avoid corrosion and deposit formation. This avoids corrosion caused by the release of SO 2 condensed with water vapor in the main units, and it is possible that the build-up of deposits on the refiner plates can be greatly reduced or avoided, thereby considerably extending the life of the plates, which leads to enormous cost savings. This also substantially prevents salt formation, in particular calcium salts.
An advantageous embodiment of the invention is characterized in that 60-80% of the chemicals are added to the impregnation and 20-40% of the chemicals are added to the refiner. A particularly good use of the chemicals is thus achieved.
A favorable further development of the invention is characterized in that the impregnation is carried out at a temperature of 80-170 ° C, preferably 130-140 ° C. In this temperature range, a particularly good and quick implementation of the chemicals can be achieved.

Eine günstige Weiterbildung der Erfindung ist dadurch gekennzeichnet, dass die Gesamtmenge der zugegebenen Chemikalien 1 -20 kg/t, vorzugsweise 10-15 kg/t, beträgt. Damit kann der spezifische Energieverbrauch des Prozesses, insbesondere der Zerkleinerung im Refiner, signifikant reduziert werden.A favorable further development of the invention is characterized in that the total amount of chemicals added is 1-20 kg / t, preferably 10-15 kg / t. This enables the specific energy consumption of the process, in particular the size reduction in the refiner, to be significantly reduced.

Die Erfindung wird nun anhand von Zeichnungen beispielhaft beschrieben, wobei die
Fig. ein Fliessschema einer Vorbehandlungsanlage mit Imprägnation und nachfolgender Zerkleinerung im Refiner darstellt.The invention will now be described by way of example with reference to drawings, the
FIG. 1 shows a flow diagram of a pretreatment system with impregnation and subsequent comminution in the refiner.

In der Fig. ist ein Beispiel für eine erfindungsgemäße Anlagenschaltung dargestellt. Aus einem Speicherbehälter 1 werden Holzhackschnitzel, die gegebenenfalls bereits vorbehandelt sind, einem Reaktor 2 zur Imprägnation zugeführt. Am Beginn dieses Reaktors wird über eine Leitung 3 eine Chemikalie zugeführt. Dies ist eine Mischung aus Natriumsulfit und Natriumbisulfit. Die hier zugeführte Chemikalie weist einen pH-Wert von ca. 6,5 -7,0 auf und beträgt etwa 60 - 80 % der Gesamtmenge an zuzugebenden Chemikalien. Es hat sich gezeigt, dass bei einem pH-Wert von 6,5 - 7,0 bereits 60 - 80 % der Reaktion nach kurzer Zeit, oft schon nach einigen Sekunden an Reaktionszeit, abgeschlossen ist. Grundsätzlich kann der pH-Wert 6,0 - 7,5 betragen. Mittels eines Förderers 4, z.B. Schneckenförderer, werden die imprägnierten Hackschnitzel einem Refiner 5 zur Zerkleinerung zugeführt. Gleichzeitig wird hier über eine Leitung 6 die restliche Menge von ca. 20 - 40 % der Chemikalien, die wiederum aus einer Mischung von Natriumsulfit und Natriumbisulfit bestehen, zugeführt. Neben einer Zufuhr der Chemikalien direkt in die Zerkleinerungszone des Refiner 5 kann die Zugabe auch mit dem Verdünnungswasser durch Löcher in den Mahlplatten der Statoren in die Zerkleinerungszone eingebracht werden. Auch hier handelt es sich um eine Mischung aus Natriumsulfit und Natriumbisulfit, wobei der pH-Wert vorzugsweise 4,0 - 4,5 beträgt. Grundsätzlich kann der pH-Wert hier 4,0 - 5,5 betragen. Dadurch ergibt sich in der Zerkleinerungszone ein pH-Wert, der Ablagerungen und Belag auf den Refinerplatten, insbesondere von Kalziumsulfit, verhindert. Sollte sich gasförmiges SO2 in der Zerkleinerungszone bilden, so würde dieses mit dem zurückgeführten Dampf 7 abtransportiert und vom lignozellulosen Material mit höherem pH-Wert absorbiert bzw. neutralisiert werden. Der Dampf 7 kann einer Stopfschnecke nach dem Speicherbehälter 1 zur Aufwärmung der Hackschnitzel zugeführt werden. Weiterer Dampf wird üblicherweise einer Wärmerückgewinnung zugeführt. Durch die erfolgte Aufteilung der Zugabe der Chemikalien, insbesondere von Bisulfit, kann der pH-Wert optimal an die Notwendigkeiten angepasst werden. Damit kann durch einen niedrigen pH-Wert im Zerkleinerungsprozess der spezifische Energieverbrauch gering gehalten werden, bei Erhalt der Festigkeit und optischen Eigenschaften des Zellstoffs bei gleichzeitiger Vermeidung der Korrosion und der Belagbildung im Refiner und anschließenden Aggregaten.An example of a system circuit according to the invention is shown in the figure. Wood chips, which may already have been pretreated, are fed from a storage container 1 to a reactor 2 for impregnation. At the beginning of this reactor, a chemical is supplied via a line 3. This is a mixture of sodium sulfite and sodium bisulfite. The chemical supplied here has a pH of approx. 6.5 -7.0 and is approx. 60 - 80% of the total amount of chemicals to be added. It has been shown that at a pH of 6.5-7.0, 60-80% of the reaction is complete after a short time, often after a few seconds of reaction time. In principle, the pH value can be 6.0 - 7.5. By means of a conveyor 4, for example a screw conveyor, the impregnated chips are fed to a refiner 5 for comminution. At the same time, the remaining amount of approximately 20-40% of the chemicals, which in turn consist of a mixture of sodium sulfite and sodium bisulfite, is fed in here via a line 6. In addition to supplying the chemicals directly into the shredding zone of the refiner 5, the addition can also be introduced into the shredding zone with the dilution water through holes in the grinding plates of the stators. This is also a mixture of sodium sulfite and sodium bisulfite, the pH value preferably being 4.0-4.5. Basically, the pH here can be 4.0 - 5.5. This results in a pH value in the comminution zone, which prevents deposits and deposits on the refiner plates, especially of calcium sulfite. Should gaseous SO 2 form in the comminution zone, this would be carried away with the returned steam 7 and with the lignocellulosic material higher pH are absorbed or neutralized. The steam 7 can be fed to a stuffing screw after the storage container 1 for heating up the wood chips. Further steam is usually fed to heat recovery. By dividing the addition of chemicals, especially bisulfite, the pH can be optimally adjusted to the requirements. With a low pH in the shredding process, the specific energy consumption can be kept low while maintaining the strength and optical properties of the pulp while avoiding corrosion and the formation of deposits in the refiner and subsequent aggregates.

Die Erfindung ist nicht auf die beschriebenen Beispiele beschränkt. Sie kann vielmehr sowohl für Hartholz als auch für Weichholz angewandt werden.The invention is not restricted to the examples described. Rather, it can be used for both hardwood and softwood.

Claims (4)

  1. Method for producing pulp from lignocellulose made from wood, preferably in the form of wood chips, where the lignocellulose material is impregnated with chemicals from a mixture of sodium sulphite and sodium bisulphite and then subjected to a grinding process in a refiner, characterized in that chemicals are fed directly to the refiner in addition in a mixture of sodium sulphite and sodium bisulphite, where the chemicals are fed to the impregnation stage at a pH of 6.0-7.5, preferably 6.5-7.0, and the additional chemicals are added in the refiner with a pH of 4.0-5.5., preferably 4.2-4.5.
  2. Method according to claim 1, characterized in that 60-80% of the chemicals are added in the impregnation stage and 20-40% are added in the refiner.
  3. Method according to one of claims 1 or 2, characterized in that impregnation takes place at a temperature of 80-170 °C, preferably at 120-140 °C.
  4. Method according to one of claims 1 to 3, characterized in that the total quantity of chemicals added amounts to 1-20 kg/t, preferably 10-15 kg/t.
EP17724804.4A 2016-06-17 2017-05-18 Method for producing a fibrous material Active EP3472383B1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA50551/2016A AT518800B1 (en) 2016-06-17 2016-06-17 METHOD FOR PRODUCING FIBROUS MATERIAL
PCT/EP2017/061926 WO2017215877A1 (en) 2016-06-17 2017-05-18 Method for producing a fibrous material

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EP3472383A1 EP3472383A1 (en) 2019-04-24
EP3472383B1 true EP3472383B1 (en) 2020-03-04

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US (1) US11535983B2 (en)
EP (1) EP3472383B1 (en)
AT (1) AT518800B1 (en)
CA (1) CA3028009C (en)
RU (1) RU2704362C1 (en)
WO (1) WO2017215877A1 (en)

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US7697967B2 (en) 2005-12-28 2010-04-13 Abbott Diabetes Care Inc. Method and apparatus for providing analyte sensor insertion

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US3225028A (en) * 1962-06-11 1965-12-21 Nordgren Robert Acrolein adducts of polygalactomannans and polyglucomannans and process of preparing same
FI42161C (en) * 1963-04-03 1970-05-11 Defibrator Ab A method for the continuous production of mechanical and semi-chemical pulps from a lignocellulosic material
GB1041995A (en) * 1964-11-24 1966-09-07 Fmc Corp Production of cellulosic pulp of increased brightness
CA1051618A (en) * 1976-05-14 1979-04-03 Prescott E. Gardner Method of producing high yield chemimechanical pulps
US4486267A (en) * 1983-11-14 1984-12-04 Mead Corporation Chemithermomechanical pulping process employing separate alkali and sulfite treatments
NZ211684A (en) * 1985-04-04 1989-07-27 Caxton Paper Ltd Manufacture of cellulose pulp: second digestion step follows initial digestion and refining steps
KR100750330B1 (en) * 2005-05-30 2007-08-20 유해일 Manufacturing method of mechanical pulp from cornstalk
US20090145564A1 (en) 2005-07-27 2009-06-11 Wolfgang Seifert Method for production of wood material articles with low emissions of chemical compounds
US8734611B2 (en) 2008-03-12 2014-05-27 Andritz Inc. Medium consistency refining method of pulp and system
DE102009057208A1 (en) * 2009-11-27 2011-06-01 Technische Universität Dresden Process for the production of lignocellulosic paper pulps and papers, cartons and boards derived therefrom
EP2348154A1 (en) * 2010-01-22 2011-07-27 Andritz AG Method for manufacturing wooden material

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CA3028009A1 (en) 2017-12-21
WO2017215877A1 (en) 2017-12-21
CA3028009C (en) 2022-12-13
RU2704362C1 (en) 2019-10-28
AT518800B1 (en) 2019-09-15
US11535983B2 (en) 2022-12-27
AT518800A1 (en) 2018-01-15
US20190352849A1 (en) 2019-11-21
EP3472383A1 (en) 2019-04-24

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