WO2003046227A1 - Verfahren zum abtrennen von xylose aus xylanreichen lignocellulosen, insbesondere holz - Google Patents
Verfahren zum abtrennen von xylose aus xylanreichen lignocellulosen, insbesondere holz Download PDFInfo
- Publication number
- WO2003046227A1 WO2003046227A1 PCT/EP2002/013377 EP0213377W WO03046227A1 WO 2003046227 A1 WO2003046227 A1 WO 2003046227A1 EP 0213377 W EP0213377 W EP 0213377W WO 03046227 A1 WO03046227 A1 WO 03046227A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- wood
- xylose
- hemicelluloses
- cellulose
- rich
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/002—Xylose
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials
Definitions
- the invention relates to a process for separating xylose from xylan-rich lignocelluloses, in particular wood, and for obtaining pulp.
- this natural composite of the framework substance in the form of cellulose chains twisted to long and solid fibrils and the hydrophobic lignin acting as a protective covering must be destroyed in order to then separate these components from one another in what is known as wood digestion.
- Another essential part of the wood are the hemicelluloses (polyoses). The aim is mostly to obtain more or less pure cellulose, with the other constituents lignin and hemicelluloses, mostly in degraded form, only as
- paper cellulose which in addition to the main constituent ⁇ -cellulose can contain up to 25% hemicellulose, and higher quality
- V Chemical pulp with an ⁇ -cellulose content of over 90%, the proportion of hemicellulose should not exceed a few percent. As is known, chemical pulp is one of the most important cost factors in the production of cellulose acetate, filter tow and other high-quality cellulose products.
- a classic method for removing xylose uses acidic pre-hydrolysis, which in practice is carried out either with dilute sulfuric acid in a concentration of 0.1 to 0.5% and a temperature of 90 to 140 ° C or in pure water at a temperature from 165 to 175 ° C is carried out (H. Sixta, G. Schild and Th. Baidinger: Das Textil Heft 9, 1992, p. 527 ff). About 70% of the xylose is considered typical for the removal during the pre-hydrolysis. Of the remaining 30%, 40 to 50%, ie absolutely 12 to 15%, of the xylose are removed during the cooking. Accordingly, a total of 82 to 85% of the xylose present is removed from the wood.
- the hydrolysis is called water hydrolysis, i.e. carried out at liquor ratios of 3 to 4: 1.
- the heating-up time is at least 60 minutes, usually up to 90 minutes.
- the hydrolyzate is usually disposed of thermally together with the cooking liquor.
- Prehydrolysis is also limited by the occurrence of side reactions that are difficult to control.
- the most important side reaction the dehydration of the pentoses to furfural, is the starting point for the undesired inter- and intramolecular condensation reactions.
- Resin-like compounds are formed which, as the reaction continues, separate from the aqueous phase and can be deposited on all existing surfaces (obstruction and blockages during operation).
- the P factor for these temperatures and times is approx. 700 + 5.
- the P-factor model is used to calculate the degree of pre-hydrolysis using the time-temperature profile. Temperature and time are combined in one variable, the P-factor.
- the P-factor can be seen analogously to the severity factor introduced in the steam explosion of wood. According to the above article by H. Sixta, G. Schild and Th. Baidinger, the viscosity decreases with this P-factor by approx. 20%. If the P factor is observed, i.e. In the above temperatures and times, the yield of undesirable by-products is low.
- the glucose concentration is largely independent of the maximum reaction temperature, and is approximately 2 g / 1.
- Known sources for xylose show a number of disadvantages.
- Known sources of xylose are, for example, the cooking liquids of the Mg and Ca sulfite processes. However, these must be subjected to an ion exchange in order to remove the lignin sulfonates, further chromatographic methods for separating the xylose from other sugar components, possibly crystallizations, being necessary.
- the object of the invention was therefore to provide a process for separating xylose which works in a simple and economical manner, with as little waste products as possible being processed. Furthermore, a high cellulose yield should be achieved with the method according to the invention.
- This object is achieved according to the invention by a method for separating xylose from xylan-rich lignocelluloses, in particular wood, and for obtaining pulp, characterized by the steps: (1) pretreating wood chips by mechanically destroying the original structure,
- the invention allows the above-described object to be achieved in an advantageous manner. It therefore contributes to a considerable improvement in the state of the art.
- a completely different procedure than in the conventional wood pulping process succeeds in achieving numerous advantages over sulfite or prehydrolysis sulfate processing. drive to lead into the field. This is primarily due to significant improvements in the treatment of wood chips. These are based on the avoidance of the disadvantages that arise with classic cooker technology, namely infestation of cookers with the chips, long heating and cooking times, high liquor ratios and hardly solvable problems with regard to heat and material exchange due to low diffusion speeds and negligible thermodynamic potential differences. These in turn necessitate high investment requirements, ie large parts of the plant due to long dwell times.
- the prehydrolysis is therefore not carried out on the chips themselves, but after their pretreatment.
- This pretreatment consists in first squeezing and shearing the wood chips in process step (1) by means of a suitable mechanical process engineering unit, such as a press screw, screw press or the like, so that their original structure is destroyed.
- a suitable mechanical process engineering unit such as a press screw, screw press or the like.
- This massive mechanical stress not only removes water stored in the wood chips.
- the air is also removed from the capillaries of the wood.
- the moisture is significantly reduced by the squeezing process, namely by up to about 50%.
- Any comminuted plant growth materials of various types can be used, such as wood, oat husks, maize or grain stalks, bagasse, wheat straw, rice, straw and oat straw.
- wood it is common to use logs or small pieces of wood in shredded form.
- fibrous raw materials such as annual plants, cut fibers are suitable.
- Shredded, in particular shredded, wood is preferably used, preference being given to the use of hardwood, in particular beech wood or eucalyptus.
- step (1) of the method according to the invention enables the wood mass obtained; wood chips can no longer be spoken after this intervention, soaking up spontaneously and in a very short time with any type of liquid offered, in order to approximate the original state again , This fact can now be exploited by impregnating the wood chips pretreated in this way in accordance with step (2) of the process of the invention with dilute mineral acid.
- the mineral acid can be any known mineral acid. Examples include: sulfuric acid, hydrochloric acid and / or nitric acid, with sulfuric acid being particularly preferred.
- the uniformity of the distribution over the entire cross-section of the wood mass can be easily recognized by the discoloration of the wood mass from light to dark.
- the distribution of the liquid is usually even, unless the wood chips have not been squeezed sufficiently.
- the wood mass pretreated in this way can be treated in a suitable apparatus, such as, for example, an "inclined screw reactor", Pandia reactor or the like, by treating with steam at a temperature of about 140 to 180 ° C., in particular about 150 to Treat for about 5 to 40 minutes, in particular about 5 to 20 minutes, preferably in a continuous mode of operation, with prehydrolyzate also being able to be taken off continuously.
- a suitable apparatus such as, for example, an "inclined screw reactor", Pandia reactor or the like
- the process-modified wood mass obtained after carrying out the pre-hydrolysis according to step (3) can expediently be obtained in a very simple manner and without a large amount
- the hemicelluloses still adhering to the fibers and broken down into sugars can then be separated quantitatively in step (4) in a washing or filtration step.
- Laundry is preferably a washing centrifuge, a double washing press, a belt press or, in general, a multi-stage washing unit.
- the process is particularly effective for woods with a high xylan content, e.g. Eucalyptus pulp. Accordingly, about 10 to 25%, in particular about 15 to 20%, aqueous xylose solutions can advantageously be obtained. In these, a super-saturated solution can be obtained by further concentration, from which the xylose can be crystallized. Experience has shown, however, that 25% xylose solutions are economically interesting for further processing.
- the combination of the process steps according to the invention makes it possible to achieve high ⁇ -cellulose contents with very low xylose fractions, that is to say high-purity chemical pulp grades, and at the same time an almost quantitative separation of the valuable xylose is possible.
- a pre-hydrolysis of the wood chips according to the method according to the invention also means a considerable saving of time and costs compared to conventional methods.
- the hydrolyzate contains the sugar in a high concentration of about 12 to 14%, which is also a favorable basis for further processing or, if desired, a concentration.
- the wood pulps only contain about 10% or less of the original hemicelluloses - depending on the intensity of the impregnation and the pre-hydrolysis conditions. Accordingly, the hemicelluloses can be almost completely removed from the wood, with no undesirable mixing of lignin and carbohydrates. Rather, a clear separation of the essential wood components in pure form is obtained from one another, ie an effective separation of all soluble carbohydrates is achieved in one separation step, with low cellulose losses also occurring.
- xylitol Marking the xylose for further processing to xylitol (xylitol) is also of great importance. This contributes significantly to improving the economy of the method of the invention.
- a prehydrolysate free of foreign substances is obtained, high xylose concentrations being achieved in the prehydrolysate.
- Complex xylose enrichment is generally not necessary and the xylose obtained can also be decolorized.
- a separation of lignosulfonates that is regularly necessary in the prior art can also be omitted.
- MSD is a screw press with the characteristic that the shaft of the screw compresses with increasing distance from the feed point of the wood chips. This means that the wood chips have less free space.
- the worm rotates slowly, with the wood chips being conveyed in a perforated steel sheet. The water escaping from squeezing / pressing the wood chips can be drained through the perforated steel sheet.
- the wood chips are receptive to the dilute acid (3), which, indicated by the arrow, is added and is required in the pre-hydrolysis to break down the hemicelluloses contained in the wood.
- a beech wood sample was impregnated with a 0.6% sulfuric acid and then hydrolyzed at 160 ° C. for 20 minutes.
- the wood chips impregnated with acid can be conveyed to the feed hopper of the digester (4).
- Wood chips can be done completely in just twenty minutes with steam.
- the wood chips are conveyed through the transport screw built into the digester and are continuously discharged via a blow valve connected to one Cyclone emptied.
- a refiner or a decnotter can also be provided in order to fiber up well-digested parts but still have the wood chip structure.
- a decnotter is a machine for shredding non-fibrillated, steam-treated wood chips.
- the hydrolyzate containing the degraded hemicelluloses in the form of monosugars must also be continuously withdrawn at the lower end of the digest.
- the possibility of continuously monitoring the hydrolyzate composition also lends itself to a production plant. This measurement signal can be used for statistical process control.
- Good fibering, for example in a refiner (6), of the prehydrolysed wood chips is advantageous for the subsequent washing step (7), in which the sugars still adhering to the fibers are separated off quantitatively.
- a multi-stage countercurrent wash is advantageous here.
- a separation can also be carried out by centrifugation, which can be sufficient for the quantitative removal of the soluble sugars from the prehydrolyzed wood, possibly in combination with one or two washing stages in the centrifuge.
- FIG. 2 shows that the pre-hydrolysis step with MSD / impregnation and digester explained in FIG. 1 is reproducible on the one hand and that there is also a linear relationship between the sulfuric acid concentration in the impregnation bath and the xylose content in the fiber after washing, which can be used for a corresponding optimization ,
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2002358051A AU2002358051A1 (en) | 2001-11-27 | 2002-11-27 | Method for separating xylose from lignocelluloses rich in xylan, in particular wood |
US10/496,853 US20050065336A1 (en) | 2001-11-27 | 2002-11-27 | Method for separating xylose from lignocelluloses rich in xylan, in particular wood |
EP02791726A EP1448801A1 (de) | 2001-11-27 | 2002-11-27 | Verfahren zum abtrennen von xylose aus xylanreichen lignocellulosen, insbesondere holz |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE10158120A DE10158120A1 (de) | 2001-11-27 | 2001-11-27 | Verfahren zum Abtrennen von Xylose aus xylanreichen Lignocellulosen, insbesondere Holz |
DE10158120.3 | 2001-11-27 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2003046227A1 true WO2003046227A1 (de) | 2003-06-05 |
Family
ID=7707109
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2002/013377 WO2003046227A1 (de) | 2001-11-27 | 2002-11-27 | Verfahren zum abtrennen von xylose aus xylanreichen lignocellulosen, insbesondere holz |
Country Status (5)
Country | Link |
---|---|
US (1) | US20050065336A1 (de) |
EP (1) | EP1448801A1 (de) |
AU (1) | AU2002358051A1 (de) |
DE (1) | DE10158120A1 (de) |
WO (1) | WO2003046227A1 (de) |
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WO2007090926A1 (en) * | 2006-02-10 | 2007-08-16 | Metso Paper, Inc. | Method for recovering hydrolysis products |
WO2007090925A1 (en) * | 2006-02-10 | 2007-08-16 | Metso Paper, Inc. | Method for recovering hydrolysis products |
WO2008048426A2 (en) * | 2006-10-18 | 2008-04-24 | International Paper Company | Modified kraft fibers |
US7771565B2 (en) * | 2006-02-21 | 2010-08-10 | Packaging Corporation Of America | Method of pre-treating woodchips prior to mechanical pulping |
US8182650B2 (en) | 2005-05-24 | 2012-05-22 | International Paper Company | Modified Kraft fibers |
WO2012097781A1 (de) * | 2010-11-25 | 2012-07-26 | Studiengesellschaft Kohle Mbh | Verfahren zur säurekatalysierten depolymerisation von cellulose |
US8317975B2 (en) | 2004-04-20 | 2012-11-27 | The Research Foundation Of The State University Of New York | Product and processes from an integrated forest biorefinery |
DE102014102972A1 (de) | 2013-03-12 | 2014-09-18 | Studiengesellschaft Kohle Mbh | Verfahren zum Aufschluss lignocellulosischer Biomasse |
CN109748895A (zh) * | 2019-03-27 | 2019-05-14 | 广州楹鼎生物科技有限公司 | 一种糠醛的制备方法 |
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US20100285534A1 (en) * | 2007-04-19 | 2010-11-11 | Mascoma Corporation | Combined thermochemical pretreatment and refining of lignocellulosic biomass |
WO2008137639A1 (en) * | 2007-05-02 | 2008-11-13 | Mascoma Corporation | Two-stage method for pretreatment of lignocellulosic biomass |
US20080277082A1 (en) * | 2007-05-07 | 2008-11-13 | Andritz Inc. | High pressure compressor and steam explosion pulping method |
CA2730766C (en) * | 2008-07-16 | 2016-11-01 | Sriya Innovations, Inc. | Method of extraction of furfural and glucose from biomass using one or more supercritical fluids |
US8546560B2 (en) * | 2008-07-16 | 2013-10-01 | Renmatix, Inc. | Solvo-thermal hydrolysis of cellulose |
RU2556496C2 (ru) | 2010-01-19 | 2015-07-10 | Ренмэтикс, Инк. | Производство сбраживаемых сахаров и лигнина из биомассы, использующее сверхкритические текучие среды |
AT509899A2 (de) | 2010-06-02 | 2011-12-15 | Chemiefaser Lenzing Ag | Verfahren zur verbesserten verarbeitbarkeit von hydrothermolysaten von lignozellulosischem material |
RU2602068C2 (ru) | 2011-05-04 | 2016-11-10 | Ренмэтикс, Инк. | Получение лигнина из лигноцеллюлозной биомассы |
US8801859B2 (en) | 2011-05-04 | 2014-08-12 | Renmatix, Inc. | Self-cleaning apparatus and method for thick slurry pressure control |
US8895265B2 (en) | 2011-05-04 | 2014-11-25 | Renmatix, Inc. | Multistage fractionation process for recalcitrant C5 oligosaccharides |
US8883451B2 (en) | 2011-05-04 | 2014-11-11 | Renmatix, Inc. | Enhanced soluble C5 saccharide yields |
US8759498B2 (en) | 2011-12-30 | 2014-06-24 | Renmatix, Inc. | Compositions comprising lignin |
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WO2015200868A1 (en) * | 2014-06-27 | 2015-12-30 | Inventure Renewables, Inc. | Methods for the production of high alpha-cellulose pulp |
BR112017006012A2 (pt) | 2014-09-26 | 2017-12-19 | Renmatix Inc | mistura por adição, adesivos de madeira curados, madeiras compensadas, painéis de partículas orientadas, e composição |
MA40922A (fr) * | 2015-01-07 | 2017-09-12 | Purdue Research Foundation | Procédés pour atténuer les effets inhibiteurs de la lignine et de composés phénoliques solubles pour la conversion enzymatique de cellulose |
MX2018009634A (es) | 2016-02-19 | 2018-12-17 | Intercontinental Great Brands Llc | Procesos para crear multiples flujos de valores a partir de fuentes de biomasa. |
RU2643724C1 (ru) * | 2017-04-06 | 2018-02-05 | Общество с ограниченной ответственностью "Петровский фарватер" | Способ переработки растительного сырья для получения гидролизатов, содержащих ксилозу, для получения ксилита |
SE1950402A1 (en) | 2019-04-01 | 2020-10-02 | Valmet Oy | Method for extracting hemicellulose from lignocellulosic material |
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WO1994023071A1 (en) * | 1993-03-26 | 1994-10-13 | Arkenol, Inc. | Method of producing sugars using strong acid hydrolysis of cellulosic and hemicellulosic materials |
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WO2002070753A2 (en) * | 2001-02-28 | 2002-09-12 | Iogen Energy Corporation | Method of processing lignocellulosic feedstock for enhanced xylose and ethanol production |
WO2003010339A1 (en) * | 2001-07-24 | 2003-02-06 | Arkenol, Inc. | Separation of xylose and glucose |
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US3479248A (en) * | 1965-07-30 | 1969-11-18 | Ledoga Spa | Process for solubilizing the hemicellulose of vegetable materials and for recovering the sugars from the solubilized hemicellulose |
JPS4943481B1 (de) * | 1971-06-14 | 1974-11-21 | ||
ES8201627A1 (es) * | 1980-02-23 | 1981-12-16 | Reitter Franz Johann | Procedimiento e instalacion para la hidrolisis continua de hemicelulosas que contienen pentosanas de celulosa. |
US5340403A (en) * | 1986-10-20 | 1994-08-23 | Zeneca Limited | Process for the production of xylose |
DE19916347C1 (de) * | 1999-04-12 | 2000-11-09 | Rhodia Acetow Ag | Verfahren zum Auftrennen lignocellulosehaltiger Biomasse |
-
2001
- 2001-11-27 DE DE10158120A patent/DE10158120A1/de not_active Ceased
-
2002
- 2002-11-27 US US10/496,853 patent/US20050065336A1/en not_active Abandoned
- 2002-11-27 AU AU2002358051A patent/AU2002358051A1/en not_active Abandoned
- 2002-11-27 WO PCT/EP2002/013377 patent/WO2003046227A1/de not_active Application Discontinuation
- 2002-11-27 EP EP02791726A patent/EP1448801A1/de not_active Withdrawn
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US4427584A (en) * | 1981-08-24 | 1984-01-24 | University Of Florida | Conversion of cellulosic fibers to mono-sugars and lignin |
WO1994023071A1 (en) * | 1993-03-26 | 1994-10-13 | Arkenol, Inc. | Method of producing sugars using strong acid hydrolysis of cellulosic and hemicellulosic materials |
WO1996040970A1 (en) * | 1995-06-07 | 1996-12-19 | Arkenol, Inc. | Method of strong acid hydrolysis |
WO2002070753A2 (en) * | 2001-02-28 | 2002-09-12 | Iogen Energy Corporation | Method of processing lignocellulosic feedstock for enhanced xylose and ethanol production |
WO2003010339A1 (en) * | 2001-07-24 | 2003-02-06 | Arkenol, Inc. | Separation of xylose and glucose |
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US8317975B2 (en) | 2004-04-20 | 2012-11-27 | The Research Foundation Of The State University Of New York | Product and processes from an integrated forest biorefinery |
US9945073B2 (en) | 2004-04-20 | 2018-04-17 | The Research Foundation For The State University Of New York | Methods of producing a paper product |
US9683329B2 (en) | 2004-04-20 | 2017-06-20 | The Research Foundation For The State University Of New York | Methods of producing a paper product |
US9273431B2 (en) | 2004-04-20 | 2016-03-01 | The Research Foundation For The State University Of New York | Product and processes from an integrated forest biorefinery |
US8940133B2 (en) | 2004-04-20 | 2015-01-27 | The Research Foundation For The State University Of New York | Product and processes from an integrated forest biorefinery |
US8668806B2 (en) | 2004-04-20 | 2014-03-11 | The Research Foundation Of The State University Of New York | Product and processes from an integrated forest biorefinery |
US8328983B2 (en) | 2005-05-24 | 2012-12-11 | International Paper Company | Modified kraft fibers |
US8182650B2 (en) | 2005-05-24 | 2012-05-22 | International Paper Company | Modified Kraft fibers |
WO2007090925A1 (en) * | 2006-02-10 | 2007-08-16 | Metso Paper, Inc. | Method for recovering hydrolysis products |
US8262854B2 (en) | 2006-02-10 | 2012-09-11 | Metso Paper, Inc. | Method for recovering hydrolysis products |
WO2007090926A1 (en) * | 2006-02-10 | 2007-08-16 | Metso Paper, Inc. | Method for recovering hydrolysis products |
US7943008B2 (en) | 2006-02-21 | 2011-05-17 | Packaging Corporation Of America | Method of pre-treating woodchips prior to mechanical pulping |
US7771565B2 (en) * | 2006-02-21 | 2010-08-10 | Packaging Corporation Of America | Method of pre-treating woodchips prior to mechanical pulping |
WO2008048426A3 (en) * | 2006-10-18 | 2009-02-19 | Int Paper Co | Modified kraft fibers |
WO2008048426A2 (en) * | 2006-10-18 | 2008-04-24 | International Paper Company | Modified kraft fibers |
EA023989B1 (ru) * | 2010-11-25 | 2016-08-31 | Штудиенгезельшафт Коле Мбх | Способ кислотно-катализируемой деполимеризации целлюлозы |
WO2012097781A1 (de) * | 2010-11-25 | 2012-07-26 | Studiengesellschaft Kohle Mbh | Verfahren zur säurekatalysierten depolymerisation von cellulose |
DE102014102972A1 (de) | 2013-03-12 | 2014-09-18 | Studiengesellschaft Kohle Mbh | Verfahren zum Aufschluss lignocellulosischer Biomasse |
WO2014139515A2 (de) | 2013-03-12 | 2014-09-18 | Studiengesellschaft Kohle Mbh | Verfahren zum aufschluss lignocellulosischer biomasse |
WO2014139515A3 (de) * | 2013-03-12 | 2014-11-13 | Studiengesellschaft Kohle Mbh | Verfahren zum aufschluss lignocellulosischer biomasse |
EA030066B1 (ru) * | 2013-03-12 | 2018-06-29 | Штудиенгезельшафт Коле Мбх | Способ переработки лигноцеллюлозной биомассы |
CN109748895A (zh) * | 2019-03-27 | 2019-05-14 | 广州楹鼎生物科技有限公司 | 一种糠醛的制备方法 |
CN109748895B (zh) * | 2019-03-27 | 2023-01-13 | 广州楹鼎生物科技有限公司 | 一种糠醛的制备方法 |
Also Published As
Publication number | Publication date |
---|---|
AU2002358051A1 (en) | 2003-06-10 |
EP1448801A1 (de) | 2004-08-25 |
DE10158120A1 (de) | 2003-06-18 |
US20050065336A1 (en) | 2005-03-24 |
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