WO2006134126A1 - A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping - Google Patents
A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping Download PDFInfo
- Publication number
- WO2006134126A1 WO2006134126A1 PCT/EP2006/063207 EP2006063207W WO2006134126A1 WO 2006134126 A1 WO2006134126 A1 WO 2006134126A1 EP 2006063207 W EP2006063207 W EP 2006063207W WO 2006134126 A1 WO2006134126 A1 WO 2006134126A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- solvent
- acid
- process according
- compound
- feed material
- Prior art date
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Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- 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
-
- 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
- D21H—PULP COMPOSITIONS; PREPARATION THEREOF NOT COVERED BY SUBCLASSES D21C OR D21D; IMPREGNATING OR COATING OF PAPER; TREATMENT OF FINISHED PAPER NOT COVERED BY CLASS B31 OR SUBCLASS D21G; PAPER NOT OTHERWISE PROVIDED FOR
- D21H25/00—After-treatment of paper not provided for in groups D21H17/00 - D21H23/00
- D21H25/04—Physical treatment, e.g. heating, irradiating
Definitions
- the present invention provides a process for organosolv pulping and the use of a gamma lactone in a solvent for organosolv pulping. Background of the invention
- organosolv pulping In order to avoid the formation of mineral waste material, organosolv pulping has been proposed and studied as an alternative for Kraft pulping.
- organosolv pulping lignocellulosic material is heated in a solvent comprising organic compounds and optionally water, in order to dissolve the greater part of the hemicellulose and lignin and to obtain a high-quality, high-molecular weight cellulose that is suitable for paper production. The solvent is separated from the dissolved hemicellulose and lignin by simple distillation for recycling.
- solvents for organosolv pulping comprise organic compounds such as lower aliphatic alcohols, for example methanol or ethanol, lower carboxylic acids, for example formic acid or acetic acid, acetone, polyhydric alcohols, for example ethylene glycol or glycerol, or mixtures thereof. Often water is part of the solvent, typically in an amount up to 50 wt%. A small amount of strong mineral acid, typically in the range of a few tenths to a few percent, may be added as catalyst to the solvent. Oxidants such as hydrogen peroxide or peroxy acids may be added to the solvent to improve bleaching.
- Organosolv pulping is typically carried out at a temperature in the range of from 80 to 180 0 C.
- the operating pressure mainly depends on the volatility of the solvent. The pressure should be such that the solvent is still in the liquid phase. Typically, organolsolv pulping is performed just below the boiling temperature of the liquor. A drawback of the use of relatively volatile solvents is therefore that relatively high operating pressures are needed.
- the present invention provides a process for organosolv pulping, wherein solid lignocellulosic feed material is heated at a temperature in the range of from 50 to 210 0 C in a solvent to obtain a solid cellulosic fraction comprising at least 50 wt% of the cellulose present in the feed material and a liquid fraction, wherein the solvent comprises at least 10 wt% of a compound according to general molecular formula
- R ⁇ to Rg each represent, independently, a hydrogen atom or an organic group connected with a carbon atom to the lactone group.
- the invention provides the use of a compound according to general molecular formula (1) in a solvent for organosolv pulping.
- An important advantage of the use of a compound having a gamma lactone group in a solvent for organosolv pulping is that it has a relatively high boiling point and that the organosolv pulping can thus be carried out at a relatively low pressure.
- a further advantage of the process and the use according to the invention is that the compound according to general molecular formula (1) is both polar and relatively inert. As a consequence, it is an effective organosolv solvent that does hardly form reaction products with the lignocellulosic feed material or with components formed during the organosolv process.
- the process according to the invention is a process for organosolv pulping wherein a solid lignocellulosic feed material is heated in a solvent comprising at least 10 wt% of a compound having a gamma lactone group to obtain a solid cellulosic fraction and a liquid fraction.
- the liquid fraction contains the solvent and dissolved hemicellulose and lignin degradation products.
- the aim of organosolv pulping is to obtain a high-quality solid cellulose fraction or cellulose pulp that is suitable for paper production. Therefore, the exact process conditions in terms of temperature, pressure, heating time and the solvent used are chosen such that the greater part of the cellulose remains intact, i.e. is not depolymerised and dissolved in the liquid fraction.
- at least 50 wt% of the cellulose present in the feed material is recovered in the solid cellulosic fraction, preferably at least 60 wt%, more preferably at least 80 wt%.
- the cellulose content of the feed material and of the solid cellulose fraction obtained may for example be determined by hydrolysing a sample of the material followed by identification and quantification of sugars by means of gas chromatography according to TAPPI method T 249 cm-00. After correction of the glucose value by subtracting the glucose portion derived from the glucomannan present in the sample, the cellulose content is calculated from the corrected glucose value.
- the solid cellulosic fraction obtained has an average degree of polymerisation of at least 300.
- Reference herein to the average degree of polymerisation of the cellulose is to the weight-average degree of polymerisation.
- the degree of polymerisation may be determined by measuring the viscosity of a solution of the cellulosic fraction of known concentration, for example according to TAPPI method T 230 om-04.
- At least 50 wt% of the lignin in the lignocellulosic feed material is removed from the feed material during the organosolv process according to the invention, more preferably at least 80 wt%.
- the lignocellulosic feed material is heated in the solvent at a temperature that is typical for organosolv processes, i.e. in the range of from 50 to 210 0 C, preferably of from 100 to 200 0 C, more preferably of from 80 to 180 0 C.
- the solvent used in the process according to the invention comprises at least 10 wt% of a compound having a gamma lactone group, i.e. a compound according to general molecular formula (1).
- the solvent comprises at least 20 wt% of such compound, more preferably at least 50 wt%, even more preferably at least 80 wt%, based on the total weight of the solvent.
- Reference herein to the solvent is to the total liquid phase in which the solid feed material is heated.
- the solvent may comprise further organic compounds that are known solvents for organosolv pulping.
- Examples of such known compounds are lower aliphatic alcohols such as methanol or ethanol, polyhydric alcohols, in particular diols with the hydroxyl groups on adjacent carbon atoms such as ethylene glycol, glycerol, 1, 2-propanediol or 2, 3-butanediol, lower carboxylic acids such as formic acid or acetic acid, and acetone.
- the solvent may also comprise water, preferably in an amount up to 50 wt%, more preferably up to 20 wt%.
- the solvent may comprise an acid catalyst. Any acid known to be suitable as catalyst in organosolv pulping may be used.
- strong mineral acids such as phosphoric acid, sulphuric acid, hydrochloric acid and nitric acid, are known to be very effective catalysts for organosolv pulping.
- the catalyst preferably is a strong mineral or organic acid with a pKa below 2.5.
- Preferred strong mineral acids are phosphoric acid and sulphuric acid, more preferably phosphoric acid.
- Preferred strong organic acids are oxalic acid, 2-oxopropanoic acid, maleic acid, 2, 4 , 6-trihydroxibenzoic acid. Combinations of acids may also be used.
- the acid catalyst in particular in case of a mineral catalyst, is therefore preferably present in a concentration of below 5 wt% of the solvent, more preferably in a concentration in the range of from 0.01 to 3.0 wt%, even more preferably of from 0.05 to 1.0 wt%.
- a heating temperature in the range of from 100 to 210 0 C it is preferred to use a solvent that is free of mineral acid. Therefore, in a preferred embodiment of the process according to the invention, the feed material is heated at a temperature in the range of from 100 to 210 0 C, more preferably of from 120 to 180 0 C, in a solvent that is free of mineral acid.
- the lignocellulosic feed material may be any lignocellulosic material known to be a suitable feedstock for pulping processes. Examples of such materials are hardwood, softwood, bagasse, wheat straw, miscanthus, switch grass, reed, or flax.
- the feed material may be in any form known to be suitable for organosolv pulping, typically in the form of particles with dimensions in the order of a few centimetres, for example wood chips or cutted stalks.
- the organosolv process according to the invention may be carried out in a batch, semi-batch or continuous operation.
- the ratio of solvent to solid feed material is preferably m the range of from 2 to 50, more preferably of from 3 to 15.
- the liquid hourly velocity of the solvent is preferably in the range of from 1 to 50 litre solvent per kg feed material per hour, more preferably of from 2 to 25 litre/kg/h.
- Reference herein to a compound having a gamma lactone group is to a compound according to general molecular formula (1), wherein R ⁇ to Rg each represent, independently, a H atom or an organic group connected with a carbon atom to the lactone group.
- the total number of carbon atoms of the compound is preferably at most 20, more preferably at most 15.
- the compound according to general molecular formula (1) preferably is a compound wherein R ⁇ , R2, R3 and R4 are a hydrogen atom, more preferably a compound wherein R ] _, R2 ? R3 and R4 are a hydrogen atom and R5 is a methyl group.
- Rg is a hydrogen atom
- Rg is a hydrogen atom
- Rg is a carboxyl group
- the compounds according to formulas (2) to (5) are levulinic acid dimers that may be obtained by contacting levulinic acid in the presence of hydrogen with a strongly acidic catalyst having a hydrogenating function, e.g. Pd/cation-exchange resin, at elevated temperature and preferably at elevated pressure.
- a strongly acidic catalyst having a hydrogenating function e.g. Pd/cation-exchange resin
- Typical process temperatures and pressures are in the range of from 60 to 170 0 C and of from 1 to 200 bar (absolute) , respectively.
- Such process for levulinic acid dimerisation is described in detail in co-pending patent application EP 04106107.8.
- the catalyst and process conditions of this process are similar to those applied in the known single-step process for the production of methyl isobutyl ketone from acetone .
- the ester preferably is an alkyl ester with an alcohol fragment with at most 10 carbon atoms, more preferably a linear alkyl ester with an alcohol fragment with at most 5 carbon atoms, even more preferably a methyl or an ethyl ester.
- the feed material is preferably heated in the solvent at a pressure in the range of from 1 to 10 bar (absolute) , more preferably of from 1 to 5 bar (absolute) . Since compounds according to general formula (1) have a relatively low volatility as compared to conventional organosolv solvents like lower aliphatic carboxylic acids or alcohols, the organosolv process according to the invention can be carried out at relatively low pressures.
- the compound (s) according to general molecular formula (1) that are used in the solvent are recovered for recycling. This may for example be done by applying the following process steps, after the heating of the feed material in the solvent as hereinabove described:
- step (d) using the compound according to general molecular formula (1) obtained in step (d) in the solvent wherein the feed material is heated.
- step (a) the solid and liquid fraction obtained in the organosolv process according to the invention are separated from each other by conventional means, e.g. filtration.
- the thus-obtained liquid fraction comprises solvent and dissolved feed material degradation products, mainly depolymerised hemicellulose and lignin.
- step (b) the liquid fraction is further hydrolysed after addition of water in order to convert the dissolved feed material degradation products into compounds that boil at a lower temperature than the compound according to general molecular formula (1) .
- Hydrolysis step (b) is carried out in the presence of an acid catalyst. In case the liquid fraction already contained an acid catalyst, i.e. the acid catalyst used in the organosolv step, no additional catalyst needs to be added.
- an homogeneous or heterogeneous acid catalyst preferably a heterogeneous acid catalyst
- a heterogeneous acid catalyst has to be added to the liquid fraction obtained in step (a) .
- step (c) the hydrolysed dissolved feed material degradation products are distilled from the compound (s) according to general molecular formula (1) . If lower boiling conventional solvent compounds were present in the solvent, for example methanol, ethanol, formic acid or acetic acid, they will also be distilled from the compound (s) according to general molecular formula (1) . If, however, high boiling conventional compounds for organosolv solvents are present in the solvent, i.e.
- step (d) the compound according to general molecular formula (1) is recycled to the organosolv step to be used in the solvent.
- the solvent boils at a relatively high temperature and, thus, the solvent may be recycled by distilling the hydrolysed dissolved feedstock degradation products from the solvent.
- the solvent boils at a lower temperature and, thus, the solvent needs to be distilled from the feed degradation products, which requires a larger distillation capacity.
- the acetone- washed residue was dried by purging it overnight with nitrogen, removed from the reactor, and weighed. During all experiments, a dark liquid fraction was discharged from the reactor tube and the acetone-washed residue obtained, i.e. the solid cellulosic fraction, had a considerably lighter colour than the feed material.
- the composition of the solvent, the reaction temperature, the amount of residue as percentage of the weight of the feed material and the cellulose content of the residue are shown for EXAMPLES 1 to 5.
- the cellulose content was determined by hydrolysing all polysaccharides followed by identification and quantification of sugars by means of gas chromatography according to TAPPI method T 249 cm-00.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI0612067A BRPI0612067A2 (en) | 2005-06-15 | 2006-06-14 | process for forming organosolv pulp, and use of a compound |
EP06763709A EP1891263A1 (en) | 2005-06-15 | 2006-06-14 | A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
CA002611152A CA2611152A1 (en) | 2005-06-15 | 2006-06-14 | A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP05105245.4 | 2005-06-15 | ||
EP05105245 | 2005-06-15 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006134126A1 true WO2006134126A1 (en) | 2006-12-21 |
Family
ID=35501005
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2006/063207 WO2006134126A1 (en) | 2005-06-15 | 2006-06-14 | A process for organosolv pulping and use of a gamma lactone in a solvent for organosolv pulping |
Country Status (6)
Country | Link |
---|---|
US (1) | US20070034345A1 (en) |
EP (1) | EP1891263A1 (en) |
CN (1) | CN101198745A (en) |
BR (1) | BRPI0612067A2 (en) |
CA (1) | CA2611152A1 (en) |
WO (1) | WO2006134126A1 (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7842161B2 (en) * | 2006-12-18 | 2010-11-30 | The University Of Maine System Board Of Trustees | Pre-extraction and solvent pulping of lignocellulosic material |
US7943009B2 (en) | 2006-12-18 | 2011-05-17 | University Of Maine System Board Of Trustees | Process of treating a lignocellulosic material with an alkali metal borate pre-extraction step |
NL2011164C2 (en) * | 2013-07-15 | 2015-01-21 | Stichting Energie | Improved process for the organosolv treatment of lignocellulosic biomass. |
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WO2005058856A1 (en) * | 2003-12-15 | 2005-06-30 | Shell Internationale Research Maatschappij B.V. | A process for the liquefaction of lignocellulosic material |
CA2591796C (en) * | 2004-12-23 | 2014-02-18 | Shell Internationale Research Maatschappij B.V. | A process for the hydrogenation of a lactone or of a carboxylic acid or an ester having a gamma-carbonyl group |
CA2701194A1 (en) * | 2009-04-23 | 2010-10-23 | Greenfield Ethanol Inc. | Separation of reactive cellulose from lignocellulosic biomass with high lignin content |
EP2435453B1 (en) | 2009-05-28 | 2022-03-02 | Suzano Canada Inc. | Derivatives of native lignin |
US8580978B2 (en) * | 2009-08-07 | 2013-11-12 | Shell Oil Company | Process for preparing a hydroxyacid or hydroxyester |
US20110112326A1 (en) * | 2009-08-07 | 2011-05-12 | Jean-Paul Lange | Process for hydrogenation |
EP2536780A4 (en) | 2010-02-15 | 2013-11-13 | Lignol Innovations Ltd | Carbon fibre compositions comprising lignin derivatives |
WO2011097720A1 (en) * | 2010-02-15 | 2011-08-18 | Lignol Innovations Ltd | Organosolv process |
EP2536798B1 (en) | 2010-02-15 | 2022-04-27 | Suzano Canada Inc. | Binder compositions comprising lignin derivatives |
WO2012000093A1 (en) * | 2010-06-30 | 2012-01-05 | Lignol Innovations Ltd. | Organosolv process |
BR112013010479A2 (en) | 2010-11-05 | 2016-08-02 | Greenfield Ethanol Inc | continuous process for fractionation of sugarcane bagasse biomass |
US9932707B2 (en) | 2010-11-05 | 2018-04-03 | Greenfield Specialty Alcohols Inc. | Bagasse fractionation for cellulosic ethanol and chemical production |
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EP2688959A4 (en) | 2011-03-24 | 2014-09-10 | Lignol Innovations Ltd | Compositions comprising lignocellulosic biomass and organic solvent |
US9255189B2 (en) | 2011-07-28 | 2016-02-09 | Greenfield Specialty Alcohols Inc. | Ethanol production with two stage continuous steam pre-treatment of lignocellulosic biomass |
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US20140370594A1 (en) * | 2013-06-14 | 2014-12-18 | Wisconsin Alumni Research Foundation | Biological conversion of biomass-derived sugars to value added chemicals |
WO2015073889A1 (en) * | 2013-11-15 | 2015-05-21 | The Regents Of The University Of California | Gasoline prepared from biomass-derived levulinic acid |
WO2017015467A1 (en) * | 2015-07-22 | 2017-01-26 | Glucan Biorenewables, Llc | High purity cellulose compositions and production methods |
CN109811585B (en) * | 2019-04-15 | 2021-08-20 | 齐鲁工业大学 | Method for improving strength performance of cardboard paper |
CN112144308B (en) * | 2020-07-24 | 2022-04-26 | 齐鲁工业大学 | Method for refining and upgrading chemical pulp into dissolving pulp |
CN112796134A (en) * | 2020-10-13 | 2021-05-14 | 中国林业科学研究院林产化学工业研究所 | Method for pretreating wood fibers in bio-based polar aprotic solvent system |
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2006
- 2006-05-30 US US11/420,981 patent/US20070034345A1/en not_active Abandoned
- 2006-06-14 WO PCT/EP2006/063207 patent/WO2006134126A1/en not_active Application Discontinuation
- 2006-06-14 BR BRPI0612067A patent/BRPI0612067A2/en not_active IP Right Cessation
- 2006-06-14 CA CA002611152A patent/CA2611152A1/en not_active Abandoned
- 2006-06-14 CN CNA2006800214447A patent/CN101198745A/en active Pending
- 2006-06-14 EP EP06763709A patent/EP1891263A1/en not_active Withdrawn
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Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7842161B2 (en) * | 2006-12-18 | 2010-11-30 | The University Of Maine System Board Of Trustees | Pre-extraction and solvent pulping of lignocellulosic material |
US7943009B2 (en) | 2006-12-18 | 2011-05-17 | University Of Maine System Board Of Trustees | Process of treating a lignocellulosic material with an alkali metal borate pre-extraction step |
US8475627B2 (en) | 2006-12-18 | 2013-07-02 | University Of Maine System Board Of Trustees | Process of treating a lignocellulosic material |
NL2011164C2 (en) * | 2013-07-15 | 2015-01-21 | Stichting Energie | Improved process for the organosolv treatment of lignocellulosic biomass. |
EP3022216A1 (en) * | 2013-07-15 | 2016-05-25 | Stichting Energieonderzoek Centrum Nederland | Improved process for the organosolv treatment of lignocellulosic biomass |
EP3022216B1 (en) * | 2013-07-15 | 2023-10-04 | Nederlandse Organisatie voor toegepast- natuurwetenschappelijk Onderzoek TNO | Improved process for the organosolv treatment of lignocellulosic biomass |
Also Published As
Publication number | Publication date |
---|---|
EP1891263A1 (en) | 2008-02-27 |
US20070034345A1 (en) | 2007-02-15 |
CN101198745A (en) | 2008-06-11 |
CA2611152A1 (en) | 2006-12-21 |
BRPI0612067A2 (en) | 2018-12-18 |
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